CN206549434U - A kind of coke oven flue gas dry-type desulphurization device, the dust removal integrated system of coke oven flue gas dry type desulfurizing - Google Patents
A kind of coke oven flue gas dry-type desulphurization device, the dust removal integrated system of coke oven flue gas dry type desulfurizing Download PDFInfo
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- CN206549434U CN206549434U CN201720181161.4U CN201720181161U CN206549434U CN 206549434 U CN206549434 U CN 206549434U CN 201720181161 U CN201720181161 U CN 201720181161U CN 206549434 U CN206549434 U CN 206549434U
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Abstract
The utility model provides a kind of coke oven flue gas dry-type desulphurization device, the dust removal integrated system of coke oven flue gas dry type desulfurizing, and desulfurizer includes inlet air stack, one-level fluid bed section, venturi section, conical section and the secondary streamsization bed section being sequentially communicated from bottom to top；The one-level fluid bed section is provided with solid sodium base absorbant feeding unit；The one-level fluid bed section is provided with solid calcium-base absorbing agent feeding unit with venturi section junction；The secondary streamsization bed section has outlet.The desulphurizing and dust-removing integral system that the utility model is provided for core, is mainly made up of with " novel desulfurizer+dust arrester " the one-level fluid bed section of high temperature, the secondary streamsization of the high turbulence of low temperature bed section, solid absorbent feeding unit etc..Pass through this system, the utility model energy efficient removal SOX, removal efficiency, and can be by the SO in coke oven flue gas more than 98%X, hydrogen sulfide, tar and the total removing of ultrafine dust particle, meet state environmental emissioning standard, realize Coke-oven flue gas governing.
Description
Technical field
The utility model is related to Coke-oven flue gas governing technical field, more particularly to a kind of coke oven flue gas dry-type desulphurization device,
The dust removal integrated system of coke oven flue gas dry type desulfurizing.
Background technology
Coke oven is the kiln with coal refining coke, coalingging, coke pushing, can produce a large amount of cigarettes in quenching and production process
Gas.Contain H in coke oven flue gas2S, front end gas desulfurizer fails to remove H completely2S, coke-stove gas participates in combustion heat supplying, generation
SO2, concentration is in 80~450mg/m3.Compared with power-plant flue gas parameter, flue gases of cock oven has the characteristics that：
1) flue gases of cock oven temperature is relatively low.Power-plant flue gas temperature is between 300~400 DEG C, coke-oven plant's coke oven flue
EGT is relatively low, generally below 250 DEG C, if using BF gas heating coke oven, stack gases temperature can be lower
(generally below 200 DEG C).In the case where flue-gas temperature is less than 250 DEG C, if the catalysis used using power-plant flue gas denitration
Agent carries out denitration, then denitration efficiency is very low, it is impossible to meet the requirement of standard limit of smog release.
2) coke oven chimney must be in hot standby state all the time.Compared with power-plant flue gas, coke oven flue waste gas is de- by desulfurization
Coke oven chimney is required to return to after nitre, air is emitted into again after heating coke oven chimney, therefore coke oven chimney is in all the time
Hot standby state.Effluent gas temperature after desulphurization denitration necessarily be greater than flue gas dew point temperature, and flue-gas temperature must not be less than 130
℃。
3)SO2Influence of the content to low-temperature denitration：In the presence of SCR (SCR) catalyst, coke oven cigarette
Part SO in gas2SO can be converted into3.In 180 DEG C to 230 DEG C of temperature range, ammonia and SO3Reaction easily generates sulfuric acid
Hydrogen ammonium.Ammonium hydrogen sulfate easily deliquescence, melting temperature is 147 DEG C, and boiling point is 350 DEG C.Ammonium hydrogen sulfate is very sticky and is difficult to clean off,
Catalyst surface is sticked to, the service efficiency of catalyst can be had a strong impact on.
In terms of Coke-oven flue gas governing, independent coke-oven plant is heated with self-produced high heating value coke-stove gas, when operating not strict
Chamber temperature is higher, easily produces nitrogen oxides.Although the coke-stove gas for melting down heating is purified, relative to blast furnace
For coal gas, still containing the nitrogen component such as higher sulfide (inorganic sulfur and organic sulfur) and ammonia, HCN, pyridine, quinoline, most
End form is into SO2And NOX.Independence coke-oven plant of China is nearly all one section of heating, and combustion chamber easily produces localized hyperthermia and forms NOX。
Therefore, the SO in independent coke-oven plant's flue gas2And NOXIt is higher, it is difficult to up to standard, it is necessary to take post-treatment measure.
Current coking field at home and abroad, the desulphurization denitration technology for flue gases of cock oven is still in development.Application
Publication No. for CN 105107349A Chinese patent literature disclose a kind of flue gases of cock oven desulphurization denitration combined purifying technique and
Device, the purification technique first carries out desulfurization before denitrating flue gas, and its desulphurization system is prepared single by desulfurizing tower, desulfurizing agent solution
Member, circulating ash solution preparation unit and solution supply unit composition, the sodium carbonate liquor prepared by desulfurizing agent solution preparation unit
Top tank at the top of desulfurizing tower is delivered to by solution supply unit, then desulfurizing agent solution gravity flow enters atomizer, and atomizer will
Desulfurizing agent solution is atomized into 50~100 microns of particulate；Flue gases of cock oven is made de- by the smoke distributor at the top of desulfurizing tower
It is uniformly distributed in sulphur tower, flue gases of cock oven is sufficiently mixed with the desulfurizing agent particulate after atomization in desulfurizing tower, sulfur dioxide is with taking off
Sulfur particle occur material chemical reaction, generate sodium sulfite, removing flue gases of cock oven in sulfur dioxide, powdery sodium sulfite with
Flue gas after coke oven flue desulfurization enters dedusting denitrating system.
Above-mentioned technology uses rotating spraying semi-dry desulphurization, but to the removal effect of sulfur dioxide and sulfur trioxide compared with
Difference.
Utility model content
In view of this, the application provides a kind of coke oven flue gas dry-type desulphurization device, coke oven flue gas dry type desulfurizing dedusting one
Change system, the desulfurizer provided using the utility model purifies coke oven flue gas, SOXRemoval effect it is preferable.
The utility model provides a kind of coke oven flue gas dry-type desulphurization device, including：
Inlet air stack, one-level fluid bed section, venturi section, conical section and the secondary streams being sequentially communicated from bottom to top
Bed section；The one-level fluid bed section is provided with solid sodium base absorbant feeding unit；The one-level fluid bed section and venturi section
Junction is provided with solid calcium-base absorbing agent feeding unit；The secondary streamsization bed section has outlet.
Preferably, the conical section is provided with humidifying cooling unit.
Preferably, the inlet air stack is additionally provided with airflow uniform distribution unit.
In the utility model, high temperature coke oven flue gas is firstly introduced into one-level fluid bed section by inlet air stack, and here
SO in the solid sodium base absorbant hybrid reaction of addition, initial absorption flue gasX.Reacted flue gas and the solid subsequently added
Calcium-base absorbing agent is admitted to secondary streamsization bed section by the acceleration of venturi section, and a large amount of calcium base and sodium base absorbant particles are formed
The Large ratio surface bed material of fierce turbulence, further by the SO in flue gasXAbsorb, remove.Meanwhile, the secondary streams of high turbulence
Bed section can cause ultrafine dust aggregation coalescence, the increase carried in its internal coke oven flue gas, be formed compared with coarse granule, more favorably
Removed in flue dust by follow-up deduster.Also, also contain hydrogen sulfide in coke oven flue gas, the pollutant such as tar is high in low-temperature zone
The secondary streamsization bed section of turbulence, gas-particle two-phase produces fierce turbulence with mixing due to the effect of air-flow, hydrogen sulfide and tar with
Absorbent is fully contacted, and then realizes efficient removing.
Compared with prior art, the utility model uses the one-level fluid bed section of high temperature plus the secondary streams of the high turbulence of low temperature
Change the novel reactor that bed section is combined, the desulfuration efficiency to coke oven flue gas can be improved to greatest extent.Also, the high turbulence of low temperature
Secondary streamsization bed section has efficient mass transfer, the turbulence environment of heat transfer, is conducive to the coalescence of ultra-fine flue dust, and dust granules increase is entered
And realize the efficient removal of ultrafine dust in coke oven flue gas.
In addition, the application preferably sets humidifying cooling unit in desulfurizer conical section, cooled by its atomizing spray, temperature
Drop is controllable to be not less than 130 DEG C for chimney entrance exhaust gas temperature, beneficial to desulfurization, reduction energy consumption etc..
The application provides a kind of dust removal integrated system of coke oven flue gas dry type desulfurizing, including：
Desulfurizer described above；
Charging aperture and the dust arrester that the outlet of secondary streamsization bed section is connected in the desulfurizer；
The air-introduced machine being connected with the dust arrester gas outlet, for drawing neat stress.
Preferably, the system also includes：The cycle flue being connected is exported with air-introduced machine, the cycle flue is filled with desulfurization
Put middle inlet air stack to be connected, the cycle flue is provided with flue gas load adjusting means.
Preferably, the dust arrester is sack cleaner；Sack cleaner lower end is by air flume, with desulfurizer
Middle one-level fluid bed section is connected with venturi section junction, and/or with being connected in the middle part of one-level fluid bed section in desulfurizer.
Preferably, the sack cleaner also has byproduct discharge, is connected with accessory substance warehouse.
The utility model also provides a kind of dust removal integrated method of coke oven flue gas dry type desulfurizing, comprises the following steps：
1) high temperature coke oven flue gas is reacted with solid sodium base absorbant in fluidization of solid mode, obtains preliminary desulfurization cigarette
Gas；
2) the preliminary desulfurization fume is mixed with solid calcium-base absorbing agent after being accelerated by venturi, with fluidization of solid
Mode is reacted, and obtains desulfurization fume；
3) by the desulfurization fume dedusting, neat stress is obtained.
Preferably, the step 2) in reaction carried out under conditions of humidifying cooling, the humidifying cooling controls the temperature drop to be
Chimney entrance exhaust gas temperature is not less than 130 DEG C.
Preferably, the step 3) by Bag filter dedusting, obtain neat stress and the complete solid material of unreacted；
The part neat stress is led back into step 1) regulation flue gas load；The complete solid material of the unreacted is returned into step
It is rapid 1) and/or step 2).
Compared with prior art, the desulphurizing and dust-removing integral system that the utility model is provided is with " novel desulfurizer+dedusting
Device " is core, is mainly supplied by the one-level fluid bed section of high temperature, the secondary streamsization of the high turbulence of low temperature bed section, solid absorbent
Unit etc. is constituted.Pass through this system, the utility model energy efficient removal SO2And SO3, removal efficiency is up to more than 98%, and energy
By the SO in coke oven flue gasX, hydrogen sulfide, tar and the total removing of ultrafine dust particle, realize SO2Control is in 30mg/m3With
Under, flue dust is controlled in 10mg/m3Following environmentally friendly minimum discharge index.
Brief description of the drawings
The dust removal integrated schematic flow sheet of coke oven flue gas dry type desulfurizing that Fig. 1 provides for the embodiment of the present application.
Embodiment
The technical scheme in the utility model embodiment is clearly and completely described below, it is clear that described reality
It is only a part of embodiment of the utility model to apply example, rather than whole embodiments.Based on the embodiment in the utility model,
The every other embodiment that those of ordinary skill in the art are obtained under the premise of creative work is not made, belongs to this reality
With novel protected scope.
The utility model provides a kind of coke oven flue gas dry-type desulphurization device, including：
Inlet air stack, one-level fluid bed section, venturi section, conical section and the secondary streams being sequentially communicated from bottom to top
Bed section；The one-level fluid bed section is provided with solid sodium base absorbant feeding unit；The one-level fluid bed section and venturi section
Junction is provided with solid calcium-base absorbing agent feeding unit；The secondary streamsization bed section has outlet.
This application provides a kind of novel desulphurization reaction unit, the desulfurizer provided using the utility model purifies coke oven
Flue gas, can obtain preferable SOXRemoval effect, and beneficial to the efficient removal of follow-up dust etc..
The bottom for the desulfurizer that the application is provided includes inlet air stack, for introducing coke oven flue gas.The desulfurizer
There can be venturi void tower structure；In the desulfurizer of the embodiment of the present application, it is connected with inlet air stack, connect is one-level stream
Change bed section.
Coke oven flue gas wide temperature range, temperature change is 190~280 DEG C.The coke oven flue gas (200~280 DEG C) of high temperature can
, also can be without waste heat boiler heat recovery and utilization with through waste heat boiler heat recovery and utilization.(200~280 DEG C) of coke oven flue gas leads to
Cross inlet air stack and be firstly introduced into one-level fluid bed section, the one-level fluid bed section is high temperature section first-stage reactor (reaction bed), is made
For first order absorption reacting environment.Wherein, a large amount of solid particles are suspended among the fluid of motion, so that particle has fluid
Some appearance features, the solid contact condition of this stream is referred to as fluidization of solid, i.e. fluid bed, also referred to as conveys bed.
In the utility model, the one-level fluid bed section is provided with solid sodium base absorbant feeding unit, and it is used to supply
Solid sodium base absorbant is answered, sodium base absorbant storehouse and connected dispenser is generally comprised.In the utility model embodiment,
The solid sodium base absorbant feeding unit is arranged on one-level fluid bed section front end.The utility model embodiment is existed by dispenser
In high temperature section first-stage reactor, solid sodium base absorbant such as NaHCO is added3Deng.
In preferred embodiment of the present utility model, the inlet air stack is additionally provided with airflow uniform distribution unit so that enter
The smoke distribution of high temperature section first-stage reactor is uniform, it is ensured that the SO in sodium base absorbant and flue gasXIt is sufficiently mixed reaction.Meanwhile,
SO that can be in flue gasXThe requirement of concentration and flue gas after desulfurization temperature, adjusts the addition of sodium base absorbant.In addition,
In embodiment of the present utility model, high temperature section first-stage reactor has substantial amounts of calcium base and sodium base absorbant recycle stock, can pass through
After rear end deduster is collected, added through mass flow air skewed slot in the middle part of one-level fluid bed section.The embodiment of the present application is by newly adding
SO in the sodium base absorbant entered and circulation returning charge, initial absorption flue gasX, complete high temperature section first-stage reactor desulphurization reaction.
In specific embodiment of the utility model, the sodium base absorbant (NaHCO of addition3) connect with coke oven high-temperature flue gas
Touch, the Na that fineness is smaller, specific surface area is bigger, activity is higher is resolved into heat smoke2CO3, while decomposing the H of generation2O energy
Increase the humidity of flue gas, be that follow-up desulphurization reaction etc. creates conditions.In high temperature section first-stage reactor sodium base absorbant and flue gas
SOXReaction is sufficiently mixed, key reaction formula is as follows：
2NaHCO3+SO2=Na2SO3+2CO2+H2O；
2NaHCO3+SO3=Na2SO4+2CO2+H2O；
Na2CO3+SO2=Na2SO3+CO2；
Na2CO3+SO3=Na2SO4+CO2；
Na2SO3+1/2O2=Na2SO4。
In specific embodiment of the utility model, the residence time of the flue gas of the one-level fluid bed section for 0.1s~
0.5s。
In the desulfurizer of the embodiment of the present application, be connected with one-level fluid bed section, connect be venturi section, for adding
Speed, introducing flue gas material.The venturi section is desulfurizer part well known to those skilled in the art, and the application can be used
Single hole or porous Venturi tube accelerating sections.In the utility model, the one-level fluid bed section is set with venturi section junction
There is solid calcium-base absorbing agent feeding unit, for supplying solid calcium-base absorbing agent such as Ca (OH)2, generally comprise calcium-base absorbing agent storehouse
With connected dispenser.
Desulfurizer described in the embodiment of the present application includes conical section and secondary streamsization bed section；The miner diameter end and Wen Qiu of conical section
In section connect, bigger diameter end and secondary streamsization a section are connected.In embodiments herein, the conical section is provided with humidifying cooling
Unit.The utility model is not particularly limited to the humidifying cooling unit, can such as be sprayed using atomized water commonly used in the art
Equipment.The application preferably desulfurizer conical section set humidifying cooling unit, cooled by its atomizing spray, temperature drop it is controllable
Chimney entrance exhaust gas temperature is not less than 130 DEG C, beneficial to desulfurization, reduction energy consumption etc..
In the embodiment of the present application, secondary streamsization bed section is located at desulfurizer top and extends to top.The secondary streams
It is the high turbulence second order reaction bed (reactor) of low-temperature zone or high turbulence second reactor to change bed section, and its top has outlet, can arranged
Go out desulfurization fume.In specific embodiment of the utility model, the residence time of the flue gas of the secondary streamsization bed section is 1s
~15s.
In specific embodiment of the utility model, high temperature section first order reaction bed rear end and the high turbulence second order reaction of low-temperature zone
Bed reactor connection, by venturi accelerating sections, a large amount of sodium bases and calcium-based material are admitted to the high turbulence second order reaction bed of low-temperature zone
In reactor, add calcium-base absorbing agent in low-temperature zone high turbulence second order reaction bed, a large amount of sodium bases and calcium-based material particle and it is new plus
The calcium-base absorbing agent entered is mixed with the fierce turbulence of flue gas, and fully contact is formed in the Large ratio surface bed material of fierce turbulence, bed
Material concentration highest position (Ca+Na)/S ratios up to more than 50, greatly enhance the heat and mass transport between gas-solid.Also,
130 DEG C can be not less than in chimney entrance exhaust gas temperature by humidifying cooling unit atomizing spray cooling, temperature drop control, further will
SO in flue gasXAbsorb, remove.Wherein, the key reaction formula in high turbulence second order reaction bed is as follows：
Na2CO3+SO2=Na2SO3+CO2；
Na2CO3+SO3=Na2SO4+CO2；
Na2SO3+1/2O2=Na2SO4；
Ca(OH)2+SO2=CaSO3·1/2H2O+1/2H2O；
Ca(OH)2+SO3=CaSO4·1/2H2O+1/2H2O；
CaSO3·1/2H2O+1/2O2=CaSO4·1/2H2O；
Ca(OH)2+H2S→CaSO3。
Meanwhile, the application uses high turbulence second reactor, and the ultrafine dust carried in coke oven flue gas can be caused in height
In the reactor of turbulence, assemble coalescence, increase and formed compared with coarse granule, be more beneficial for flue dust and removed by follow-up deduster.And
And also contain hydrogen sulfide in coke oven flue gas, the pollutant such as tar, gas-particle two-phase in the high turbulence second order reaction bed reactor of low-temperature zone
Due to the effect of air-flow, fierce turbulence is produced with mixing, hydrogen sulfide and tar are fully contacted with absorbent, and then realize efficient
Removing.
Therefore, the application adds the novel trans that the high turbulence second order reaction bed of low-temperature zone is combined using high temperature section first-stage reactor
Device is answered, desulfuration efficiency can be improved to greatest extent.Meanwhile, can be according to the characteristics of project, the reduction of control flue-gas temperature, temperature well
Drop control is not less than 130 DEG C in chimney entrance exhaust gas temperature, and the high turbulence second order reaction bed accessory of low-temperature zone has efficient mass transfer, heat transfer
Turbulence environment, be conducive to the coalescence of ultra-fine flue dust, dust granules increase, and then realize the efficient of ultrafine dust in coke oven flue gas
Removing.
This application provides a kind of dust removal integrated system of coke oven flue gas dry type desulfurizing, including：
Desulfurizer described above；
Charging aperture and the dust arrester that the outlet of secondary streamsization bed section is connected in the desulfurizer；
The air-introduced machine being connected with the dust arrester gas outlet, for drawing neat stress.
The desulphurizing and dust-removing integral cleaning system designed using the application, can be realized with relatively low investment and operating cost
Effective improvement of coking industry coke oven flue gas.
The desulphurizing and dust-removing integral system that the utility model is provided includes desulfurizer, and the content of the desulfurizer is as before
It is literary described.In embodiment of the present utility model, the desulfurizer of the integral system includes inlet air stack, and it is provided with gas
Uniform unit is flowed, can make it that the smoke distribution into high temperature section first-stage reactor is uniform, it is ensured that in sodium base absorbant and flue gas
SOXIt is sufficiently mixed reaction.
In embodiment of the present utility model, the desulfurizer of the integral system include high temperature section first order reaction bed and
Venturi section, high temperature section first order reaction bed is connected with sodium base absorbant storehouse, high temperature section first order reaction bed and literary mound by dispenser
In section junction calcium-base absorbing agent storehouse is connected with by dispenser.The embodiment of the present application mainly passes through the sodium base absorbant of addition
Deng the SO in high temperature section first-stage reactor initial absorption flue gasX。
In embodiment of the present utility model, the desulfurizer of the integral system includes conical section and low-temperature zone is high rapid
Dynamic second order reaction bed, atomized water spraying equipment is set in the conical section.In specific embodiment of the utility model, high temperature section
First order reaction bed rear end is connected with low-temperature zone high turbulence second order reaction bed reactor, by venturi accelerating sections, a large amount of sodium bases and
Calcium-based material is admitted in the high turbulence second order reaction bed of low-temperature zone, and adding calcium base in the high turbulence second order reaction bed of low-temperature zone absorbs
Agent, a large amount of sodium bases and calcium-based material particle and the calcium-base absorbing agent newly added are mixed with the fierce turbulence of flue gas, and fully contact is formed
Material concentration highest position (Ca+Na)/S ratios up to more than 50 in the Large ratio surface bed material of fierce turbulence, bed, greatly
Enhance the heat and mass transport between gas-solid.Also, it can be dropped by this humidifying cooling unit atomizing water spray of atomized water spraying equipment
Temperature, temperature drop control is not less than 130 DEG C in chimney entrance exhaust gas temperature, further by the SO in flue gasXAbsorb, remove.Meanwhile, this
Application is also beneficial to the efficient removal of flue dust, hydrogen sulfide and tar etc..
The dust removal integrated system of dry type desulfurizing that the application is provided includes dust arrester, its charging aperture and in desulfurizer two
Level fluid bed section outlet connection, to carry out dedusting to desulfurization fume.In this application, the dust arrester is preferably bag-type dust
Device.
The application is not particularly limited to the sack cleaner, using commonly used in the art.In the reality of the application
Apply in example, sack cleaner lower end passes through one-level fluid bed section in air flume, with desulfurizer and venturi section junction phase
Even, and/or with being connected in the middle part of one-level fluid bed section in desulfurizer, Matter Transfer is realized.Cloth bag in the embodiment of the present application is removed
Dirt device bottom has byproduct discharge, i.e. by-product beyond the region of objective existence row mouth, can be connected with accessory substance warehouse (desulfurizing byproduct storehouse).
In the embodiment of the present application, the high turbulence second order reaction bed outlet of low-temperature zone is directly connected on sack cleaner, filter bag
Muffin layer material in also contain a certain amount of absorbent, can remove exhaust gas dust while, further absorbing and removing cigarette
SO in gas2.The complete absorbent of a large amount of unreacteds then returns to conveying bed by mass flow air skewed slot from cloth bag lower end and repeats profit
With；Small part reacts complete by-product beyond the region of objective existence and drains into accessory substance warehouse.
The dust removal integrated system of dry type desulfurizing that the embodiment of the present application is provided includes air-introduced machine, itself and dust arrester gas outlet
Connection, and by drawing neat stress toward smoke stack emission flue.Such as, the coarse granule that reunion coalescence is formed in final flue gas is through cloth bag
Chimney is drained into by air-introduced machine after deduster purification.
In the preferred embodiment of the application, the system also includes：The cycle flue being connected is exported with air-introduced machine；It is described
Cycle flue is connected with inlet air stack in desulfurizer, realizes flue gas recirculation.Preferably, the cycle flue is provided with cigarette
Gas weight adjustment device.
In the embodiment of the present application, coke oven flue gas range of load fluctuation is 0%~100%, in order to ensure high temperature section one-level
Reactor adds the high turbulence second order reaction bed novel reaction device of low-temperature zone to have good adaptability under each operating mode, and the application can
Conventional weight adjustment device is added, high temperature section first-stage reactor entrance is negative pressure, can be by after air-introduced machine by connecting flue
Neat stress is led back to reaction unit entrance, so as to ensure the stable operation of novel reactor in low- load conditions.
Pass through this system, the utility model energy efficient removal SO2And SO3, and can be by the SO in coke oven flue gasX, vulcanization
Hydrogen, tar and the total removing of ultrafine dust particle.The utility model system investments and operating cost are relatively low, compared with SDA desulfurization road
Line apparatus can reduce investment outlay expense 20%~40% even more than, save operating cost more than 40%, with obvious technology and
Economic Application advantage.
Correspondingly, the utility model additionally provides a kind of dust removal integrated method of coke oven flue gas dry type desulfurizing, including：
1) high temperature coke oven flue gas is reacted with solid sodium base absorbant in fluidization of solid mode, obtains preliminary desulfurization cigarette
Gas；
2) the preliminary desulfurization fume is mixed with solid calcium-base absorbing agent after being accelerated by venturi, with fluidization of solid
Mode is reacted, and obtains desulfurization fume；
3) by the desulfurization fume dedusting, neat stress is obtained.
The dust removal integrated technical method of coke oven flue gas dry type desulfurizing that the utility model is provided can realize coking industry flue gas
Effective improvement, meet state environmental emissioning standard, realize the minimum discharge of atmosphere pollution.Also, the utility model technique
Flow is simple, and investment and operating cost are relatively low.
Referring to Fig. 1, the dust removal integrated schematic flow sheet of coke oven flue gas dry type desulfurizing that Fig. 1 provides for the embodiment of the present application.
190~280 DEG C of coke oven flue gas is introduced high temperature section first-stage reactor, absorbent by the utility model embodiment by flue first
The solid sodium base absorbant in storehouse is added by dispenser in transport bed reactor front end, and one-level is used as using high temperature section first-stage reactor
Absorbing reaction place, the sodium base absorbant (NaHCO of addition3) contacted with coke oven high-temperature flue gas, reacted in fluidization of solid mode,
SO in absorbing and removing flue gasX, obtain preliminary desulfurization fume.
Wherein, the NaHCO of addition3It is smaller that absorbent resolves into fineness in heat smoke, and specific surface area is bigger, activity is higher
Na2CO3, while decomposing the H of generation2O, increases the humidity of flue gas, is calcium-base absorbing agent in the high turbulence second order reaction bed of low-temperature zone
With SOXReaction create conditions.In addition, dispenser is VFC, can be according to SO in flue gasXThe requirement of concentration and smoke temperature drop,
Adjust the addition of sodium base absorbant.In embodiment of the present utility model, mole of the sodium base absorbant and (S) in flue gas
Than preferably between 0.1~0.4, corresponding temperature drop is 30~0 DEG C.
Meanwhile, it is provided with airflow uniform distribution device in high temperature section first-stage reactor front end so that enter the cigarette of transport bed reactor
Gas is evenly distributed, it is ensured that the SO in high temperature section first-stage reactor sodium base absorbant and flue gasXIt is sufficiently mixed reaction.This practicality is new
Type embodiment can also design flue gas conditioning device, it is ensured that under different coke-oven load, and flue gas flow rate exists in high temperature section first-stage reactor
More than 18m/s, beneficial to device stable operation.
Obtain after preliminary desulfurization fume, the utility model embodiment mixes it with solid calcium-base absorbing agent by venturi
After acceleration, in this two grades of absorbing reaction places of the high turbulence second reactor of low-temperature zone, the calcium-base absorbing agent of addition is with efflux of solids
SO in state mode, reactive absorption, removing flue gasX, obtain desulfurization fume.The embodiment of the present application uses high temperature section first-stage reactor
The novel desulphurization reaction unit that the high turbulence second reactor of+low-temperature zone is combined, two-stage absorbing and removing, SOXAbsorbing and removing efficiency
It is higher.
In the specific embodiment of the application, the complete calcium base of unreacted and sodium base that rear end sack cleaner is collected absorb
Agent, can be added from the high turbulence second reactor front end of low-temperature zone by mass flow air skewed slot, can also be added to high temperature section one-level
Reactor, is recycled.High temperature section first-stage reactor rear end is connected with the high turbulence second reactor of low-temperature zone, the calcium in absorbent storehouse
Base absorbant such as Ca (OH)2Added by dispenser in the high turbulence second reactor bottom of low-temperature zone；Calcium-base absorbing agent dispenser
For VFC, according to flue gas SOXThe requirement of concentration of emission adjusts the addition of calcium-base absorbing agent, the calcium-base absorbing agent of addition with
The mol ratio of (S) is preferably 1~1.2 in flue gas.
In preferred embodiment of the present utility model, the fresh calcium-base absorbing agent of addition, from high temperature section first-stage reactor
The sodium substratess material brought and the sodium base and calcium-based material that loop back, accelerate into two grades of the high turbulence of low-temperature zone anti-by venturi
Device is answered, by humidifying cooling unit atomizing spray cooling, humidifying cooling unit adjusts injection flow rate, temperature drop control according to smoke moisture
It is not less than 130 DEG C in chimney entrance exhaust gas temperature, creates SOXWith Ca (OH)2Reaction be converted into the ionic that can be completed with moment
Reaction, further by the SO in flue gasXAbsorbing and removing.
The sodium base that the utility model embodiment is brought by the fresh calcium-base absorbing agent of addition, from high temperature section first-stage reactor
Material and the sodium base and calcium-based material looped back, accelerate into the high turbulence second reactor of low-temperature zone, largely by venturi
Calcium base and sodium base absorbant particle are mixed with the fierce turbulence of flue gas, and fully contact forms the Large ratio surface bed of material of fierce turbulence
(Ca+Na)/S ratios up to more than 50 at material concentration highest position, greatly enhance the mass transfer and biography between gas-solid in layer, bed
Heat, realizes SOXEfficient absorbing and removing.
In addition, in the utility model, coke oven fine particulates are in all the time in the high turbulence second reactor of low-temperature zone
Humidification, reunite, the environment of coalescence, fine particulates dust accumulation coalescence, increase into compared with coarse granule, be more beneficial for by follow-up cloth
Bag dust collector is removed.
Obtain after desulfurization fume, the utility model is preferably by the desulfurization fume by sack cleaner dedusting, and cloth bag is removed
Also contain a certain amount of sodium base and calcium-base absorbing agent in muffin layer material on dirt device filter bag, can be in the same of removing exhaust gas dust
When, the SO in absorbing and removing flue gas againX, can obtain neat stress and the complete solid material of unreacted.Implement in the utility model
In example, the high turbulence second reactor outlet connection sack cleaner of low-temperature zone, the neat stress that sack cleaner comes out passes through air inducing
Machine is discharged into chimney.
In preferred embodiment of the present utility model, air-introduced machine outlet sets cycle flue, with high temperature section first-stage reactor
Preceding flue is connected, and by flue gas recirculation, the part neat stress is returned and drawn；Connect flue and adjusting means is set, according to front end
Load exhaust gas volumn situation of change, adjustment adjusting means regulation flue gas load, it is ensured that flue gas flow rate exists in high temperature section first-stage reactor
More than 18m/s, it is ensured that the stable operation of reactor.
In preferred embodiment of the present utility model, sack cleaner largely passes through the complete material collection of unreacted
Air flume adds transport bed reactor and continues to participate in reaction, realizes Matter Transfer；A small amount of reacted by-product beyond the region of objective existence drains into pair
Product warehouse, is transported by closed tank truck.
In summary, the utility model can mutually be tied using the high turbulence second reactor of high temperature section first-stage reactor+low-temperature zone
The novel desulphurization reaction unit of conjunction, the reaction mechanism of two-stage absorbing and removing, SOXAbsorbing and removing is more efficient.SO3And SO2It is efficient
Removing, can solve SO3And SO2The problem of ammonium hydrogen sulfate of generation is to the denitration efficiency of denitrating catalyst；Dry type desulfurizing dedusting can be solved
Certainly the problems such as atomizer blocking, abrasion and the waste of agglomeration problems and material.
The utility model realizes coke oven flue gas desulfurization by the dust removal integrated method and system of coke oven flue gas dry type desulfurizing
Dust removal integrated control, it is ensured that coke oven flue gas SO2Emission control is in 30mg/m3Hereinafter, soot emissions control is in 10mg/m3Hereinafter,
Realize " minimum discharge " of atmosphere pollution.
In the utility model, sodium base absorbant is contacted with coke oven high-temperature flue gas, and generation H is decomposed in heat smoke2O, increases
The humidity of smoke adding gas, is calcium-base absorbing agent and SO in the high turbulence second order reaction bed of low-temperature zoneXReaction create conditions, reduce low temperature
The penetrating of the high turbulence second reactor reclaimed water of section, reduces cooling, and smoke temperature drop can be controlled in chimney entrance exhaust gas temperature and is not less than
130℃.Smoke stack emission flue-gas temperature of the utility model after desulfurization and dedusting is not less than 130 DEG C, meets the hot standby of chimney, protects
Card is when desulfurization dust-removal system breaks down, and coke oven flue gas can be by bypassing from can smoothly be discharged from pull out force by chimney.
The utility model realizes desulphurizing and dust-removing integral control, and technological process is simple, easy to operate, stable, can
Cooperate with efficient removal SO3, hydrogen sulfide, tar, and produced, without preservative treatment without waste water (slag) secondary pollution, suitable for industrialization
Promote.
For a further understanding of the application, the coke oven flue gas dry type desulfurizing provided with reference to embodiment the utility model
Device, the dust removal integrated system of coke oven flue gas dry type desulfurizing are specifically described.
Embodiment 1：
The t coke ovens of certain coke-oven plant 2,*40 ten thousand use the utility model flue gases of cock oven desulfurization dust-removing technique system, and exhaust gas volumn is
180000Nm3/ h (mark condition)；Entrance flue gas temperature is 190 DEG C, former flue gas SO2Concentration is 500mg/Nm3.Use solid Ca (OH)2
And solid NaHCO3Make absorbent, Na/S ratios are that 0.1, Ca/S ratios are 1.2, material concentration highest position (Ca+Na)/S ratios are 50,
Temperature drop is 30 DEG C.
The coke oven flue gas of purification is needed to enter high temperature section first-stage reactor (residence time is 0.1s), flue gas flow rate is 18m/
s；Sodium base absorbant is added in high temperature section first-stage reactor by dispenser, the SO in flue gasXWith the sodium base absorbant of addition and
Reaction is sufficiently mixed, preliminary desulfurization fume is obtained.The calcium-base absorbing agent in absorbent storehouse is by dispenser in the high turbulence two of low-temperature zone
Stage reactor bottom is added, logical from the high temperature section first-stage reactor sodium substratess material brought and the sodium base and calcium-based material that loop back
Venturi acceleration is crossed, into the high turbulence second reactor of low-temperature zone (residence time is 11s), is carried out by atomized water spraying equipment
Atomizing spray cools, and temperature drop is controlled at 30 DEG C, further by the SO in flue gasXAbsorbing and removing, obtains desulfurization fume.
Due to the environment of humidification, reunion, coalescence, fine particle dust are in the high turbulence second reactor of low-temperature zone all the time
Assemble coalescence, increase into compared with coarse granule, be more beneficial for by follow-up sack cleaner removing.Desulfurization fume is through rear end bag-type dust
Device dedusting, obtains neat stress, and smoke stack emission flue-gas temperature is not less than 130 DEG C.
Rear end sack cleaner collects the complete material of unreacted, and most of material returns to transport bed reactor through air flume
Continue to participate in circular response in middle part.Also absorbed on sack cleaner filter bag in muffin layer material containing a certain amount of sodium base and calcium base
Agent, SO while exhaust gas dust is removed again in absorbing and removing flue gas2.Neat stress after multistep treatment is through air-introduced machine
It is discharged into chimney.Coke oven flue gas range of load fluctuation is 30%~100%, when coke oven load reduction, opens flue gas conditioning device,
Keep that there is enough flue gas flow rates in reactor.In addition, solid by-product is mainly Na2SO3、Na2SO4、CaSO3、CaSO4、
And a small amount of unreacted Ca (OH)2And NaHCO3, a small amount of reacted by-product beyond the region of objective existence drains into accessory substance warehouse, passes through hermetically sealed can
Car is transported.
This utility model device desulfuration efficiency is 98%, coke oven flue gas SO2Discharge as 10mg/m3, soot emissions are 4.5mg/
m3.The utility model overcomes the drawbacks of traditional half-dried subtraction unit is present, and realizes overall-in-one control schema, and technological process is simple, operation letter
Just, it is stable, efficient removal SO can be cooperateed with3、H2S and tar, and produced, without preservative treatment without waste water (slag) secondary pollution.
Embodiment 2：
Certain t coke oven of coke-oven plant 2,000,000 uses the utility model flue gases of cock oven desulfurization dust-removing technique system.Exhaust gas volumn is
380000Nm3/ h (mark condition)；Entrance flue gas temperature is 280 DEG C, former flue gas SO2Concentration is 200mg/Nm3.Use solid Ca (OH)2
And solid NaHCO3Make absorbent, Na/S ratios are that 0.4, Ca/S ratios are 1.0, material concentration highest position (Ca+Na)/S ratios are 50,
Temperature drop is 0 DEG C.
The coke oven flue gas of purification is needed to enter high temperature section first-stage reactor (residence time is 0.2s), flue gas flow rate is 18m/
s；Sodium base absorbant is added in high temperature section first-stage reactor by dispenser, the SO in flue gasXWith the sodium base absorbant of addition and
Reaction is sufficiently mixed, preliminary desulfurization fume is obtained.The calcium-base absorbing agent in absorbent storehouse is by dispenser in the high turbulence two of low-temperature zone
Stage reactor bottom is added, logical from the high temperature section first-stage reactor sodium substratess material brought and the sodium base and calcium-based material that loop back
Venturi acceleration is crossed, into the high turbulence second reactor of low-temperature zone (residence time is 6s), cools without atomizing spray, enters one
Walk the SO in flue gasXAbsorbing and removing, obtains desulfurization fume.
Due to the environment of humidification, reunion, coalescence, fine particle dust are in the high turbulence second reactor of low-temperature zone all the time
Assemble coalescence, increase into compared with coarse granule, be more beneficial for by follow-up sack cleaner removing.Desulfurization fume is through rear end bag-type dust
Device dedusting, obtains neat stress, and effluent gas temperature is not less than 130 DEG C.
Rear end sack cleaner collects the complete material of unreacted, and most of material returns to transport bed reactor through air flume
Continue to participate in circular response in middle part.Also absorbed on sack cleaner filter bag in muffin layer material containing a certain amount of sodium base and calcium base
Agent, SO while exhaust gas dust is removed again in absorbing and removing flue gas2.Neat stress after multistep treatment is through air-introduced machine
It is discharged into chimney.Coke oven flue gas range of load fluctuation is 30%~100%, when coke oven load reduction, opens flue gas conditioning device,
Keep that there is enough flue gas flow rates in reactor.In addition, solid by-product is mainly Na2SO3、Na2SO4、CaSO3、CaSO4、
And a small amount of unreacted Ca (OH)2And NaHCO3, a small amount of reacted by-product beyond the region of objective existence drains into accessory substance warehouse, passes through hermetically sealed can
Car is transported.
This utility model device desulfuration efficiency is 97.5%, coke oven flue gas SO2Emission control is in 5mg/m3, flue dust control exist
4mg/m3.The utility model overcomes the drawbacks of traditional half-dried subtraction unit is present, and realizes overall-in-one control schema, and technological process is simple, behaviour
Make easy, it is stable, efficient removal SO can be cooperateed with3、H2S and tar, and produced, without anti-corrosion without waste water (slag) secondary pollution
Processing.
Described above is only preferred embodiment of the present utility model, it is noted that the specialty for making the art
Technical staff, on the premise of the utility model technical principle is not departed from, is that by a variety of modifications to these embodiments
, and these modifications also should be regarded as the scope that the utility model should be protected.
Claims (7)
1. a kind of coke oven flue gas dry-type desulphurization device, including：
Inlet air stack, one-level fluid bed section, venturi section, conical section and the secondary streamsization bed being sequentially communicated from bottom to top
Section；The one-level fluid bed section is provided with solid sodium base absorbant feeding unit；The one-level fluid bed section and venturi Duan Lian
The place of connecing is provided with solid calcium-base absorbing agent feeding unit；The secondary streamsization bed section has outlet.
2. coke oven flue gas dry-type desulphurization device according to claim 1, it is characterised in that the conical section is provided with humidification
Temperature reducing unit.
3. coke oven flue gas dry-type desulphurization device according to claim 1, it is characterised in that the inlet air stack is additionally provided with
Airflow uniform distribution unit.
4. a kind of dust removal integrated system of coke oven flue gas dry type desulfurizing, including：
Desulfurizer according to any one of claims 1 to 3；
Charging aperture and the dust arrester that the outlet of secondary streamsization bed section is connected in the desulfurizer；
The air-introduced machine being connected with the dust arrester gas outlet, for drawing neat stress.
5. the dust removal integrated system of coke oven flue gas dry type desulfurizing according to claim 4, it is characterised in that the system is also
Including：The cycle flue being connected is exported with air-introduced machine, the cycle flue is connected with inlet air stack in desulfurizer, the circulation
Flue is provided with flue gas load adjusting means.
6. the dust removal integrated system of coke oven flue gas dry type desulfurizing according to claim 4 or 5, it is characterised in that described to remove
Dirt device is sack cleaner；The sack cleaner lower end by one-level fluid bed section in air flume, with desulfurizer with
Venturi section junction is connected, and/or with being connected in the middle part of one-level fluid bed section in desulfurizer.
7. the dust removal integrated system of coke oven flue gas dry type desulfurizing according to claim 6, it is characterised in that the cloth bag is removed
Dirt device also has byproduct discharge, is connected with accessory substance warehouse.
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| CN201720181161.4U CN206549434U (en) | 2017-02-27 | 2017-02-27 | A kind of coke oven flue gas dry-type desulphurization device, the dust removal integrated system of coke oven flue gas dry type desulfurizing |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720181161.4U CN206549434U (en) | 2017-02-27 | 2017-02-27 | A kind of coke oven flue gas dry-type desulphurization device, the dust removal integrated system of coke oven flue gas dry type desulfurizing |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106731585A (en) * | 2017-02-27 | 2017-05-31 | 福建龙净脱硫脱硝工程有限公司 | A kind of coke oven flue gas dry-type desulphurization device, the dust removal integrated system and method for coke oven flue gas dry type desulfurizing |
| CN108380016A (en) * | 2018-05-09 | 2018-08-10 | 福建龙净脱硫脱硝工程有限公司 | A kind of system and method for baking flue gas desulfurization depitching cigarette defluorinate dust separation |
| CN109631598A (en) * | 2018-12-06 | 2019-04-16 | 海南中航特玻科技有限公司 | A kind of all-oxygen combustion glass kiln denitration system and method based on flue gas recirculating technique |
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2017
- 2017-02-27 CN CN201720181161.4U patent/CN206549434U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106731585A (en) * | 2017-02-27 | 2017-05-31 | 福建龙净脱硫脱硝工程有限公司 | A kind of coke oven flue gas dry-type desulphurization device, the dust removal integrated system and method for coke oven flue gas dry type desulfurizing |
| CN108380016A (en) * | 2018-05-09 | 2018-08-10 | 福建龙净脱硫脱硝工程有限公司 | A kind of system and method for baking flue gas desulfurization depitching cigarette defluorinate dust separation |
| CN109631598A (en) * | 2018-12-06 | 2019-04-16 | 海南中航特玻科技有限公司 | A kind of all-oxygen combustion glass kiln denitration system and method based on flue gas recirculating technique |
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