CN209033989U - A kind of device being layered emission reduction sintering flue gas pollutant - Google Patents
A kind of device being layered emission reduction sintering flue gas pollutant Download PDFInfo
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- CN209033989U CN209033989U CN201821745479.1U CN201821745479U CN209033989U CN 209033989 U CN209033989 U CN 209033989U CN 201821745479 U CN201821745479 U CN 201821745479U CN 209033989 U CN209033989 U CN 209033989U
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Abstract
The utility model discloses a kind of devices for being layered emission reduction sintering flue gas pollutant, belong to flue gas pollutant processing technology field.The utility model includes admission line, subsidiary conduit and catalyst filter cylinder, and the bottom of admission line is provided with air inlet, and gas outlet is arranged in the top of admission line, and the air inlet of subsidiary conduit is connected with the gas outlet of admission line；Catalyst filter cylinder is set to the bottom of subsidiary conduit, and molecular sieve layer, denitration catalyst oxidant layer and V-Ce-Ti catalyst layer are from top to bottom disposed in catalyst filter cylinder.Sintering flue gas passes sequentially through molecular sieve layer, denitration catalyst oxidant layer and V-Ce-Ti catalyst layer in the utility model, catalyst carries out catalytic degradation to sintering flue gas respectively, remove the pollutant in sintering flue gas, improve the removal efficiency of dioxin and nitrogen oxides, the discharge for reducing dioxin and nitrogen oxides, achievees the purpose that environment purification.
Description
Technical field
The utility model relates to flue gas pollutant processing technology fields, are sintered more specifically to a kind of layering emission reduction
The device of flue gas pollutant.
Background technique
Steel and iron industry is the pillar industry of Chinese national economy, makes tremendous contribution for China's economic development, but simultaneously I
State's steel and iron industry Environmental Protection Level low pollution object discharge amount is high, and typical pollutant mainly includes in iron and steel enterprise's discharge exhaust gas
Dust, SO2, dioxin pollution object etc., and sintered fume nitric oxide, dioxin removing sulfuldioxide mainly have three both at home and abroad at present
Class, the first kind are compound of the addition containing amino or sulphur in raw materials for sintering, form network using the lone pair electrons and catalyst of sulphur
Closing object inhibits dioxin to generate reaction, or is reacted using sulfur dioxide, amine groups with chloride ion, reduces chlorine source and inhibits two to dislike
English generates, very low to the inhibitory effect of PCDF although the method effect is that above have preferable inhibition to PCDD, and cannot take off
Sulphide removal；Second class is active carbon adsorption, using the porous adsorption capacity of active carbon, reaches the effect of adsorbing and removing dioxin
Fruit, but activated carbon method equipment investment operating cost is high, it is also new problem that how the active carbon after absorption, which is handled,；Third class is
Selective catalytic reduction takes off dioxin, and key is to select suitable catalyst, although vanadium Ti-base catalyst can achieve
Higher dioxin removal efficiency, but it is at high price；Catalyst window temperature is unreasonable, and sintering flue gas needs to be again heated to 300-
450 DEG C or so carry out de- dioxin, and the generation again of dioxin can occur for this temperature；The V that catalyst after reaction contains2O5
For extremely toxic substance, there is serious pollution to environment and biology, the catalyst after how handling reaction is also new problem.Therefore, mesh
There is an urgent need to study the pollutant removing technology being directed in sintering flue gas in preceding society, providing for steel industry clean manufacturing has by force
The guarantee of power, and to ensuring that clean environment and human health have far reaching significance.
Through retrieving, the title of innovation and creation are as follows: it is a kind of removing sintering flue gas in nitrogen oxides and dioxin device (specially
Sharp application number: CN201520065234.4, the applying date: 2015.01.29) comprising front and back sets gradually and end to end changes
Hot device, preheater, reducing agent injection premixed device, static mixer and catalytic reactor, reducing agent spray premixed device and are equipped with Sheng
There is the reducing agent spray gun of ammonia, the catalytic reduction catalysts layer and catalyst for catalytic oxidation of front and back setting are equipped in catalytic reactor
Layer, the catalytic reduction catalysts layer includes denitration catalyst oxidant layer and rare earth metal layer.By by after flue gas with reducing agent
Mixing, then reacts with catalytic reduction catalysts again, reaches nitre and dioxin in removing flue gas, and the purpose of purifying smoke.
This application is disadvantageous in that: cannot carry out the catalytic treatment of denitration and de- dioxin to sintering flue gas under cryogenic.
Through retrieving, a kind of title of innovation and creation are as follows: denitration decarbonization device and its technique (patent Shen for sintering flue gas
Please number: CN201510743269.3, the applying date: 2016.01.13) comprising desulfurizing tower, deduster, heat exchanger, catalytic unit,
Blower, chimney, catalytic unit inner horizontal are arranged multi-layer gas channel, catalyst carrier are arranged in gas passage.Sintering flue gas
Enter deduster after desulfurization dechlorination and carries out dust purification processing, treated, and flue gas enters heat exchanger is instantaneously heated up,
After heating flue gas enter catalytic unit carry out denitration carbonization treatment, it is up to standard after flue gas chimney is entered by blower and is finally arranged
It puts.This application is disadvantageous in that: it needs by multiple subtractive process, it is complicated for operation, and although can reduce in sintering flue gas
The content of nitrogen oxides, but the dioxin in the sintering flue gas that cannot degrade.
Utility model content
1. utility model technical problems to be solved
The purpose of the utility model is to overcome in the prior art, flue gas emission reduction device to the emission reduction effect of flue gas not
Foot provides a kind of device for being layered emission reduction sintering flue gas pollutant, carries out catalytic degradation to sintering flue gas under cryogenic, keep away
Non-sintered flue gas enters atmosphere, it is possible to further solve pollution of the sintering flue gas to environment.
2. technical solution
In order to achieve the above objectives, technical solution provided by the utility model are as follows:
A kind of device of layering emission reduction sintering flue gas pollutant of the utility model, including admission line, the admission line
Bottom be provided with air inlet, gas outlet is arranged in the top of admission line, is provided with filter plate on the gas outlet；Subsidiary conduit, should
The air inlet of subsidiary conduit is connected with the gas outlet of admission line；Catalyst filter cylinder, the catalyst filter cylinder are set to subsidiary conduit
Bottom, be from top to bottom disposed with molecular sieve layer and V-Ce-Ti catalyst layer in catalyst filter cylinder.
Preferably, it is additionally provided with denitration catalyst oxidant layer in catalyst filter cylinder, which is set to molecular sieve layer
Between V-Ce-Ti catalyst layer.
Preferably, the top droop of admission line is provided with deflector.
Preferably, the outside of catalyst filter cylinder is provided with vibrator.
Preferably, strainer is provided at the top of catalyst filter cylinder.
Preferably, V is filled in V-Ce-Ti catalyst layeraCebTicOxCatalyst, and VaCebTicOxThe grain of catalyst
Diameter is 2~3mm, and the oxide mass ratio that wherein the oxide mass ratio of V and Ce is 0.5~1, Ce and Ti is 0.05~0.16.
Preferably, the angle between filter plate and deflector is α, and the value of α is 30~75 °.
Preferably, it is filled with Co-Mn-Ce catalyst in denitration catalyst oxidant layer, the partial size of the Co-Mn-Ce catalyst is 4~
5mm。
Preferably, the upper end of deflector is connected with the top of filter plate；The lower end of deflector and admission line side wall phase
Even, the lower end of deflector is lower than the bottom of filter plate.
Preferably, subsidiary conduit lower part is provided with collapsible tube, and subsidiary conduit passes through the top of collapsible tube and catalyst filter cylinder
It is connected.
3. beneficial effect
Using technical solution provided by the utility model, compared with existing well-known technique, there is following remarkable result:
(1) device of a kind of layering emission reduction sintering flue gas pollutant of the utility model, including admission line, subsidiary conduit
With catalyst filter cylinder, the bottom of admission line is provided with air inlet, and gas outlet is arranged in top；The air inlet of subsidiary conduit and air inlet
The gas outlet of pipeline is connected；Catalyst filter cylinder is set to the bottom of subsidiary conduit, from top to bottom sets gradually in catalyst filter cylinder
There are molecular sieve layer, denitration catalyst oxidant layer and V-Ce-Ti catalyst layer；The device is layered the sintering flue gas in access equipment
The pollutant, it can be achieved that in efficient cryogenic catalytic degradation sintering flue gas is handled, nitrogen oxides and dioxin in sintering flue gas are reduced
Discharge, achieve the purpose that purifying smoke；
(2) device of a kind of layering emission reduction sintering flue gas pollutant of the utility model is provided at the top of admission line
Port is provided with filter plate on gas outlet, and the top droop of admission line is provided with deflector, the angle between filter plate and deflector
There is α, filter plate obstructs the particulate matter in sintering flue gas outside catalyst filter cylinder, and then can accelerate catalytic efficiency, deflector
Sintering flue gas is drained in subsidiary conduit and is catalyzed, the sintering flue gas generated in sintering process is urged convenient for catalyst
Change degradation, reduces the discharge of pollutant in flue gas；
(3) device of a kind of layering emission reduction sintering flue gas pollutant of the utility model is filled in V-Ce-Ti catalyst layer
There is VaCebTicOxCatalyst, the oxide mass ratio that wherein the oxide mass ratio of V and Ce is 0.5~1, Ce and Ti is 0.05
~0.16, so as to combine removing NOx and dioxin, it is filled with Co-Mn-Ce catalyst in denitration catalyst oxidant layer, molecular sieve,
Co-Mn-Ce catalyst and VaCebTicOxThe partial size of catalyst successively reduces, can make molecular sieve, Co-Mn-Ce catalyst and
VaCebTicOxIt is set gradually between catalyst and will not be intermixed between catalyst, and then realizes and sintering flue gas is divided
Layer processing, and improve the catalytic effect and catalytic efficiency to sintering flue gas.
Detailed description of the invention
Fig. 1 is a kind of overall structure diagram of device for being layered emission reduction sintering flue gas pollutant；
Fig. 2 is the deflector of the utility model and the structural schematic diagram of collapsible tube；
Fig. 3 is the structural schematic diagram of the catalyst filter cylinder of the utility model；
Fig. 4 is the mixed liquor A whipping process structural schematic diagram of the utility model；
Fig. 5 is the filter plate schematic diagram of the embodiments of the present invention 2.
Label declaration in schematic diagram:
100, catalyst filter cylinder；110, molecular sieve layer；120, denitration catalyst oxidant layer；130, V-Ce-Ti catalyst layer；140,
Strainer；
200, admission line；210, filter plate；220, deflector；221, upper end；222, lower end；230, vertical angle；
300, vibrator；
400, subsidiary conduit；410, collapsible tube；
A00, reaction kettle；Point is added dropwise in A01, solution；A10, whirlpool face；A11, swirl center；A12, whirlpool edge.
Specific embodiment
Hereafter the detailed description of the utility model and example embodiment are more fully understood in combination with attached drawing, wherein this reality
It is identified with novel element and feature by appended drawing reference.
Structure depicted in this specification attached drawing, ratio, size etc., only to cooperate the revealed content of specification,
So that those skilled in the art understands and reads, enforceable qualifications are not intended to limit the utility model, therefore are not had
Technical essential meaning, the modification of any structure, the change of proportionate relationship or the adjustment of size, is not influencing the utility model
Under the effect of can be generated and the purpose that can reach, it should all still fall in the revealed technology contents of the utility model and obtain and can cover
In the range of.Meanwhile cited such as "upper", "lower", "left", "right", " centre " term in this specification, it is merely convenient to
Narration is illustrated, rather than to limit enforceable range, relativeness is altered or modified, in without substantive change technology
It holds, when being also considered as the enforceable scope of the utility model；In addition to this, it is not between each embodiment of the utility model
It is mutually independent, but can be combined.
Embodiment 1
Referring to figs. 1 and 2, the device of a kind of layering emission reduction sintering flue gas pollutant of the utility model, including into
Feed channel 200, subsidiary conduit 400 and catalyst filter cylinder 100.The bottom of admission line 200 is provided with air inlet, the air inlet with
It is sintered large flue to be connected, the sintering flue gas generated in sintering process enters in admission line 200 through air inlet；The admission line
Gas outlet is arranged in 200 top, is provided with filter plate 210 on the gas outlet, and the top droop of admission line 200 is provided with water conservancy diversion
Plate 220.
The sintering flue gas that sintering process generates moves up in admission line 200 along air inlet, and continues along air inlet pipe
Road 200 moves upwards, and the top droop of admission line 200 is provided with deflector 220, while the top setting of admission line 200
Gas outlet, when sintering flue gas moves near deflector 220, sintering flue gas moves under the guiding role of deflector 220
The upper end 221 of filter plate 210, deflector 220 is connected with the top of filter plate 210；The lower end 222 of deflector 220 and air inlet pipe
The side wall in road 200 is connected, and the lower end 222 of deflector 220 is lower than the bottom of filter plate 210, while also avoiding sintering flue gas
It is moved downward under the double action of deflector 220 and air-flow along admission line 200, it is ensured that the sintering generated in sintering process
Flue gas can enter filter plate 210；Angle between filter plate 210 and deflector 220 is α, and the value range of α is 30~75 °, this implementation
Middle α value is 45 °, and deflector 220 can prevent sintering flue gas from moving at the vertical angle 230 of admission line 200 and condensing attachment
On 230 surface of vertical angle, the device of multilayer removing sintering flue gas pollutant is avoided to cause to be lost.
When sintering flue gas is moved by filter plate 210 to subsidiary conduit 400, the air inlet and air inlet pipe of subsidiary conduit 400
The gas outlet in road 200 is connected, and when containing particulate matter in sintering flue gas, the partial size of particulate matter is greater than the diameter of filter plate 210, so that
Particulate matter is without can enter in subsidiary conduit 400 under the blocking of filter plate 210, while filter plate 210 is inclined at admission line
200 top, particulate matter are not easy to be attached to the surface of filter plate 210 and filter plate 210 are caused to be blocked, thus hinder sintering flue gas into
Enter in subsidiary conduit 400, and particulate matter promotees under the effect of gravity and towards movement at the air inlet of admission line 200
Make sintering flue gas and particulate separation, the catalytic effect of sintering flue gas can be improved.400 lower part of subsidiary conduit is provided with collapsible tube
410, subsidiary conduit 400 is connected by collapsible tube 410 with the top of catalyst filter cylinder 100, and catalyst filter cylinder 100 is set to auxiliary
The bottom of pipeline 400, collapsible tube 410 is in the truncated cone shape stood upside down, it is ensured that between subsidiary conduit 400 and catalyst filter cylinder 100
Seamless connection, so that in sintering flue gas entire motion to catalyst filter cylinder 100.
Further, the top of catalyst filter cylinder 100 is provided with strainer 140, and the outside of catalyst filter cylinder 100 is provided with vibration
Dynamic device 300.For sintering flue gas after entering in catalyst filter cylinder 100, vibrator 300 vibrates catalyst filter cylinder 100, burns
Flue gas is tied to be flowed out after 100 catalytic degradation of catalyst filter cylinder by the outlet of bottom.When vibration, strainer 140 can prevent catalyst
Catalyst in filter cylinder 100 is shaked out because of vibration outside catalyst filter cylinder 100, so that catalyst content is lossy.
A kind of method using multilayer catalytic degradation sintering flue gas pollutant of the utility model, the burning that sintering process generates
Knot flue gas moves up in admission line 200 along air inlet, and continues horizontal direction subsidiary conduit 400 by filter plate 210 and move,
It is moved in catalyst filter cylinder 100 into the sintering flue gas in subsidiary conduit 400 through collapsible tube 410, in catalyst filter cylinder 100
V-Ce-Ti catalyst layer 130 carries out catalytic degradation to the pollutant in sintering flue gas.This method can be under cryogenic to burning
Pollutant in knot flue gas cleans, so that catalysis process simplification, catalyst is denaturalized caused by can also avoiding because of high temperature
Extremely toxic substance is generated, and then generates secondary pollution.
Further, specific step is as follows for a kind of method using multilayer catalytic degradation sintering flue gas pollutant:
Step 1: sintering flue gas moves upwards after entering admission line 200, and moves under the guiding role of deflector 220
To subsidiary conduit 400, sintering flue gas is turned to when flowing into subsidiary conduit 400 by admission line 200；Detailed step are as follows:
Sintering flue gas is filtered, when sintering flue gas passes through filter when entering subsidiary conduit 400 by admission line 200 by filter plate 210
When plate 210 is moved to subsidiary conduit 400, the air inlet of subsidiary conduit 400 is connected with the gas outlet of admission line 200, works as sintering
When containing particulate matter in flue gas, the partial size of particulate matter is greater than the diameter of filter plate 210, so that particulate matter is under the blocking of filter plate 210
Without can enter in subsidiary conduit 400, while filter plate 210 is inclined at the top of admission line 200, and particulate matter is not easy to adhere to
Filter plate 210 is caused to be blocked on the surface of filter plate 210, to hinder sintering flue gas to enter in subsidiary conduit 400, and particulate matter
Under the effect of gravity and towards movement at the air inlet of admission line 200, promote sintering flue gas and particulate separation, it can
To improve the catalytic effect of sintering flue gas.
Step 2: sintering flue gas moves downward in subsidiary conduit 400, and moves to catalyst filter cylinder by collapsible tube 410
In 100；
Step 3: sintering flue gas successively passes through molecular sieve layer 110 and V-Ce-Ti after entering in catalyst filter cylinder 100
Catalyst layer 130, while vibrator 300 vibrates catalyst filter cylinder 100, sintering flue gas is catalyzed through catalyst filter cylinder 100
It is flowed out after degradation by the outlet of bottom.Detailed description is: sintering flue gas is after entering in catalyst filter cylinder 100, successively
By molecular sieve layer 110, denitration catalyst oxidant layer 120 and V-Ce-Ti catalyst layer 130, molecular sieve layer 110 accommodates 5A molecular sieve
Catalyst, the pollutant in flue gas are adsorbed in molecular sieve layer 110.After sintering flue gas enters catalyst filter cylinder 100, first pass through point
Sub- screen layers 110.5A molecular sieve catalyst is filled in molecular sieve layer 110, which is a kind of calcium A type alumino-silicate, can
To adsorb the substance that cut off diameter in sintering flue gas is not more than 5A, it is mainly used for adsorbing the H in flue gas2O and SO2, and molecular sieve layer
The granularity of 5A molecular sieve catalyst is 8~12mm in 110, and the granularity of 5A molecular sieve catalyst is 8mm, molecular sieve in the present embodiment
The a height of 1m of layer of layer 110.Further, sintering flue gas enters denitration catalyst oxidant layer 120, and denitration catalyst oxidant layer 120 accommodates Co-
Mn-Ce catalyst, the NO in flue gasXBy Co-Mn-Ce catalytic degradation in denitration catalyst oxidant layer 120, Co-Mn-Ce catalyst
Granularity is 4~5mm, the preferred 4mm of granularity of Co-Mn-Ce catalyst, a height of 1.5m of layer, Co-Mn-Ce catalyst in the present embodiment
Partial size be less than 5A molecular sieve catalyst partial size, 5A molecular sieve catalyst can be prevented to be mixed into Co-Mn-Ce catalyst.Sintering
Flue gas continues to move downwardly to V-Ce-Ti catalyst layer 130, is filled with V in V-Ce-Ti catalyst layer 130aCebTicOxCatalysis
Agent, and VaCebTicOxThe partial size of catalyst is 2~3mm, a height of 1.8m of layer.
The NO at 200 air inlet of admission line is detected simultaneouslyXConcentration 313mg/m-3, dioxin concentration is 0.86ng/
m-3, then detect the NO at 100 bottom gas outlet of catalyst filter cylinderXConcentration 187mg/m-3, dioxin concentration is 0.25ng/
m-3；NOXEmission reduction efficiency reach 40.26%；The emission reduction efficiency of dioxin reaches 70.93%；To realize NOXAnd dioxin
Joint emission reduction.
It is worth noting that specific preparation process is as follows for above-mentioned V-Ce-Ti catalyst:
Step 1: butyl titanate, glacial acetic acid and dehydrated alcohol are mixed, adds cerous nitrate and stir evenly obtained mixing
Liquid A；
Step 2: by oxalic acid obtained oxalic acid solution soluble in water, then ammonium metavanadate is added to oxalic acid solution obtained and is made
Mixed liquid B；
Step 3: mixed liquid B is added dropwise in mixed liquor A, gel is made；
Step 4: by V is made after the drying of above-mentioned gel, calciningaCebTicOxCatalyst.
VaCebTicOxCatalyst is made using sol-gal process one-step method, it can be ensured that ensures the element of institute's additive
Match constant, raising production efficiency.And allow the V-Ce-Ti catalyst being prepared on cryogenic conditions (about 200 DEG C of left sides
It is right) catalytic treatment is carried out to the sintering flue gas generated in sintering process, it can be to the dioxin and nitrogen oxides in sintering flue gas
Removal effect is played, while reducing the discharge of the dioxin in sintering flue gas and nitrogen oxides.
The mass ratio of water in butyl titanate and oxalic acid solution is 3.5~4, can be added dropwise to by mixed liquid B
Uniform and stable gel is formed during mixed liquor A, in mixed liquor A, provides basis to prepare catalyst；Ammonium metavanadate and grass
The mass ratio of acid solution is 0.028~0.035, can metavanadic acid is uniformly dissolved in oxalic acid solution, so that will mix
Close liquid B be added dropwise to during mixed liquor A, react it is more abundant, enable V more evenly, be effectively adhere on Ce-Ti carrier, into
And the catalytic effect of catalyst can be improved.In the present embodiment, the mass ratio of the water in butyl titanate and oxalic acid solution is
3.8, the mass ratio of ammonium metavanadate and oxalic acid solution is 0.032.Therefore the dosage of the present embodiment concrete component are as follows: butyl titanate
38.36g, glacial acetic acid 15g, dehydrated alcohol 40g, cerous nitrate 1.26g, oxalic acid 0.40g, water 10g, ammonium metavanadate 0.32g.This implementation
The specific preparation step of example are as follows:
Step 1: butyl titanate 38.36g, glacial acetic acid 15g and dehydrated alcohol mixing 40g are added cerous nitrate stirring
Uniformly obtained mixed liquor A；Glacial acetic acid and butyl titanate are mixed, butyl titanate dissolves in glacial acetic acid first and water
Solution coordination forms stable Ti (OH)x(OAc)y(wherein x+y=4) complex, wherein glacial acetic acid not only has butyl titanate molten
Solution effect, and play catalytic action；
Oxalic acid solution is made Step 2: the oxalic acid of 0.40g is dissolved in the water of 10g, then is added to oxalic acid solution obtained
Mixed liquid B is made in ammonium metavanadate, so that ammonium metavanadate is completely dissolved in oxalic acid solution；Mixed liquid B is gradually being added drop-wise to mixed liquor A
During, butyl titanate is reacted with water, and gradually complete hydrolysis is [Ti (OH)6]2-Jelly, and make Ce3+It is adsorbed on
After Ti jelly surface forms Ce-Ti carrier, V is then being attached to Ce-Ti carrier.
Step 3: mixed liquid B is added dropwise in mixed liquor A, while mixed liquor A is stirred；Mixed liquid B is added dropwise to mixed
Close the step in liquid A specifically:
Step (1): control magneton revolving speed is 180~220r/min, while being added dropwise to mixed liquid B with 3 drops/sec of speed
In mixed liquor A；The time for adding of step (1) is t1=1min；
Step (2): keeping magneton revolving speed constant, while adjusting the speed that mixed liquid B is added dropwise, and will be mixed with 1 drop/sec of speed
Liquid B is closed to be added dropwise in mixed liquor A；The time for adding of step (2) is t2=2min；So that being added dropwise by mixed liquid B
The early period of mixed liquor A quickly forms gel, after quickly forming gel, by the way that mixed liquid B is added dropwise under slower speed, so that
React relatively stable, so that gel prepares relatively uniform stabilization.
Step (3): raising magneton revolving speed to 280~320r/min, and change the speed that mixed liquid B is added dropwise, with 2 drops/sec
Speed mixed liquid B is added dropwise in mixed liquor A completely, be made gel；It is further illustrated: forming colloidal sol in the early stage
When, suitably slow down rate of addition, so that mixed liquor A gradually forms colloidal sol, and guarantees that the sol ingredient generated is uniformly distributed；When
When the hydrolysis of butyl titanate, polycondensation reaction are carried out to a certain extent, colloidal particle concentration is not further added by, at this moment shear rate
Variation no longer influences hydrolytic-polymeric reaction, and the variation of viscosity is unrelated with shear rate at this time, shows the feature of Newton type fluid,
It being cross-linked with each other between colloidal particle later, colloidal sol gradually to gel transition, forms certain network structure, and mobility is deteriorated, this
When increase with shear rate, bigger to the destructiveness of cross-linked network, so that apparent viscosity reduces, fluid shows false modeling
Property type characteristic of fluid, the network cross-linked of last whole system forms gel together, therefore setting procedure (2) and step (3)
Rate of addition first reduce and improve afterwards.
It is worth noting that: as shown in figure 4, mixed liquid B is added dropwise in mixed liquor A in reaction kettle A00, while to mixed
It closes liquid A to be stirred, mixed liquor A surface forms whirlpool face A10, and solution is added dropwise point A01 and is located at the whirlpool face surface A10, and solution
It is D1 that swirl center A11 distance of the point A01 apart from whirlpool face A10, which is added dropwise, and point A01 is added dropwise at the top of the A10 of whirlpool face in solution
A12 distance in whirlpool edge is D2, and D1 > D2, and mixed liquid B is quickly mixed with mixed liquor A, promotes mixed liquid B quick
React forming gel with mixed liquor A, and micelle is reset, forms chaotic space structure so that
The more uniform stabilization of the catalyst being prepared, improves the catalytic effect of catalyst.
Step 4: above-mentioned gel is stood 12h, gel is dried after the completion of standing under conditions of 100 DEG C, is dried
Gel is ground after the completion, then the powder after grinding is put into oxidizing roasting in not closed Muffle furnace, oxidizing roasting
Temperature is 400~500 DEG C, and V-Ce-Ti catalyst is made after roasting, and wherein the maturing temperature of the present embodiment is 450 DEG C, when roasting
Between be 3h.The V-Ce-Ti catalyst being prepared is VaCebTicOxCatalyst, wherein the oxide mass ratio of V and Ce is 0.5
The oxide mass of~1, Ce and Ti ratio are 0.05~0.16, wherein V in the present embodimentaCebTicOxV, Ce, Ti in catalyst
The mass ratio of oxide is 1:1:18, and detects the VaCebTicOxThe specific surface area of catalyst is 95.7219m2/g。
The catalyst of powdery will be obtained after V-Ce-Ti catalyst obtained grinding, then by its binder with 2%~10%
Mixing granulation, wherein the binder used is polymer alumina, the proportion of binder is 2%, then above-mentioned mixing granulation is obtained
Catalyst be made beaded catalyst, the diameter of beaded catalyst is 2.0mm~3.0mm, under same catalyst volume,
Grain catalyst has biggish surface area, while also there are gaps between beaded catalyst and beaded catalyst, so that particle is urged
Agent can be contacted sufficiently with sintering flue gas, and carry out catalytic degradation to sintering flue gas.
It is worth noting that, it is complete to can be prepared by Ce-Ti carrier using one-step method in the step of preparation V-Ce-Ti catalyst
At initial reaction, production cost and production time can be greatlyd save.Mixed liquid B, which is added dropwise in mixed liquor A, is made gel, colloidal sol
Gel method mainly hydrolyzes to form gel by butyl titanate, be added deionized water it is excessive or it is very few can not all be formed it is solidifying
Glue.In addition, all reagent orders of addition can all influence the formation of colloidal sol.Therefore in the utility model, all process ginsengs
Several and chemical constituent is to be mutually related, and any change of these parameters will not most possibly generate target capabilities value.
Embodiment 2
The basic content of the present embodiment with embodiment 1, as shown in figure 3, the difference is that: in catalyst filter cylinder 100 by
It is disposed with molecular sieve layer 110 and V-Ce-Ti catalyst layer 130 under, is additionally provided with denitration in catalyst filter cylinder 100 and urges
Agent layer 120, the denitration catalyst oxidant layer 120 are set between molecular sieve layer 110 and V-Ce-Ti catalyst layer 130.
It is worth noting that as shown in figure 5, be provided with angle γ between filter plate 210 and vertical direction, the value of angle γ
Range is 10~15 °, in the present embodiment, and the value of angle γ is 15 °, and the sintering flue gas of the utility model is by admission line
It when 200 entrance subsidiary conduit 400, is filtered by filter plate 210, angle γ is provided between filter plate 210 and vertical direction, pressed from both sides
The value range of angle γ is 10~15 °, in the present embodiment, and the value of angle γ is 15 °, when sintering flue gas by filter plate 210 to
When subsidiary conduit 400 moves, the air inlet of subsidiary conduit 400 is connected with the gas outlet of admission line 200, when containing in sintering flue gas
When having particulate matter, the partial size of particulate matter is greater than the diameter of filter plate 210, so that particulate matter cannot be under the blocking of filter plate 210
Enter in subsidiary conduit 400, while filter plate 210 is inclined at the top of admission line 200, particulate matter is not easy to be attached to filter plate
210 surface and cause filter plate 210 be blocked, to hinder sintering flue gas to enter in subsidiary conduit 400, and particulate matter is at itself
Under the action of gravity and towards movement at the air inlet of admission line 200, promotes sintering flue gas and particulate separation, can be improved
The catalytic effect of sintering flue gas.
After sintering flue gas enters catalyst filter cylinder 100, molecular sieve layer 110 is first passed through.Filled with 5A points in molecular sieve layer 110
Sub- sieve catalyst, the 5A molecular sieve are a kind of calcium A type alumino-silicates, can adsorb cut off diameter in sintering flue gas and be not more than 5A's
Substance is mainly used for adsorbing the H in flue gas2O and SO2, and the partial size of 5A molecular sieve catalyst is 1cm, the layer of molecular sieve layer 110
A height of 1m.
Further, sintering flue gas enters denitration catalyst oxidant layer 120, is filled with Co-Mn-Ce in denitration catalyst oxidant layer 120
Catalyst, can remove the part NOx in sintering flue gas, and the partial size of the Co-Mn-Ce catalyst is 4~5mm, a height of 1.5m of layer,
The partial size of Co-Mn-Ce catalyst is less than the partial size of 5A molecular sieve catalyst, and 5A molecular sieve catalyst can be prevented to be mixed into Co-Mn-Ce
In catalyst.Specific preparation process is as follows for Co-Mn-Ce catalyst:
S100, the CoCl for taking 4g2·6H2O, the MnCl of 12g2·4H2O, the Ce (NO of 1g3)3·6H2O, 1480g deionization
Water, and it is mixed to get catalyst activity component A；
S200, the oxalic acid for taking 23g and 550g water, and it is mixed to prepare oxalic acid aqueous solution B；
When S300,20 DEG C, catalyst activity component A is stirred, the revolving speed for controlling magneton is 200r/min, when stirring
Between 30min；
When S400,20 DEG C, oxalic acid aqueous solution B is stirred, the revolving speed for controlling magneton is 200r/min, mixing time
30min；
S500, under conditions of being evenly heated stirring, oxalic acid solution B is added dropwise in catalyst activity component A, it is heavy to be made
Shallow lake solution C；
S600, precipitation solution C obtained is stirred into cooling, and precipitation solution C is washed using deionized water, is taken out
Filter, process in triplicate, then with ethanol solution are washed precipitation solution C, are filtered, the step in triplicate, by institute
The precipitation solution C obtained is dried for 24 hours at 70 DEG C, and oxidizing roasting under the conditions of keeping the temperature 3 hours after being warming up to 400 DEG C obtains after cooling
Catalyst fines are ground into 60 mesh.
S700, catalyst fines obtained are uniformly mixed with certain binder, are 5mm's in being rolled into diameter on pellet processing machine
Spherical catalyst, then formed after 100 DEG C of dryings of low temperature.
Using a kind of device of layering emission reduction sintering flue gas pollutant of the present embodiment, 200 air inlet of admission line is detected
The NO at placeXConcentration 328mg/m-3, dioxin concentration is 0.91ng/m-3, then detect 100 bottom gas outlet of catalyst filter cylinder
The NO at placeXConcentration 53mg/m-3, dioxin concentration is 0.27ng/m-3；NOXEmission reduction efficiency reach 80.79%；Dioxin
Emission reduction efficiency reach 70.33%；To realize NOXWith the joint emission reduction of dioxin.
The utility model is described in detail above in conjunction with specific exemplary embodiment.It is understood, however, that can be
It is carry out various modifications in the case where not departing from the scope of the utility model being defined by the following claims and modification.It is detailed to retouch
State should be to be considered only as with attached drawing it is illustrative and not restrictive, if there is any such modifications and variations, then
They fall in the scope of the utility model described herein.In addition, background technique is intended to grinding in order to illustrate this technology
It was found that shape and meaning, it is no intended to limit the application field of the utility model or the application and the utility model.
Claims (10)
1. a kind of device for being layered emission reduction sintering flue gas pollutant, it is characterised in that:
Admission line (200), the bottom of the admission line (200) are provided with air inlet, and admission line is provided at the top of (200)
Port is provided with filter plate (210) on the gas outlet；
The air inlet of subsidiary conduit (400), the subsidiary conduit (400) is connected with the gas outlet of admission line (200)；
Catalyst filter cylinder (100), the catalyst filter cylinder (100) are set to the bottom of subsidiary conduit (400), catalyst filter cylinder
(100) molecular sieve layer (110) and V-Ce-Ti catalyst layer (130) are from top to bottom disposed in.
2. a kind of device for being layered emission reduction sintering flue gas pollutant according to claim 1, it is characterised in that: catalyst filter
Denitration catalyst oxidant layer (120) are additionally provided in cylinder (100), which is set to molecular sieve layer (110) and V-
Between Ce-Ti catalyst layer (130).
3. a kind of device for being layered emission reduction sintering flue gas pollutant according to claim 1, it is characterised in that: admission line
(200) top droop is provided with deflector (220).
4. a kind of device for being layered emission reduction sintering flue gas pollutant according to claim 1, it is characterised in that: catalyst filter
The outside of cylinder (100) is provided with vibrator (300).
5. a kind of device for being layered emission reduction sintering flue gas pollutant according to claim 1, it is characterised in that: catalyst filter
Strainer (140) are provided at the top of cylinder (100).
6. a kind of device for being layered emission reduction sintering flue gas pollutant according to claim 1, it is characterised in that: V-Ce-Ti
V is filled in catalyst layer (130)aCebTicOxCatalyst, and VaCebTicOxThe partial size of catalyst is 2~3mm, wherein V and Ce
Oxide mass ratio be 0.5~1, Ce and Ti oxide mass ratio be 0.05~0.16.
7. a kind of device for being layered emission reduction sintering flue gas pollutant according to claim 1, it is characterised in that: filter plate
(210) angle between deflector (220) is α, and the value of α is 30~75 °.
8. a kind of device for being layered emission reduction sintering flue gas pollutant according to claim 2, it is characterised in that: denitration catalyst
Co-Mn-Ce catalyst is filled in oxidant layer (120), the partial size of the Co-Mn-Ce catalyst is 4~5mm.
9. a kind of device for being layered emission reduction sintering flue gas pollutant according to claim 3, it is characterised in that: deflector
(220) upper end (221) is connected with the top of filter plate (210)；The lower end (222) of deflector (220) and admission line
(200) side wall is connected, and the lower end (222) of deflector (220) is lower than the bottom of filter plate (210).
10. a kind of described in any item devices for being layered emission reduction sintering flue gas pollutant, feature exist according to claim 1~9
In: subsidiary conduit (400) lower part is provided with collapsible tube (410), and subsidiary conduit (400) is filtered by collapsible tube (410) and catalyst
The top of cylinder (100) is connected.
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| CN201821745479.1U CN209033989U (en) | 2018-10-26 | 2018-10-26 | A kind of device being layered emission reduction sintering flue gas pollutant |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109157926A (en) * | 2018-10-26 | 2019-01-08 | 安徽工业大学 | A kind of device of layering removing sintering flue gas pollutant |
| CN113060510A (en) * | 2021-03-18 | 2021-07-02 | 龙岩市东元矿粉有限公司 | Environment-friendly energy-saving fly ash production device and manufacturing method thereof |
| CN109157926B (en) * | 2018-10-26 | 2024-07-12 | 安徽工业大学 | Device for layered removal of sintering flue gas pollutants |
-
2018
- 2018-10-26 CN CN201821745479.1U patent/CN209033989U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109157926A (en) * | 2018-10-26 | 2019-01-08 | 安徽工业大学 | A kind of device of layering removing sintering flue gas pollutant |
| CN109157926B (en) * | 2018-10-26 | 2024-07-12 | 安徽工业大学 | Device for layered removal of sintering flue gas pollutants |
| CN113060510A (en) * | 2021-03-18 | 2021-07-02 | 龙岩市东元矿粉有限公司 | Environment-friendly energy-saving fly ash production device and manufacturing method thereof |
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