CN208839349U - A kind of dry cleaning device being able to achieve flue gas minimum discharge - Google Patents

A kind of dry cleaning device being able to achieve flue gas minimum discharge Download PDF

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CN208839349U
CN208839349U CN201821146949.2U CN201821146949U CN208839349U CN 208839349 U CN208839349 U CN 208839349U CN 201821146949 U CN201821146949 U CN 201821146949U CN 208839349 U CN208839349 U CN 208839349U
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layer
reaction tower
flue gas
main reaction
main
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李鹏飞
朱晓华
李昆
王雨清
王博如
李洪全
陈媛
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Zhong Ye Energy-Conserving And Environment-Protective LLC
Central Research Institute of Building and Construction Co Ltd MCC Group
China Jingye Engineering Corp Ltd
MCC Energy Saving and Environmental Protection Co Ltd
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Zhong Ye Energy-Conserving And Environment-Protective LLC
Central Research Institute of Building and Construction Co Ltd MCC Group
China Jingye Engineering Corp Ltd
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    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02ATECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters

Abstract

The utility model relates to a kind of dry cleaning device for being able to achieve flue gas minimum discharge, described device includes preposition catalytic unit (2), main reaction tower, pulsed bag filter (16), technique water tank, main absorbent powder feed system and additive powder feed system;Flue gas after preliminary dust removal successively passes through preposition oxidation unit, main reaction tower and pulse bag type dust collector;The part in the preposition catalytic unit NOx is catalytically converted into NO2;Absorbent sulfur dioxide absorption, nitrogen oxides and other sour gas in main reaction tower, while absorbent also has preferable control action to heavy metal etc..NO partial oxidation in flue gas is generated into NO2, and and SO2Enter main reaction tower together, in conjunction with the adjustment of main reaction tower arrangement form and reaction temperature, so that main reaction tower is to SO2、NOxRemoval effect greatly enhance, while absorbent may be implemented to the removing of volatilization/half volatile heavy metal.

Description

A kind of dry cleaning device being able to achieve flue gas minimum discharge
Technical field
The utility model relates to a kind of dry cleaning devices for being able to achieve flue gas minimum discharge, and in particular to one kind is able to achieve SO 2 from fume, nitrogen oxides, heavy metal and the dry cleaning device of dust minimum discharge, belong to environmental engineering technology The Pollutant Control Technology in field, for removing the multiple pollutant in flue gas simultaneously in a set of technique.
Background technique
China is the country using coal as main energy sources, and coal burning will form multiple pollutant, such as dust, heavy metal, Nitrogen oxides, oxysulfide etc..The discharge of control pollutant is the important content of clean coal utilization.Large-scale coal fired power plant one As use electrostatic precipitation, desulfurization by lime gypsum method, ammonia-SCR method denitration.But desulfurization by lime gypsum method, ammonia-SCR method skill When art is used in scale relatively small unit, there are a series of problems, and such as desulfurization by lime gypsum method complex process, cost is high; Ammonia-SCR method the problems such as there is ammonia area security risk is big, and operating cost is high.
Small-load generators are to the characteristics of pollutant catabolic gene: it is more sensitive to cost, it is more sensitive to operating cost, it is desirable that technology It is simple as far as possible, it is relatively low to efficiency requirements.The pollution control technology level of small-load generators is far below large sized unit, compels to be essential Want reliable for operation, cost and operating cost are low, the Pollutant Control Technology of simple process.
Existing power station unit Pollutant Control Technology only removes a kind of pollutant, multiple reactor strings in one reactor Connection removing multiple pollutant, such as SCR+FGD+ESP.This mode is high to the removal efficiency of Single Pollution, but invests big, operation It is costly, it is not suitable for the transformation of existing device;The joint removing for how realizing multiple pollutant, becomes pollutant catabolic gene gradually Hot technology.Occurred now it is a variety of in a reactor while removing the technologies of various pollutants, although equipment is simple, Investment is low with operating cost, but because various pollutants have the characteristics that different removings, reaches height simultaneously in a reactor Effect removing, is technically difficult to realize.
Utility model content
The utility model patent is designed to provide a kind of dry cleaning device for being able to achieve flue gas minimum discharge, preferably SO 2 from fume, nitrogen oxides, heavy metal and the dry cleaning device of dust minimum discharge are able to achieve to be a kind of;On solving State technical problem.
The dry cleaning device include preposition catalytic unit, main reaction tower, pulsed bag filter, technique water tank, Main absorbent powder feed system and additive powder feed system;Technique water tank connects main reaction tower, main for feeding the water into main reaction tower Absorbent powder feed system, additive powder feed system are separately connected main reaction tower, main anti-for main absorbent and additive to be sent into Tower is answered, catalyst is filled in preposition catalytic unit, preposition catalytic unit connects main reaction tower bottom end, for that will pass through preposition urge Makeup sets that treated, and flue gas is sent into main reaction tower is handled, and main reaction tower upper end connects pulsed bag filter, is used for It will be sent into pulsed bag filter by main reaction tower treated flue gas, pulsed bag filter is provided with cleaning flue gases Outlet is discharged through bag filter treated cleaning flue gases by cleaning flue gases outlet.
Wherein, the dry cleaning device further includes product circulation slot and product warehouse;Product circulation slot is preferably returning charge Device and the lower end that pulsed bag filter is arranged in, flue gas pass through the solids that pulsed bag filter is separated Material enters in product circulation slot, and fraction solids material directly returns to main reaction tower through feed back pipeline, participates in main reaction tower again Chemical reaction process, fraction solids material are discharged to product warehouse from weary material outlet, to maintain the solid material of whole device Balance.
Wherein, the preposition catalytic unit has catalytic unit inlet flue duct, preposition catalytic unit shell and catalytic unit Exhaust pass, preposition catalytic unit shell one end connect the inlet flue duct, and the other end connects the exhaust pass, preposition catalysis Catalyst is filled in crust of the device.
Wherein, catalyst is loaded in preposition catalytic unit, the catalyst is preferably honeycomb fashion, by the part NO in flue gas It is oxidized to NO2, one of catalyst activity component Fe, V, Mn oxide or a variety of, carrier is titanium dioxide, active oxidation One of aluminium, 4A molecular sieve are a variety of.Catalyst can also be quaterfoil or plate configuration.
Wherein, catalyst includes titanium dioxide, FeO, V2O5And MnO2;It is preferred that catalyst is using titanium dioxide as carrier, matter Amount content be 70-90%, preferably 80%;It is preferred that with FeO, V2O5、MnO2For active constituent;Wherein the mass content of FeO is 3- 6%, preferably 5%;V2O5Mass content is 0.5-2%, preferably 1%;MnO2Mass content 12-18%, preferably 14%.
Wherein, catalyst configuration is cellular catalyst, Catalyst packing certain volume, so that catalysis reaction velocity is 3000-6000h-1, flue gas flow rate 3-6m/s;It is preferred that so that in preposition catalytic unit, 40-65% volume fraction in flue gas NO is oxidized to NO2
Wherein, in preposition catalytic unit by NO partial oxidation at NO2;NOx, SO are completed in main reaction tower2, heavy metal etc. It removes simultaneously;Volatilization/half volatile heavy metal is absorbed in main reaction tower, pulse bag type dust collector supplies circulation takes off simultaneously The dust in flue gas is removed, the filter cake on sack cleaner also has removing NOx and SO2Effect.
Wherein, main reaction column structure is fluidized-bed reactor, and with orifice plate air-distribution device, cloth wind form uses orifice plate cloth Wind arranges that orifice plate air-distribution device is the following are main reaction tower entrance, and the above are conversion zones for orifice plate air-distribution device, i.e., using double sections Main reaction tower upper section.It is preferred that the ratio of height to diameter of conversion zone is controlled in 3-7, conversion zone superficial gas flow control is in 2-5m/s.It is preferred that Main reaction tower inlet temperature is 90-160 DEG C, and Matter Transfer multiplying power is 20~200, and exit gas temperature is higher than exhanst gas outlet dew point 15~35 DEG C of temperature.
Wherein, first layer technique water spray gun to be opened/closed is installed more than main reaction tower conversion zone orifice plate air-distribution device, Second layer technique water spray gun to be opened/closed is set above first layer technique water spray gun, and technique water tank can be separately connected the first layer process Water spray gun and second layer technique water spray gun to be opened/closed.It is preferred that only as SO in inlet flue gas2Content is higher than 1500mg/cm3When, Or amount of water sprayed demand be greater than 10t/h when, just use second layer technique water spray gun to be opened/closed, it is same with first layer technique water spray gun When spray water.
Wherein, first layer technique water spray gun to be opened/closed is arranged in main reaction tower conversion zone orifice plate air-distribution device or more, excellent Only, preferably 1-2 first layer technique water spray gun to be opened/closed, spray gun type are two-fluid spray to choosing arrangement 1-5 again Rifle;Second layer technique water spray gun to be opened/closed is arranged in the altitude range of conversion zone, and is arrived apart from orifice plate air-distribution device 1/2 In 2/3 height, only, preferably 1-2 second layer technique water spray gun to be opened/closed, spray gun type are excellent again by preferably arrangement 1-5 It is selected as double-current spray gun body.
Wherein, the main absorbent entrance of first layer, the main absorbent entrance of the second layer, first layer additive are set on reaction tower The setting position of entrance and second layer additive entrance, the main absorbent entrance of first layer and first layer additive entrance is located at first Layer technique water spray gun to be opened/closed top 0.5-2m, the setting position of the second layer main absorbent entrance and second layer additive entrance Positioned at second layer technique water spray gun to be opened/closed top 0.5-2m, main absorbent powder feed system is separately connected the main absorbent of first layer Entrance and the main absorbent entrance of the second layer;Additive powder feed system is separately connected first layer additive entrance and second layer additive Entrance.It is preferred that the main absorbent of first layer is identical with the height of additive entrance, the straying quatity of each main absorbent entrance is 100-3000kg/h, it is 100-1500kg/h that each additive, which sprays into point straying quatity,.It is preferred that working as NOxContent is more than 500mg/m3, Perhaps when main absorbent straying quatity demand is greater than 3000kg/h or additive straying quatity demand and is greater than 1500kg/h, the is enabled Two layers of main absorbent entrance and second layer additive entrance, simultaneously with the main absorbent entrance of first layer and first layer additive entrance Work, the main absorbent of the second layer is identical with the height of additive entrance, and it is 100- that each main absorbent, which sprays into point straying quatity, 3000kg/h, it is 100-1500kg/h that each additive, which receives agent and sprays into point straying quatity,.In such a way that two layers sprays into, it is able to achieve object Material is evenly distributed, and realizes and reacts in the layering of main reaction tower upper section, improves removal efficiency.
Wherein, main absorbent is calcium hydroxide, the Ca (OH) in calcium hydroxide2Mass content is greater than 80%, and additive includes sulphur One or more of iron ash, carbide slag, red mud, white clay, slime, silicon manganese slag, the effective component in additive are wherein institute The basic anhydride and alkaline hydrated oxide contained.It is preferred that the mass ratio of main absorbent and additive, it is desirable that are as follows:
Wherein, Ca (OH) in main absorbent2Molar ratio control with pollutant is in 1-4, the i.e. niter of unit time penetrating Ca (OH) in ash2Molar content mca, SO in the unit time in flue gas in total2Molar content is ms, the molar content of NO is mN, It should ensure that mca: (ms+0.5*mN)=1-4 guarantees SO2With the efficient removal of NOx, " * " is the meaning multiplied, and "+" is the meaning added.
Wherein, the partial size D of main absorbent and additive90< 10 μm, tower is interior to be presented fast bed state, main absorbent and addition Agent present it is dilute under close distribution, the pressure difference imported and exported in tower control main absorbent in 0.5-3kPa, fluidized bed and Additive has very strong absorption to heavy metals such as mercury, arsenic, selenium, to achieve the purpose that remove heavy metal;D90It is screening Middle particular expression mode is exactly when being sieved with the sieve of special pore size distribution, and special pore size distribution is 10 μm herein, can pass through 90% or more The particle of mass fraction.
Wherein, the utility model also provides one kind to be able to achieve SO 2 from fume, nitrogen oxides, heavy metal and dust ultralow The dry purification process of discharge, it is preferable that purification process is using a kind of above-mentioned dry cleaning dress for being able to achieve flue gas minimum discharge Set the purification process purified;It includes the following steps:
Step (1), flue gas initially enter preposition catalytic unit and are handled, and pass through the catalysis loaded in preposition catalytic unit Nitric oxide (NO) in flue gas is catalytically conveted to nitrogen dioxide (NO by agent2);
Step (2), the nitrogen dioxide NO generated2Entering main reaction tower with flue gas, technique water tank feeds the water into main reaction tower, Main absorbent and additive are sent into main reaction tower respectively by main absorbent powder feed system, additive powder feed system, in absorbent, are added Under the action of adding agent and moisture, nitrogen oxides in effluent and sulfur dioxide (SO are realized2) absorption, while to the huge sum of money in flue gas Category is removed;
Step (3) is sent into pulsed bag filter, pulsed bag filter by main reaction tower treated flue gas It is provided with cleaning flue gases outlet, is discharged through bag filter treated cleaning flue gases by cleaning flue gases outlet, thus Realize flue gas minimum discharge.
The principles of the present invention are NOxPart is catalytically converted into NO in preposition catalytic unit2;In main reaction tower Absorbent sulfur dioxide absorption, nitrogen oxides and other sour gas, while absorbent also has preferable control to heavy metal etc. Production is used.Flow regime is fast fluidized bed in main reaction tower, and Matter Transfer multiplying power is 20-200 times in main reaction tower, absorbent It is made of main absorbent and additive, is divided into 1-2 layers of penetrating, process water spray is installed at 0.5-1.5m below absorbent entrance Mouthful.Flue gas removes the dust in flue gas by pulsed sack cleaner after main reaction tower.It crosses the part NO in flue gas Oxidation generates NO2, and and SO2Enter main reaction tower together makes in conjunction with the adjustment of main reaction tower arrangement form and reaction temperature Winner's reaction tower is to SO2、NOxRemoval effect greatly enhance, while absorbent may be implemented to a volatilization/half volatile huge sum of money The removing of category.To realize that single process circuit removes multiple pollutant.
The utility model provides that a kind of techniqueflow is simple, and low cost, good reliability especially can be in 75-140 DEG C of temperature In section, while realizing sulfur dioxide, nitrogen oxides, dust, the dry purification process of heavy metal removing.
Nitric oxide (NO) is catalytically conveted to nitrogen dioxide by increasing preposition catalytic unit by this patent purification process (NO2), the NO of generation2Enter main reaction tower with flue gas, into after main reaction tower, realizes nitrogen oxides and sulfur dioxide (SO2) It absorbs, while also thering is preferable removing to act on to heavy metal, dust emission is controlled by pulse bag type dust collector, to realize a variety of The purpose of pollutant simultaneous removing.
The utility model has the beneficial effects that purification process provided by the utility model, by the way that NO is oxidized to NO2, and SO2Under promotion, it can greatly promote main reaction tower to NOx removal effect;Highdensity recycle stock and lower simultaneously Under conditions of water spray, the removing of volatilization/half volatile heavy metal is may be implemented in main reaction tower, for related unit installation and change It makes existing flue gas purification device and provides inexpensive, performance efficiency, stable removing process.This technique can for power plant and Environmental protection company provides the technology arrangement scheme and operation of accurate sulfur dioxide, nitrogen oxides, heavy metal, dust while control Parameter improves the technical level of domestic pollution Collaborative Control, and device is simple, reliable for operation, reduce pollutant catabolic gene at This.
Detailed description of the invention
Fig. 1 is sulfur dioxide, nitrogen oxides, heavy metal and dust minimum discharge dry cleaning device technique flow chart;
Fig. 2 is the layout drawing of dry cleaning device;
Fig. 3 is the preposition oxidation unit cross-sectional view of dry purification process;
Fig. 4 is NO and SO2Subtractive process figure
Marked in the figure: 1- inlet flue gas, the preposition catalytic unit of 2-, vertical gas pass before 3- entrance, 4- main reaction tower entrance, 5- orifice plate air-distribution device, 6- first layer technique water spray gun, the main absorbent entrance of 7- first layer, 8- first layer additive entrance, 9- Main reaction tower upper section, 10- second layer technique water spray gun, 11- second layer calcium hydroxide entrance, 12- second layer additive entrance, The weary material mouth of 13- discharge, the weary material outlet of 14-, 15- material-returning device, 16- pulsed bag filter, the discharge of 17- cleaning flue gases Mouthful.The preposition oxidation unit inlet flue duct of 18-, the preposition catalytic unit shell of 19-, the preposition catalytic unit apparatus with catalyst inside of 20-, 21- Preposition oxidation unit exhaust pass.
Specific embodiment
As shown in Figure 1, 2, a kind of dry cleaning device being able to achieve flue gas minimum discharge, preferably one kind are able to achieve flue gas Sulfur dioxide, nitrogen oxides, heavy metal and the dry cleaning device of dust minimum discharge comprising preposition catalytic unit 2, master are anti- Answer tower, pulsed bag filter 16, technique water tank, main absorbent powder feed system and additive powder feed system;Technique water tank connects Main reaction tower is connect, for feeding the water into main reaction tower, main absorbent powder feed system, additive powder feed system are separately connected main reaction Tower is filled with catalyst 20, preposition catalysis in preposition catalytic unit 2 for main absorbent and additive to be sent into main reaction tower Device 2 connects main reaction tower bottom end, and treated for will pass through preposition catalytic unit 2, and flue gas is sent at main reaction tower Reason, main reaction tower upper end connect pulsed bag filter 16, for that will be sent into pulse by main reaction tower treated flue gas Formula bag filter 16, pulsed bag filter 16 are provided with cleaning flue gases outlet 17, after the processing of bag filter 16 Cleaning flue gases pass through cleaning flue gases outlet 17 be discharged.The dry cleaning device further includes product circulation slot and product storage Storehouse;Product circulation slot is preferably material-returning device 15 and the lower end that pulsed bag filter 16 is arranged in, and flue gas passes through pulsed The solid material that bag filter 16 is separated enters in product circulation slot, and fraction solids material is directly returned through feed back pipeline Main reaction tower is returned, participates in chemical reaction process in main reaction tower again, fraction solids material is discharged to production from weary material outlet 14 Object warehouse, to maintain the solid material of whole device to balance.
As shown in figure 3, the preposition catalytic unit 2 has catalytic unit inlet flue duct 18, preposition catalytic unit shell 19 With catalytic unit exhaust pass 21, preposition 19 one end of catalytic unit shell connects the inlet flue duct 18, described in other end connection Exhaust pass 21 is filled with catalyst 20 in preposition catalytic unit shell 19.Catalyst is loaded in preposition catalytic unit 2, it is described Catalyst is preferably honeycomb fashion, is NO by the NO partial oxidation in flue gas2, in catalyst activity component Fe, V, Mn oxide It is one or more, carrier be one of titanium dioxide, activated alumina, 4A molecular sieve or a variety of.It is preferred that catalyst 20 wraps Include titanium dioxide, FeO, V2O5And MnO2;It is preferred that catalyst is using titanium dioxide as carrier, mass content 70-90%, preferably 80%;It is preferred that with FeO, V2O5、MnO2For active constituent;Wherein the mass content of FeO be 3-6%, preferably 5%;V2O5Quality Content is 0.5-2%, preferably 1%;MnO2Mass content 12-18%, preferably 14%.Wherein, catalyst configuration is honeycomb The catalyst of formula, Catalyst packing certain volume, so that catalysis reaction velocity is 3000-6000h-1, flue gas flow rate 3-6m/s; It is preferred that so that the NO of 40-65% volume fraction is oxidized to NO in flue gas in preposition catalytic unit 22
As shown in Figure 1, 2, in preposition catalytic unit 2 by NO partial oxidation at NO2;NOx, SO are completed in main reaction tower2、 It is removed whiles heavy metal etc.;Volatilization/half volatile heavy metal is absorbed in main reaction tower, pulse bag type dust collector supplies follow Ring, while removing the dust in flue gas, the filter cake on sack cleaner also has removing NOx and SO2Effect.Main reaction tower structure It makes as fluidized-bed reactor, with orifice plate air-distribution device 5, cloth wind form uses orifice plate cloth wind, is arranged using double sections, orifice plate cloth Wind apparatus 5 is the following are main reaction tower entrance 4, and the above are conversion zones, i.e. main reaction tower upper section 9 for orifice plate air-distribution device 5.It is preferred that The ratio of height to diameter of conversion zone is controlled in 3-7, and conversion zone superficial gas flow control is in 2-5m/s.It is preferred that main reaction tower inlet temperature is 90-160 DEG C, Matter Transfer multiplying power is 20~200, and exit gas temperature is higher than 15~35 DEG C of exhanst gas outlet dew-point temperature.In master 5 or more reaction tower conversion zone orifice plate air-distribution device installs first layer technique water spray gun 6 to be opened/closed, in first layer technique water spray gun Second layer technique water spray gun 10 to be opened/closed is arranged in 6 tops, and technique water tank can be separately connected first layer technique water spray gun 6 and second Layer technique water spray gun 10 to be opened/closed.It is preferred that only as SO in inlet flue gas2Content is higher than 1500mg/cm3When or amount of water sprayed When demand is greater than 10t/h, second layer technique water spray gun 10 to be opened/closed is just used, is sprayed water simultaneously with first layer technique water spray gun 6. First layer technique water spray gun to be opened/closed is arranged in 5 or more main reaction tower conversion zone orifice plate air-distribution device, preferably arrangement 1-5, It is preferably again 1-2 first layer technique water spray gun to be opened/closed, spray gun type is double-current spray gun body;The second layer can be opened The technique water spray gun closed is arranged in the altitude range of conversion zone, and in the height apart from orifice plate air-distribution device 51/2 to 2/3, It is preferred that arrangement 1-5 is only, preferably 1-2 second layer technique water spray gun to be opened/closed, spray gun type are two-fluid again Spray gun.
Shown in Fig. 2, the main absorbent entrance 7 of first layer, the main absorbent entrance 11 of the second layer, first layer are set on reaction tower Additive entrance 8 and second layer additive entrance 12, the setting of first layer main absorbent entrance 7 and first layer additive entrance 8 Position is located at first layer 6 top 0.5-2m of technique water spray gun to be opened/closed, the main absorbent entrance 11 of the second layer and second layer addition The setting position of agent entrance 12 is located at the second layer 10 top 0.5-2m of technique water spray gun to be opened/closed, main absorbent powder feed system point It Lian Jie not the main absorbent entrance 7 of first layer and the main absorbent entrance 11 of the second layer;Additive powder feed system is separately connected first layer Additive entrance 8 and second layer additive entrance 12.It is preferred that the main absorbent of first layer is identical with the height of additive entrance, The straying quatity of each main absorbent entrance is 100-3000kg/h, and it is 100-1500kg/h that each additive, which sprays into point straying quatity,. It is preferred that working as NOxContent is more than 500mg/m3Perhaps main absorbent straying quatity demand is greater than 3000kg/h or additive straying quatity When demand is greater than 1500kg/h, the main absorbent entrance 11 of the second layer and second layer additive entrance 12 are enabled, with the main suction of first layer It receives agent entrance 7 and first layer additive entrance 8 works at the same time, the main absorbent of the second layer is identical with the height of additive entrance, It is 100-3000kg/h that each main absorbent, which sprays into point straying quatity, and it is 100- that each additive, which receives agent and sprays into point straying quatity, 1500kg/h.It in such a way that two layers sprays into, is able to achieve material and is evenly distributed, realize and reacted in the layering of main reaction tower upper section, Improve removal efficiency.Main absorbent is calcium hydroxide, the Ca (OH) in calcium hydroxide2Mass content is greater than 80%, and additive includes sulphur iron One or more of ash, carbide slag, red mud, white clay, slime, silicon manganese slag, the effective component in additive are contained therein Some basic anhydride and alkaline hydrated oxide.It is preferred that the mass ratio of main absorbent and additive, it is desirable that are as follows:
Wherein, Ca (OH) in main absorbent2Molar ratio control with pollutant is in 1-4, the i.e. niter of unit time penetrating Ca (OH) in ash2Molar content mca, SO in the unit time in flue gas in total2Molar content is ms, the molar content of NO is mN, It should ensure that mca: (ms+0.5*mN)=1-4 guarantees SO2With the efficient removal of NOx, * is the meaning multiplied ,+it is the meaning added.Main suction Receive the partial size D of agent and additive90< 10 μm, be presented fast bed state in tower, main absorbent and additive present it is dilute under close point Cloth state, main absorbent and additive of the interior pressure difference control imported and exported of tower in 0.5-3kPa, fluidized bed are to mercury, arsenic, selenium etc. Heavy metal has very strong absorption, to achieve the purpose that remove heavy metal;D90It is particular expression mode in screening, is exactly When being sieved with the sieve of special pore size distribution, special pore size distribution is 10 μm herein, can pass through the particle of 90% or more mass fraction.
As shown in Figs. 1-2, a kind of dry purification process being able to achieve flue gas minimum discharge, preferably one kind are able to achieve flue gas Sulfur dioxide, nitrogen oxides, heavy metal and the dry purification process of dust minimum discharge, it is preferable that purification process is using Fig. 1-2 Shown in a kind of purification process that the dry cleaning device for being able to achieve flue gas minimum discharge is purified;It is characterized in that, it is wrapped Include following steps:
(1) flue gas initially enters preposition catalytic unit 2 and is handled, and passes through the catalyst loaded in preposition catalytic unit 2 Nitric oxide (NO) in flue gas is catalytically conveted to nitrogen dioxide (NO by 202);
(2) the nitrogen dioxide NO generated2Enter main reaction tower with flue gas, technique water tank feeds the water into main reaction tower, main suction It receives agent powder feed system, additive powder feed system and main absorbent and additive is sent into main reaction tower respectively, in absorbent, additive Under the action of moisture, nitrogen oxides in effluent and sulfur dioxide (SO are realized2) absorption, while to the heavy metal in flue gas into Row removing;
(3) pulsed bag filter 16, pulsed bag filter 16 are sent by main reaction tower treated flue gas It is provided with cleaning flue gases outlet 17, passes through 17 row of cleaning flue gases outlet through treated the cleaning flue gases of bag filter 16 Out, to realize flue gas minimum discharge.
The further explanation of the utility model are as follows:
1) preposition catalytic unit 2 (attached drawing 3), is equipped with catalyst 20, and after flue gas flows through, the part nitrogen oxides NO is by quilt It is oxidized to NO2, for catalyst using Mn system or Fe series catalysts, catalyst mode is honeycomb fashion, the nitrogen oxides part after oxidation Meeting and SO2In conjunction with generation sulfur-nitrogen compound is gone successively in subsequent reactions tower.
2) the preposition outlet of catalytic unit 2 is needed through water spray control flue-gas temperature, it is desirable that enters flue-gas temperature before reaction tower Control is at 95~135 DEG C of reasonable temperature range.Amount of water sprayed is calculated according to flue gas cool-down amplitude.
3) absorbent is made of main absorbent and additive, and main absorbent is calcium hydroxide, the Ca (OH) in calcium hydroxide2Quality Content is greater than 80%, and additive includes one or more of sulphur iron ash, carbide slag, red mud, white clay, slime, silicon manganese slag, is added Adding the effective component in agent is basic anhydride contained therein and alkaline hydrated oxide.From the angle for realizing best removal effect It spends and says, the mass ratio of main absorbent and additive, it is desirable that:
4) in the main absorbent of the requires of the utility model effective component and the control of the molar ratio of pollutant 1~4, i.e., unit when Between Ca (OH) in the calcium hydroxide that sprays into2Molar content mca, the SO2 molar content in the unit time in flue gas in total is ms, NO's Molar content is mN, should ensure that mca: (ms+0.5*mN)=1~4 guarantees SO2With the efficient removal of NOx.
5) the requires of the utility model main reaction tower is fluidized-bed reactor, and cloth wind form uses orifice plate cloth wind, using double sections Arrangement, orifice plate is the following are inducer, and orifice plate is the above are conversion zone, and the ratio of height to diameter control of conversion zone is 3~7, the apparent gas of conversion zone Body flow control is in 1~4m/s.Enter the partial size D of tower material90< 10 μm, be presented fast bed state in tower, material present it is upper it is dilute under it is close Distribution, the pressure difference imported and exported in tower controls in 1~3kPa.Main absorbent and additive in fluidized bed is to mercury, arsenic, selenium Equal heavy metals have very strong absorption, to achieve the purpose that remove heavy metal.
6) 1~3m installs 1~2 technique water spray gun of first layer, spray gun type more than main reaction tower conversion zone air distribution plate For double-current spray gun body.It, can also be in the reaction apart from air distribution plate 1/2 to 2/3 other than using second layer spray gun to be opened/closed Second segment spray gun mounting hole is reserved in the position of Duan Gaodu, with flangeseal, as SO in inlet flue gas2Content is higher than 1500mg/ cm3When or amount of water sprayed be greater than 10t/h when, using two layers of spray gun, also arrange 1~2 spray gun in the second layer.Every spray gun Amount of water sprayed is identical, and amount of water sprayed range is 1~5t/h, the straying quatity of process water, according to desired SO2It adjusts, takes off with NOx removal rate Except rate requires higher amount of water sprayed bigger, using two layers of spout, the water layer sprayed into can be made more uniform, and realize that layering is anti- It answers, to improve removal efficiency.After the penetrating of water, it need to guarantee that main reaction tower outlet temperature is higher than exhanst gas outlet dew-point temperature 15~35 ℃。
7) composite absorber is divided into 1~2 layer of penetrating, and first layer sprays into point and is set to first layer technique water spray gun top 0.5 The position~2m, the second layer spray into point in the second layer technique water spray gun top position 0.5~2m.The main absorbent of same layer and addition The height that agent sprays into point is identical, and it is 100~3000kg/h that each main absorbent, which sprays into point straying quatity, and each additive is received agent and sprayed into Point straying quatity is 100~1500kg/h, when NOx content is more than 500mg/m3Or main absorbent straying quatity is greater than 3000kg/h, Or additive straying quatity enables the second layer and sprays into point, each main absorbent of the second layer sprays into point and sprays into when being greater than 1500kg/h Amount is 100~3000kg/h, and it is 100~1500kg/h that each additive, which receives agent and sprays into point straying quatity,.The side sprayed into using two layers Formula is able to achieve material and is evenly distributed, and realizes and reacts in the layering of main reaction tower upper section, improves removal efficiency.
8) into after crossing main reaction tower, the solid materials such as flue gas and the absorbent carried out out of absorption tower enter pulse cloth In sack cleaner, solid material is separated by deduster, and purified flue gas passes through the cleaning flue gases outlet 17 in Fig. 2 Discharge.The solid material separated mainly contains Ca (OH)2And desulfurization product, denitration product etc., to improve absorbent The fraction solids Matter Transfer separated is used, is directly returned through the material-returning device 15 in feed back pipeline attached drawing 2 by utilization rate Flow back fluidized bed reactor, participates in chemical reaction process in main reaction tower again.Fraction solids material is from weary in ash discharging hole attached drawing 2 Expect that outlet 14 is discharged, to maintain the solid material of whole system to balance.
9) it by the adjustment of operating parameter parameter and reaction tower transformation, and after installing preposition oxidation reactor additional, can be used for The technique for realizing scrubbing CO_2, nitrogen oxides, dust, heavy metal simultaneously obtains the effect that multiple pollutant controls simultaneously.
The technical process of the utility model is as follows: the flue gas out that burns such as sintering machine, rotary kiln, coal-burning boiler (contains two Sulfur oxide, nitrogen oxides, heavy metal and dust), after electric precipitator preliminary dust removal, just as described in the utility model The inlet flue gas 1 of purification process.Flue gas passes through preposition catalytic unit 2, is filled with catalyst in device 2.The embodiment of catalyst: Catalyst is using titanium dioxide as carrier, mass fraction 80%, with FeO, V2O5、MnO2For active constituent, mass content is respectively 5%, 1% and 14%, catalyst configuration is cellular catalyst.Catalyst packing certain volume, so that catalysis reaction velocity For 3000~6000h-1, flue gas flow rate is 3~6m/s.In preposition catalyst reaction device, the NO quilt of 40~65% volume fractions It is oxidized to NO2, subsequently into the main reaction tower of Fig. 1.Main absorbent and additive are by powder feed system, via the in Fig. 2 One layer of main absorbent entrance 7, first layer additive entrance 8 or second layer calcium hydroxide entrance 11, second layer additive entrance 12 be sent into main reaction towers in, process water via in Fig. 2 first layer technique water spray gun 6 or second layer technique water spray gun 10 enter In main reaction tower.
As shown in figure 4, following reaction occurs for main absorbent, additive, moisture and flue gas in main reaction tower:
(M) low temperature catalyst is represented;
(M) main absorbent, additive, CaSO are represented3Deng;
NO first under the action of catalyst partial oxidation at NO2, NO2It is combined with NO and generates N2O3, subsequent N2O3And SO2In master Absorbent, additive surface hydroxyl, adsorption moisture and O2Under the action of, it is combined into a kind of sulfur-nitrogen compound, sulfur-nitrogen compound Also known as chamber crystal can resolve into SO3And N2O3, and reacted with absorbent and generate CaSO4With Ca (NO3)2
Main reaction section inlet temperature is 135 DEG C, and NO content is 450mg/Nm in import flue gas3, import SO2Content is 1700mg/Nm3, O2Content is 5%, and inlet flue gas flow is 100000Nm3/ h is filled with 40m in preposition catalytic unit3Urge Agent, the sectional area perpendicular to the catalyst in flow of flue gas direction are 10m2, flue gas flow rate is 4.05m/ in preposition catalytic unit S, by preposition catalytic unit, NO is oxidized to NO2Ratio be 45%.Flue gas enters main reaction via main reaction tower entrance Tower.After orifice plate air-distribution device, into main reaction tower upper section, the diameter of section of main reaction tower is 4m, the apparent velocity of flue gas For 3.22m/s.First layer amounts to two spray guns, every 0.523t/h, and the second layer amounts to two spray guns, every 0.523t/h.It inhales It receives agent to spray into from first layer, first layer main absorbent straying quatity 328kg/h, additive straying quatity 100kg/h.Ca in calcium hydroxide (OH)2Content is the molar ratio m of 80%, at this time Ca and pollutantca: (ms+0.5*mN)=1.3;Exporting smoke temperature is 100 DEG C.Instead Answering pressure difference in tower is 1.5kPa, and Matter Transfer multiplying power is 100 times or so at this time.By weary material, the weary of 428kg is discharged in row per hour Material.After this dry purification process, SO2It exports content removal efficiency and is greater than 98%, outlet SO2 concentration is lower than 35mg/Nm3; The removal efficiency of NOx is greater than 89%, and NO concentration at the outlet is lower than 50mg/Nm3Volatility and half volatile heavy metal Hg, As, Se, Pb etc. Removal efficiency is greater than 80%, and dust emission concentration is less than 5mg/m3

Claims (9)

1. a kind of dry cleaning device for being able to achieve flue gas minimum discharge, which is characterized in that it include preposition catalytic unit (2), Main reaction tower, pulsed bag filter (16), technique water tank, main absorbent powder feed system and additive powder feed system;Technique Water tank connects main reaction tower, and for feeding the water into main reaction tower, main absorbent powder feed system, additive powder feed system are separately connected Main reaction tower is filled with catalyst in preposition catalytic unit (2) for main absorbent and additive to be sent into main reaction tower (20), preposition catalytic unit (2) connects main reaction tower bottom end, and for that will pass through preposition catalytic unit (2), treated, and flue gas will be sent It becomes owner of reaction tower to be handled, main reaction tower upper end connects pulsed bag filter (16), at will be by main reaction tower Flue gas after reason is sent into pulsed bag filter (16), and pulsed bag filter (16) is provided with cleaning flue gases outlet (17), pass through cleaning flue gases outlet (17) through bag filter (16) treated cleaning flue gases to be discharged.
2. a kind of dry cleaning device for being able to achieve flue gas minimum discharge according to claim 1, which is characterized in that described Dry cleaning device further includes product circulation slot and product warehouse;Product circulation slot is material-returning device (15) and is arranged in pulsed The lower end of bag filter (16), flue gas enter product by the solid material that pulsed bag filter (16) are separated In circulating slot, fraction solids material directly returns to main reaction tower through feed back pipeline, participates in chemically reacting in main reaction tower again Journey, fraction solids material are discharged to product warehouse from weary material outlet (14), to maintain the solid material of whole device to balance.
3. a kind of dry cleaning device for being able to achieve flue gas minimum discharge, feature described in one of -2 exist according to claim 1 In the preposition catalytic unit (2) has catalytic unit inlet flue duct (18), preposition catalytic unit shell (19) and catalytic unit Exhaust pass (21), preposition catalytic unit shell (19) one end connect the inlet flue duct (18), and the other end connects the outlet Flue (21) is filled with catalyst (20) in preposition catalytic unit shell (19).
4. a kind of dry cleaning device for being able to achieve flue gas minimum discharge, feature described in one of -2 exist according to claim 1 In filling catalyst in preposition catalytic unit (2), the catalyst is honeycomb fashion, is NO by the NO partial oxidation in flue gas2
5. a kind of dry cleaning device for being able to achieve flue gas minimum discharge, feature described in one of -2 exist according to claim 1 In main reaction column structure is fluidized-bed reactor, and with orifice plate air-distribution device (5), cloth wind form uses orifice plate cloth wind, is used Double sections of arrangements, orifice plate air-distribution device (5) the following are main reaction tower entrance (4), orifice plate air-distribution device (5) the above are conversion zone, That is main reaction tower upper section (9).
6. a kind of dry cleaning device for being able to achieve flue gas minimum discharge, feature described in one of -2 exist according to claim 1 In the installation first layer technique water spray gun to be opened/closed more than main reaction tower conversion zone orifice plate air-distribution device (5), in first layer work Second layer technique water spray gun to be opened/closed is set above skill water spray gun, and technique water tank can be separately connected first layer technique water spray gun With second layer technique water spray gun to be opened/closed.
7. a kind of dry cleaning device for being able to achieve flue gas minimum discharge according to claim 6, which is characterized in that first Layer technique water spray gun to be opened/closed is arranged in main reaction tower conversion zone orifice plate air-distribution device (5) or more;Second layer work to be opened/closed Skill water spray gun is arranged in the altitude range of conversion zone, and in the height apart from orifice plate air-distribution device (5) 1/2 to 2/3.
8. a kind of dry cleaning device for being able to achieve flue gas minimum discharge according to claim 6, which is characterized in that anti- Answer be arranged on tower the main absorbent entrance (7) of first layer, the main absorbent entrance (11) of the second layer, first layer additive entrance (8) and The setting position of second layer additive entrance (12), the main absorbent entrance (7) of first layer and first layer additive entrance (8) is located at First layer technique water spray gun to be opened/closed top 0.5-2m, the main absorbent entrance (11) of the second layer and second layer additive entrance (12) setting position is located at second layer technique water spray gun to be opened/closed top 0.5-2m, and main absorbent powder feed system is separately connected The main absorbent entrance (7) of first layer and the main absorbent entrance (11) of the second layer;Additive powder feed system is separately connected first layer and adds Add agent entrance (8) and second layer additive entrance (12).
9. a kind of dry cleaning device for being able to achieve flue gas minimum discharge, feature described in one of -2 exist according to claim 1 In the dry cleaning device is able to achieve the dry of SO 2 from fume, nitrogen oxides, heavy metal and dust minimum discharge to be a kind of Method purification device.
CN201821146949.2U 2018-07-19 2018-07-19 A kind of dry cleaning device being able to achieve flue gas minimum discharge Active CN208839349U (en)

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