CN107930659A - A kind of mesoporous F, Ce codope SCR catalyst - Google Patents

A kind of mesoporous F, Ce codope SCR catalyst Download PDF

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CN107930659A
CN107930659A CN201711251392.9A CN201711251392A CN107930659A CN 107930659 A CN107930659 A CN 107930659A CN 201711251392 A CN201711251392 A CN 201711251392A CN 107930659 A CN107930659 A CN 107930659A
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CN107930659B (en
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延海港
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HEFEI ZHONGYA ENVIRONMENTAL PROTECTION TECHNOLOGY Co.,Ltd.
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/06—Halogens; Compounds thereof
    • B01J27/135—Halogens; Compounds thereof with titanium, zirconium, hafnium, germanium, tin or lead
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8628—Processes characterised by a specific catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/24—Chromium, molybdenum or tungsten
    • B01J23/30—Tungsten
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0201—Impregnation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/06—Washing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08—Heat treatment
    • B01J37/082—Decomposition and pyrolysis
    • B01J37/086—Decomposition of an organometallic compound, a metal complex or a metal salt of a carboxylic acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts

Abstract

The invention discloses a kind of mesoporous F, Ce codope V2O5‑WO3/TiO2The selective catalytic denitrification process catalyst.Halogens F and rare earth element ce are doped to the commercial catalysts V generally used by the catalyst2O5‑WO3/TiO2In, and the mode of loading of the load capacity of V and W elements and W elements in catalyst is optimized, so as to widen V2O5‑WO3/TiO2Catalyst activity temperature window.The present invention solves V2O5‑WO3/TiO2Catalyst does not reach the technical problems such as denitration purpose when coal-fired flue-gas temperature is too low, air speed changes greatly, the flue gas produced suitable for the selective catalytic denitrification process processing industrial coal.

Description

A kind of mesoporous F, Ce codope SCR catalyst
Technical field
The present invention relates to a kind of SCR catalyst and its preparation method and application, particularly a kind of mesoporous Heteroatom doping V2O5-WO3/TiO2Catalyst, its content is low, high catalytic efficiency and light-off temperature are low SCR catalyst and its in stationary source flue gas The application of middle catalytic denitration.
Background technology
At present, AND ENERGY RESOURCES CONSUMPTION IN CHINA quickly increases, and vehicle guaranteeding organic quantity increases year by year, and NOx discharge constantly rises, its acid It is compound that rain type from sulfuric acid type has been converted to sulfonitric.With SO2Removing sulfuldioxide is increasingly mature, and NOx removal has just become The hot spot of people's research.
Relevant art means are taken to control NOx before combustion, after burning neutralization burning according to the relation of fuel and unit.Combustion Control technology is mainly concerned with processing to bunker coal or using alternative fuel before burning, fuel is primarily referred to as before combustion, by it In nitrogenous compound removing, control of the technology to fuel type NOx has a certain effect, but acts on thermal NO x little, effect Fruit is limited and cost is higher, not yet forms mature and stable technology at present.Control technology is mainly fired using low NOx in burning Burning technology, the technology are mainly the concentration and temperature by improving combustion method, as far as possible reduction combustion zone oxygen, so that Reduce the generation of NOx.The characteristics of low NOx combusting technology is technical maturity, and investment is low with operating cost.Required to NOx emission Very stringent country, is to carry out denitrating flue gas again after first reducing the NOx of more than half using low-NOx combustor, to reduce The NOx concentration of denitrification apparatus entrance, reduces investment and operating cost.The post-control technology that burns mainly carries out denitrating flue gas.Cigarette Qi exhaustion nitre is the method for the reduction NOx emission that current developed country generally uses, and has very high NOx removal efficiency.Flue gas takes off Nitre technology have a variety of, main technologies for selective non-catalytic reduction (Selective Non-catalytic Reduction, SNCR) and selective catalytic reduction (Selective Catalytic Reduction, SCR) technology, SNCR methods are to utilize reduction Agent ammonia or urea react generation N under no catalyst existence condition, with NOx2And H2O, its reaction temperature 900~1000 DEG C it Between, denitration rate is 30~50%.Due to temperature change with boiler load and the cycle of operation and boiler NOx concentration it is irregular Property, become more complicated when applying the technique.The whole world covers business SNCR devices more at present about 300.To Coal-fired Thermal Power machine For group, technology maturation, commercial Application are widely mainly used with V2O5-WO3/TiO2For the SCR denitration technology of catalyst, The technology denitration efficiency is high, can reach current most stringent of Abgasgesetz and standard requirement.
Catalyst is the core of SCR technology, V2O5-WO3/TiO2Catalyst is as commercial catalysts, because its greater activity With strong mithridatism and heat endurance, achieve and be widely applied in fossil-fired unit denitrating flue gas field.But the catalyst Active temperature windows belong to middle warm type denitrating catalyst only between 300~400 DEG C, and for the low work of fossil-fired unit Less than 300 DEG C of flue gas under the conditions of condition, V2O5-WO3/TiO2Catalyst denitration effect can be very restricted, in reaction temperature Degree is under the inhibitory action of catalyst, ammonia nitrogen even occurs than the process complications such as control, part generating set in denitrating technique Stop the appearance for the problems such as spray ammonia or flue gas bypass denitrating catalyst by bypass, cause the exhaust emission of NOx.Therefore, such as What improves the denitration activity below 300 DEG C of SCR catalyst, is the main problem that current commercial denitrating catalyst is faced.Separately Outside, after long-haul operations, catalyst granules easily occur reunite, surface it is easy to pollute, cause catalytic activity reduce, stability compared with Difference.Therefore, the structure on nanoscale to active component and pattern are designed adjusting, increase its specific surface area, increase table The catalytic active site of face exposure, improve structural stability, and develops that cost is low, and the wide active temperature window that light-off temperature is low The SCR catalyst of mouth is imperative for the denitrating flue gas cause for developing China.
The content of the invention
The shortcomings that in order to overcome the above-mentioned prior art, it is an object of the invention to provide a kind of mesoporous SCR catalysis of doping Agent, and the catalyst is applied on catalytic denitration.
Realizing the technical solution of the object of the invention is：A kind of SCR catalyst of mesoporous F, Ce doping, in V2O5-WO3/ TiO2F, Ce are adulterated on catalyst, wherein, the molar ratio of doped chemical F and V are 1:5-1:The molar ratio of 8, Ce and V is 0.1- 10, WO3Load capacity be 0.8%-1.5wt%, V2O5Load capacity be 0.2-0.8wt%.
A kind of preparation method of the SCR catalyst of mesoporous F, Ce doping, includes the following steps：
（1）Acetylacetone,2,4-pentanedione is added into butyl titanate, then adds the ammonium titanium fluoride of stoichiometry and the methanol solution of cerium salt, Stirring obtains colloidal sol after a certain period of time, is calcined after dry and obtains fluorine, cerium dopping titanium dioxide carrier；
（2）To step（1）In obtained fluorine, cerium dopping titanium dioxide carrier be immersed in ammonium paratungstate aqueous solution, after drying and calcining Obtain the WO of F, Ce doping3/TiO2；
（3）Use step（2）In be made F, Ce doping WO3/TiO2Be immersed in ammonium metavanadate aqueous solution, obtained after drying and calcining F, The V of Ce doping2O5-WO3/TiO2；
（4）Mesoporous doping shape V2O5-WO3/TiO2Preparation：
A. mesoporous SCR catalyst is prepared using hard template method, the silicon substrate template and 10-20mL absolute ethyl alcohols for weighing 1.0-1.8g exist 2h is stirred under conditions of 800-1000rpm rotating speeds, colourless solution A is obtained after the dissolving completely of silicon substrate template；
B. the V of 1.0-2.0g F, Ce doping is weighed2O5-WO3/TiO2With 10-20mL absolute ethyl alcohols in 800-1200rpm rotating speed bars Disperse 0.5h under part and obtain solution B；
C. solution B is added in solution A and continues to stir 1h, then this mixed liquor is placed under the conditions of 50-70 DEG C of constant temperature and is dried 12h, then room temperature is down to naturally after 600 DEG C roast 6h, powder is made.With the sodium hydroxide solution and powder of 1M at 50-60 DEG C Under the conditions of be vigorously stirred after 1h and centrifuge to remove silicon substrate template, be finally placed at 50-70 DEG C of constant temperature dry 24h, be made and be situated between The V of hole F, Ce doping2O5-WO3/TiO2Denitrating catalyst.
The cerium salt is at least one of cerous chlorate, cerous nitrate, ammonium ceric nitrate or cerous sulfate.
Step（1）Described in mixing time be 2~4h, with molar ratio computing, acetylacetone,2,4-pentanedione/Ti is 2, drying temperature 80~ 120 DEG C, calcining heat is 400~600 DEG C, and calcination time is 2~6h；The molar ratio of ammonium titanium fluoride and butyl titanate is 0.005~0.154.
Step（2）With（3）In, the dip time is 4~8h, 80 DEG C~140 DEG C of drying temperature；Calcining heat is 400 DEG C~600 DEG C, calcination time is 2~6h.
To catalyst activity evaluation experimental, wherein flue gas condition is：NO=NH3=500ppm, O2=5.0%, SO2=250ppm, H2O=10%, N2Balance, the h of air speed=35000-1~60000h-1, reaction temperature is 200-400 DEG C.
Compared with prior art, the present invention has the following advantages：
1st, F adulterates TiO2More powered Lacking oxygen, WO is presented in surface3Rear catalyst surface reduction state is acted on powered Lacking oxygen WO3Quantity increase；Reduction-state WO3With O2After effect, itself is oxidized to WO3, O2Obtain electronics and be changed into superoxide radical, so as to promote Oxidation into catalyst to NO；
2nd, by the doping of F, WO in catalyst is reduced3、V2O5Content requirement, so as to reduce Catalyst Production cost, make It is more easy to be received by factory；
3rd, by the doping of F, the light-off temperature of catalyst is high, and it is de- effective catalysis can be carried out to fossil-fired unit flue gas Nitre；
4th, after Ce doping, the performance of the alkali resistant metal poisoning of V, Ti oxide catalyst is lifted, the Ce especially adulterated is improved While catalyst alkali resistant metal poisoning performance, on SCR activity without influence；
5th, catalyst stability is good, in certain space velocity range, ammonia nitrogen ratio between 0.8~1.0 when, the catalytic denitration of catalyst Rate can be maintained at very high degree.
Embodiment
The present invention is made with reference to specific embodiment further to explain.
Embodiment 1
0.128mol acetylacetone,2,4-pentanediones are added into 0.064mol butyl titanates, make acetylacetone,2,4-pentanedione/Ti molar ratio=2；Then plus Enter the ethanol solution of the ammonium titanium fluoride of 50mL stoichiometries, stir 2h, obtain colloidal sol；After colloidal sol is concentrated under 60 DEG C of water-baths, Dry 6h, 3h is calcined at 500 DEG C at 120 DEG C, obtains the titanium dioxide carrier of F doping, and wherein ammonium titanium fluoride addition is to rub You are than F/Ti=0.005~0.02.The F adulterated TiOxes carrier impregnation prepared in the ammonium paratungstate aqueous solution of 50mL, in Flow back in 60 DEG C of water-baths after 4h, dry 6h at 120 DEG C, F doping WO is obtained then at 500 DEG C of calcining 2h3/TiO2, wherein WO3It is negative Carrying capacity is 1wt%, is denoted as F-WTi；F is adulterated into WO3/TiO2It is impregnated in the ammonium metavanadate aqueous solution of 50mL, in 60 DEG C of water-baths Flow back after 4h, dry 6h at 120 DEG C, then at 500 DEG C of calcining 2h, obtains F doping V2O5-WO3/TiO2Catalyst, wherein V2O5's Load capacity is 0.5%, is denoted as F-VWTi；
Mesoporous SCR catalyst is prepared using hard template method, the silicon substrate template and 10-20mL absolute ethyl alcohols for weighing 1.0-1.8g exist 2h is stirred under conditions of 800-1000rpm rotating speeds, colourless solution A is obtained after the dissolving completely of silicon substrate template；
B. the V of 1.0-2.0g F doping is weighed2O5-WO3/TiO2With 10-20mL absolute ethyl alcohols in 800-1200rpm speed conditions Disperse 0.5h down and obtain solution B；
C. solution B is added in solution A and continues to stir 1h, then this mixed liquor is placed under the conditions of 50-70 DEG C of constant temperature and is dried 12h, then room temperature is down to naturally after 600 DEG C roast 6h, powder is made.With the sodium hydroxide solution and powder of 1M at 50-60 DEG C Under the conditions of be vigorously stirred after 1h and centrifuge to remove silicon substrate template, be finally placed at 50-70 DEG C of constant temperature dry 24h, be made and be situated between The V of hole F doping2O5-WO3/TiO2Denitrating catalyst, is denoted as m-F-VWTi.
Using fixed bed, in NO concentration 500ppm, NH3/ NO=1.2, O25%th, N2Balance and air speed 30000h-1Under the conditions of (catalyst usage amount 0.3g), influence of the evaluation F doping to titanium dioxide load vanadium oxide-tungsten oxide catalyst NO removal efficiencies.
Embodiment 2
On the basis of embodiment 1,50mLization is added while the ethanol solution of ammonium titanium fluoride of 50mL stoichiometries is added The methanol solution of the cerous chlorate of metering is learned, other steps are identical with embodiment 1, and the V of F, Ce codope is made2O5-WO3/ TiO2Denitrating catalyst, is denoted as m-FCe-VWTi.Its NO removal efficiency is evaluated by the way of same as Example 1.
Comparative example 1
On the basis of embodiment 1, the V of no F, Ce doping is prepared2O5-WO3/TiO2Denitrating catalyst, is denoted as VWTi and without F, Ce The mesoporous V of doping2O5-WO3/TiO2Denitrating catalyst, is denoted as m-VWTi.
1. mesoporous F of table adulterates the influence to SCR catalyst NO removal efficiencies
As can be seen from Table 1, meso-hole structure and F doping can lift V2O5-WO3/TiO2The NO conversion ratios of denitrating catalyst, And the synergistic effect between meso-hole structure and F doping improves V2O5-WO3/TiO2The low-temperature denitration activity of denitrating catalyst.
Embodiment 3
M-F-VWTi is subjected to K element poisoning：By KNO3It is dissolved in aqueous solution, according to KNO3Liquor capacity and catalyst fines Mass ratio is 2:1 is impregnated, and K additive amounts are that K/V molar ratios are 4.Catalyst fines is impregnated in KNO3After solution 12h, drying 100 DEG C of dryings in case, powdered poisoned catalyst is made through roasting 3h in 500 DEG C of air of Muffle furnace.By obtained poison guard catalyst Agent is ground up, sieved, and is taken 40-60 mesh spare, is denoted as K-m-F-VWTi.Alkali resistant metallicity of the introducing of Ce elements to denitrating catalyst 2 can be the results are shown in Table.
Embodiment 4
K element poisoning is carried out according to the identical method of embodiment 3 to m-FCe-VWTi, sample is denoted as K-m-FCe-VWTi.
The influence to the poisoning of SCR catalyst alkali metal of 2. Ce elements of table
Introducing Ce elements in SCR catalyst as can be seen from Table 2 can be right while its alkali resistant metal poisoning performance is improved SCR activity is without influence.
The foregoing is only a preferred embodiment of the present invention, but protection scope of the present invention be not limited thereto, Any one skilled in the art the invention discloses technical scope in, technique according to the invention scheme and its Inventive concept is subject to equivalent substitution or change, should be covered by the protection scope of the present invention.

Claims (9)

  1. A kind of 1. mesoporous F, Ce codope SCR catalyst, it is characterised in that carrier TiO2, active component V2O5And WO3, urge F, Ce are adulterated in agent, catalyst is meso-hole structure.
  2. 2. mesoporous F, Ce codope SCR catalyst according to claim 1, it is characterised in that wherein WO3Load capacity be 0.8wt%-1.5wt%, V2O5Load capacity be 0.2-0.8wt%.
  3. 3. mesoporous F, Ce codope SCR catalyst according to claim 1 or 2, it is characterised in that wherein doped chemical F Molar ratio with V is 1:5-1:The molar ratio of 8, Ce and V is 0.1-10.
  4. 4. mesoporous F, Ce codope the SCR catalyst preparation method of claim 1-3 any one of them, it is characterised in that including Following preparation process：
    （1）Acetylacetone,2,4-pentanedione is added into butyl titanate, then adds the ammonium titanium fluoride of stoichiometry and the methanol solution of cerium salt, Stirring obtains colloidal sol after a certain period of time, is calcined after dry and obtains fluorine, cerium dopping titanium dioxide carrier；
    （2）To step（1）In obtained fluorine, cerium dopping titanium dioxide carrier be immersed in ammonium paratungstate aqueous solution, after drying and calcining Obtain the WO of F, Ce doping3/TiO2；
    （3）Use step（2）In be made F, Ce doping WO3/TiO2Be immersed in ammonium metavanadate aqueous solution, obtained after drying and calcining F, The V of Ce doping2O5-WO3/TiO2；
    （4）Mesoporous F, Ce codope V is prepared using hard template method2O5-WO3/TiO2。
  5. 5. mesoporous F, Ce codope SCR catalyst preparation method according to claim 4, it is characterised in that hard template method Prepare mesoporous F, Ce codope V2O5-WO3/TiO2Method include the following steps：
    A. the silicon substrate template for weighing 1.0-1.8g is stirred with 10-20mL absolute ethyl alcohols under conditions of 800-1000rpm rotating speeds 2h, colourless solution A is obtained after the dissolving completely of silicon substrate template；
    B. the V of 1.0-2.0g F, Ce doping is weighed2O5-WO3/TiO2With 10-20mL absolute ethyl alcohols in 800-1200rpm rotating speed bars Disperse 0.5h under part and obtain solution B；
    C. solution B is added in solution A and continues to stir 1h, then this mixed liquor is placed under the conditions of 50-70 DEG C of constant temperature and is dried 12h, then room temperature is down to naturally after 600 DEG C roast 6h, powder is made.With the sodium hydroxide solution and powder of 1M at 50-60 DEG C Under the conditions of be vigorously stirred after 1h and centrifuge to remove silicon substrate template, be finally placed at 50-70 DEG C of constant temperature dry 24h, be made and be situated between The V of hole F, Ce doping2O5-WO3/TiO2Denitrating catalyst.
  6. 6. preparation method according to claim 4 or 5, it is characterised in that step（1）Described in mixing time be 2~4h, With molar ratio computing, acetylacetone,2,4-pentanedione/Ti is 2,80~120 DEG C of drying temperature, and calcining heat is 400~600 DEG C, calcination time 2 ~6h.
  7. 7. preparation method according to claim 4 or 5, it is characterised in that the molar ratio of ammonium titanium fluoride and butyl titanate For 0.005~0.154.
  8. 8. preparation method according to claim 4 or 5, it is characterised in that step（2）With（3）In, the dip time is 4~8h, 80 DEG C~140 DEG C of drying temperature；Calcining heat is 400 DEG C~600 DEG C, and calcination time is 2~6h.
  9. 9. a kind of SCR denitration technique, it is characterised in that unstripped gas uses N2Balance, the h of air speed=35000-1~60000h-1, reaction Temperature is 200-400 DEG C, and the catalyst used is catalyzed for mesoporous F, Ce codope SCR any one of claim 1-3 Agent.
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Publication number Priority date Publication date Assignee Title
CN110142054A (en) * 2019-03-28 2019-08-20 北京工业大学 Using rare earth and anion modified synergic titanium dioxide as the denitrating catalyst of carrier and preparation
CN114832867A (en) * 2021-02-02 2022-08-02 国家能源投资集团有限责任公司 Activation method for improving low-temperature activity of honeycomb denitration catalyst
CN115282991A (en) * 2022-08-22 2022-11-04 盐城市兰丰环境工程科技有限公司 Cement kiln flue gas SCR denitration catalyst and preparation and application methods thereof

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CN106268779A (en) * 2016-08-11 2017-01-04 重庆大学 A kind of middle high temperature SCR denitration with alkali resistant metal poisoning and preparation method thereof
CN106552652A (en) * 2015-09-28 2017-04-05 南京理工大学 A kind of F doping SCR catalyst, preparation and the application on catalytic denitration
CN106582615A (en) * 2016-11-29 2017-04-26 凯龙蓝烽新材料科技有限公司 Preparation method for low-temperature V-W-TiO2 based selective reduction catalyst

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Publication number Priority date Publication date Assignee Title
CN106552652A (en) * 2015-09-28 2017-04-05 南京理工大学 A kind of F doping SCR catalyst, preparation and the application on catalytic denitration
CN106268779A (en) * 2016-08-11 2017-01-04 重庆大学 A kind of middle high temperature SCR denitration with alkali resistant metal poisoning and preparation method thereof
CN106582615A (en) * 2016-11-29 2017-04-26 凯龙蓝烽新材料科技有限公司 Preparation method for low-temperature V-W-TiO2 based selective reduction catalyst

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110142054A (en) * 2019-03-28 2019-08-20 北京工业大学 Using rare earth and anion modified synergic titanium dioxide as the denitrating catalyst of carrier and preparation
CN114832867A (en) * 2021-02-02 2022-08-02 国家能源投资集团有限责任公司 Activation method for improving low-temperature activity of honeycomb denitration catalyst
CN114832867B (en) * 2021-02-02 2023-09-29 国家能源投资集团有限责任公司 Start-up method for improving low-temperature activity of honeycomb denitration catalyst
CN115282991A (en) * 2022-08-22 2022-11-04 盐城市兰丰环境工程科技有限公司 Cement kiln flue gas SCR denitration catalyst and preparation and application methods thereof
CN115282991B (en) * 2022-08-22 2023-10-27 盐城市兰丰环境工程科技有限公司 Cement kiln flue gas SCR denitration catalyst and preparation and application methods thereof

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