CN101822983B - Catalyst for catalyzing and oxidizing oxynitride in flue gas and preparation process thereof - Google Patents
Catalyst for catalyzing and oxidizing oxynitride in flue gas and preparation process thereof Download PDFInfo
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- CN101822983B CN101822983B CN2009101557350A CN200910155735A CN101822983B CN 101822983 B CN101822983 B CN 101822983B CN 2009101557350 A CN2009101557350 A CN 2009101557350A CN 200910155735 A CN200910155735 A CN 200910155735A CN 101822983 B CN101822983 B CN 101822983B
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Abstract
The invention discloses a catalyst for catalyzing and oxidizing oxynitride in flue gas, which is prepared by using mesoporous silica as a vector, one or mixture of two of kalium and molybdenum as a doping component and platinum as an active component by adopting an equal-volume stepwise impregnation method. The invention also discloses a process for preparing the catalyst, and simultaneously discloses application of the catalyst in flue gas denitration process. Under the action of the catalyst, by utilizing oxygen contained in the flue gas per se, nitrogen oxide is oxidized into nitrogen dioxide which is easily dissolved in water, so that the oxidizability of nitric oxide in the flue gas can be improved, and the flue gas is absorbed and denitrated by utilizing alkali liquor. The kalium and polybdenum doped platinum-based catalyst prepared by the process has catalytic oxidation performance obviously superior to an undoped platinum-based catalyst, and has high denitration efficiency; and under the catalytic oxidation action of the kalium and polybdenum doped platinum-based catalyst, the NOx oxidizability in the oxidized flue gas is just between 45 and 65 percent, and the denitration side product nitrite can be reclaimed so as to realize recycling of the denitration product.
Description
Technical field
The present invention relates to the Air Pollution Control field, specifically is the catalyst and the preparation technology thereof of nitrogen oxide in a kind of catalytic oxidation flue gas.
Background technology
In the existing denitration technology, " oxidation-absorptions " two goes on foot denitration technology and enjoys researcher's concern because of its high efficiency and economy, adaptable across the boiler of various scales.Its key technology is to control oxidation step, makes flue gas nitrogen oxide NO
xThe middle less nitric oxide NO of solubility is oxidized to the bigger nitrogen dioxide NO of solubility
2, nitrogen trioxide N
2O
3Or dinitrogen pentoxide N
2O
5Etc. high valence state oxynitrides, be beneficial to follow-up absorption step.Be that main, common vapour phase oxidation process mainly contains direct oxidation method, photocatalytic oxidation and catalytic oxidation generally in the oxidation step with vapour phase oxidation process.With other vapour phase oxidation processes comparatively speaking, catalytic oxidation has and can reduce the oxidant consumption, effectively reduces plurality of advantages such as reaction temperature.
Chemical reaction
Be reversible reaction, the fire coal boiler fume temperature is below 200 ℃, oxygen O in the flue gas
2Volume fraction is about 5%, with this understanding by O
2Generate NO with NO
2Reaction speed very slow, so flue gas NO
xMiddle NO
2/ (NO+NO
2) volume ratio (oxidizability) very low (5%-10%), obviously if flue gas is fed absorption liquid, denitration effect is very poor.Adopt catalytic oxidation can quicken O
2With the reaction of NO, improve flue gas NO
xMiddle NO
2Content is beneficial to liquid phase and absorbs.This method does not need expensive ozone O
3Deng strong oxidizer, avoided the transportation and the storage of strong oxidizer, improved the economy and the security of denitrating system.
Publication number adopts O for the CN1768902 Chinese invention patent
3Directly the NO in the flue gas is oxidized to NO soluble in water as oxidant
2, N
2O
3Or N
2O
5, combine alkali lye to absorb denitration again, the denitrating flue gas effect is more than 80%, but the ozone-depleting amount is big, and price is more expensive, has influenced the economy of this method.Publication number is that the Chinese invention patent of CN101028596 has prepared a kind of manganese base nano-powder oxide catalyst, and reaction temperature can realize the oxidizability of 70%-92% in the time of 200 ℃-400 ℃, knows the catalytic effect (oxidizability about 15%) of catalyst far above public affairs; Publication number is that the Chinese invention patent of CN101028596 discloses a kind of flue gas catalytic oxidation denitration technique, and its characteristics are to adopt with TiO
2Or ZrO
2-TiO
2Be carrier, Co is the catalyst of active component, utilizes the O that itself contains in the flue gas
2, do not need oxidant applying just can the NO partial oxygen be changed into and be easy to water-soluble NO
2(oxidizability 40%-60%) utilizes alkali lye to absorb denitration again, and can realize the recycling of denitration accessory substance nitrite resource.
For realizing " oxidation-absorption " two step denitration technology, need the further catalyst preparation process of exploitation catalytic oxidation of nitric oxide.
Summary of the invention
The invention provides the catalyst and the preparation technology thereof of nitrogen oxide in a kind of catalytic oxidation flue gas, the application of this catalyst in denitrating flue gas is provided simultaneously, utilize the O that contains in catalyst and the flue gas
2With the NO partial oxidation is NO
2, know the effect that wet absorption technology can reach efficient denitration and reclaim accessory substance in conjunction with public affairs.
The catalyst of nitrogen oxide in a kind of catalytic oxidation flue gas is a carrier with the mesoporous silicon oxide, and one or both mixtures of potassium, molybdenum are doping component, and platinum is active component, adopts the catalyst of equal-volume step impregnation method preparation.
K in the catalyst: Mo: Pt: SiO
2Mol ratio=(0～2): (0～0.5): (0.003～0.015): 1, and K and Mo are not zero simultaneously.
The Preparation of catalysts technology of nitrogen oxide comprises the steps: in a kind of catalytic oxidation flue gas
(1) carrier preliminary treatment
Mesoporous silicon oxide is vacuumized drying in 60 ℃-70 ℃, or 100 ℃ of-110 ℃ of freeze-day with constant temperature;
(2) doping component load
With KNO
3And/or (NH
4)
6Mo
7O
24Be configured to solution I with water, the mesoporous silicon oxide that will pass through step (1) processing impregnated in the solution I, dip time at least 12 hours, and drying is again in 600 ℃ of-800 ℃ of roastings;
(3) active constituent loading
With H
2PtCl
6Be configured to solution II with water, it impregnated in the solution II will to pass through mesoporous silicon oxide that step (2) handles, dip time at least 12 hours, and drying, again in 600 ℃ of-800 ℃ of roastings, 400 ℃ of-600 ℃ of reduction in hydrogen at last.
Drying in step (2) and the step (3) adopts the method for same step (1) to get final product.
The application of described catalyst in denitrating flue gas, a kind of preferred application process do, catalyst breakage to the 40-60 order, is arranged in temperature range and is in 150-300 ℃ the flue, utilizes the O that contains in the flue gas
2Flue gas is carried out oxidation processes; Flue gas with after the alkali lye absorption oxidation removes the nitrogen oxide in the flue gas.
After using this catalyst oxidation, flue gas NO
xOxidizability can be strict controlled in 45-65%, be nitrite with the product after guarantee absorbing.
Catalyst of the present invention mainly contains following characteristics:
1) adopts the host of Pt, the active sites of catalytic reaction can be provided, reactant NO and O as catalyst
2Adsorb, and react, wherein O
2The absorption (Pt-O) of dissociating to be considered to the rate determining step of this reaction rapid.
2) K, Mo are as the auxiliary agent of catalyst, and its main existence form is K
2O and MoO
3, an amount of K
2The doping of O can reduce Pt-NO absorption bond energy through electronic effect, makes the NO on the Pt adsorption potential that desorption take place, and increases Pt-O and becomes the key possibility, promotes NO and O
2Reaction; In addition, an amount of MoO
3Doping can increase catalyst surface acidity, SO draws up
2Oxidation, protection host Pt, the NO on the Pt-NO adsorption potential is moved to adjacent with it Mo and is upward formed Mo-NO adsorption potential (overflow phenomena) simultaneously, makes Pt vacate part adsorption potential absorption O (Pt-O), also can promote NO and O
2Reaction.
3) catalyst carrier is mesoporous SiO
2, have bigger specific surface, do not change original specific surface behind load host and the auxiliary agent basically; Carrier S iO
2There is adsorption potential hardly in inert material, itself possesses good anti-SO
2Ability; Mesoporous material has bigger duct simultaneously, helps flue gas through beds, has improved the mechanical stability of catalyst.
The catalytic oxidation performance of the platinum based catalyst after gained potassium of the present invention, molybdenum mix significantly is superior to unadulterated platinum based catalyst, under the effect of catalyst of the present invention, utilizes the oxygen in the flue gas that part NO is oxidized to NO
2, improve NO in the flue gas
xOxidizability, need not to add other oxidants, know alkali lye and absorb and can realize denitration effect preferably in conjunction with public.NO in the flue gas after the oxidation
xOxidizability just between 45%-65%, recyclable denitration by-product nitrite.Compare with other method of denitration, this method efficient is high, can realize the resource of denitration product.
Description of drawings
Fig. 1 is a denitrating technique flow chart of the present invention.
Wherein, 1-deduster 2-catalyst 3-absorption tower 4-circulating pump 5-resource recovering system 6-chimney.
The specific embodiment
As shown in Figure 1, the flue gas of coal-burning boiler gets into NO catalyst oxidation reactor 2, flue gas NO through deduster 1 back
xMiddle part NO is oxidized to NO
2, get into absorption tower 3 washings, with SO
2With NO
xAbsorbing and removing together, absorption liquid through circulating pump 4 on the absorption tower inner loop, the flue gas after the absorption gets into chimney 6 qualified discharges.When treating that absorption liquid is accumulated to certain high concentration, absorption liquid is delivered to resource recovering system 5 separates, crystallization.
Reference examples 1:
1) equi-volume impregnating prepares catalyst Pt/SiO
2
Mesoporous silicon oxide was vacuumized dry 3 hours in 65 ℃ of vacuum drying chambers;
With H
2PtCl
6Be configured to solution with water, treated mesoporous silicon oxide impregnated in H
2PtCl
6In the solution, dipping is 12 hours under the room temperature, and wherein the addition of chloroplatinic acid is Pt: SiO
2(mol ratio)=0.008: 1; 65 ℃ vacuumized dry 3 hours in the vacuum drying chamber, 750 ℃ of roastings 2 hours in Muffle furnace again, 550 ℃ of reductase 12s hour in hydrogen at last.Grind at last and obtain catalyst.
2) denitrating technique
Smoke treatment O
2Concentration 5%, NO
xConcentration 550ppm, GHSV (gas space velocity)=50000h
-1, catalytic reactor is installed in the upper reaches of dust arrester, 200 ℃ of reaction temperatures, reactor outlet NO
xOxidizability is about 28%, and flue gas after the oxidation gets into spray column, in the absorption tower with SO
2With NO
xTogether remove.
Embodiment 1:
1) equi-volume impregnating prepares catalyst Pt-K/SiO
2
With mesoporous silicon oxide in 105 ℃ of dryings of thermostatic drying chamber 8 hours;
With KNO
3Be configured to solution I with water, treated mesoporous silicon oxide impregnated in the solution I, dipping is 12 hours under the room temperature, 105 ℃ of dryings of thermostatic drying chamber 8 hours, 700 ℃ of roastings 2 hours in Muffle furnace again;
With H
2PtCl
6Be configured to solution II with water, with load the mesoporous silicon oxide of K impregnated in the solution II, dipping is 12 hours under the room temperature; 105 ℃ of dryings of thermostatic drying chamber 8 hours, 700 ℃ of roastings 2 hours in Muffle furnace again, 500 ℃ of reductase 12s hour in hydrogen at last.
Wherein, the addition of potassium nitrate, chloroplatinic acid is K: Pt: SiO
2(mol ratio)=1: 0.005: 1.
Grind at last and obtain catalyst.
2) denitrating technique
Smoke treatment O
2Concentration 5%, NO
xConcentration 550ppm, GHSV (per hour gas space velocity)=50000h
-1, catalytic reactor is installed in the upper reaches of dust arrester, 200 ℃ of reaction temperatures, reactor outlet NO
xOxidizability is about 51%, and flue gas after the oxidation gets into spray column, in the absorption tower with SO
2With NO
xTogether remove.
Embodiment 2:
1) equi-volume impregnating prepares catalyst Pt-Mo/SiO
2
With mesoporous silicon oxide in vacuum drying chamber 65 ℃ vacuumized dry 3 hours;
With (NH
4)
6Mo
7O
24Be configured to solution I with water, treated mesoporous silicon oxide impregnated in the solution I, dipping is 12 hours under the room temperature, and 65 ℃ vacuumized dry 3 hours in the vacuum drying chamber, 750 ℃ of roastings 2 hours in Muffle furnace again;
With H
2PtCl
6Be configured to solution II with water; With load the mesoporous silicon oxide of Mo impregnated in the solution II, dipping is 12 hours under the room temperature, 65 ℃ vacuumized dry 3 hours in the vacuum drying chamber; 750 ℃ of roastings 2 hours in Muffle furnace again, 500 ℃ of reductase 12s hour in hydrogen at last.
Wherein, the addition of ammonium heptamolybdate, chloroplatinic acid is Mo: Pt: SiO
2(mol ratio)=0.25: 0.005: 1.
Grind at last and obtain catalyst.
2) denitrating technique
Smoke treatment O
2Concentration 5%, NO
xConcentration 550ppm, GHSV (per hour gas space velocity)=50000h
-1, catalytic reactor is installed in the upper reaches of dust arrester, 200 ℃ of reaction temperatures, reactor outlet NO
xOxidizability is 47%, and flue gas after the oxidation gets into spray column, in the absorption tower with SO
2With NO
xTogether remove.
Embodiment 3:
1) equi-volume impregnating prepares catalyst Pt-K-Mo/SiO
2
With mesoporous silicon oxide in vacuum drying chamber 65 ℃ vacuumized dry 3 hours;
With KNO
3(NH
4)
6Mo
7O
24Be configured to solution I with water, treated mesoporous silicon oxide impregnated in the solution I, dipping is 12 hours under the room temperature, and 65 ℃ vacuumized dry 3 hours in the vacuum drying chamber, 700 ℃ of roastings 2 hours in Muffle furnace again;
With H
2PtCl
6Be configured to solution II with water; With load the mesoporous silicon oxide of K and Mo impregnated in the solution II, dipping is 12 hours under the room temperature, 65 ℃ vacuumized dry 3 hours in the vacuum drying chamber; 700 ℃ of roastings 2 hours in Muffle furnace again, 550 ℃ of reductase 12s hour in hydrogen at last.
Wherein, the addition of potassium nitrate, ammonium heptamolybdate and chloroplatinic acid is K: Mo: Pt: SiO
2(mol ratio)=1: 0.2: 0.01: 1.
Grind at last and obtain catalyst.
2) denitrating technique
Smoke treatment O
2Concentration 5%, NO
xConcentration 550ppm, GHSV (per hour gas space velocity)=50000h
-1, catalytic reactor is installed in the upper reaches of dust arrester, 200 ℃ of reaction temperatures, reactor outlet NO
xOxidizability is 63%, and flue gas after the oxidation gets into spray column, in the absorption tower with SO
2With NO
xTogether remove.
Embodiment 4:
1) equi-volume impregnating prepares catalyst Pt-K-Mo/SiO
2
With mesoporous silicon oxide in 105 ℃ of dryings of thermostatic drying chamber 8 hours;
With KNO
3(NH
4)
6Mo
7O
24Be configured to solution I with water, treated mesoporous silicon oxide impregnated in the solution I, dipping is 12 hours under the room temperature, 105 ℃ of dryings of thermostatic drying chamber 8 hours, 750 ℃ of roastings 2 hours in Muffle furnace again;
With H
2PtCl
6Be configured to solution II with water, with load the mesoporous silicon oxide of K and Mo impregnated in the solution II, dipping is 12 hours under the room temperature, 105 ℃ of dryings of thermostatic drying chamber 8 hours, 750 ℃ of roastings 2 hours in Muffle furnace again, 550 ℃ of reductase 12s hour in hydrogen at last.
Wherein, the addition of potassium nitrate, ammonium heptamolybdate and chloroplatinic acid is K: Mo: Pt: SiO
2(mol ratio)=0.5: 0.25: 0.01: 1.
Grind at last and obtain catalyst.
2) denitrating technique
Smoke treatment O
2Concentration 5%, NO
xConcentration 550ppm, GHSV (per hour gas space velocity)=50000h
-1, catalytic reactor is installed in the upper reaches of dust arrester, 200 ℃ of reaction temperatures, reactor outlet NO
xOxidizability is 56%, and flue gas after the oxidation gets into spray column, in the absorption tower with SO
2With NO
xTogether remove.
Claims (2)
1. the Preparation of catalysts technology of nitrogen oxide in the catalytic oxidation flue gas; Said catalyst is carrier with the mesoporous silicon oxide; One or both mixtures of potassium, molybdenum are doping component; Platinum is active component, it is characterized in that: said preparation technology adopts equi-volume impregnating, comprises the steps:
(1) carrier preliminary treatment
Mesoporous silicon oxide is vacuumized drying in 60 ℃-70 ℃, or 100 ℃ of-110 ℃ of freeze-day with constant temperature;
(2) doping component load
With KNO
3And/or (NH
4)
6Mo
7O
24Be configured to solution I with water, the mesoporous silicon oxide that will pass through step (1) processing impregnated in the solution I, dip time at least 12 hours, and drying is again in 600 ℃ of-800 ℃ of roastings;
(3) active constituent loading
With H
2PtCl
6Be configured to solution II with water, the mesoporous silicon oxide that will pass through step (2) processing impregnated in the solution II, dip time at least 12 hours, and drying, again in 600 ℃ of-800 ℃ of roastings, 400 ℃ of-600 ℃ of reduction in hydrogen at last;
K in the catalyst: Mo: Pt: SiO
2Mol ratio=(0～2): (0～0.5): (0.003～0.015): 1, and K and Mo are not zero simultaneously.
2. the application of catalyst in denitrating flue gas of preparation technology preparation according to claim 1 is characterized in that: catalyst breakage to the 40-60 order, is arranged in temperature range and is in 150-300 ℃ the flue, utilize the O that contains in the flue gas
2Flue gas is carried out oxidation processes; Flue gas with after the alkali lye absorption oxidation removes the nitrogen oxide in the flue gas.
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| CN2009101557350A CN101822983B (en) | 2009-12-25 | 2009-12-25 | Catalyst for catalyzing and oxidizing oxynitride in flue gas and preparation process thereof |
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|---|---|---|---|
| CN2009101557350A CN101822983B (en) | 2009-12-25 | 2009-12-25 | Catalyst for catalyzing and oxidizing oxynitride in flue gas and preparation process thereof |
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| CN101822983B true CN101822983B (en) | 2012-05-23 |
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| CN103638792A (en) * | 2013-12-17 | 2014-03-19 | 张继惟 | LSCO-AS (low-temperature selective catalytic-oxidation-as simulating system) technology system for purifying oxygen-enriched combustion smoke |
| CN104492471B (en) * | 2014-12-24 | 2017-04-26 | 中南大学 | Medium-low temperature SCR denitration mesoporous molecular sieve catalyst and preparation method and application method thereof |
| CN104624031A (en) * | 2015-01-29 | 2015-05-20 | 成都华西堂投资有限公司 | Method for synchronously removing sulfur oxide and nitric oxide in smoke |
| CN109621714B (en) * | 2018-12-29 | 2022-01-18 | 盐城工学院 | Flue gas denitration process method for generating precipitate |
| CN109806882A (en) * | 2019-03-18 | 2019-05-28 | 山东大业联合新能源设备有限公司 | A kind of SCO denitration new energy composite material |
| CN111939755B (en) * | 2019-05-17 | 2023-02-17 | 中国石油化工股份有限公司 | Method for reducing concentration of NO in incomplete regeneration flue gas |
| CN111944557B (en) * | 2019-05-17 | 2023-05-05 | 中国石油化工股份有限公司 | FCC method for reducing concentration of NO in regenerated flue gas |
| CN111939754B (en) * | 2019-05-17 | 2023-03-10 | 中国石油化工股份有限公司 | Method for treating gas containing sulfur oxide and NO |
| CN112844395B (en) * | 2019-11-28 | 2023-10-31 | 中冶京诚工程技术有限公司 | Oxidative denitration catalyst and flue gas catalytic oxidation denitration method and device |
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| CN1289388A (en) * | 1998-02-04 | 2001-03-28 | 高林环境技术公司 | Regeneration of catalyst/absorber |
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| CN1289388A (en) * | 1998-02-04 | 2001-03-28 | 高林环境技术公司 | Regeneration of catalyst/absorber |
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| Jazaer Dawody et al..The effect of metal oxide additives (WO3, MoO3, V2O5, Ga2O3) on the oxidation of NO and SO2 over Pt/Al2O3 and Pt/BaO/Al2O3 catalysts.《Journal of Molecular Catalysis A: Chemical》.2004,第209卷215-225. * |
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