CN101574660A - Method for preparing mixed compound catalyst used for catalyzing null-valence mercury in flue-gas to be oxidized - Google Patents
Method for preparing mixed compound catalyst used for catalyzing null-valence mercury in flue-gas to be oxidized Download PDFInfo
- Publication number
- CN101574660A CN101574660A CNA2009100528967A CN200910052896A CN101574660A CN 101574660 A CN101574660 A CN 101574660A CN A2009100528967 A CNA2009100528967 A CN A2009100528967A CN 200910052896 A CN200910052896 A CN 200910052896A CN 101574660 A CN101574660 A CN 101574660A
- Authority
- CN
- China
- Prior art keywords
- catalyst
- component
- mercury
- catalyzing
- oxide
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Catalysts (AREA)
Abstract
The invention relates to a method for preparing mixed compound catalyst used for catalyzing null-valence mercury in flue-gas to be oxidized. The active component of the catalyst comprises a main catalyzing component, a compound component and a mixed modified component, and the method comprises the steps of: adopting an immersion method to mix precursors of the three components and load the mixture on surface of a carrier; and the preparation process comprises immersion, drying and calcining. The main catalyzing component is one or two of manganic oxides and cobaltic oxides and plays a significant part in catalyzing process; the compound component is one or a plurality of oxides of copper, iron, zirconium and titanium and can be compounded with the main catalyzing component to reinforce the activity of the catalyst; and the mixed modified component is one or a plurality of molybdenum, tungsten and vanadium and can dramatically reinforce the anti-sulfur-dioxide property of the catalyst and enhance the low-temperature catalyzing activity of the catalyst. The catalyst prepared by the method can be applied to the catalyzing and oxidizing of null-valence mercury in coal-fired flue-gas to convert the null-valence mercury in the flue-gas into bivalence mercury which can be easily removed so as to realize the high-effective removal of mercury from flue-gas.
Description
Technical field
The present invention relates to a kind of preparation method of mixed compound catalyst, prepared catalyst has the advantages that activity is high, sulfur resistance is strong, low temperature adaptability is good, can be used for the catalytic oxidation of nonvalent mercury in the coal-fired flue-gas.Belong to environmental protection technical field.
Background technology
Contain Trace Mercury in the coal, because global annual Coal-fired capacity is huge, fire coal has become main artificial mercury emissions source.The coal-fired mercury emission of nineteen ninety-five China is 202 tons, is increased to 257 tons in 2003, and average annual growth rate reaches 3%.Mercury in the coal-fired flue-gas is mainly with nonvalent mercury (Hg
0), divalence mercury (Hg
2+) and particle mercury (Hg
P) three kinds of forms exist.Studies show that Hg
PAnd Hg
2+Easily from flue gas, removed by dust arrester and desulfurizer; And Hg
0Volatile and be insoluble in water, be difficult to from flue gas, efficiently remove.
Take suitable ancillary method to realize Hg
0To Hg
2+Efficient conversion, to make full use of desulfurizer efficient absorption Hg
2+Be to control Hg at present
0Most economical feasible approach, and become the research focus gradually.But Hg
0To Hg
2+Efficient conversion be the key and the difficult point place of high-efficiency mercury removal, at present the researcher does not obtain maturation method for transformation efficiently as yet.Confirmed that now (Selective catalytic reduction, SCR) catalyst can promote significantly that HCl is to Hg in the flue gas to SCR
0Oxidation, SCR catalyst Hg in the time of 300 ℃
0The efficient of oxidation can reach 80～90%, thereby helps to improve the clearance of mercury.By changing each operational factor of SCR such as NO concentration, NH
3Discoveries such as/NO, temperature and coal: during chlorinity 400～600ppm, it is best that the oxygenation efficiency of mercury can reach; But sulfide can significantly reduce the mercury oxidation rate, because SO
2And SO
3Cause the oxygenation efficiency of mercury to reduce with the active sites of chloride competition catalyst surface; SO in addition
2And SO
3Can make the catalyst poisoning inactivation with the sulphate form deposition at catalyst surface.For this reason, must be in conjunction with the special catalyst of oxidation characteristics exploitation of nonvalent mercury.
The catalyst of the nonvalent mercury of research catalysis at present oxidation has been obtained certain progress, and wherein the SCR catalyst has obtained paying attention to the transformation of nonvalent mercury.When HCl content was higher in the flue gas, this class catalyst strengthened the effect of nonvalent mercury catalyzed conversion, and the product that is produced is (as HgCl
2) taken away by air-flow very soon.But the existence of sulfur dioxide in flue gas has the obvious suppression effect to general transition-metal catalyst, and single metal oxides is difficult to bring into play effective catalytic action mostly, and the temperature range of reacting required is high and narrow, generally need be higher than 250 ℃.Chinese invention patent 200510024939.2 has proposed a kind of flue gas hydrargyrum-removing method by catalytic oxidation, utilize iron, cobalt, nickel, copper, manganese and oxide thereof as active component catalytic oxidation nonvalent mercury, Lattice Oxygen by oxygen in the flue gas or catalyst is converted into mercury oxide to nonvalent mercury, and is adsorbed on catalyst surface.But, do not consider the influence of factor such as hydrogen chloride and sulfur dioxide in the flue gas in this patent.Generally contain a certain amount of HCl in the actual flue gas, the catalytic oxidation product of nonvalent mercury is mainly HgCl when HCl exists
2And, when sulfur dioxide exists this class activity of such catalysts is suppressed highly significant.In addition, the use operating temperature of the catalyst that this patent is mentioned is generally just being brought into play catalysis suction-operated preferably more than 200 ℃, is difficult to use in the flue gas section (temperature is generally below 160 ℃) behind the conventional electric cleaner.In addition, patents such as US2003170159, WO2006009079 report part noble metal or catalyst of transition metal oxide, but these patents are paid close attention to seldom the sulfur resistance of catalyst, catalytic activity under the cryogenic conditions.
Summary of the invention
The objective of the invention is at the existing deficiency of present nonvalent mercury catalyst, the preparation method of the mixed compound catalyst of nonvalent mercury oxidation in a kind of catalysis flue gas is proposed, with certain metallic element by compound and doping treatment to the transition metal oxide modification, realize that it possesses advantages of high catalytic activity and sulfur resistance under cryogenic conditions.
For achieving the above object, activity of such catalysts component of the present invention is made of main catalytic component, compounding ingredients and mixed modified component, the presoma of three kinds of components is mixed and load to carrier surface by infusion process, preparation process comprises dipping, drying, calcines.The main catalytic component is one or both mixing in the oxide of oxide, cobalt of manganese, the main effect of performance in catalytic process; Compounding ingredients is the oxide of oxide, the zirconium of oxide, the iron of copper, in the titanyl compound one or more, by with the compound activity of such catalysts that strengthens of main catalytic component; Mixed modified component is one or more in molybdenum, tungsten, the vanadium, can significantly improve the anti-sulfur dioxide murder by poisoning ability of catalyst by the doping of this dvielement, and improves the low-temperature catalytic activity of catalyst.
Method concrete steps of the present invention are as follows:
1, get in the oxide of oxide, cobalt of manganese one or both as the main catalytic component, this class main catalytic component has absorption and catalytic action preferably to the gaseous state nonvalent mercury, the main effect of performance in catalytic process; Get the oxide of oxide, the zirconium of oxide, the iron of copper, in the titanyl compound one or more as compounding ingredients, this class material also has catalytic action to nonvalent mercury, by with the compound enhancing activity of such catalysts of main catalytic component; Get in molybdenum, tungsten, the vanadium one or more as mixed modified component, the doping by this dvielement can significantly improve the anti-sulfur dioxide of catalyst and poison ability, and improves the low-temperature catalytic activity of catalyst.Respectively the pairing separately presoma of main catalytic component, compounding ingredients and mixed modified component 1: 0.1 in molar ratio～1: 0.01～0.1 is mixed, add water and stir, obtain containing main catalytic constituent mass mark and be 0.5～30% dipping solution.
2, the proper catalyst carrier is immersed in the above-mentioned dipping solution stir; Dip time is 2-6 hour; Catalyst carrier after will flooding after the Separation of Solid and Liquid was dried 5-24 hour under 40 ℃～100 ℃ temperature.
3, in the catalyst carrier transposition Muffle furnace after will drying, be 1～30 ℃/minute with heating rate and rise to 300 ℃ of roastings 0.5～2 hour, rise to 400 ℃ of roastings 0.5～4 hour with 1～30 ℃/minute heating rate, be cooled to normal temperature with 1～2 ℃/minute cooldown rate again, make mixed compound catalyst.
Among the present invention, described presoma is one or more in the nitrate, carbonate, oxalates, acetate of metal.
Described catalyst carrier is one or more in the porous materials such as aluminium oxide, titanium dioxide, silica, molecular sieve, imvite or active carbon, and the catalyst carrier form is spherical, graininess, tabular or cellular.
The catalyst of the present invention's preparation can be applicable to the catalytic oxidation of nonvalent mercury in the coal-fired flue-gas, makes oxidant carry out low temperature with nonvalent mercury at catalyst surface and contacts, and the nonvalent mercury in the flue gas is converted into easy removed divalence mercury, realizes the efficient removal of mercury of flue gas.
The present invention possesses remarkable novelty and practicality, by the mixed compound metal oxide catalyst of the inventive method preparation to the catalytic oxidation ability of nonvalent mercury much larger than single component catalyst, and can be under lower temperature (100～200 ℃) and higher sulfur dioxide concentration the efficiently catalyzing and oxidizing nonvalent mercury.Interpolation compound, doped chemical functions as follows catalyst: (1) transforms by valence state between multiple metallic element, changes the electronic state of metal oxide surface, improves the ability of catalytic oxidation nonvalent mercury; (2) be entrained in and introduce impurity in the crystal, cause defective, thereby improve the catalytic activity of metal oxide; (3) doping metals (M) at catalyst surface with MO
3Form exist and to make above part sulphur is adsorbed onto, form certain anti-sulphur mechanism; Doping metals can also form alloy with transition metal, forms a kind of effective anti-sulphur phase, and two kinds of mechanism can both improve the anti-SO of catalyst
2, SO
3Performance prevents the catalyst poisoning inactivation.
The specific embodiment
Below by specific embodiment technical scheme of the present invention is further described.Following examples do not constitute limitation of the invention.
Embodiment 1
The main catalytic component adopts the oxide of manganese, and compounding ingredients adopts the oxide of copper, and doped chemical adopts molybdenum element.
Get 3g concentration and be 50% manganese nitrate solution, 0.5g copper nitrate, 0.2g five water nitric acid molybdenums, add deionized water and be diluted to 20ml and make dipping solution; Utilize diameter be the inertia alumina globule of 2～3mm as catalyst carrier, take by weighing 20g and immerse above-mentioned solution; Soak and after 4 hours unnecessary maceration extract is poured out, alumina globule has absorbed the maceration extract of 5g approximately; Alumina globule behind the dipping was dried 6 hours under 60 ℃ temperature, rose to 300 ℃ of roastings 1 hour with 5 ℃/minute of heating rates in the transposition Muffle furnace; Rising to 400 ℃ of roastings with 2 ℃/minute speed made presoma nitrate fully decompose in 4 hours; With 2 ℃/minute cooldown rate catalyst is cooled to normal temperature again, makes mixed compound catalyst.
Take by weighing the above-mentioned composite catalyst of 2g, it is inserted in the tubular fixed-bed reactor, feeding contains nonvalent mercury 100 μ g/m
3With oxidant HCl concentration be the simulated flue gas of 10ppm.Temperature is that 150 ℃, air speed are 10000h
-1Condition under, when catalyst reached stably catalyzed stage, composite catalyst reached 98% to the transformation efficiency of nonvalent mercury.Other condition is constant, only the operating temperature of reactor is reduced to 100 ℃, and composite catalyst is 92% to the catalytic conversion efficiency of nonvalent mercury.Operating temperature still is 150 ℃, and when other condition was constant, when adding the sulfur dioxide of 500ppm in simulated flue gas, then composite catalyst was 94% to the catalytic conversion efficiency of nonvalent mercury.
Control experiment 1: the manganese nitrate solution of only getting 3g 50% adds deionized water and is diluted to 20ml and makes dipping solution, adopts catalyst carrier and preparation process same as described above, makes the required single component catalyst of control experiment 1.
Take by weighing the above-mentioned single component catalyst of 2g and insert in the tubular fixed-bed reactor, feeding contains nonvalent mercury 100 μ g/m
3With oxidant HCl concentration be the simulated flue gas of 10ppm.Temperature is that 150 ℃, air speed are 10000h
-1Condition under, the transformation efficiency of nonvalent mercury only is 75%.Other condition is constant, only the operating temperature of reactor is reduced to 100 ℃, and single component catalyst reduces to 57% to the catalytic conversion efficiency of nonvalent mercury.Operating temperature still is 150 ℃, and when other condition was constant, when adding the sulfur dioxide of 500ppm in simulated flue gas, then composite catalyst only was 48% to the catalytic conversion efficiency of nonvalent mercury.
Control experiment 2: get manganese nitrate solution, the 0.5g anhydrous nitric acid copper of 3g 50%, add deionized water and be diluted to 20ml and make dipping solution, adopt catalyst carrier and preparation process same as described above, make the required non-impurity-doped catalyst of control experiment 2.
Take by weighing the above-mentioned non-impurity-doped catalyst of 2g and insert in the tubular fixed-bed reactor, feeding contains nonvalent mercury 100 μ g/m
3With oxidant HCl concentration be the simulated flue gas of 10ppm.Temperature is that 150 ℃, air speed are 10000h
-1Condition under, the transformation efficiency of nonvalent mercury only is 83%.Other condition is constant, only the operating temperature of reactor is reduced to 100 ℃, and single component catalyst reduces to 66% to the catalytic conversion efficiency of nonvalent mercury.Operating temperature still is 150 ℃, and when other condition was constant, when adding the sulfur dioxide of 500ppm in simulated flue gas, then composite catalyst only was 61% to the catalytic conversion efficiency of nonvalent mercury.
Control experiment is the result show, compares with the one pack system Mn catalyst, and with copper, manganese is compound can improve activity of such catalysts to a certain extent, and after molybdenum was doped to copper-composite catalyst, activity of such catalysts can significantly improve.
Embodiment 2
With the main catalytic component change the oxide of cobalt into, oxide, the doped chemical that compounding ingredients changes iron into changes elemental tungsten into, catalyst carrier changes Powdered activated alumina (granular size is 40 orders) into.
Get 2.3g cobalt nitrate hexahydrate, 0.95g nine water ferric nitrates, 0.1g five tungstic acid hydrate ammonia, add deionized water and be diluted to 20ml and make dipping solution; Utilize Powdered activated alumina as catalyst carrier, take by weighing 20g and immerse above-mentioned solution; Soak and after 4 hours unnecessary maceration extract is poured out, alumina powder has absorbed the maceration extract of 8g approximately; Alumina powder behind the dipping was dried 6 hours under 60 ℃ temperature, rose to 300 ℃ of roastings 1 hour with 5 ℃/minute of heating rates in the transposition Muffle furnace; Rising to 400 ℃ of roastings with 2 ℃/minute speed made presoma nitrate fully decompose in 4 hours; With 2 ℃/minute cooldown rate catalyst is cooled to normal temperature again, makes cobalt-Fe compound type catalyst that tungsten mixes, wherein, the content of cobalt on catalyst is 2.5%, and the mol ratio of element cobalt, iron and tungsten is 1: 0.3: 0.05.
Get the cobalt-iron composite catalyst of the above-mentioned tungsten doping of 2g and insert in the tubular fixed-bed reactor, feeding contains nonvalent mercury 100 μ g/m
3With oxidant HCl concentration be the flue gas of 10ppm.Temperature is that 100 ℃, air speed are 30000h
-1Condition under, when catalyst reaches stably catalyzed stage, catalyst to the transformation efficiency of nonvalent mercury near 100%.The sulfur dioxide that contains 500ppm in flue gas, above-mentioned catalyst is 96% to the oxidation efficiency of nonvalent mercury.
Embodiment 3
Select for use the oxide of manganese and the oxide of cobalt, oxide, the mixed modified component that compounding ingredients is selected zirconium for use to select vanadium for use, catalyst carrier choice of powder shape titanium dioxide (granular size is 60 orders, based on anatase) simultaneously the main catalytic component.
Get 13g 50% manganese nitrate, 10.5g cobalt nitrate hexahydrate, 6.15g zirconium nitrate, 0.42g ammonium metavanadate, add deionized water and be diluted to 20ml and make dipping solution; Utilize titania powder as catalyst carrier, take by weighing 20g and immerse above-mentioned solution; Soak and after 4 hours unnecessary maceration extract is poured out, titania powder has absorbed the maceration extract of 6g approximately; Titania powder behind the dipping was dried 6 hours under 60 ℃ temperature, rose to 300 ℃ of roastings 1 hour with 5 ℃/minute of heating rates in the transposition Muffle furnace; Rising to 400 ℃ of roastings with 2 ℃/minute speed fully decomposed presoma in 4 hours; With 2 ℃/minute cooldown rate catalyst is cooled to normal temperature again, makes required catalyst, wherein, cobalt and the manganese content on catalyst respectively is 3%, and the mol ratio of element cobalt, manganese, zirconium and vanadium is 1: 1: 0.5: 0.1.
The method that is provided according to embodiment 1 is investigated catalytic effect, and the result shows: when no sulfur dioxide, catalyst to the transformation efficiency of nonvalent mercury near 100%; When sulfur dioxide concentration was 500ppm, catalyst was 94% to the clearance of nonvalent mercury.
Embodiment 4
Get 15g concentration and be 50% manganese nitrate solution, 2g nitrate trihydrate copper, 0.9g five water nitric acid molybdenums, add deionized water and be diluted to 20ml and make dipping solution; Utilize cylindrical ceramic honey comb as catalyst carrier, the cylindrical ceramic honey comb of cut-off footpath 50mm, length 80mm immerses above-mentioned solution; Soak and after 4 hours unnecessary maceration extract is poured out, ceramic honey comb has absorbed the maceration extract of 3g approximately; Ceramic honey comb behind the dipping was dried 6 hours under 60 ℃ temperature, rose to 300 ℃ of roastings 1 hour with 5 ℃/minute of heating rates in the transposition Muffle furnace; Rise to 400 ℃ of roastings 4 hours with 2 ℃/minute speed; With 2 ℃/minute cooldown rate catalyst is cooled to normal temperature again, makes manganese-copper composite catalyst that molybdenum mixes, the amount of contained Mn oxide is 3%, and the mol ratio of element manganese, copper and molybdenum is 1: 0.2: 0.05.Get 5 of above-mentioned catalyst, series connection is used in reactor.
The actual flue gas that uses coal-burning boiler to produce, wherein the content of sulfur dioxide is about 800g/m
3, the content of nonvalent mercury is about 20 μ g/m
3, HCl content is 15ppm.Get 5m
3The exhaust gas volumn of/h feeds above-mentioned reactor, and the temperature of reactor keeps 150 ℃.The result shows that in preceding 5 hours, catalyst is 93% to the catalytic oxidation efficient of nonvalent mercury; As time goes on, catalyst has good stability, continuous operation 80 hours, and the transformation efficiency of nonvalent mercury also can remain on about 90%.
Claims (4)
1, the preparation method of the mixed compound catalyst of nonvalent mercury oxidation in a kind of catalysis flue gas is characterized in that comprising the steps:
1) gets in the oxide of oxide, cobalt of manganese one or both as the main catalytic component, get the oxide of oxide, the zirconium of oxide, the iron of copper, in the titanyl compound one or more as compounding ingredients, get in molybdenum, tungsten, the vanadium one or more as mixed modified component; Respectively the pairing separately presoma of main catalytic component, compounding ingredients and mixed modified component 1: 0.1 in molar ratio～1: 0.01～0.1 is mixed, add water and stir, obtain containing main catalytic constituent mass mark and be 0.5～30% dipping solution;
2) catalyst carrier is immersed in the above-mentioned dipping solution stir; Dip time is 2-6 hour; Catalyst carrier after will flooding after the Separation of Solid and Liquid was dried 5-24 hour under 40 ℃～100 ℃ temperature;
3) in the catalyst carrier transposition Muffle furnace after will drying, be 1～30 ℃/minute with heating rate and rise to 300 ℃ of roastings 0.5～2 hour, rise to 400 ℃ of roastings 0.5～4 hour with 1～30 ℃/minute heating rate, be cooled to normal temperature with 1～2 ℃/minute cooldown rate again, make mixed compound catalyst.
2,, it is characterized in that described presoma is one or more in the nitrate, carbonate, oxalates, acetate of metal according to the preparation method of the mixed compound catalyst of nonvalent mercury oxidation in the catalysis flue gas of claim 1.
3, according to the preparation method of the mixed compound catalyst of nonvalent mercury oxidation in the catalysis flue gas of claim 1, it is characterized in that described catalyst carrier is one or more in aluminium oxide, titanium dioxide, silica, molecular sieve, imvite, the active carbon, the catalyst carrier form is spherical, graininess, tabular or cellular.
4, utilize the application of mixed compound catalyst of the method preparation of claim 1, it is characterized in that being used for the catalytic oxidation of coal-fired flue-gas nonvalent mercury.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009100528967A CN101574660A (en) | 2009-06-11 | 2009-06-11 | Method for preparing mixed compound catalyst used for catalyzing null-valence mercury in flue-gas to be oxidized |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009100528967A CN101574660A (en) | 2009-06-11 | 2009-06-11 | Method for preparing mixed compound catalyst used for catalyzing null-valence mercury in flue-gas to be oxidized |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101574660A true CN101574660A (en) | 2009-11-11 |
Family
ID=41269810
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2009100528967A Pending CN101574660A (en) | 2009-06-11 | 2009-06-11 | Method for preparing mixed compound catalyst used for catalyzing null-valence mercury in flue-gas to be oxidized |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101574660A (en) |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102266769A (en) * | 2011-06-14 | 2011-12-07 | 张丽莉 | Catalyst applied to synchronous denitration and demercuration and preparation method thereof |
| CN101699252B (en) * | 2009-11-12 | 2012-03-07 | 上海交通大学 | Method for measuring total mercury in flue gas |
| CN102698753A (en) * | 2012-05-15 | 2012-10-03 | 中国科学院过程工程研究所 | Catalyst for mercury oxidation and preparation method and purpose thereof |
| CN102764655A (en) * | 2011-12-23 | 2012-11-07 | 盐城工学院 | Novel demercuration catalyst |
| CN102814180A (en) * | 2012-06-07 | 2012-12-12 | 盐城工学院 | Attapulgite carrier catalyst for oxidation of elemental mercury in flue gas and preparation method thereof |
| CN102872871A (en) * | 2012-09-20 | 2013-01-16 | 广东电网公司电力科学研究院 | Catalytic agent for catalytic oxidation of elemental mercury in coal-fired flue gas and preparation method thereof |
| CN103084165A (en) * | 2013-01-23 | 2013-05-08 | 广东电网公司电力科学研究院 | Demercuration catalyst for elemental mercury in oxidated coal-fired flue gas and preparation method thereof |
| CN103111128A (en) * | 2013-02-22 | 2013-05-22 | 广东电网公司电力科学研究院 | Dust-removal mercury-removal filter bag for bag-type dust remover and preparation method of filter bag |
| CN103547356A (en) * | 2011-06-30 | 2014-01-29 | 环球油品公司 | Processes and apparatuses for oxidizing elemental mercury in flue gas using oxychlorination catalysts |
| CN103648636A (en) * | 2011-08-15 | 2014-03-19 | 英派尔科技开发有限公司 | Oxalate sorbents for mercury removal |
| CN104028265A (en) * | 2014-05-28 | 2014-09-10 | 淮阴工学院 | Attapulgite-based catalyst for removing elemental mercury in smoke |
| WO2014201782A1 (en) * | 2013-06-18 | 2014-12-24 | 广州博能能源科技有限公司 | Mercury-removing agent and preparation method therefor |
| CN105126604A (en) * | 2015-07-06 | 2015-12-09 | 华能国际电力股份有限公司 | Method for oxidizing elemental mercury of coal-fired flue gas |
| CN107899543A (en) * | 2017-11-29 | 2018-04-13 | 太原理工大学 | A kind of vanadium copper is modified demercuration sorbing material and its preparation method and application |
| CN109200812A (en) * | 2018-11-19 | 2019-01-15 | 中南大学 | A kind of method of gaseous mercury in cobalt sulfide/biomass carbon composite material catalytic oxidative desulfurization flue gas |
| CN112619595A (en) * | 2020-12-18 | 2021-04-09 | 武汉大学 | Attapulgite-based regenerable flue gas demercuration adsorbent and preparation method thereof |
-
2009
- 2009-06-11 CN CNA2009100528967A patent/CN101574660A/en active Pending
Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101699252B (en) * | 2009-11-12 | 2012-03-07 | 上海交通大学 | Method for measuring total mercury in flue gas |
| CN102266769A (en) * | 2011-06-14 | 2011-12-07 | 张丽莉 | Catalyst applied to synchronous denitration and demercuration and preparation method thereof |
| CN103547356A (en) * | 2011-06-30 | 2014-01-29 | 环球油品公司 | Processes and apparatuses for oxidizing elemental mercury in flue gas using oxychlorination catalysts |
| CN103648636A (en) * | 2011-08-15 | 2014-03-19 | 英派尔科技开发有限公司 | Oxalate sorbents for mercury removal |
| CN102764655A (en) * | 2011-12-23 | 2012-11-07 | 盐城工学院 | Novel demercuration catalyst |
| CN102764655B (en) * | 2011-12-23 | 2015-03-04 | 盐城工学院 | Demercuration catalyst |
| CN102698753A (en) * | 2012-05-15 | 2012-10-03 | 中国科学院过程工程研究所 | Catalyst for mercury oxidation and preparation method and purpose thereof |
| CN102698753B (en) * | 2012-05-15 | 2014-09-24 | 中国科学院过程工程研究所 | Catalyst for mercury oxidation and preparation method and purpose thereof |
| CN102814180A (en) * | 2012-06-07 | 2012-12-12 | 盐城工学院 | Attapulgite carrier catalyst for oxidation of elemental mercury in flue gas and preparation method thereof |
| CN102814180B (en) * | 2012-06-07 | 2017-12-22 | 盐城工学院 | For attapulgite carrier catalyst for oxidation of elemental mercury in flue gas and preparation method thereof |
| CN102872871A (en) * | 2012-09-20 | 2013-01-16 | 广东电网公司电力科学研究院 | Catalytic agent for catalytic oxidation of elemental mercury in coal-fired flue gas and preparation method thereof |
| CN103084165A (en) * | 2013-01-23 | 2013-05-08 | 广东电网公司电力科学研究院 | Demercuration catalyst for elemental mercury in oxidated coal-fired flue gas and preparation method thereof |
| CN103111128A (en) * | 2013-02-22 | 2013-05-22 | 广东电网公司电力科学研究院 | Dust-removal mercury-removal filter bag for bag-type dust remover and preparation method of filter bag |
| WO2014201782A1 (en) * | 2013-06-18 | 2014-12-24 | 广州博能能源科技有限公司 | Mercury-removing agent and preparation method therefor |
| CN104028265A (en) * | 2014-05-28 | 2014-09-10 | 淮阴工学院 | Attapulgite-based catalyst for removing elemental mercury in smoke |
| CN104028265B (en) * | 2014-05-28 | 2015-10-28 | 淮阴工学院 | The attapulgite removed for Elemental Mercury in flue gas is catalyst based |
| CN105126604A (en) * | 2015-07-06 | 2015-12-09 | 华能国际电力股份有限公司 | Method for oxidizing elemental mercury of coal-fired flue gas |
| CN107899543A (en) * | 2017-11-29 | 2018-04-13 | 太原理工大学 | A kind of vanadium copper is modified demercuration sorbing material and its preparation method and application |
| CN107899543B (en) * | 2017-11-29 | 2020-06-16 | 太原理工大学 | Vanadium-copper modified demercuration adsorption material and preparation method and application thereof |
| CN109200812A (en) * | 2018-11-19 | 2019-01-15 | 中南大学 | A kind of method of gaseous mercury in cobalt sulfide/biomass carbon composite material catalytic oxidative desulfurization flue gas |
| CN109200812B (en) * | 2018-11-19 | 2020-05-15 | 中南大学 | Method for removing gaseous mercury in flue gas by catalytic oxidation of cobalt sulfide/biomass charcoal composite material |
| CN112619595A (en) * | 2020-12-18 | 2021-04-09 | 武汉大学 | Attapulgite-based regenerable flue gas demercuration adsorbent and preparation method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101574660A (en) | Method for preparing mixed compound catalyst used for catalyzing null-valence mercury in flue-gas to be oxidized | |
| Li et al. | Preferred enhancement of fast-SCR by Mn/CeSiOx catalyst: Study on Ce/Si promotion and shape dependence | |
| Kang et al. | Insights into the co-doping effect of Fe3+ and Zr4+ on the anti-K performance of CeTiOx catalyst for NH3-SCR reaction | |
| CN101829573B (en) | Composite oxidant SCR (Selective Catalytic Reduction) denitrating catalyst, preparation method and applications thereof | |
| Chen et al. | Effect of MnO2 crystal types on CeO2@ MnO2 oxides catalysts for low-temperature NH3-SCR | |
| CN102513123B (en) | Rare-earth perovskite type catalyst for treating industrial waste gas as well as preparation method and application thereof | |
| CN101602018B (en) | Method for preparing rare-earth element doped composite metal oxide mercury removal catalyst | |
| CN104474890B (en) | A kind of method of Engineering of Supported Metal Oxide Catalysts catalysis Direct Resolution NO denitration | |
| JP6595088B2 (en) | SCR catalyst for removing nitrogen oxides and method for producing the same | |
| CN109999829A (en) | A kind of bimetallic manganese iron low temperature SCR denitration catalyst, preparation method and applications | |
| CN101745405A (en) | Perovskite type composite oxide catalyst for purifying tail gas of internal combustion engine | |
| CN109351358A (en) | A kind of transition metal oxide composite catalyst and its preparation method and application | |
| WO2020179891A1 (en) | Denitration catalyst and method for manufacturing same | |
| CN110605114A (en) | Application of mullite oxide supported catalyst in low-temperature selective catalytic reduction denitration | |
| CN101972652A (en) | Preparation method of compound SCR catalyst with zero-valent mercury conversion function | |
| CN110124710B (en) | Composite metal oxide catalyst and preparation method thereof | |
| CN113694933A (en) | High-entropy co-doped low-temperature SCR denitration catalyst and preparation method and application thereof | |
| CN102068994A (en) | Catalyst and preparation method thereof | |
| CN102091616B (en) | Preparation method of ruthenium-containing composite catalyst used for catalytic oxidation of zero-valent mercury | |
| CN107185523A (en) | Preparation method of denitrating catalyst that a kind of holmium is modified and products thereof | |
| CN108355606B (en) | Low-temperature NOx adsorption catalyst with good water resistance and preparation method thereof | |
| CN104028265A (en) | Attapulgite-based catalyst for removing elemental mercury in smoke | |
| Long et al. | Promotional effects of Nb5+ and Fe3+ co-doping on catalytic performance and SO2 resistance of MnOx-CeO2 low-temperature denitration catalyst | |
| CN108745369A (en) | A kind of B doping type double-perovskite catalyst and the preparation method and application thereof | |
| CN102179252B (en) | Cu/CeOx-TiO2 catalyst for selective catalytic oxidization of ammonia and preparation method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20091111 |