CN102068905B - Catalyst for removing dioxin substance in flue gas and preparation method thereof - Google Patents
Catalyst for removing dioxin substance in flue gas and preparation method thereof Download PDFInfo
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Abstract
The invention discloses a catalyst for removing a dioxin substance in flue gas and a preparation method thereof. The method comprises the following steps of: soaking a honeycomb monomer which contains catalyst components such as TiO2, V2O5 and WO3 in oxalic acid vanadium solution; and drying and calcining so as to obtain the catalyst. In the method, only the oxalic acid vanadium solution is taken as soaking solution, is easy to prepare, has low toxicity, and is beneficial to the realization of industrial application. A production process is simple, can be directly applied to a drying furnace and a calcining furnace for secondary drying and secondary calcining, temperatures required by secondary drying and secondary calcining are low, secondary drying time and secondary calcining time are short, and production cost is saved; the catalyst produced by the method hardly has any micro crack and has very high catalyst activity at the temperature of between 150 DEG C and 330 DEG C; and dioxin removing efficiency is up to 99.5 percent in maximum.
Description
Technical field
The invention belongs to catalyst research and make the field; Especially the catalyst and the manufacturing approach that belong to a kind of highly active catalytic oxidation removal flue gas Zhong dioxins materials; Be about urban domestic garbage incinerator waste gas, danger wastes such as Biohazard Waste incinerator waste gas, steel and iron industry waste gas, remove the honeycomb fashion catalyst of dioxin technology and its manufacturing approach based on catalytic oxidation.
Background technology
At present, the vent gas treatment technology of the flue gas Zhong dioxin of urban domestic garbage incinerator, danger wastes such as generations such as Biohazard Waste incinerator, steel and iron industry mainly contains: charcoal absorption technology, oxidation catalyst filter are technological, plasma high-temperature decomposition technique, catalytic oxidation technology or the like.
The principle of charcoal absorption technology is to utilize the suction-operated of active carbon to remove bioxin, promptly in flue, sprays active carbon powder or adopts the ADSORPTION IN A FIXED BED technology.This method belongs to physical adsorption process, fails to reduce the toxicity of adsorbent Zhong bioxin, and adsorbent and flue dust must recycle and carry out the secondary high temperature incineration.This method is simple to operate, but causes secondary pollution easily, and operating cost is high, if misoperation has the danger of catching fire.
The oxidation catalyst filter technology is the technology that catalytic decomposition that Gore company puts forward combines with bag-type dust.The REMEDIA oxidation catalyst filter system of Gore company exploitation adopts the incorporate design philosophy of dedusting catalytic decomposition, organic micro-pollutants such as catalytic decomposition polycyclic aromatic hydrocarbon, bioxin in dedusting.This method (160～260 ℃) is at a lower temperature removed gas-solid Tai bioxin and dust simultaneously, and flying dust Zhong bioxin content is low, non-secondary pollution.But this method concentration of treatment scope is narrower, and inlet gas Zhong bioxin concentration has certain restriction.
The plasma high-temperature decomposition technique is to adopt the very high hot plasma of energy density to handle the method for pollutant.Dioxins materials at first is dissociated into state of atom under the argon-arc plasma field effect, get into pyrolysis furnace through blender then and be reassembled as hydrogen, carbon monoxide, hydrogen chloride and carbon granule, realizes effectively removing the purpose of bioxin.The advantage of this method is that reaction speed is fast, reactor volume is little, tail is narrow-minded, can also reclaim imflammable gas and slag simultaneously, reduces operating cost; Shortcoming is that energy consumption is high, high to the requirement of refractory material and insulation material, control technology is complicated.At present, this technology has had commercial applications in developed country, and at home because technology and cost aspect also are in the starting stage.
The catalytic oxidation technology is meant under oxidation environment, and in the certain reaction temperature range, Yu bioxin carries out the contact oxidation reaction, the Shi bioxin is decomposed and generates CO by the activity site of catalyst surface
2, H
2The technology of mineral products such as O, HCl.This technology adopts to have and removes nitrogen oxide simultaneously with the SCR of dioxin function (SCR) reaction system; And the SCR reactor is arranged in after the terminal sack cleaner; Can adopt the catalytic oxidation reaction device that removes bioxin separately, need not add other oxidants this moment yet.This method is safe, can decompose bioxin fully, and treatment effeciency is high, and environment protecting is obvious, and the concentration of treatment scope is wider, and operating cost is low.
The SCR reaction system adopts the honeycomb fashion catalyst usually, and the base material of catalyst is TiO
2(titanium white powder), active component V
2O
5, WO
3, the monolithic extruded moulding of honeycomb monomer, entire body has catalytic activity, and microcosmic is a gap structure.
At present, adopt catalytic oxidative desulfurization dioxin technology to have very wide range of commercial use in developed countries such as America and Europes, and domestic still be at the early-stage in this field.Along with the formulation of China about the laws and regulations of house refuse, danger wastes and Biohazard Waste burning; More and more stricter to the emission control of flue gas bioxin; Catalytic oxidative desulfurization dioxin technology will be widely used as the treatment technology the most ripe, that security reliability is the highest.In this technological commercial application, what play the role of a nucleus is to remove the dioxin catalyst.
Remove (like United States Patent (USP) United States Patent 6475952) in the existing related patent U.S. Patent No. of dioxin catalyst in the catalytic oxidation technology, ubiquity catalyst soakage solution composition complicated (dipping solution is two kinds of the sulfuric acid solutions of titanium and vanadium), dipping be baking temperature higher (250-400 ℃), calcining heat higher (500-600 ℃), the lower shortcomings such as (the lowest activity temperature are a little less than 250 ℃) of activity afterwards.
Summary of the invention
The invention discloses a kind of catalyst and manufacturing approach thereof that removes flue gas Zhong dioxins materials; First problem that the present invention will solve provides a kind of catalyst of highly active catalytic oxidation removal flue gas Zhong dioxins materials, and second problem that the present invention will solve provides a kind of manufacturing approach that removes flue gas Zhong dioxins materials catalyst.
The present invention realizes through following technical scheme:
A kind of catalyst that removes flue gas Zhong dioxins materials is characterized in that: will contain catalyst component TiO
2, V
2O
5, WO
3The honeycomb fashion monomer after the vanadium oxalate solution impregnation, carry out drying and calcining again and make.
Further said catalyst is with containing catalyst component TiO
2, V
2O
5, WO
3The calcining monomer, make according to the following steps:
(1) monomer is immersed in the vanadium oxalate solution of 65～135g/L fully, dip time is 0.5～3h;
(2) from vanadium oxalate solution, take out and drain, the time of draining is 30～90min.;
(3) put into drying oven and carry out dried, baking temperature is 60～100 ℃;
(4) put into calcining furnace and calcine, calcining heat is 300～550 ℃, makes catalyst.
The said manufacturing approach that removes flue gas Zhong dioxins materials catalyst may further comprise the steps:
(1) will contain catalyst component TiO
2, V
2O
5, WO
3The calcining monomer be immersed in fully in the vanadium oxalate solution of 65～135g/L, dip time is 0.5～3h;
(2) from vanadium oxalate solution, take out, drain, the time of draining is 30～90min.;
(3) put into drying oven and carry out dried, baking temperature is 60～100 ℃;
(4) put into calcining furnace and calcine, calcining heat is 300～550 ℃, makes catalyst.
In order to improve activity of such catalysts and to guarantee behind redrying and secondary clacining, not produce micro-crack, flood concentration with vanadium oxalate solution and remain in 65～135g/L scope and be advisable.If concentration is lower than lower limit, activity component concentration is low excessively in the maceration extract, and the catalyst activity property improvement is little, and big water gaging is evaporated the thermal stress that is produced and can makes catalyst produce micro-crack in redrying and secondary clacining process; If concentration surpasses higher limit, activity component concentration is too high in the maceration extract, and the active component vanadium oxalate very easily crystallizes out in the maceration extract, and can be because of catalyst component (TiO
2, V
2O
5, WO
3) produce micro-crack with the shrinkage factor difference of maceration extract active ingredient in the secondary clacining process.Therefore, to remain in 65～135g/L scope be appropriate to impregnation concentration.
Simultaneously, improve activity of such catalysts and also guarantee not produce micro-crack, the dip time of catalyst monomer in maceration extract remains on was advisable in 0.5～3 hour.If dip time is lower than 0.5 hour, active component does not infiltrate in the catalyst pores as yet fully in the maceration extract, and catalyst activity improves not obvious; If dip time surpasses 3 hours, then maceration extract is superfluous in the catalyst pores, and the thermal stress that superfluous maceration extract is evaporated generation in the secondary clacining process can make catalyst produce micro-crack equally.
Dipping also must drain 30～90min. after accomplishing, otherwise in the secondary clacining process, can produce micro-crack because the local impregnation concentration of catalyst is too high.If but drained overlong time, could occupy big quantity space, and reduce production efficiency.Experiment showed, that the time of draining is advisable with 30～90min..
Compared with prior art the present invention has following beneficial effect:
1. only use a kind of vanadium oxalate solution as dipping solution, preparation is simple, and vanadium exists with positive tetravalence attitude in the vanadium oxalate solution, and toxicity is very low, helps realizing commercial Application;
2. production technology of the present invention is simple, can directly use drying oven and calcining furnace to carry out redrying and secondary clacining, and the temperature of required redrying, secondary clacining is lower, the time is shorter, saves production cost;
3. the catalyst of the present invention's production does not almost have micro-crack, and simultaneously very high 150～330 ℃ of temperature range inner catalyst activity, Dui bioxin removal efficiency reaches as high as 99.5%.
The specific embodiment
Below, according to embodiment the present invention is specified, but scope of the present invention is not limited to following embodiment.
Embodiment 1
To contain catalyst component (TiO
2, V
2O
5, WO
3) calcining monomer (this catalyst calcination monomer manufacturing approach is a prior art) sawing become specific length (demands of different of taking off dioxin engineering project flue gas condition according to difference, general sawing length is between 300-1100mm), follow these steps to make catalyst:
(1) monomer is immersed in the vanadium oxalate solution of 110g/L fully, dip time is 1h;
(2) from vanadium oxalate solution, take out and drain, the time of draining is 60min.;
(3) put into drying oven and carry out dried, baking temperature is 90 ℃, and the time is 2h;
(4) put into calcining furnace and calcine, calcining heat is 350 ℃, and the time is 3h, makes catalyst.
Embodiment 2
The vanadium oxalate impregnation concentration is adjusted into 135g/L, and other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Embodiment 3
The vanadium oxalate impregnation concentration is adjusted into 100g/L, and other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Embodiment 4
The vanadium oxalate impregnation concentration is adjusted into 65g/L, and other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Embodiment 5
Dip time is adjusted into 0.5h, and other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Embodiment 6
Dip time is adjusted into 2h, and other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Embodiment 7
Dip time is adjusted into 3h, and other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Embodiment 8
To the time of draining be adjusted into 30min., other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Embodiment 9
To the time of draining be adjusted into 45min., other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Embodiment 10
To the time of draining be adjusted into 90min., other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Comparative example 1 (the vanadium oxalate impregnation concentration is lower than the requirement of normal concentration scope lower limit)
The vanadium oxalate impregnation concentration is adjusted into 60g/L, and other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Comparative example 2 (the vanadium oxalate impregnation concentration is higher than the requirement of normal concentration scope lower limit)
The vanadium oxalate impregnation concentration is adjusted into 140g/L, and other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Comparative example 3 (vanadium oxalate maceration extract dip time does not satisfy regulation dip time lower limit and requires)
Dip time is adjusted into 20min., and other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Comparative example 4 (the dipping back monomer time that drains does not satisfy regulation and drains time lower limit requirement)
To the time of draining be adjusted into 20min., other conditions and drying, calcination process are the same with embodiment 1, make catalyst.
Comparative example 5 (the calcining monomer is convection drying, calcining without vanadium oxalate maceration extract dipping)
Contain catalyst component (TiO after will calcining
2, V
2O
5, WO
3) the honeycomb monomer, through vanadium oxalate maceration extract dipping operation, directly be placed in the drying oven 90 ℃ of dryings 2 hours, be placed in the calcining furnace 350 ℃ of calcinings 3 hours again, make catalyst.
To get the inwall fritter at same position with the catalyst that comparative example 1～5 is made according to embodiment 1～10, adopt the face crack situation of sem observation catalyst.
Meanwhile, catalyst being installed in flue gas flow is 10000m
3/ h, flue-gas temperature is 200 ℃, inlet dioxin concentration is 0.4ng TEQ/m
3, oxygen concentration is that the question response device is sampled to exhanst gas outlet after stablizing 24 hours in 11% the smoke reaction device, bioxin concentration in the test outlet flue gas.
Result of the test
Above-mentioned various catalyst micro-crack situation and Tuo dioxin The performance test results are listed in following table 1:
Table 1: various catalyst performance test results
Catalyst as shown in table 1, as to utilize the embodiment of the invention 1～10 to produce does not almost have or only has a small amount of micro-crack in the catalyst inner wall surface.At the comparative example 1,2 that the vanadium oxalate impregnation concentration is adjusted into 60g/L, 140g/L, perhaps dip time is reduced to the comparative example 4 of 20min., all seen more micro-crack in the catalyst inner wall surface.But do not pass through in the comparative example 5 of vanadium oxalate maceration extract impregnation process will draining comparative example 3 and the catalyst monomer that time decreased is 20min., almost do not see micro-crack.Simultaneously, in removing the experiment of dioxin flue gas, the catalyst exhanst gas outlet bioxin concentration that the embodiment of the invention 1～10 is produced is all less than 0.1ng TEQ/m
3, satisfy European Union's discharge standard; And the catalyst exhanst gas outlet bioxin concentration that comparative example 1,3,5 is produced is all greater than 0.1ngTEQ/m
3
Can confirm according to above-mentioned test, utilize method of the present invention can make highly active catalytic oxidative desulfurization bioxin catalyst.And can confirm that the concentration of vanadium oxalate maceration extract was advisable in the scope at 30～90 minutes 0.5～3 hour, the time that drains at 65～135g/L, dip time.
Claims (2)
1. a catalyst that removes dioxins materials in the flue gas is characterized in that: will contain catalyst component TiO
2, V
2O
5, WO
3The honeycomb fashion monomer after the vanadium oxalate solution impregnation, carry out drying and calcining again and make; Concrete steps are:
(1) monomer is immersed in the vanadium oxalate solution of 65～135g/L fully, dip time is 0.5～3h;
(2) from vanadium oxalate solution, take out and drain, the time of draining is 30～90min.;
(3) put into drying oven and carry out dried, baking temperature is 60～100 ℃;
(4) put into calcining furnace and calcine, calcining heat is 300～550 ℃, makes catalyst.
2. manufacturing approach that removes dioxins materials catalyst in the flue gas is characterized in that may further comprise the steps:
(1) will contain catalyst component TiO
2, V
2O
5, WO
3The calcining monomer be immersed in fully in the vanadium oxalate solution of 65～135g/L, dip time is 0.5～3h;
(2) from vanadium oxalate solution, take out, drain, the time of draining is 30～90min.;
(3) put into drying oven and carry out dried, baking temperature is 60～100 ℃;
(4) put into calcining furnace and calcine, calcining heat is 300～550 ℃, makes catalyst.
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Families Citing this family (9)
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| CN102794107A (en) * | 2012-08-31 | 2012-11-28 | 中持依迪亚（北京）环境研究所有限公司 | Method and system for catalyzing and degrading dioxin |
| CN102974405A (en) * | 2012-12-04 | 2013-03-20 | 成都东方凯特瑞环保催化剂有限责任公司 | SCR (selective catalytic reduction) denitration catalyst regenerated liquid and preparation and regeneration methods thereof |
| CN103495417B (en) * | 2013-09-30 | 2016-02-03 | 山东爱亿普环保科技有限公司 | Denitrating flue gas Tuo bioxin special cermacis Catalysts and its preparation method |
| CN104324717B (en) * | 2013-12-19 | 2019-03-05 | 南京环境再生能源有限公司 | Remove the catalyst and preparation method thereof of dioxin in waste incineration furnace exhaust |
| CN103657638B (en) * | 2013-12-31 | 2015-09-23 | 重庆远达催化剂制造有限公司 | Zheng body Shi bioxin Removal of catalyst and preparation method thereof |
| CN104801296A (en) * | 2015-04-13 | 2015-07-29 | 宜兴市宜刚环保工程材料有限公司 | Novel dioxin removing catalyst and preparation method thereof |
| CN106391096A (en) * | 2016-08-19 | 2017-02-15 | 四川天壹环保科技有限公司 | Monolithic catalyst for catalytic degradation of flue gas dioxin from small-sized household refuse incinerator and preparation method thereof |
| CN107497094A (en) * | 2017-06-20 | 2017-12-22 | 青岛理工大学 | Method for treating waste incineration fly ash by using biogas residues |
| CN107583433A (en) * | 2017-09-30 | 2018-01-16 | 中晶蓝实业有限公司 | Flue gas integral treatment method |
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