CN106362582A - Method and apparatus for catalytic oxidation treatment of ammonia-containing exhaust gas - Google Patents
Method and apparatus for catalytic oxidation treatment of ammonia-containing exhaust gas Download PDFInfo
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Abstract
The invention relates to a method for catalytic oxidation treatment of ammonia-containing exhaust gas. An apparatus for enforcing the method comprises a heat exchange system, a heating system and a catalytic oxidation system. Ammonia is oxidized in the catalytic oxidation system by adopting a catalyst including several substances of CuO, CeO2, ZrO2, Al2O3, SiO2 and Fe2O3 in order to generate nitrogen and water, and reacted high temperature gas exchanges heat with gas to be reacted in the heat exchange system to preheat the gas to be reacted and cool discharge flue gas in order to fully recycle the heat of the flue gas. The method has the advantages of high ammonia gas purifying efficiency, no secondary pollution, low energy consumption and wide application range.
Description
Technical field
The invention belongs to industrial waste gas Treatment process field is and in particular to a kind of catalytic oxidation treatment ammonia-contaminated gas
Method and device, for purifying industrial waste gas containing ammonia.
Background technology
Ammonia is a kind of important industrial chemicals, is widely used in synthesizing the industries such as ammonia, chemical fertilizer, pharmacy, fuel；
Ammonia is also typical industrial waste gas simultaneously, easily causes serious harm to health and environment.In recent years,
With the industrialized continuous development of society, the demand of ammonolysis product is continuously increased, causes increasingly severe simultaneously
Ammonia pollution.
At present the conventional administering method of industrial waste gas containing ammonia mainly include acid solution absorption process, strong aqua ammonia method, burning method,
The methods such as photocatalytic oxidation.But above-mentioned traditional method respectively has pluses and minuses and certain scope of application, such as acid solution
Absorption process is passed through ammonia and neutralization reaction is occurred thus removing ammonia with acid wash liquid in pickling tower, but the method
Stronger to the corrosivity of equipment, easily cause secondary pollution.Strong aqua ammonia method is used as suction by soft water or weak ammonia
Receive Absorption of Medium industrial waste gas in ammonia, by absorbing medium recycle with produce certain density, there is industry
The ammonia of using value, the product purity of the method is not high, and easily causes the heavy corrosion of equipment.Burning method
Mainly using the method that auxiliary fuel ignites, ammonia is aoxidized, the clearance of ammonia is high, but the method high energy consumption, and
Produce a certain amount of nox, cause secondary pollution serious problems.Photocatalytic oxidation energy consumption is low, does not produce secondary dirt
Dye, but the ammonia of low concentration can only be processed, limitation is big.
Content of the invention
Present invention aims to conventional art has the defect of secondary pollution, propose at a kind of catalysis oxidation
The method and device of reason ammonia-contaminated gas, the method and device do not produce secondary pollution, and equipment operating cost is low, should
Wide with scope.
In order to solve above-mentioned technical problem, the present invention proposes a kind of method of catalytic oxidation treatment ammonia-contaminated gas, adopts
With catalyst, the active component of described catalyst is cuo, ceo2、zro2、mno2One or more of,
The mass fraction of active component is 1%～10%；The carrier of described catalyst is al2o3、sio2、tio2In
One or more, the mass fraction of carrier is 90%～99%.
The present invention also proposes a kind of device of catalytic oxidation treatment ammonia-contaminated gas, comprises heating system and catalysis oxidation
System；Described heating system is used for heating ammonia-contaminated gas；Described catalytic oxidation system includes catalytic bed；Catalysis oxygen
Change reaction to carry out in catalytic bed, the active component of catalyst is cuo, ceo2、zro2、mno2In one
Plant or several, the mass fraction of active component is 1%～10%；The carrier of described catalyst is al2o3、sio2、
tio2One or more of, the mass fraction of carrier is 90%～99%.
In the present invention, the principle of catalytic oxidation treatment ammonia-contaminated gas is: ammonia and oxygen in high temperature and have catalysis
Agent participation effect is lower to be occurred to react as follows:
4nh3+3o2→2n2+6h2o
The present invention utilizes catalyst choice that ammonia catalysis oxidation is generated free of contamination nitrogen and water, ammonia simultaneously
Oxidation reaction liberated heat can reduce ability needed for reaction further, and energy consumption therefore of the present invention is low, does not produce two
Secondary pollution, this catalyst life is longer simultaneously, and is carrier using non-noble metal oxide, reduce further
Application cost.
Compared with prior art, its remarkable advantage is the present invention, and (1) catalyst of the present invention is multiple
Close oxide catalyst, be with non-noble metal oxide as raw material, ensure the decline of catalyst efficient premise
Low catalyst preparation cost；(2) catalyst light-off temperature of the present invention is 350 DEG C, i.e. ignition temperature
Degree is low, is beneficial to reduce operation energy consumption；(3) operating temperature range of catalyst of the present invention exists
Between 350～500 DEG C, that is, catalyst operating temperature scope is wide, and the strong adaptability to temperature is difficult high temperature sintering；
(4) present invention is higher than 96% to the removal efficiency of ammonia, is more than 95% to the selectivity of nitrogen, therefore to ammonia
Governance efficiency high, and do not produce secondary pollution；(5) present invention adopts the higher heat-exchange system of heat exchange efficiency,
The high-temp waste gas preheating question response gas producing after reaction can be made full use of, and then reducing energy consumption；(6) this
The heating means of bright employing are electrical heating, convert electrical energy into the heat energy of waste gas by the effect of resistance wire, plus
The thermal efficiency is high, heating system life-span length.
Brief description
Fig. 1 is the composition schematic diagram of catalytic oxidation treatment ammonia-contaminated gas device of the present invention.
Specific embodiment
Refer to the attached drawing, the present invention is described in detail in conjunction with specific embodiments.
Embodiment 1
Catalyst activity component mass fraction is 1%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 99%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 350 DEG C, the clearance of ammonia is more than 96.21%, and the selectivity of nitrogen is more than 95.62%.
Embodiment 2
Catalyst activity component mass fraction is 1%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 99%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 420 DEG C, the clearance of ammonia is more than 97.03%, and the selectivity of nitrogen is more than 96.25%.
Embodiment 3
Catalyst activity component mass fraction is 1%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 99%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 500 DEG C, the clearance of ammonia is more than 98.18%, and the selectivity of nitrogen is more than 96.82%.
Embodiment 4
Catalyst activity component mass fraction is 1%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 99%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.3s, in catalytic bed
When temperature is 350 DEG C, the clearance of ammonia is more than 96.54%, and the selectivity of nitrogen is more than 95.95%.
Embodiment 5
Catalyst activity component mass fraction is 1%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 99%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.3s, in catalytic bed
When temperature is 420 DEG C, the clearance of ammonia is more than 97.29%, and the selectivity of nitrogen is more than 96.52%.
Embodiment 6
Catalyst activity component mass fraction is 1%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 99%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.3s, in catalytic bed
When temperature is 500 DEG C, the clearance of ammonia is more than 98.33%, and the selectivity of nitrogen is more than 97.02%.
Embodiment 7
Catalyst activity component mass fraction is 1%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 99%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.5s, in catalytic bed
When temperature is 350 DEG C, the clearance of ammonia is more than 96.91%, and the selectivity of nitrogen is more than 96.22%.
Embodiment 8
Catalyst activity component mass fraction is 1%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 99%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.5s, in catalytic bed
When temperature is 420 DEG C, the clearance of ammonia is more than 97.45%, and the selectivity of nitrogen is more than 96.8%.
Embodiment 9
Catalyst activity component mass fraction is 1%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 99%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.5s, in catalytic bed
When temperature is 500 DEG C, the clearance of ammonia is more than 98.64%, and the selectivity of nitrogen is more than 97.25%.
Embodiment 10:
Catalyst activity component mass fraction is 5%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 95%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 350 DEG C, the clearance of ammonia is more than 98.12%, and the selectivity of nitrogen is more than 97.88%.
Embodiment 11:
Catalyst activity component mass fraction is 5%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 95%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 420 DEG C, the clearance of ammonia is more than 98.94%, and the selectivity of nitrogen is more than 98.66%.
Embodiment 12:
Catalyst activity component mass fraction is 5%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 95%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 500 DEG C, the clearance of ammonia is more than 99.44%, and the selectivity of nitrogen is more than 99.01%.
Embodiment 13:
Catalyst activity component mass fraction is 5%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 95%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 350 DEG C, the clearance of ammonia is more than 98.72%, and the selectivity of nitrogen is more than 98.28%.
Embodiment 14:
Catalyst activity component mass fraction is 5%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 95%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 420 DEG C, the clearance of ammonia is more than 99.24%, and the selectivity of nitrogen is more than 98.76%.
Embodiment 15:
Catalyst activity component mass fraction is 5%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 95%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 500 DEG C, the clearance of ammonia is more than 99.64%, and the selectivity of nitrogen is more than 99.21%.
Embodiment 16:
Catalyst activity component mass fraction is 5%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 95%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.5s, in catalytic bed
When temperature is 350 DEG C, the clearance of ammonia is more than 99.11%, and the selectivity of nitrogen is more than 98.58%.
Embodiment 17:
Catalyst activity component mass fraction is 5%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 95%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.5s, in catalytic bed
When temperature is 420 DEG C, the clearance of ammonia is more than 99.57%, and the selectivity of nitrogen is more than 98.96%.
Embodiment 18:
Catalyst activity component mass fraction is 5%, and active component is cuo, ceo2、zro2、mno2's
One or more, the mass fraction of carrier is 95%, and composition is al2o3、sio2、tio2Therein a kind of or
Several hopcalites；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.5s, in catalytic bed
When temperature is 500 DEG C, the clearance of ammonia is more than 99.81%, and the selectivity of nitrogen is more than 99.52%.
Embodiment 19:
Catalyst activity component mass fraction is 10%, and active component is cuo, ceo2、zro2、mno2
One or more, the mass fraction of carrier is 90%, and composition is al2o3、sio2、tio2One kind therein
Or several hopcalite；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 350 DEG C, the clearance of ammonia is more than 96.54%, and the selectivity of nitrogen is more than 95.82%.
Embodiment 20:
Catalyst activity component mass fraction is 10%, and active component is cuo, ceo2、zro2、mno2
One or more, the mass fraction of carrier is 90%, and composition is al2o3、sio2、tio2One kind therein
Or several hopcalite；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 420 DEG C, the clearance of ammonia is more than 97.33%, and the selectivity of nitrogen is more than 96.45%.
Embodiment 21:
Catalyst activity component mass fraction is 10%, and active component is cuo, ceo2、zro2、mno2
One or more, the mass fraction of carrier is 90%, and composition is al2o3、sio2、tio2One kind therein
Or several hopcalite；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.1s, in catalytic bed
When temperature is 500 DEG C, the clearance of ammonia is more than 98.08%, and the selectivity of nitrogen is more than 96.91%.
Embodiment 22:
Catalyst activity component mass fraction is 10%, and active component is cuo, ceo2、zro2、mno2
One or more, the mass fraction of carrier is 90%, and composition is al2o3、sio2、tio2One kind therein
Or several hopcalite；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.3s, in catalytic bed
When temperature is 350 DEG C, the clearance of ammonia is more than 96.84%, and the selectivity of nitrogen is more than 96.25%.
Embodiment 23:
Catalyst activity component mass fraction is 10%, and active component is cuo, ceo2、zro2、mno2
One or more, the mass fraction of carrier is 90%, and composition is al2o3、sio2、tio2One kind therein
Or several hopcalite；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.3s, in catalytic bed
When temperature is 420 DEG C, the clearance of ammonia is more than 97.59%, and the selectivity of nitrogen is more than 96.76%.
Embodiment 24:
Catalyst activity component mass fraction is 10%, and active component is cuo, ceo2、zro2、mno2
One or more, the mass fraction of carrier is 90%, and composition is al2o3、sio2、tio2One kind therein
Or several hopcalite；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.3s, in catalytic bed
When temperature is 500 DEG C, the clearance of ammonia is more than 98.39%, and the selectivity of nitrogen is more than 97.21%.
Embodiment 25:
Catalyst activity component mass fraction is 10%, and active component is cuo, ceo2、zro2、mno2
One or more, the mass fraction of carrier is 90%, and composition is al2o3、sio2、tio2One kind therein
Or several hopcalite；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.5s, in catalytic bed
When temperature is 350 DEG C, the clearance of ammonia is more than 97.15%, and the selectivity of nitrogen is more than 96.54%.
Embodiment 26:
Catalyst activity component mass fraction is 10%, and active component is cuo, ceo2、zro2、mno2
One or more, the mass fraction of carrier is 90%, and composition is al2o3、sio2、tio2One kind therein
Or several hopcalite；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.5s, in catalytic bed
When temperature is 420 DEG C, the clearance of ammonia is more than 97.63%, and the selectivity of nitrogen is more than 96.93%.
Embodiment 27:
Catalyst activity component mass fraction is 10%, and active component is cuo, ceo2、zro2、mno2
One or more, the mass fraction of carrier is 90%, and composition is al2o3、sio2、tio2One kind therein
Or several hopcalite；Catalyst amount is 10l (liter), and in reacting gas, ammonia concentration is
5200mg/m3, background gas are air, and reaction velocity is 30000h-1, the time of staying is 0.5s, in catalytic bed
When temperature is 500 DEG C, the clearance of ammonia is more than 98.81%, and the selectivity of nitrogen is more than 97.37%.
In conjunction with Fig. 1, a kind of device realizing Above-mentioned catalytic oxidation processes ammonia-contaminated gas method includes heat-exchange system
1st, heating system 2, catalytic oxidation system 3, blower fan 4.Carry out ammonia-contaminated gas purification using Fig. 1 described device
Basic implementation process as follows:
Step one, ammonia-contaminated gas are passed through heat-exchange system 1, ammonia-contaminated gas in entering heat-exchange system 1 with urge
Change high temperature purification gas (nitrogen and vapor) the generation energy exchange that oxidative system 3 produces, thus preheating contains
Ammonia waste gas；
Step 2, the ammonia-contaminated gas through preheating enter in heating system 2 and heat further, heating system 2
Using Resistant heating ammonia-contaminated gas, convert electrical energy into the heat energy of ammonia-contaminated gas thus providing the temperature of ammonia-contaminated gas
Degree；Nitrogen after cooling and vapor blower fan 4 are expelled to air；
Step 3, the ammonia-contaminated gas through heating enter in catalytic oxidation system 3, under catalyst action, ammonia
Gas is converted into high temperature nitrogen and vapor；
Step 4, through catalytic oxidation system 3 purify after produce high temperature nitrogen and vapor enter heat-exchange system with
There is reverse energy exchange in the new ammonia-contaminated gas entering, through aiutage after the temperature reduction of high temperature nitrogen and vapor
Discharge.
Since then it is achieved that containing the catalyzing, oxidizing and purifying of ammonia industrial waste gas.
Claims (9)
1. a kind of method of catalytic oxidation treatment ammonia-contaminated gas is it is characterised in that adopt catalyst, described urges
The active component of agent is cuo, ceo2、zro2、mno2One or more of, the quality of active component
Fraction is 1%～10%；The carrier of described catalyst is al2o3、sio2、tio2One or more of, carry
The mass fraction of body is 90%～99%.
2. the method for catalytic oxidation treatment ammonia-contaminated gas as claimed in claim 1 is it is characterised in that be catalyzed oxygen
Change reaction to carry out in catalytic bed, the operating temperature range of described catalytic bed is 350～500 DEG C.
3. the method for catalytic oxidation treatment ammonia-contaminated gas as claimed in claim 1 is it is characterised in that give up containing ammonia
After gas is heated again in catalytic bed with catalyst reaction.
4. the method for catalytic oxidation treatment ammonia-contaminated gas as claimed in claim 1 is it is characterised in that give up containing ammonia
Gas in catalytic bed the time of staying between 0.1～0.5s.
5. a kind of device of catalytic oxidation treatment ammonia-contaminated gas is it is characterised in that comprise heating system and catalysis
Oxidative system；Described heating system is used for heating ammonia-contaminated gas；Described catalytic oxidation system includes catalytic bed；Urge
Oxidation is carried out in catalytic bed, and the active component of catalyst is cuo, ceo2、zro2、mno2
One or more of, the mass fraction of active component is 1%～10%；The carrier of described catalyst is al2o3、
sio2、tio2One or more of, the mass fraction of carrier is 90%～99%.
6. the device of catalytic oxidation treatment ammonia-contaminated gas as claimed in claim 5 is it is characterised in that described urge
The operating temperature range changing bed is 350～500 DEG C.
7. the device of catalytic oxidation treatment ammonia-contaminated gas as claimed in claim 5 is it is characterised in that give up containing ammonia
Gas in catalytic bed the time of staying between 0.1～0.5s.
8. the device of catalytic oxidation treatment ammonia-contaminated gas as claimed in claim 5 is it is characterised in that also include
Heat-exchange system, the ammonia-contaminated gas that the high-temperature gas Buddhist monk of purified acquisition is non-purified carry out heat in heat-exchange system
Exchange, after ammonia-contaminated gas are preheated, enter heating system, nitrogen and vapor are discharged after cooling.
9. the device of catalytic oxidation treatment ammonia-contaminated gas as claimed in claim 5 is it is characterised in that heating is
System adopts Resistant heating mode.
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| CN103721563A (en) * | 2013-12-18 | 2014-04-16 | 浙江省环境保护科学设计研究院 | Device and method for treating organic waste gas by catalysis and ozonation |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100300078A1 (en) * | 2009-05-27 | 2010-12-02 | Gm Global Technology Operations, Inc. | Exhaust After Treatment System |
| CN101979140A (en) * | 2010-10-19 | 2011-02-23 | 大连理工大学 | Metal loaded catalyst used for selective catalytic oxidation of ammonia, preparation method and application thereof |
| CN101966451A (en) * | 2010-11-06 | 2011-02-09 | 大连理工大学 | Preparation method and application of nanometer ceria-zirconia solid solution-based catalyst for selectively catalytically oxidizing ammonia |
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Application publication date: 20170201 |