CN105435599B - A kind of processing system and processing method of polluted gas - Google Patents
A kind of processing system and processing method of polluted gas Download PDFInfo
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- B01D53/34—Chemical or biological purification of waste gases
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Abstract
The present invention relates to the processing system and processing method of a kind of polluted gas based on burning chemistry chains principle, the polluted gas processing system includes the 1st burning chemistry chains reactor, the 2nd burning chemistry chains reactor, gas pipeline and triple valve；Oxygen carrier is filled in burning chemistry chains reactor；Gas pipeline includes polluted gas, air, reduction reaction product gas and oxidation reaction product gas pipeline；The polluted gas contains the amines such as the sulphur compounds such as hydrogen sulfide or ammonia, trimethylamine.Processing method of the present invention includes: that reduction reaction occurs for polluted gas and oxidation state oxygen carrier, oxygen occurs oxidation regeneration with reduction-state oxygen carrier or metal sulfide and reacts, when the gas concentration in two burning chemistry chains reactors reaches setting value, switching three-way valve, processing enter next circulation.The present invention selects the strong and weak oxygen carrier appropriate of oxidability not generate NO in polluted gas treatment processx, and SO can be trapped2, treatment conditions are easy to control, are more suitable for practical.
Description
Technical field
The present invention relates to a kind of gas handling systems, more particularly to a kind of polluted gas based on burning chemistry chains principle
Processing system and processing method.
Background technique
In people daily production and life, many polluted gas, such as exhaust gas, the spray of industrial production generation can be generated
The foul smell etc. that exhaust gas, the garbage loading embeading that workshop generates generate is applied, there are many harmful components type in these exhaust gas, mainly include
H2S, the sulphur compounds such as methyl mercaptan, NH3And the amines such as trimethylamine, butanediamine, the various volatile organic matters such as " triphen ", formaldehyde
(VOCs) gas etc..These polluted gas can perplex the life of neighbouring resident, also cause photochemical fog, acid rain, temperature to environment
The adverse effect such as room effect, therefore the research and development of efficient polluted gas processing system have been a hot spot of research.
Currently, for H2S、NH3Mainly there are absorption method, Production by Catalytic Combustion Process with the processing technique of the polluted gas such as VOCs and burns
Burning method etc..Absorption method is suitable for purifying the polluted gas that quantity is big but harmful substance contents are low, but the adsorbent absorption of the method is full
It needs to carry out desorption and regeneration, the H parsed with after2S、NH3Etc. still needing to harmless treatment；Production by Catalytic Combustion Process contains H in processing2S etc.
When the polluted gas of sulphur compound, H2The SO that the oxidations such as S generate2By the N in combustion air2And other reaction product gas institutes
Dilution, concentration does not rise anti-drop, so that the cost and energy consumption of subsequent sulfur removal technology are increased, in addition, H2S etc. also easily makes in catalyst
Poison and cause catalytic activity to reduce.In processing NH3When, if carrying out denitrogenation (i.e. by NH using selective catalytic oxidation method (SCO)3
It is converted into N2), NO is otherwise also easy to produce so needing strict control process conditions since it reacts warm widthx, cause the choosing of denitrogenation
The decline of selecting property.In addition, needing to adjust combustion-supporting air quantity in time to ensure when harmful components fluctuation of concentration is larger in polluted gas
Otherwise suitable air-fuel ratio will cause the resolution ratio decline of harmful substance, therefore the requirement to process regulation is very high.It burns
Burning method is due to ignition temperature height, often due to the calorific value of polluted gas is insufficient and needs to add auxiliary fuel, and NH3Or amine meeting
It is converted into fuel type NO at high temperaturex。
Synthesis is existing to H2S, the sulphur compounds such as methyl mercaptan, NH3And the amines such as trimethylamine, butanediamine, " triphen ", first
The processing method of the polluted gas such as the various VOCs gases such as aldehyde exists and catalyst sulfur poisoning, NO easily generated easily occursxWith to technique
Condition control requires the problems such as high.
Summary of the invention
It is a primary object of the present invention to, the processing system and processing method of a kind of polluted gas are provided, it is to be solved
Technical problem is that the processing of polluted gas is carried out using the principle of burning chemistry chains, makes it during processing, is not in carry
Oxysome sulfur poisoning, does not generate NOx, process conditions are easy to control, thus more suitable for practical.
The object of the invention to solve the technical problems adopts the following technical solutions to realize.
A kind of processing system of polluted gas proposed according to the present invention, including the 1st burning chemistry chains reactor, the 2nd change
Learn chain combustion reactor, gas pipeline and triple valve；The 1st burning chemistry chains reactor and the reaction of the 2nd burning chemistry chains
Oxygen carrier is filled in device；The gas pipeline includes polluted gas pipeline, air pipeline, reduction reaction product gas pipeline
With oxidation reaction product gas pipeline；The polluted gas contains the amines such as the sulphur compounds such as hydrogen sulfide, ammonia and trimethylamine
One or more of harmful components.
The object of the invention to solve the technical problems also can be used following technical measures and further realize.
Preferably, the processing system of polluted gas above-mentioned, wherein the oxygen carrier is copper-based oxygen carrier, iron-based oxygen carrier
One of body and Ni-based oxygen carrier or two or more mixtures.
Preferably, the processing system of polluted gas above-mentioned, wherein the active material of the copper-based oxygen carrier is CuO,
Carrier is Al2O3、SiO2Or TiO2One of or two or more mixtures；The active material of iron-based oxygen carrier is
Fe2O3, carrier Al2O3、SiO2Or TiO2One of or two or more mixtures；The active material of Ni-based oxygen carrier
For NiO, carrier Al2O3、SiO2Or TiO2One of or two or more mixtures.
Preferably, the processing system of polluted gas above-mentioned, wherein the polluted gas simultaneously also containing benzene, toluene,
One or more of volatile organic matters such as dimethylbenzene and formaldehyde.
Preferably, the processing system of polluted gas above-mentioned further includes sulfur dioxide capturing device, is arranged in described
On oxidation reaction product gas pipeline.
Preferably, the processing system of polluted gas above-mentioned, wherein the sulfur dioxide capturing device is with calcium oxide
Make the dry desulfurization device of desulfurizing agent, make the wet desulphurization device or concentrated sulfuric acid production dress of desulfurizing agent with limestone/lime slurries
It sets.
Also the following technical solution is employed for the object of the invention to solve the technical problems to realize.
A kind of processing system of polluted gas proposed according to the present invention, including
(1) reduction process of oxidation state oxygen carrier enters the polluted gas by the polluted gas pipeline
In the 1st burning chemistry chains reactor, reduction reaction occurs with the oxygen carrier；
(2) oxidative regeneration process of reduction-state oxygen carrier or metal sulfide passes through air, oxygen-enriched or purity oxygen described
Air, oxygen-enriched or pure oxygen feed channel enter the 2nd burning chemistry chains reactor in, with reduction-state oxygen carrier or metal sulphur
Oxidation regeneration reaction occurs for compound；
(3) handoff procedure of burning chemistry chains reactor, when the product of the reduction reaction in the 1st burning chemistry chains reactor
In harmful components concentration reach setting value, the oxygen concentration in the product of the oxidation reaction in the 2nd burning chemistry chains reactor
When reaching setting value, switching three-way valve makes the polluted gas enter the 2nd burning chemistry chains reactor, air, richness
Oxygen or purity oxygen enter the 1st burning chemistry chains reactor.
The object of the invention to solve the technical problems also can be used following technical measures and further realize.
Preferably, the processing system of polluted gas above-mentioned further includes by the dioxy in the product of the oxidation reaction
Change sulphur to be trapped with the sulfur dioxide capturing device.
Preferably, the processing system of polluted gas above-mentioned, wherein the temperature of the reduction reaction is 200 DEG C~500
℃；The temperature of the oxidation regeneration reaction is 150 DEG C~500 DEG C.
By above-mentioned technical proposal, the processing system and processing method of polluted gas of the present invention are at least had the advantage that
(1) desulfurization trapping and the SO of sulphur compound in polluted gas can be achieved2Enrichment.In reduction process, H2The vulcanizations such as S are closed
Sulphur in object is captured down in the form of metal sulfide.In oxidative regeneration process then, by be passed through it is oxygen-enriched can be real
Existing SO2Enrichment method, so as to save the cost and energy consumption of subsequent dry or wet sulfur removal technology.If being passed through purity oxygen
Then available pure SO2, it can be translated into concentrated sulfuric acid etc., to realize SO2Effective use；
(2) ammonia and the selectivity of amine denitrogenation are high, and denitrification effect is significant.For the denitrogenation of ammonia and amine, with oxygen
Too strong oxidability is compared, and the oxidation state of copper-based equal oxygen carriers has strong and weak oxidability appropriate, can be by NH3In amine
Nitrogen oxidation be zeroth order nitrogen, and be difficult to be further oxidized to the NO of the NO of positive divalent or positive tetravalence2；
(3) compared with Production by Catalytic Combustion Process, the present invention since oxygen carrier can provide a large amount of Lattice Oxygen without carry out air-fuel
The control of ratio, thus the polluted gas of the concentration and flow fluctuation for not oxygenous or oxygen and harmful components
Processing has the apparent advantage such as stable, easy to operate；
(4) different from Production by Catalytic Combustion Process, sulfur poisoning will not occur for oxygen carrier.The active constituent metal oxide of oxygen carrier is
It largely, although during the reaction can be with H2S etc. generates metal sulfide, but can be weighed in subsequent oxidation regeneration reaction
It newly is converted into metal oxide, because of the problem of oxygen carrier sulfur poisoning may be not present.
The above description is only an overview of the technical scheme of the present invention, in order to better understand the technical means of the present invention,
And can be implemented in accordance with the contents of the specification, the following is a detailed description of the preferred embodiments of the present invention and the accompanying drawings.
Detailed description of the invention
Fig. 1 is the schematic diagram of the processing system of 1 polluted gas of embodiment.
Fig. 2 is the schematic diagram of the processing system of embodiment 2-4 polluted gas.
Fig. 3 is the schematic diagram of the processing system of embodiment 5-7 polluted gas.
Specific embodiment
It is of the invention to reach the technical means and efficacy that predetermined goal of the invention is taken further to illustrate, below in conjunction with
Attached drawing and preferred embodiment, processing system and processing method its specific implementation to a kind of polluted gas proposed according to the present invention
Mode, structure, feature and its effect, detailed description is as follows.In the following description, different " embodiment " or " embodiment "
What is referred to is not necessarily the same embodiment.In addition, the special characteristic, structure or feature in one or more embodiments can be by any conjunction
Conformal formula combination.
Embodiment 1
Please refer to Fig. 1.Shown in the processing system of polluted gas include: to be filled with the oxidation state 107 of copper-based oxygen carrier
1st burning chemistry chains reactor 101, be filled with copper-based oxygen carrier reduction-state 108 the 2nd burning chemistry chains reactor 102, dirty
Contaminate gas pipeline 109, air blower 111, air pipeline 112, reduction reaction product gas pipeline 110, oxidation reaction product gas
Body pipeline 113 and electric three passes valve group 103~106.The active material of the copper-based oxygen carrier is CuO, carrier SiO2。
The polluted gas contains NH3。
Polluted gas enters in the 1st burning chemistry chains reactor 101 through the triple valve 103 on polluted gas pipeline 109, with
Reduction reaction: the NH in polluted gas occurs for oxidation state oxygen carrier 1073It is reacted with oxidation state oxygen carrier 107 and generates nitrogen and water
Steam, simultaneous oxidation state oxygen carrier 107 are converted into reduction-state；Reduction reaction product gas is through reduction reaction product gas pipeline
Triple valve 104 on 110 is discharged.The temperature of the reduction reaction is 200 DEG C.
Air enters in the 2nd burning chemistry chains reactor 102 through the triple valve 105 on air pipeline 112, carries with reduction-state
Oxysome 108 carries out oxidation regeneration reaction, and reduction-state oxygen carrier 108 is reacted with the oxygen in air generates oxidation state oxygen carrier.Oxygen
Change reaction product gas to be discharged through the triple valve 106 on oxidation reaction product gas pipeline 113.The oxidation regeneration reacts temperature
Degree is 150 DEG C.
Reduction-state is wholly or largely converted into when the oxidation state oxygen carrier 107 in the 1st burning chemistry chains reactor 101
The total concentration of oxygen carrier, i.e. harmful components in reduction reaction product gas reaches setting value 10mg/m3, while the 2nd chemical chain
Reduction-state oxygen carrier 108 in combustion reactor 102 is wholly or largely converted into oxidation state oxygen carrier, i.e. oxidation reaction produces
When oxygen concentration in object gas reaches setting value 2%, the switching of electric three passes valve group 103~106 is carried out, polluted gas is passed through
Triple valve 103 enters in the 2nd burning chemistry chains reactor 102, and air enters the 1st burning chemistry chains through triple valve 105 and reacts
In device 101.By the reasonable setting to each pipeline gas flow and each valve transfer time, it can be achieved that the continuous place of polluted gas
Reason.
The oxidation state and NH of copper-based oxygen carrier3Reduction reaction and reduction-state and O2Oxidation regeneration reaction reaction side
Standard free energy variation and reaction heat under formula and reaction temperature is as follows:
3CuO+2NH3(g)=3Cu+N2(g)+3H2O (g) △ G °=- 78.56kcal/mol
△ H °=- 40.05kcal/mol
2Cu+O2(g)=2CuO △ G °=- 55.72kcal/mol
△ H °=- 74.16kcal/mol
Embodiment 2
Please refer to Fig. 2.The present embodiment compared with Example 1, the difference is that: oxygen carrier be iron-based oxygen carrier, live
Property substance be Fe2O3, carrier Al2O3.The temperature of reduction reaction and oxidation reaction is 300 DEG C.In oxidation reaction product flue
Sulfur dioxide capturing device 200 is set on road 113, for trapping the SO in oxidation reaction product gas2, the sulfur dioxide
Capturing device 200 is the wet desulphurization device for making desulfurizing agent with the slurries of lime stone or lime.Polluted gas contain trimethylamine and
H2S。
The oxidation state and trimethylamine and H of iron-based oxygen carrier2The reduction reaction and reduction-state and iron sulfide and O of S2Oxidation
The reaction equation of regenerative response and the standard free energy under reaction temperature change as follows with reaction heat:
63Fe2O3+2C3H9N (g)=42Fe3O4+N2(g)+9H2O(g)+6CO2(g)
Fe2O3+3H2S (g)=Fe2S3+3H2O (g) △ G °=- 29.12kcal/mol
△ H °=- 34.20kcal/mol
4Fe3O4+O2(g)=6Fe2O3△ G °=- 74.26kcal/mol
△ H °=- 111.95kcal/mol
Fe2S3+4.5O2(g)=Fe2O3+3SO2(g) △ G °=- 310.75kcal/mol
△ H °=- 337.83kcal/mol
Embodiment 3
Please refer to Fig. 2.The present embodiment compared with Example 2, the difference is that: oxygen carrier be Ni-based oxygen carrier, live
Property substance be NiO, carrier TiO2.The temperature of reduction reaction and oxidation reaction is 350 DEG C, in oxidation reaction product gas pipeline
Sulfur dioxide capturing device 200 is set on 113, for trapping the SO in oxidation reaction product gas2, the sulfur dioxide catches
Acquisition means 200 are the dry desulfurization device for making desulfurizing agent with calcium oxide.Polluted gas contains methyl mercaptan and toluene.
The oxidation state of Ni-based oxygen carrier and the reduction reaction and reduction-state and nickel sulfide and O of methyl mercaptan and toluene2Oxygen
Change the reaction equation of regenerative response and the standard free energy under reaction temperature changes and reaction heat is as follows:
4NiO+CH3SH (g)=NiS+3Ni+CO2+2H2O(g)
△ G °=- 43.90kcal/mol
△ H °=2.50kcal/mol
18NiO+C7H8(g)=18Ni+7CO2(g)+4H2O(g)
Ni+O2(g)=NiO △ G °=- 86.90kcal/mol
△ H °=- 113.44kcal/mol
NiS+1.5O2(g)=NiO+SO2(g) △ G °=- 96.07kcal/mol
△ H °=- 107.18kcal/mol
Embodiment 4
Please refer to Fig. 2.The present embodiment compared with Example 2, the difference is that: oxygen carrier is copper-based oxygen carrier and iron-based
The mixture of oxygen carrier, carrier Al2O3And SiO2Mixture, polluted gas be ammonia, benzene,toluene,xylene and formaldehyde.Also
The temperature of original reaction and oxidation reaction is 400 DEG C.Sulfur dioxide capturing device is set on oxidation reaction product gas pipeline 113
200, for trapping the SO in oxidation reaction product gas2, the sulfur dioxide capturing device 200 is to make desulfurization with calcium oxide
The dry desulfurization device of agent.
Embodiment 5
Please refer to Fig. 3.The present embodiment compared with Example 3, the difference is that: oxygen carrier is copper-based oxygen carrier and Ni-based
The mixture of oxygen carrier, carrier SiO2And TiO2Mixture, polluted gas be hydrogen sulfide, ammonia, benzene,toluene,xylene and first
Aldehyde.The temperature of reduction reaction and oxidation reaction is 450 DEG C.Air pipeline 112 is changed to oxygen rich gas pipeline 300, it is anti-in oxidation
Setting sulfur dioxide capturing device 200 on product gas pipeline 113 is answered, for trapping the SO in oxidation reaction product gas2, institute
The sulfur dioxide capturing device 200 stated is concentrated sulfuric acid process units.
Embodiment 6
Please refer to Fig. 3.The present embodiment compared with Example 3, the difference is that: oxygen carrier is iron-based oxygen carrier and Ni-based
The mixture of oxygen carrier, carrier Al2O3And TiO2Mixture, polluted gas be hydrogen sulfide, methyl mercaptan, ammonia, trimethylamine,
Butanediamine, benzene,toluene,xylene and formaldehyde.The temperature of reduction reaction and oxidation reaction is 500 DEG C.Air pipeline 112 is changed to
Sulfur dioxide capturing device 200 is arranged, on oxidation reaction product gas pipeline 113 for trapping oxygen in pure oxygen gas pipeline 300
Change the SO in reaction product gas2, the sulfur dioxide capturing device 200 is concentrated sulfuric acid process units.
Embodiment 7
Please refer to Fig. 3.The present embodiment compared with Example 6, the difference is that: oxygen carrier is copper-based oxygen carrier, iron-based
The mixture of oxygen carrier and Ni-based oxygen carrier.Carrier is Al2O3、SiO2And TiO2Mixture, polluted gas are hydrogen sulfide, carbonyl
Sulphur, methyl mercaptan, ammonia, trimethylamine, butanediamine, benzene,toluene,xylene and formaldehyde.
The above described is only a preferred embodiment of the present invention, be not intended to limit the present invention in any form, according to
According to technical spirit any simple modification, equivalent change and modification to the above embodiments of the invention, this hair is still fallen within
In the range of bright technical solution.
Claims (6)
1. a kind of processing method of polluted gas characterized by comprising
Make the oxygen carrier in polluted gas and the 1st burning chemistry chains reactor that reduction reaction occur；
Make air, oxygen-enriched or purity oxygen that oxidation regeneration occur with the reduction-state oxygen carrier in the 2nd burning chemistry chains reactor to react；
When the harmful components concentration in the product of the reduction reaction in the 1st burning chemistry chains reactor reaches setting value, institute
When stating the oxygen concentration in the product of the oxidation reaction in the 2nd burning chemistry chains reactor and reaching setting value, switching three-way valve makes
The polluted gas enters the 2nd burning chemistry chains reactor, and air, oxygen-enriched or purity oxygen are fired into the 1st chemical chain
Burn reactor；
Wherein, the polluted gas contains one or more of ammonia, amine, benzene,toluene,xylene and formaldehyde.
2. the processing method of polluted gas according to claim 1, it is characterised in that:
The oxygen carrier is one of copper-based oxygen carrier, iron-based oxygen carrier and Ni-based oxygen carrier or two or more mixing
Object.
3. the processing method of polluted gas according to claim 2, it is characterised in that:
The active material of the copper-based oxygen carrier is CuO, carrier Al2O3、SiO2Or TiO2One of or two kinds with
On mixture；
The active material of the iron-based oxygen carrier is Fe2O3, carrier Al2O3、SiO2Or TiO2One of or two kinds
Above mixture；
The active material of the Ni-based oxygen carrier is NiO, carrier Al2O3、SiO2Or TiO2One of or two kinds with
On mixture.
4. the processing method of polluted gas according to claim 1, it is characterised in that:
The setting value of harmful components concentration in the product of the reduction reaction is 10mg/m3, oxygen in the product of oxidation reaction
The setting value of gas concentration is 2%.
5. the processing method of polluted gas according to claim 1, it is characterised in that:
The temperature of the reduction reaction is 200 DEG C~500 DEG C；
The temperature of the oxidation regeneration reaction is 150 DEG C~500 DEG C.
6. the processing method of polluted gas according to claim 1, it is characterised in that:
The amine includes trimethylamine and/or butanediamine.
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Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102183152A (en) * | 2011-01-12 | 2011-09-14 | 浙江大学 | Steel enterprise associated energy combined cycle power generation system and method |
| CN102533389A (en) * | 2011-12-05 | 2012-07-04 | 华北电力大学 | Method for applying mesocellular silica hollow sphere iron-based oxygen carrier |
| CN202382432U (en) * | 2011-12-05 | 2012-08-15 | 北京科技大学 | Chemical-looping combustion system |
| WO2013098328A1 (en) * | 2011-12-27 | 2013-07-04 | Shell Internationale Research Maatschappij B.V. | Improved method for recovery of elemental sulphur |
| JP2013164235A (en) * | 2012-02-13 | 2013-08-22 | Tokyo Gas Co Ltd | Chemical loop type combustion device suitable for nitrogen production, and method for producing nitrogen and hydrogen using the same |
| GB2514809A (en) * | 2013-06-05 | 2014-12-10 | Gas Recovery & Recycle Ltd | Chemical looping combustion process |
| CN205340522U (en) * | 2015-12-16 | 2016-06-29 | 北京科技大学 | Gaseous pollutants's processing system |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102183152A (en) * | 2011-01-12 | 2011-09-14 | 浙江大学 | Steel enterprise associated energy combined cycle power generation system and method |
| CN102533389A (en) * | 2011-12-05 | 2012-07-04 | 华北电力大学 | Method for applying mesocellular silica hollow sphere iron-based oxygen carrier |
| CN202382432U (en) * | 2011-12-05 | 2012-08-15 | 北京科技大学 | Chemical-looping combustion system |
| WO2013098328A1 (en) * | 2011-12-27 | 2013-07-04 | Shell Internationale Research Maatschappij B.V. | Improved method for recovery of elemental sulphur |
| JP2013164235A (en) * | 2012-02-13 | 2013-08-22 | Tokyo Gas Co Ltd | Chemical loop type combustion device suitable for nitrogen production, and method for producing nitrogen and hydrogen using the same |
| GB2514809A (en) * | 2013-06-05 | 2014-12-10 | Gas Recovery & Recycle Ltd | Chemical looping combustion process |
| CN205340522U (en) * | 2015-12-16 | 2016-06-29 | 北京科技大学 | Gaseous pollutants's processing system |
Non-Patent Citations (2)
| Title |
|---|
| 化学链燃烧中镍基载氧体与H2S反应机理研究;高正平;《工程热物理学报》;20100415;第31卷(第4期);第713-716页 * |
| 化学链燃烧技术的研究进展;秦翠娟等;《锅炉技术》;20080928;第39卷(第05期);第64-73页 * |
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