CN216654084U - Pore and denitration catalytic system with same - Google Patents
Pore and denitration catalytic system with same Download PDFInfo
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- CN216654084U CN216654084U CN202122675895.7U CN202122675895U CN216654084U CN 216654084 U CN216654084 U CN 216654084U CN 202122675895 U CN202122675895 U CN 202122675895U CN 216654084 U CN216654084 U CN 216654084U
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- 230000003197 catalytic effect Effects 0.000 title claims abstract description 26
- 239000011148 porous material Substances 0.000 title claims abstract description 25
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 306
- 239000003054 catalyst Substances 0.000 claims abstract description 222
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 87
- 239000001257 hydrogen Substances 0.000 claims abstract description 87
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 87
- 239000007789 gas Substances 0.000 claims abstract description 84
- 238000005336 cracking Methods 0.000 claims abstract description 78
- 238000004519 manufacturing process Methods 0.000 claims abstract description 72
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 19
- 239000003546 flue gas Substances 0.000 claims abstract description 19
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 14
- 239000000919 ceramic Substances 0.000 claims description 14
- 239000000758 substrate Substances 0.000 claims description 9
- 229910052878 cordierite Inorganic materials 0.000 claims description 6
- JSKIRARMQDRGJZ-UHFFFAOYSA-N dimagnesium dioxido-bis[(1-oxido-3-oxo-2,4,6,8,9-pentaoxa-1,3-disila-5,7-dialuminabicyclo[3.3.1]nonan-7-yl)oxy]silane Chemical compound [Mg++].[Mg++].[O-][Si]([O-])(O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2)O[Al]1O[Al]2O[Si](=O)O[Si]([O-])(O1)O2 JSKIRARMQDRGJZ-UHFFFAOYSA-N 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- KZHJGOXRZJKJNY-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Si]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O.O=[Al]O[Al]=O KZHJGOXRZJKJNY-UHFFFAOYSA-N 0.000 claims description 4
- 239000011159 matrix material Substances 0.000 claims description 4
- 229910052863 mullite Inorganic materials 0.000 claims description 4
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 33
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 20
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 230000009471 action Effects 0.000 description 12
- 230000002829 reductive effect Effects 0.000 description 11
- 229910021529 ammonia Inorganic materials 0.000 description 10
- 239000013543 active substance Substances 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical group O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 239000008367 deionised water Substances 0.000 description 6
- 229910021641 deionized water Inorganic materials 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 230000003647 oxidation Effects 0.000 description 6
- 238000007254 oxidation reaction Methods 0.000 description 6
- RMAQACBXLXPBSY-UHFFFAOYSA-N silicic acid Chemical compound O[Si](O)(O)O RMAQACBXLXPBSY-UHFFFAOYSA-N 0.000 description 6
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- 239000012752 auxiliary agent Substances 0.000 description 4
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 description 4
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 description 4
- VCJMYUPGQJHHFU-UHFFFAOYSA-N iron(3+);trinitrate Chemical compound [Fe+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O VCJMYUPGQJHHFU-UHFFFAOYSA-N 0.000 description 4
- YIXJRHPUWRPCBB-UHFFFAOYSA-N magnesium nitrate Chemical compound [Mg+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O YIXJRHPUWRPCBB-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- JKQOBWVOAYFWKG-UHFFFAOYSA-N molybdenum trioxide Chemical compound O=[Mo](=O)=O JKQOBWVOAYFWKG-UHFFFAOYSA-N 0.000 description 4
- 229910000510 noble metal Inorganic materials 0.000 description 4
- PIBWKRNGBLPSSY-UHFFFAOYSA-L palladium(II) chloride Chemical compound Cl[Pd]Cl PIBWKRNGBLPSSY-UHFFFAOYSA-L 0.000 description 4
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 4
- 239000000779 smoke Substances 0.000 description 4
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- ZNOKGRXACCSDPY-UHFFFAOYSA-N tungsten trioxide Chemical group O=[W](=O)=O ZNOKGRXACCSDPY-UHFFFAOYSA-N 0.000 description 4
- ONDPHDOFVYQSGI-UHFFFAOYSA-N zinc nitrate Chemical compound [Zn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ONDPHDOFVYQSGI-UHFFFAOYSA-N 0.000 description 4
- 150000003863 ammonium salts Chemical class 0.000 description 3
- 238000010531 catalytic reduction reaction Methods 0.000 description 3
- 230000010354 integration Effects 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 239000012298 atmosphere Substances 0.000 description 2
- UFMZWBIQTDUYBN-UHFFFAOYSA-N cobalt dinitrate Chemical compound [Co+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O UFMZWBIQTDUYBN-UHFFFAOYSA-N 0.000 description 2
- 229910001981 cobalt nitrate Inorganic materials 0.000 description 2
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 235000010333 potassium nitrate Nutrition 0.000 description 2
- 239000004323 potassium nitrate Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 235000010344 sodium nitrate Nutrition 0.000 description 2
- 239000004317 sodium nitrate Substances 0.000 description 2
- 239000004408 titanium dioxide Substances 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- BIGPRXCJEDHCLP-UHFFFAOYSA-N ammonium bisulfate Chemical compound [NH4+].OS([O-])(=O)=O BIGPRXCJEDHCLP-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000006479 redox reaction Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
Images
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T10/00—Road transport of goods or passengers
- Y02T10/10—Internal combustion engine [ICE] based vehicles
- Y02T10/12—Improving ICE efficiencies
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- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The utility model provides a pore channel and a denitration catalytic system with the pore channel, which comprise a plurality of pore channels, and a tail gas treatment catalyst layer, a denitration catalyst layer and a methanol cracking hydrogen production catalyst layer which correspond to the pore channels in number; a methanol cracking hydrogen production catalyst layer, a denitration catalyst layer and a tail gas treatment catalyst layer are sequentially arranged on the inner wall of the pore channel along the flue gas inlet direction; the catalyst layer for hydrogen production by methanol cracking, the denitration catalyst layer and the tail gas treatment catalyst layer are arranged in a gradient manner. According to the utility model, the denitration catalytic system is provided with the pore channel, the tail gas treatment catalyst layer, the denitration catalyst layer and the methanol cracking hydrogen production catalyst layer, so that the system can not only carry out denitration by using methanol as a reducing agent, but also effectively purify VOC in tail gas.
Description
Technical Field
The utility model relates to the technical field of environmental protection and purification, in particular to a denitration catalytic pore channel taking methanol as a reducing agent and a denitration catalytic system with the pore channel.
Background
The nitrogen oxide is an atmospheric pollutant with strong harmfulness, and the excessive content in the atmosphere can cause environmental problems such as acid rain, photochemical smog, haze and the like, and has great threat to human health; in order to relieve the pollution of nitrogen oxides to the atmosphere, strict emission standards are established by countries and places; the current technology for removing nitrogen oxides mainly comprises the following steps: selective Catalytic Reduction (SCR), selective non-catalytic reduction (SNCR), and non-selective catalytic reduction (NSCR), and the SCR denitration technology is the most mature and efficient technology at present, and in the technology, the reducing agent mainly includes ammonia such as ammonia and urea.
Ammonia is explosive and toxic, and if the input amount of ammonia is unreasonable, part of ammonia escapes to generate secondary environmental pollution, in addition, sulfur oxides in the flue gas and the ammonia can generate ammonium bisulfate to be deposited on the surface of the catalyst to inactivate the catalyst, so that the service life of the catalyst is shortened; therefore, the SCR removal of nitrogen oxides by using non-ammonia as a reducing agent is paid much attention, for example, methanol is an SCR denitration reducing agent which is low in cost, easily available in raw materials and safe to use, but the methanol generates VOC byproducts in an oxidation-reduction reaction to generate secondary pollution to air.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a denitration catalytic system which not only takes methanol as a reducing agent, but also can effectively purify tail gas.
The utility model solves the technical problems through the following technical means:
a denitration catalytic pore channel taking methanol as a reducing agent comprises a tail gas treatment catalyst layer (1), a denitration catalyst layer (2), a methanol cracking hydrogen production catalyst layer (3) and a shell (4); the inner wall of the shell (4) is sequentially provided with the methanol cracking hydrogen production catalyst layer (3), the denitration catalyst layer (2) and the tail gas treatment catalyst layer (1) along the flue gas inlet direction; the catalyst layer (3) for hydrogen production by methanol cracking, the denitration catalyst layer (2) and the tail gas treatment catalyst layer (1) are arranged in a gradient manner.
Has the advantages that: according to the utility model, the catalyst layer for hydrogen production by methanol cracking, the denitration catalyst layer and the tail gas treatment catalyst layer are sequentially arranged in a gradient manner along the flue gas inlet direction, so that the integration of the catalyst layers with three different catalytic effects is achieved; the denitration catalytic pore channel can only use methanol as a reducing agent and can effectively purify VOC in tail gas, so that the problems of ammonium salt blockage and ammonia escape are solved, the content of VOC in the finally obtained tail gas is very low, and secondary pollution of incompletely-reacted methanol and micromolecule VOC generated in the methanol cracking process to air is avoided.
Furthermore, the tail gas treatment catalyst layer (1), the denitration catalyst layer (2) and the methanol cracking hydrogen production catalyst layer (3) are sequentially arranged on the inner wall of the shell (4) from outside to inside.
Has the advantages that: when the flue gas is introduced from bottom to top, methanol in the flue gas firstly contacts the methanol cracking hydrogen production catalyst layer at the lower part and is decomposed into reductive gases such as hydrogen and VOC under the action of the methanol cracking hydrogen production catalyst layer, then the reductive gases such as hydrogen and VOC selectively reduce nitrogen oxides into nitrogen under the action of the denitration catalyst layer, and finally the tail gas treatment catalyst layer carries out catalytic oxidation treatment on the incompletely reacted VOC to prevent the VOC from generating secondary pollution to the environment.
Furthermore, the inner wall of the shell (4) is sequentially provided with a methanol cracking hydrogen production catalyst layer (3), a denitration catalyst layer (2) and a tail gas treatment catalyst layer (1) from outside to inside.
Has the advantages that: when the flue gas is introduced from top to bottom, methanol in the flue gas firstly contacts the methanol cracking hydrogen production catalyst layer on the upper part and is decomposed into reducing gases such as hydrogen and VOC under the action of the methanol cracking hydrogen production catalyst layer, then the reducing gases such as hydrogen and VOC selectively reduce nitrogen oxides into nitrogen under the action of the denitration catalyst layer, and finally the tail gas treatment catalyst layer carries out catalytic oxidation treatment on the incompletely reacted VOC to prevent the VOC from generating secondary pollution to the environment.
Further, the tail gas treatment catalyst layer (1) is fixed on the inner wall of the shell (4), the denitration catalyst layer (2) is fixed on the inner layer of the tail gas treatment catalyst layer (1), and the methanol cracking hydrogen production catalyst layer (3) is fixed on the inner layer of the denitration catalyst layer (2).
Further, the height of the tail gas treatment catalyst layer (1) is 30cm, and the thickness is 1-5 μm; the height of the denitration catalyst layer (2) is 1/3-2/3 of the total height of the tail gas treatment catalyst layer (1), and the thickness is 1-5 mu m; the height of the methanol cracking hydrogen production catalyst layer (3) is 1/6-1/3 of the total height of the tail gas treatment catalyst layer (1), and the thickness is 1-5 mu m.
Further, the methanol cracking hydrogen production catalyst layer (3) is fixed on the inner wall of the shell (4), the denitration catalyst layer (2) is fixed on the inner layer of the methanol cracking hydrogen production catalyst layer (3), and the tail gas treatment catalyst layer (1) is fixed on the inner layer of the denitration catalyst layer (2).
Further, the height of the methanol cracking hydrogen production catalyst layer (3) is 30cm, and the thickness is 1-5 μm; the height of the denitration catalyst layer (2) is 1/3-2/3 of the total height of the methanol cracking hydrogen production catalyst layer (3), and the thickness is 1-5 mu m; the height of the tail gas treatment catalyst layer (1) is 1/6-1/3 of the total height of the methanol cracking hydrogen production catalyst layer (3), and the thickness is 1-5 mu m.
Has the advantages that: according to the utility model, the methanol cracking hydrogen production catalyst layer, the denitration catalyst layer and the tail gas treatment catalyst layer are integrated and fixed in sequence, so that the denitration tower does not need to be modified in a complex way, and the preparation process is simple.
The utility model also discloses a denitration catalytic system comprising the pore channel in any technical scheme, which comprises a plurality of pore channels, and a tail gas treatment catalyst layer (1), a denitration catalyst layer (2) and a methanol cracking hydrogen production catalyst layer (3) which correspond to the pore channels in number; the pore passages (4) are integrally and fixedly connected to form a matrix of the denitration catalytic system.
Has the advantages that: according to the utility model, the catalyst layer for hydrogen production by methanol cracking, the denitration catalyst layer and the tail gas treatment catalyst layer are sequentially arranged in a gradient manner along the flue gas inlet direction, so that the integration of the catalyst layers with three different catalytic effects is achieved; the denitration catalytic system can only use methanol as a reducing agent and can effectively purify VOC in tail gas, so that the problems of ammonium salt blockage and ammonia escape are solved, the VOC content in the finally obtained tail gas is very low, and secondary pollution of incompletely reacted methanol and micromolecular VOC generated in the methanol cracking process to air is avoided.
Further, the length, width and height of the substrate are 10cm, 10cm and 30 cm.
Further, the base body is made of one of cordierite honeycomb ceramic, mullite honeycomb ceramic and alumina honeycomb ceramic.
The utility model has the advantages that:
according to the utility model, the catalyst layer for hydrogen production by methanol cracking, the denitration catalyst layer and the tail gas treatment catalyst layer are sequentially arranged in a gradient manner along the flue gas inlet direction, so that the integration of the catalyst layers with three different catalytic effects is achieved; the denitration catalytic system can only use methanol as a reducing agent and can effectively purify VOC in tail gas, so that the problems of ammonium salt blockage and ammonia escape are solved, the content of VOC in the finally obtained tail gas is very low, secondary pollution to air caused by incompletely-reacted methanol and micromolecular VOC generated in the cracking process of the methanol is avoided, selective nitrogen oxide reduction using the methanol as the reducing agent is achieved, and no pollutant is discharged completely.
According to the utility model, the tail gas treatment catalyst layer, the denitration catalyst layer and the methanol cracking hydrogen production catalyst layer are sequentially arranged on the inner wall of the pore passage from outside to inside, when flue gas is introduced from bottom to top, methanol in the flue gas firstly contacts the lower methanol cracking hydrogen production catalyst layer and is decomposed into reductive gases such as hydrogen and VOC under the action of the methanol cracking hydrogen production catalyst layer, then the nitrogen oxide is selectively reduced into nitrogen by the reductive gases such as hydrogen and VOC under the action of the denitration catalyst layer, and finally the tail gas treatment catalyst layer carries out catalytic oxidation treatment on the incompletely reacted VOC, so that the secondary pollution of the VOC to the environment is prevented.
According to the utility model, the methanol cracking hydrogen production catalyst layer, the denitration catalyst layer and the tail gas treatment catalyst layer are sequentially arranged from outside to inside on the inner wall of the pore passage, when flue gas is introduced from top to bottom, methanol in the flue gas firstly contacts the upper methanol cracking hydrogen production catalyst layer and is decomposed into reductive gases such as hydrogen and VOC under the action of the methanol cracking hydrogen production catalyst layer, then the reductive gases such as hydrogen and VOC selectively reduce nitrogen oxides into nitrogen under the action of the denitration catalyst layer, and finally the tail gas treatment catalyst layer carries out catalytic oxidation treatment on the incompletely reacted VOC, so that secondary pollution of the VOC to the environment is prevented.
According to the utility model, the methanol cracking hydrogen production catalyst layer, the denitration catalyst layer and the tail gas treatment catalyst layer are integrated and fixed in sequence, so that the denitration tower does not need to be modified in a complex way, and the preparation process is simple.
Drawings
FIG. 1 is a schematic front sectional view of a channel in a denitration catalyst system of example 1;
fig. 2 is a schematic front sectional view of a pore channel in the denitration catalyst system in example 2.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are some embodiments of the present invention, but not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example one
The embodiment provides a denitration catalyst system using methanol as a reducing agent, which comprises a plurality of channels, and a tail gas treatment catalyst layer 1, a denitration catalyst layer 2 and a methanol cracking hydrogen production catalyst layer 3 which correspond to the channels in number.
The plurality of pore passages are integrally and fixedly connected to form a matrix of the denitration catalytic system; the length, width and height of the substrate are 30cm 10 cm; the material of the substrate is one of cordierite honeycomb ceramic, mullite honeycomb ceramic and alumina honeycomb ceramic, and the material of the substrate is cordierite honeycomb ceramic in the example of the embodiment, and the mesh number is 50 meshes.
As shown in fig. 1, the duct comprises a housing 4, and the housing 4 is a hollow cylinder.
As shown in fig. 1, the exhaust gas treatment catalyst layer 1 is fixed to the inner wall of the casing 4; the height of the tail gas treatment catalyst layer 1 is 30cm, and the thickness is 1-5 mu m; the exhaust gas treatment catalyst layer 1 has a ring shape.
As shown in fig. 1, the denitration catalyst layer 2 is fixed on the inner layer of the exhaust gas treatment catalyst layer 1; the height of the denitration catalyst layer 2 is 1/3-2/3 of the total height of the exhaust gas treatment catalyst layer 1, and the thickness is 1-5 μm, and the embodiment exemplifies that the height of the denitration catalyst layer 2 is 2/3 of the total height of the exhaust gas treatment catalyst layer 1; the denitration catalyst layer 2 has a ring shape.
As shown in fig. 1, the methanol cracking hydrogen production catalyst layer 3 is fixed on the inner layer of the denitration catalyst layer 2; the height of the methanol cracking hydrogen production catalyst layer 3 is 1/6-1/3 of the total height of the tail gas treatment catalyst layer 1, and the thickness is 1-5 μm, in the embodiment, the height of the methanol cracking hydrogen production catalyst layer 3 is 1/3 of the total height of the tail gas treatment catalyst layer 1; the catalyst layer 3 for hydrogen production by methanol cracking is annular.
The tail gas treatment catalyst layer 1, the denitration catalyst layer 2 and the methanol cracking hydrogen production catalyst layer 3 can be directly purchased.
The tail gas treatment catalyst layer 1 comprises noble metal, silica sol solution and solvent; the noble metal is chloroplatinic acid or palladium chloride or a mixture of the chloroplatinic acid and the palladium chloride; the solvent is deionized water or absolute ethyl alcohol or a mixture of the deionized water and the absolute ethyl alcohol.
The denitration catalyst layer 2 comprises nano industrial titanium dioxide, vanadium pentoxide, a denitration catalyst active substance, a silica sol solution and water; the active substance of the denitration catalyst is tungsten trioxide or molybdenum trioxide.
The methanol cracking hydrogen production catalyst layer 3 comprises a methanol cracking hydrogen production catalyst active substance, zinc nitrate, a methanol cracking hydrogen production catalyst auxiliary agent, deionized water and a silica sol solution; one of active substances of the catalyst for preparing hydrogen by cracking methanol, namely ferric nitrate, cobalt nitrate, nickel nitrate and copper nitrate; the methanol cracking hydrogen production catalyst auxiliary agent is one of potassium nitrate, sodium nitrate, magnesium nitrate and calcium nitrate.
When in use, the smoke is introduced from bottom to top, and the components of the smoke comprise NO, methanol and O2、N2The flue gas sequentially contacts a methanol cracking hydrogen production catalyst layer 3, a denitration catalyst layer 2 and a tail gas treatment catalyst layer 1 to carry out denitration and VOC removal; specifically, methanol in the flue gas is decomposed into reductive gases such as hydrogen and VOC under the action of the methanol cracking hydrogen production catalyst layer 3, then the reductive gases such as hydrogen and VOC selectively reduce nitrogen oxides into nitrogen under the action of the denitration catalyst layer 2, and finally the tail gas treatment catalyst layer 1 carries out catalytic oxidation treatment on the incompletely reacted VOC to prevent the VOC from generating secondary pollution to the environment.
Example two
The embodiment provides a denitration catalyst system using methanol as a reducing agent, which comprises a plurality of channels, and a tail gas treatment catalyst layer 1, a denitration catalyst layer 2 and a methanol cracking hydrogen production catalyst layer 3 which correspond to the channels in number.
The plurality of pore passages are integrally and fixedly connected to form a matrix of the denitration catalytic system; the length, width and height of the substrate are 30cm 10 cm; the material of the substrate is one of cordierite honeycomb ceramic, mullite honeycomb ceramic and alumina honeycomb ceramic, and the material of the substrate is cordierite honeycomb ceramic in the example of the embodiment, and the mesh number is 50 meshes.
As shown in fig. 2, the duct comprises a housing 4, the housing 4 being a hollow cylinder.
As shown in fig. 2, the methanol cracking hydrogen production catalyst layer 3 is fixed on the inner wall of the casing 4; the height of the catalyst layer 3 for preparing hydrogen by cracking methanol is 30cm, and the thickness is 1-5 mu m; the catalyst layer 3 for hydrogen production by methanol cracking is annular.
As shown in fig. 2, the denitration catalyst layer 2 is fixed on the inner layer of the methanol cracking hydrogen production catalyst layer 3; the height of the denitration catalyst layer 2 is 1/3-2/3 of the total height of the methanol cracking hydrogen production catalyst layer 3, and the thickness is 1-5 μm, which is exemplified in the embodiment that the height of the denitration catalyst layer 2 is 2/3 of the total height of the methanol cracking hydrogen production catalyst layer 3; the denitration catalyst layer 2 has a ring shape.
As shown in fig. 2, the exhaust gas treatment catalyst layer 1 is fixed on the inner layer of the denitration catalyst layer 2; the height of the tail gas treatment catalyst layer 1 is 1/6-1/3 of the total height of the methanol cracking hydrogen production catalyst layer 3, and the thickness is 1-5 μm, which is exemplified in the embodiment that the height of the tail gas treatment catalyst layer 1 is 1/3 of the total height of the methanol cracking hydrogen production catalyst layer 3; the exhaust gas treatment catalyst layer 1 has a ring shape.
The tail gas treatment catalyst layer 1, the denitration catalyst layer 2 and the methanol cracking hydrogen production catalyst layer 3 can be directly purchased.
The tail gas treatment catalyst layer 1 comprises noble metal, silica sol solution and solvent; the noble metal is chloroplatinic acid or palladium chloride or a mixture of the chloroplatinic acid and the palladium chloride; the solvent is deionized water or absolute ethyl alcohol or a mixture of the deionized water and the absolute ethyl alcohol.
The denitration catalyst layer 2 comprises nano industrial titanium dioxide, vanadium pentoxide, a denitration catalyst active substance, a silica sol solution and water; the denitration catalyst active substance is tungsten trioxide or molybdenum trioxide.
The methanol cracking hydrogen production catalyst layer 3 comprises a methanol cracking hydrogen production catalyst active substance, zinc nitrate, a methanol cracking hydrogen production catalyst auxiliary agent, deionized water and a silica sol solution; one of active substances of the catalyst for preparing hydrogen by cracking methanol, namely ferric nitrate, cobalt nitrate, nickel nitrate and copper nitrate; the methanol cracking hydrogen production catalyst auxiliary agent is one of potassium nitrate, sodium nitrate, magnesium nitrate and calcium nitrate.
When in use, smoke is introduced from top to bottom, and the smoke comprises NO, methanol, and O2、N2The flue gas sequentially contacts a methanol cracking hydrogen production catalyst layer 3, a denitration catalyst layer 2 and a tail gas treatment catalyst layer 1 to carry out denitration and VOC removal; specifically, methanol in the flue gas is decomposed into reductive gases such as hydrogen and VOC under the action of the methanol cracking hydrogen production catalyst layer 3, then the reductive gases such as hydrogen and VOC selectively reduce nitrogen oxides into nitrogen under the action of the denitration catalyst layer 2, and finally the tail gas treatment catalyst layer 1 carries out catalytic oxidation treatment on the incompletely reacted VOC to prevent the VOC from generating secondary pollution to the environment.
The above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (10)
1. A denitration catalytic pore channel taking methanol as a reducing agent is characterized by comprising a tail gas treatment catalyst layer (1), a denitration catalyst layer (2), a methanol cracking hydrogen production catalyst layer (3) and a shell (4); the inner wall of the shell (4) is sequentially provided with the methanol cracking hydrogen production catalyst layer (3), the denitration catalyst layer (2) and the tail gas treatment catalyst layer (1) along the flue gas inlet direction; the catalyst layer (3) for hydrogen production by methanol cracking, the denitration catalyst layer (2) and the tail gas treatment catalyst layer (1) are arranged in a gradient manner.
2. The denitration catalyst channel of claim 1, wherein: the tail gas treatment catalyst layer (1), the denitration catalyst layer (2) and the methanol cracking hydrogen production catalyst layer (3) are sequentially arranged on the inner wall of the shell (4) from outside to inside.
3. The denitration catalyst channel of claim 1, wherein: the inner wall of the shell (4) is sequentially provided with a methanol cracking hydrogen production catalyst layer (3), a denitration catalyst layer (2) and a tail gas treatment catalyst layer (1) from outside to inside.
4. The denitration catalyst channel of claim 2, wherein: the tail gas treatment catalyst layer (1) is fixed on the inner wall of the shell (4), the denitration catalyst layer (2) is fixed on the inner layer of the tail gas treatment catalyst layer (1), and the methanol cracking hydrogen production catalyst layer (3) is fixed on the inner layer of the denitration catalyst layer (2).
5. The denitration catalyst channel of claim 2, wherein: the height of the tail gas treatment catalyst layer (1) is 30cm, and the thickness of the tail gas treatment catalyst layer is 1-5 mu m; the height of the denitration catalyst layer (2) is 1/3-2/3 of the total height of the tail gas treatment catalyst layer (1), and the thickness is 1-5 mu m; the height of the methanol cracking hydrogen production catalyst layer (3) is 1/6-1/3 of the total height of the tail gas treatment catalyst layer (1), and the thickness is 1-5 mu m.
6. The denitration catalyst channel of claim 3, wherein: the methanol cracking hydrogen production catalyst layer (3) is fixed on the inner wall of the shell (4), the denitration catalyst layer (2) is fixed on the inner layer of the methanol cracking hydrogen production catalyst layer (3), and the tail gas treatment catalyst layer (1) is fixed on the inner layer of the denitration catalyst layer (2).
7. The denitration catalyst channel of claim 3, wherein: the height of the methanol cracking hydrogen production catalyst layer (3) is 30cm, and the thickness is 1-5 mu m; the height of the denitration catalyst layer (2) is 1/3-2/3 of the total height of the methanol cracking hydrogen production catalyst layer (3), and the thickness is 1-5 mu m; the height of the tail gas treatment catalyst layer (1) is 1/6-1/3 of the total height of the methanol cracking hydrogen production catalyst layer (3), and the thickness is 1-5 mu m.
8. A denitration catalyst system comprising the cell channels of any one of claims 1 to 7, wherein: the catalyst comprises a plurality of pore channels, and a tail gas treatment catalyst layer (1), a denitration catalyst layer (2) and a methanol cracking hydrogen production catalyst layer (3) which correspond to the pore channels in number; the pore passages (4) are integrally and fixedly connected to form a matrix of the denitration catalytic system.
9. The denitration catalyst system of claim 8, wherein: the length, width and height of the substrate are 10cm 30 cm.
10. The denitration catalyst system of claim 8, wherein: the material of the substrate is one of cordierite honeycomb ceramic, mullite honeycomb ceramic and alumina honeycomb ceramic.
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