WO2003068390A1 - Nuevo catalizador para la reduccion de no a n2 con hidrogeno en condiciones de nox oxidantes - Google Patents
Nuevo catalizador para la reduccion de no a n2 con hidrogeno en condiciones de nox oxidantes Download PDFInfo
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- WO2003068390A1 WO2003068390A1 PCT/ES2003/000083 ES0300083W WO03068390A1 WO 2003068390 A1 WO2003068390 A1 WO 2003068390A1 ES 0300083 W ES0300083 W ES 0300083W WO 03068390 A1 WO03068390 A1 WO 03068390A1
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- catalyst
- mgo
- ceo
- platinum
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- 239000003054 catalyst Substances 0.000 title claims abstract description 205
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 33
- 239000001257 hydrogen Substances 0.000 title claims abstract description 27
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 26
- 230000009467 reduction Effects 0.000 title claims description 15
- 230000003647 oxidation Effects 0.000 title abstract 2
- 238000007254 oxidation reaction Methods 0.000 title abstract 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims abstract description 220
- 238000006243 chemical reaction Methods 0.000 claims abstract description 115
- 229910052697 platinum Inorganic materials 0.000 claims abstract description 43
- 230000000694 effects Effects 0.000 claims abstract description 29
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 25
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 claims abstract description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000001301 oxygen Substances 0.000 claims abstract description 13
- 239000003638 chemical reducing agent Substances 0.000 claims abstract description 11
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims abstract description 8
- 239000013078 crystal Substances 0.000 claims abstract description 3
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 38
- 238000000034 method Methods 0.000 claims description 30
- 230000003197 catalytic effect Effects 0.000 claims description 22
- 239000000395 magnesium oxide Substances 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- 229910001868 water Inorganic materials 0.000 claims description 18
- 230000008569 process Effects 0.000 claims description 14
- 238000005470 impregnation Methods 0.000 claims description 12
- 239000002243 precursor Substances 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 9
- 239000007864 aqueous solution Substances 0.000 claims description 8
- 238000002360 preparation method Methods 0.000 claims description 8
- 229910052751 metal Inorganic materials 0.000 claims description 7
- 239000002184 metal Substances 0.000 claims description 7
- 229910002651 NO3 Inorganic materials 0.000 claims description 5
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 4
- 238000001354 calcination Methods 0.000 claims description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 3
- 238000000354 decomposition reaction Methods 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000011777 magnesium Substances 0.000 claims description 3
- 239000006185 dispersion Substances 0.000 claims description 2
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 2
- MBUJACWWYFPMDK-UHFFFAOYSA-N pentane-2,4-dione;platinum Chemical compound [Pt].CC(=O)CC(C)=O MBUJACWWYFPMDK-UHFFFAOYSA-N 0.000 claims description 2
- CLSUSRZJUQMOHH-UHFFFAOYSA-L platinum dichloride Chemical compound Cl[Pt]Cl CLSUSRZJUQMOHH-UHFFFAOYSA-L 0.000 claims description 2
- NWAHZABTSDUXMJ-UHFFFAOYSA-N platinum(2+);dinitrate Chemical compound [Pt+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O NWAHZABTSDUXMJ-UHFFFAOYSA-N 0.000 claims description 2
- MGWGWNFMUOTEHG-UHFFFAOYSA-N 4-(3,5-dimethylphenyl)-1,3-thiazol-2-amine Chemical compound CC1=CC(C)=CC(C=2N=C(N)SC=2)=C1 MGWGWNFMUOTEHG-UHFFFAOYSA-N 0.000 claims 4
- JCXJVPUVTGWSNB-UHFFFAOYSA-N nitrogen dioxide Inorganic materials O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 claims 4
- 238000001035 drying Methods 0.000 claims 3
- 238000001704 evaporation Methods 0.000 claims 3
- 230000008020 evaporation Effects 0.000 claims 3
- 230000003993 interaction Effects 0.000 claims 3
- 229910052684 Cerium Inorganic materials 0.000 claims 2
- 150000001875 compounds Chemical class 0.000 claims 2
- 229910052749 magnesium Inorganic materials 0.000 claims 2
- 238000003801 milling Methods 0.000 claims 2
- 150000001785 cerium compounds Chemical class 0.000 claims 1
- 229910000420 cerium oxide Inorganic materials 0.000 claims 1
- 238000000227 grinding Methods 0.000 claims 1
- 150000002681 magnesium compounds Chemical class 0.000 claims 1
- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 claims 1
- 150000003058 platinum compounds Chemical class 0.000 claims 1
- 230000035484 reaction time Effects 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 20
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 10
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 abstract description 6
- -1 5 % vol) Chemical compound 0.000 abstract description 2
- CETPSERCERDGAM-UHFFFAOYSA-N ceric oxide Chemical compound O=[Ce]=O CETPSERCERDGAM-UHFFFAOYSA-N 0.000 abstract 1
- 239000011541 reaction mixture Substances 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 description 29
- 230000001590 oxidative effect Effects 0.000 description 21
- 229910004298 SiO 2 Inorganic materials 0.000 description 20
- 238000006722 reduction reaction Methods 0.000 description 11
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 10
- 230000007423 decrease Effects 0.000 description 10
- 229910000510 noble metal Inorganic materials 0.000 description 9
- 229910052721 tungsten Inorganic materials 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 7
- 238000002485 combustion reaction Methods 0.000 description 7
- 229930195733 hydrocarbon Natural products 0.000 description 7
- 150000002430 hydrocarbons Chemical class 0.000 description 7
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 230000009849 deactivation Effects 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 230000002195 synergetic effect Effects 0.000 description 6
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 5
- 229910021645 metal ion Inorganic materials 0.000 description 5
- 229910044991 metal oxide Inorganic materials 0.000 description 5
- 150000004706 metal oxides Chemical class 0.000 description 5
- 238000002156 mixing Methods 0.000 description 5
- 230000019635 sulfation Effects 0.000 description 5
- 238000005670 sulfation reaction Methods 0.000 description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 239000000919 ceramic Substances 0.000 description 4
- 235000012239 silicon dioxide Nutrition 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 238000010531 catalytic reduction reaction Methods 0.000 description 3
- 229910052681 coesite Inorganic materials 0.000 description 3
- 229910052906 cristobalite Inorganic materials 0.000 description 3
- 231100000572 poisoning Toxicity 0.000 description 3
- 230000000607 poisoning effect Effects 0.000 description 3
- 239000000377 silicon dioxide Substances 0.000 description 3
- 238000003980 solgel method Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 229910052682 stishovite Inorganic materials 0.000 description 3
- 229910052905 tridymite Inorganic materials 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 229910018663 Mn O Inorganic materials 0.000 description 2
- 229910003176 Mn-O Inorganic materials 0.000 description 2
- 229910017313 Mo—Co Inorganic materials 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 2
- 229910010413 TiO 2 Inorganic materials 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 description 2
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 2
- 229910052737 gold Inorganic materials 0.000 description 2
- 239000010931 gold Substances 0.000 description 2
- MUMZUERVLWJKNR-UHFFFAOYSA-N oxoplatinum Chemical compound [Pt]=O MUMZUERVLWJKNR-UHFFFAOYSA-N 0.000 description 2
- 229910003446 platinum oxide Inorganic materials 0.000 description 2
- 230000000750 progressive effect Effects 0.000 description 2
- LIVNPJMFVYWSIS-UHFFFAOYSA-N silicon monoxide Inorganic materials [Si-]#[O+] LIVNPJMFVYWSIS-UHFFFAOYSA-N 0.000 description 2
- 241000894007 species Species 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 230000001988 toxicity Effects 0.000 description 2
- 231100000419 toxicity Toxicity 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 229910002839 Pt-Mo Inorganic materials 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
- 229940050494 j-max Drugs 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002923 metal particle Substances 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
- B01J27/053—Sulfates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8628—Processes characterised by a specific catalyst
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/92—Chemical or biological purification of waste gases of engine exhaust gases
- B01D53/94—Chemical or biological purification of waste gases of engine exhaust gases by catalytic processes
- B01D53/9404—Removing only nitrogen compounds
- B01D53/9409—Nitrogen oxides
- B01D53/9413—Processes characterised by a specific catalyst
- B01D53/9418—Processes characterised by a specific catalyst for removing nitrogen oxides by selective catalytic reduction [SCR] using a reducing agent in a lean exhaust gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/10—Magnesium; Oxides or hydroxides thereof
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/63—Platinum group metals with rare earths or actinides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/202—Hydrogen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/10—Noble metals or compounds thereof
- B01D2255/102—Platinum group metals
- B01D2255/1021—Platinum
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/204—Alkaline earth metals
- B01D2255/2047—Magnesium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
- B01D2255/206—Rare earth metals
- B01D2255/2065—Cerium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
- B01J23/56—Platinum group metals
- B01J23/58—Platinum group metals with alkali- or alkaline earth metals
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
- B01J35/391—Physical properties of the active metal ingredient
- B01J35/394—Metal dispersion value, e.g. percentage or fraction
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/03—Precipitation; Co-precipitation
- B01J37/036—Precipitation; Co-precipitation to form a gel or a cogel
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/12—Oxidising
- B01J37/14—Oxidising with gases containing free oxygen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/16—Reducing
- B01J37/18—Reducing with gases containing free hydrogen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/20—Sulfiding
Definitions
- This invention refers to a new platinum-based catalyst with excellent activity, stability and selectivity for the reduction of NO to N 2 by using H 2 as a reducing agent in the low temperature range of 100-200 ° C and in the presence of excess oxygen (eg, 5% vol), 5% vol H 2 O and / or 20 ppm of SO 2 in the reactor feed.
- This catalyst can be used in the selective conversion of nitric oxide, produced in many industrial combustion processes, to N 2 gas. It is known that hydrogen is available in numerous industrial facilities. Using said catalyst, only a very small percentage of the available hydrogen is necessary for the reduction of NO to N 2 under purely oxidizing NOx conditions in the low temperature range of 100-200 ° C.
- HC-SCR The selective catalytic reduction of NO with hydrocarbons
- the main advantage of this catalytic reaction is the potential use of hydrocarbons as reducing species that can be found in the combustion process exhaust gases that operate under purely oxidizing NOx conditions.
- Catalysts that have attracted attention for the HC-SCR process of NO can be divided into three main groups: (a), supported noble metals; (b), zeolites exchanged with metal ions; and (c), metal oxide catalysts [3].
- the noble metals supported have shown the best and only catalytic behavior for the reduction of NO with hydrocarbons under oxidizing conditions at reaction temperatures as low as 120-250 ° C [8-16]. Furthermore, it was found that these catalysts are more resistant to deactivation in the presence of water and / or SO 2 [17,18]. However, despite their exceptional activity in this low temperature region, the supported Pt and Pd catalysts have low selectivity values at N 2 [19,20] and a relatively narrow operating temperature range. In contrast, zeolites exchanged with metal ions are very active and selective for the SCR of NO with hydrocarbons at relatively low temperatures. However, these catalysts have an even narrower operating temperature range compared to that of the noble metals supported.
- Platinum supported catalysts such as Pt / Al 2 O 3 and Pt / SiO 2
- Pt / Al 2 O 3 and Pt / SiO 2 have been found to be the most active for the NO / H / O 2 reaction under purely oxidizing NOx conditions at low temperature (T ⁇ 200 ° C) [47-51].
- Yokota et al. [50] reported results of catalytic activity in the reduction of NO with H 2 in the presence of O on a Pt-Mo-Na / SiO 2 catalyst, while Frank et al. [47] reported kinetic results of the NO H 2 / O reaction on a Pt-Mo-Co / ⁇ -Al 2 O 3 catalyst.
- a new platinum-based catalyst which exhibits excellent activity, selectivity and stability for the reduction of nitric oxide using hydrogen as a reducing agent in the low temperature range of 100-200 ° C and in the presence of excess oxygen.
- the catalyst consists of platinum crystals in contact with the two phases of MgO and CeO 2 or in the platinum form supported on a support of the MgO-CeO 2 mixed oxide previously selectively sulfated. Prior to the impregnation of the oxide phases with the platinum precursor, pre-sulphation of the support (50% MgO-CeO 2 ) is necessary. This is achieved by impregnating the support with an aqueous solution of NH NO 3 followed by (NH) 2 SO 4 as collected in Example 1.
- the 0.1 wt% Pt / 50% MgO-CeO 2 catalyst can be prepared by any means known to those practicing in this art, including the wet impregnation technique of the pre-sulfated support with an aqueous solution of the Pt precursor (p. eg, hexachloroplatinic acid solution (H 2 PtCl 6 ). After preparation of the supported Pt catalyst, at least 2 h of air calcination at 600 ° C is required for the complete transformation of the platinum precursor into platinum oxide.
- the catalyst was prepared by the wet impregnation method described previously. Identical catalysts can be prepared using other preparation techniques, known to practitioners of this art, and other metal precursors such as platinum nitrate, platinum acetyl acetone, platinum chloride, etc. However, it has been found in this work that the preparation of the catalyst mentioned above using the sol-gel method [58] provided better results, in terms of catalytic activity and selectivity to N 2 in the NO / H 2 / O 2 reaction ( see Fig. 3). Eight different mixtures of MgO-CeO 2 were used as supports with magnesium oxide content (x% p MgO) ranging from 0 to 100%.
- the pre-sulfated MgO-CeO 2 mixed oxide support (see Example 1) is essential to achieve high stability towards SO 2 deactivation (Example 8, Fig. 7). It should be noted here that the catalyst 0.1% p Pt / MgO-CeO 2 not sulfated showed selectivity values at N 2 in the range 65-72%, while the pre-sulfated catalyst showed higher selectivity values at N 2 at 80%, see Example 6 and Fig. 5).
- the Pt / s-50% MgO-CeO catalyst has an extraordinarily wide operating temperature range ( ⁇ T, see Table 1), much wider than that obtained on the Pt / SiO 2 and Pt / Lao.5Ce catalysts 0 . 5 min 3 .
- ⁇ T operating temperature range
- the last catalyst is more active and selective of all reported for the NO / H 2 / O 2 reaction under oxidizing NOx conditions [54].
- the rate of integral nitrogen production on the Pt / MgO-CeO 2 catalyst can even be increased by increasing the partial pressure of hydrogen.
- the rate of integral production of N 2 on the mentioned catalyst can increase up to about four times when the partial pressure of H 2 increases from 1 to 3% vol to 200 ° C (Example 9, Fig. 8).
- the MgO to CeO 2 ratio is an important factor that affects the catalytic behavior (reaction rate and selectivity) of the Pt / MgO-CeO 2 catalyst. It is shown (see Example 2, Fig. 1) that the catalyst with a weight ratio of MgO to CeO 2 equal to the unit has the highest integral production rate of N 2 both at low and high reaction temperature. As shown in Fig. 1, almost all compositions have higher speeds than those predicted by the mixing rule (dashed line) at 150 ° C (Example 2, Eq. [1]). Thus, a positive synergistic effect results. However, when the reaction temperature increases to 300 ° C the behavior of the reaction rate against the MgO content is different (Fig. 1).
- the catalyst Pt / s-50% MgO-CeO 2 showed excellent stability over time in reaction in the presence of 5% vol H 2 O in the feed (Example 7, Fig. 6), which is superior to that observed with the Pt / SiO 2 and Pt / Lao catalysts. 5 Ce 0 . 5 MnO 3 previously investigated [54,59]. Constant production rates of N 2 were observed even after 24 h in current on the catalyst 0.1% ⁇ Pt / s-50% MgO-CeO 2 . On the other hand, the integral production speed of N 2 obtained with the Pt / Lao catalysts. 5 Ce 0 .
- the fresh catalyst Pt / MgO-CeO is deactivated in the presence of 20 ppm SO 2 in the feed stream (Fig. 7).
- This is a well known phenomenon in NOx catalysts.
- Deactivation of the Pt / MgO-CeO 2 catalyst probably occurs by adsorption and reaction of the gaseous SO 2 with the oxide phases of the catalyst resulting in a progressive sulfation of the support (eg, MgSO 4 , Ce 2 (SO 4 ) 3 ).
- these processes probably cause irreversible poisoning of the active centers by nitrate / nitrite formation according to the literature [51,61].
- the catalyst Pt / s-MgO-CeO 2 exhibits excellent stability in the presence of SO 2 .
- the adsorption of SO in such centers also inhibits the subsequent sulfation of the support and the development of the crystalline phases MgSO and / or Ce 2 (SO 4 ) 3 under reaction conditions.
- the effective sulfation of the MgO-CeO 2 solid can also be ensured by wet impregnation of the original sample with a nitrate solution.
- the results obtained in this case are the same as those described above.
- Hodjati et al. [62] also reported similar behavior on a NOx BaSnO 3 catalyst.
- the present invention eg the catalyst 0.1% Pt / s-50% MgO-CeO 2 pre-sulfated, is a new catalyst in which the main differences with respect to catalysts based on noble metals and other NOx catalysts reported for the NO / H 2 / O 2 reaction are as follows:
- the metal oxide catalysts have selectivity levels elevated to N 2 in the NO / H 2 / O 2 reaction, very similar to those obtained with the new Pt / s-MgO-CeO 2 catalyst.
- oxide catalysts are much less active than compared to the last noble metal.
- the metal oxide catalyst is active only at temperatures above 400 ° C while the Pt / s-MgO-CeO 2 catalyst exhibits a maximum conversion of NO to 150 ° C.
- metal oxide catalysts cannot be considered as candidates for NOx applications under low temperature oxidizing conditions.
- - Zeolites exchanged with metal ions are very active and selective for NO SCR with hydrocarbons at relatively low temperatures.
- these catalysts have a very narrow operating temperature range compared to the new Pt / s-MgO-CeO 2 catalyst.
- the activity of catalysts exchanged with metal ions decreases strongly in the presence of water and / or SO, while the new catalyst Pt / s-MgO-CeO 2 remains stable in the presence of water or SO 2 .
- the new Pt / s-MgO-CeO 2 catalyst is the most active, selective and stable reported to date for the NO / H 2 / O 2 reaction under oxidizing NOx conditions.
- this catalyst has the widest operating temperature window reported for the aforementioned reaction (Example 5, Table 1).
- - NH-SCR is widely used as anti-pollution technology for NO removal from stationary sources, mainly in conventional thermal power plants [1].
- the problems of toxicity and manipulation of ammonia [1,4] constitute the greatest obstacles to using this technology by the general public. Additionally, the problems related to the corrosion of NH 3 and the poisoning of catalysts by SO 2 seem difficult to solve.
- H 2 -SCR hydrogen-based NO x SCR technology
- This example illustrates the synthesis of platinum-based catalysts, supported on a mixed MgO-CeO 2 oxide.
- the pre-sulfated Pt / s-MgO-CeO 2 catalysts were prepared by the wet impregnation method as follows: lg of MgO (Aldrich 34,279-3, 99 +%) and 1 g of CeO 2 (Aldrich 34,295-5, 99.9 %) were impregnated with 50 ml of an aqueous solution containing 7.1 mg (90 ⁇ moles) of NH NO 3 (Aldrich, ultra pure). The water was evaporated under continuous stirring and the residue was dried at 100 ° C for 4 h.
- the residue was then screened and heated at 300 ° C in the presence of air for 2 h for complete decomposition of the ammonium cations. This procedure was followed to ensure the protection (of sulfation) of the centers for the adsorption of nitrate by the support.
- the resulting solid was then impregnated with 50 ml of an aqueous solution containing 24 mg (90 ⁇ moles) of (NH 4 ) 2 SO 4 (Aldrich, ultra pure). The water was then evaporated under continuous stirring and the residue was dried at 100 ° C for 4 h. The dried residue was screened and heated in air at 600 ° C for 2 h with subsequent cooling to room temperature.
- the 2 g of the sulfated support were then impregnated with an aqueous solution containing the desired amount of hexachloroplatinic acid (Aldrich, 26,258-7).
- the excess water was evaporated under continuous stirring and the residue was dried at 80 ° C for 24 h.
- the dried residue was screened and heated at 600 ° C in air flow for at least 2 h for complete decomposition of hexachloroplatinic acid.
- the catalyst was reduced then in H 2 flow at 300 ° C for at least 2 h.
- the metallic platinum content varied in the range 0.1-0.2% by weight.
- MgO-CeO 2 catalysts Two 0.5% p Pt / 50% MgO-CeO 2 catalysts were also prepared by the sol-gel procedure following the experimental conditions described by Balakrishnan et al. [58]. Heavy amounts of Mg (OEt) 2 , Ce (NO 3 ) 3 , and Pt (NH 3 ) 2 (NO 3 ) 2 were dissolved in a solution of EtOH / H 2 O followed by continuous stirring and heating at 60 ° C until a gel is formed. The mixed oxide support 50% p MgO-CeO 2 was also prepared by the ceramic method [63] using pure oxides as starting materials. On the resulting solid was then deposited 0.5% p of Pt by wet impregnation.
- the platinum dispersion of the Pt / MgO-CeO 2 catalysts was measured by chemisorption of H 2 at 25 ° C followed by the programmed thermal desorption (TPD) in He flow. Before the TPD of H 2 TPD the sample was purged in He for 45 min at room temperature. A platinum dispersion of 83% in the catalyst 0.1% p Pt / 50% MgO-CeO 2 was determined .
- Integral nitrogen production rates for the reaction on platinum supported catalysts in the range of 100-400 ° C were determined as follows:
- R m (x / 100).
- R Ce02 ( ⁇ moles / gs) [1] Equation [1] allows to calculate the reaction rate (R m ) of the mixture of the two catalytic phases of Pt / CeO 2 and Pt / MgO based on the individual velocities of each catalytic phase and the content x% p of the phase in the mix. If there is no cooperation (synergy) between the two phases, then the experimental reaction rate observed on the mixture of the two solids must also be predicted by Eq. [one]. As seen in Fig.
- This example illustrates the effect of the preparation method on the temperature profile of the integral production rate of N 2 for the NO / H / O 2 reaction under oxidizing NOx conditions on the catalysts 0.5% p Pt / 50% MgO -CeO 2 . 100 mg of each catalyst 0.5% wt Pt / 50% MgO-CeO 2 prepared by the wet, sol-gel and ceramic impregnation methods were used.
- Figure 3 presents the temperature profile of the integral production rate of N 2 per gram of the total platinum obtained on the three catalysts mentioned for NO / H 2 / O 2 reaction in the range 100-400 ° C. From Fig. 3 it is clear that the catalyst 0.5% p Pt / 50% oMgO-CeO 2 prepared by the sol-gel method has substantially higher production rates of N 2 in the range 120-200 ° C compared to catalysts prepared by the ceramic method and the wet impregnation method. The last two solids show a very similar catalytic behavior in the 100-400 ° C range. Thus, the sol-gel method is preferred for the preparation of the Pt / 50% MgO-CeO 2 catalyst instead of the wet ceramic or impregnation methods described previously.
- Table 1 below compiles the catalytic behavior of several Pt supported catalysts for the NO / H 2 / O 2 reaction under oxidizing NOx conditions reported in the open literature. The corresponding results obtained with the catalyst 0.1% p Pt / s-50% MgO-CeO 2 for the mentioned reaction are also included in Table 1.
- ⁇ T is the temperature range in which XN O is greater than 1/2 of the maximum NO conversion observed. The last parameter could be used to define the quality of the operating temperature window. For example, a high value of ⁇ T corresponds to the best desired operation of the catalyst under practical conditions.
- Table 1 also compiles the integral production speed of N 2 per gram of total Pt (Rm) evaluated according to the values obtained from XN O and SN 2 for each catalyst.
- the average conversion value of NO (XNO) in the range 100-400 ° C is also included in Table 1. This parameter was calculated using the following formula: 400 400 X N0 dT ⁇ XNO dT
- T ! and T 2 are the lowest and highest temperatures, respectively, and where the catalytic activity can be measured.
- the catalyst present 0.1% p Pt / s- 50% MgO-CeO 2 is better in terms of the catalytic behavior of all tabulated catalysts. Since the reaction orders with respect to the three reactants must not exceed 1.5, it is evident from the data in Table 1 that the catalyst 0.1% p Pt / s-50% MgO-CeO 2 has the highest activity, selectivity and operating temperature window ( ⁇ T) never reported for the NO / H 2 / O 2 reaction. However, the comparison between the Pt / s-MgO-CeO 2 , Pt / La-Ce-Mn-O Pt / Al 2 O 3 and Pt / SiO 2 catalysts is direct when the same experimental conditions are used.
- the average NO conversion value increases by approximately 50% when the Pt is supported on s-50%> MgO-CeO 2 with respect to the Lao support. 5 Ce 0 . 5 MnO 3 , while the increase becomes wider (230%) if the comparison is made with the SiO 2 support.
- the average N 2 selectivity value of 86.5% obtained with the Pt / s-50% MgO-CeO 2 catalyst is the same as that obtained with the Pt / Lao catalyst. 5 Ce 0 . 5 MnO 3 but it is much higher than that obtained with the rest of the catalysts reported in Table 1.
- This example compares the activity (in terms of NO, X NO conversion) of the catalysts 0.1% p Pt / s-50% MgO-CeO 2 (•), 0.1% p Pt / La 0 . 5 Ce 0 . 5 MnO 3 (A) and 0.1% p Pt / SiO 2 (B) for the NO / H / O reaction under oxidizing NOx conditions with 5% vol H 2 O in the feed and in the range 100-400 ° C.
- the results indicate that the catalyst 0.1% p Pt / La 0.5 Ceo. 5 MnO 3 has the highest activity than any other reported to date for the NO / H 2 / O 2 reaction [54].
- the catalyst 0.1% p Pt / s- 50% MgO-CeO2 presents values .DELTA.T two and three times higher than those observed with the catalysts 0.1% wt Pt / 0. 5 Ce 0. 5 MnO 3 and 0.1% w Pt / SiO2, respectively (see Table 1) It is observed that the Pt / SiO 2 catalyst exhibits practically zero activity at temperatures above 250 ° C.
- the ⁇ T value obtained with the catalyst 0.1% p Pt / s-50% MgO-CeO 2 is the highest of all reported in l to bibliography (Table 1).
- Table 1 Catalytic activity of several Pt supported catalysts for the NO / H 2 / O 2 reaction in the temperature range 100- ⁇ 100 or C rp C
- ⁇ T Temperature range where X N or > ⁇ N ⁇ ma / 2, maximum formation speed of N 2 (per gram of Pt), Temperature at which maximum NO conversion is measured
- X N0 average NO conversion value in the range 100-400 ° C: 10% H 2 0 is present in the feed, 5% H 2 0 is present in the feed.
- This example compares the selectivity to N 2 (S N2 ) of the NO / H 2 / O 2 reaction under oxidizing NOx conditions as a function of the reaction temperature in the range 100-400 ° C obtained with the catalysts 0.1% p Pt / s-50% MgO-CeO 2 (•), 0.1% p Pt / La 0 . 5 Ce 0 . MnO 3 (A) and 0.1% p Pt / SiO 2 (1).
- the experimental reaction conditions used in this example are the same as those used in example 5.
- the Pt / s-50% MgO-CeO 2 and Pt / Lao .5 Ce 0.5 MnO 3 catalysts have high selectivity values at N 2 in the range 100-400 ° C.
- the catalyst Pt / s-50% MgO-CeO 2 shows selectivity values at N 2 between 82 and 85%, while the catalyst Pt / Lao. 5 ceo. 5 MnO 3 has S N2 values in the 82-90% range.
- the selectivity to N 2 is approximately constant at levels of 96 and 93% with the catalysts Pt / s-50% MgO-CeO 2 and Pt / Lao.
- the Pt / s-50% MgO-CeO 2 catalyst has an average N 2 selectivity value of 86.5% which is practically the same as that obtained with the Pt / La 0 catalyst. 5 Ce 0. MnO 3 (86.4%). Much lower selectivity values (50-65%) are obtained in the case of the Pt / SiO 2 catalyst having an average value of S> j 2 of 60.7% (Table 1). The average value S N2 obtained with the catalyst 0.1% p Pt / s-50% MgO-CeO 2 is the highest of those reported in the literature to date (Table 1).
- the stability of the catalyst 0.1% p Pt / 50% MgO-CeO 2 is studied for the NO / H 2 / O 2 reaction under oxidizing NOx conditions in the presence of SO 2 in the feed.
- Sulfur dioxide is one of the known poisons of many of the NOx catalysts [17].
- the NO / H 2 / O 2 / SO 2 reaction was studied at 200 ° C using 150 mg of the catalyst 0.1% p Pt / 50% MgO-CeO 2 and a feed composition of 0.25% vol NO, 1% vol H 2.5 % vol O 2 , 23 ppm SO 2 and 93.75% vol He.
- a flow rate of 100 ml (STP) / min was used which is equivalent to a GHSV of approximately 80,000 h "1.
- Figure 7 presents the NO conversion profiles with the current time at 200 ° C on the catalyst 0.1% p Pt / 50% MgO-CeO 2 when the 50% MgO-CeO 2 sulfate and unsulfated support is used (see example 1)
- the Pt / MgO-CeO 2 catalyst with the unsulfated support is it quickly deactivates with the current time and becomes completely deactivated after 20 h in reaction, however, the Pt / MgO-CeO 2 catalyst with the previously sulfated support has a completely different behavior (Example 1, Fig. 7).
- This catalyst shows only a slight decrease in the NO conversion during the first 4 hours in current, at the same time it shows a practically constant NO conversion after the first 4 hours for a total current time of 24 h.
- stability result exceeds nte and of industrial importance since no stable catalysts have been reported in the NO / H 2 / O 2 reaction in the presence of low concentrations of SO 2 .
- concentration of SO 2 in many industrial combustion streams is in the range of 5-20 ppm.
- the 0.1% p Pt / 50% MgO-CeO catalyst with the pre-sulfated support can find practical applications even in cases of maximum SO concentrations present in the combustion streams.
- This example shows the effect of hydrogen partial pressure on the temperature profile of the integral production speed N 2 in the NO / H 2 / O 2 reaction under oxidizing NOx conditions on the catalyst 0.1% p Pt / 50% MgO -CeO 2 catalyst.
- the experimental reaction conditions used in this example are the same as in Example 3.
- Figure 8 shows the temperature profiles of the N 2 production rate obtained with the catalyst 0.1% p Pt / 50% MgO-CeO 2 ( unsulfated support) for the NO / H 2 / O reaction using hydrogen concentrations 1 and 3% vol.
- the integral production rate of N 2 improves substantially for all reaction temperatures when the concentration of H 2 increases from 1 to 3% vol.
- This last example describes the effect of contact time (in terms of the ratio / F) on the conversion of NO with the catalyst 0.1% p Pt / 50% MgO-CeO 2 .
- the feed consisted of 0.25% vol NO, 1.0% vol Efe, 5.0% vol O 2 and 93.75% vol He.
- the W / F variation was achieved by adjusting the amount of catalyst (75-150 mg) and the flow rate (50-200 ml / min).
- Figure 9 shows the effect of contact time on the conversion of NO with the catalyst 0.1% p Pt / MgO-CeO 2 at 150 ° C.
- the NO conversion increases rapidly with increasing contact time from 0.02 to 0.09 gs / ml.
- the contact time in the NH 3 -SCR NO reactors on commercial catalysts have typical contact times in the range of 0.04-0.6 gs / ml [1.55-57].
- the low contact time required to obtain high conversions of NO on the Pt / MgO-CeO 2 catalyst indicates that the activity of this catalyst is quite high for industrial application.
- Figure 1 shows the integral reaction rates of N 2 production per gram of catalyst as a function of the MgO content (x,% p) in the catalysts 0.5 t% Pt / xMgO-CeO 2 , obtained during the NO / H reaction 2 / O 2 at 150 ° and 300 ° C.
- Figure 2 shows the influence of the content of Pt metal (% wt) on the integral reaction rate of N 2 production during the NO / H 2 / O 2 reaction under NOx conditions on the catalysts x% p Pt / 50% MgO-CeO 2 in the range 100-
- Figure 3 shows the effect of the preparation method on the temperature profile of the integral production rate of N 2 for the NO / H 2 / O 2 reaction under NOx conditions on the catalyst 0.5% p Pt / 50% MgO- CeO 2 .
- Figure 4 compares the NO (XN O ) conversion temperature profiles of the NO / H 2 / O 2 reaction under NOx conditions on the catalyst 0.1% p Pt / s-50% MgO-
- Figure 6 compares the stability (in terms of integral reaction rates of N 2 ) with the current time of the catalysts 0.1% p Pt / s-50% MgO- CeO 2 (•), 0.1% p Pt / Lao. 5 Ce 0 . 5 MnO 3 (A) and 0.1% p Pt / SiO 2 (u).
- Figure 7 shows the influence of the presence of SO 2 in the reaction stream on the conversion of NO (XN O ) during the NO / H 2 / O 2 reaction under oxidizing NOx conditions on the catalyst 0.1% p Pt / 50 MgO-CeO 2 pre-sulfated (•) and not sulfated (A).
- Figure 8 shows the effect of the partial pressure of hydrogen on the integral production speed of N 2 versus the temperature for the NO / H / O 2 reaction under oxidizing NOx conditions at 1 bar of total pressure on the catalyst 0.1% p Pt / 50% MgO-CeO 2 .
- Figure 9 shows the influence of contact time (in terms of W / F) on the conversion of NO in the NO / H 2 / O reaction under oxidizing NOx conditions on the catalyst 0.1% p Pt / 50% MgO-CeO 2 .
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AU2003206981A AU2003206981A1 (en) | 2002-02-15 | 2003-02-14 | Novel catalyst for the reduction of no to n2 with hydrogen under nox oxidation conditions |
DE60321136T DE60321136D1 (de) | 2002-02-15 | 2003-02-14 | PRESULFATIERTER UND PRENITRIERTER KATALYSATOR, ENHALTEND PLATINUM AUF TRÄGER BESTEHEND AUS MAGNESIUMOXID UND CEROXID FÜR DIE REDUKTION VON NO ZU N2 MIT WASSERSTOFF UNTER NOx-OXIDATIONSBEDINGUNGEN |
AT03704721T ATE395972T1 (de) | 2002-02-15 | 2003-02-14 | Presulfatierter und prenitrierter katalysator, enhaltend platinum auf träger bestehend aus magnesiumoxid und ceroxid für die reduktion von no zu n2 mit wasserstoff unter nox- oxidationsbedingungen |
EP03704721A EP1475149B1 (en) | 2002-02-15 | 2003-02-14 | CATALYST CONTAINING PLATINUM ON A SUPPORT CONSISTING OF MAGNESIUM OXIDE AND CERIUM OXIDE FOR THE REDUCTION OF NO TO N2 WITH HYDROGEN UNDER NOx OXIDATION CONDITIONS |
JP2003567568A JP2005516767A (ja) | 2002-02-15 | 2003-02-14 | NOx酸化条件下で水素を用いてNOをN2へ還元するための新規な触媒 |
US10/915,961 US7105137B2 (en) | 2002-02-15 | 2004-08-11 | Catalyst for the reduction of NO to N2 with hydrogen under NOx oxidation conditions |
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- 2002-02-15 ES ES200200368A patent/ES2192985B1/es not_active Expired - Fee Related
-
2003
- 2003-02-14 ES ES03704721T patent/ES2306855T3/es not_active Expired - Lifetime
- 2003-02-14 AT AT03704721T patent/ATE395972T1/de active
- 2003-02-14 EP EP03704721A patent/EP1475149B1/en not_active Expired - Lifetime
- 2003-02-14 DE DE60321136T patent/DE60321136D1/de not_active Expired - Lifetime
- 2003-02-14 WO PCT/ES2003/000083 patent/WO2003068390A1/es active IP Right Grant
- 2003-02-14 AU AU2003206981A patent/AU2003206981A1/en not_active Abandoned
- 2003-02-14 JP JP2003567568A patent/JP2005516767A/ja active Pending
-
2004
- 2004-08-11 US US10/915,961 patent/US7105137B2/en not_active Expired - Fee Related
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Also Published As
Publication number | Publication date |
---|---|
ATE395972T1 (de) | 2008-06-15 |
DE60321136D1 (de) | 2008-07-03 |
EP1475149B1 (en) | 2008-05-21 |
ES2306855T3 (es) | 2008-11-16 |
ES2192985B1 (es) | 2005-02-16 |
EP1475149A1 (en) | 2004-11-10 |
US20050090393A1 (en) | 2005-04-28 |
ES2192985A1 (es) | 2003-10-16 |
US7105137B2 (en) | 2006-09-12 |
AU2003206981A1 (en) | 2003-09-04 |
JP2005516767A (ja) | 2005-06-09 |
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