WO2005044426A1 - 窒素酸化物を接触還元する方法をそのための触媒 - Google Patents
窒素酸化物を接触還元する方法をそのための触媒 Download PDFInfo
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- WO2005044426A1 WO2005044426A1 PCT/JP2004/016910 JP2004016910W WO2005044426A1 WO 2005044426 A1 WO2005044426 A1 WO 2005044426A1 JP 2004016910 W JP2004016910 W JP 2004016910W WO 2005044426 A1 WO2005044426 A1 WO 2005044426A1
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- Prior art keywords
- catalyst
- catalyst component
- exhaust gas
- oxide
- oxides
- Prior art date
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- 239000003054 catalyst Substances 0.000 title claims abstract description 641
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- 230000001603 reducing effect Effects 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims description 64
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims abstract description 180
- 239000007789 gas Substances 0.000 claims abstract description 98
- 229910052697 platinum Inorganic materials 0.000 claims abstract description 88
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims abstract description 79
- CETPSERCERDGAM-UHFFFAOYSA-N ceric oxide Chemical compound O=[Ce]=O CETPSERCERDGAM-UHFFFAOYSA-N 0.000 claims abstract description 69
- 229910000422 cerium(IV) oxide Inorganic materials 0.000 claims abstract description 69
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- 239000000446 fuel Substances 0.000 claims abstract description 49
- 239000000203 mixture Substances 0.000 claims abstract description 48
- 229910000510 noble metal Inorganic materials 0.000 claims abstract description 46
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- PUDIUYLPXJFUGB-UHFFFAOYSA-N praseodymium atom Chemical compound [Pr] PUDIUYLPXJFUGB-UHFFFAOYSA-N 0.000 claims abstract description 25
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- 229910052792 caesium Inorganic materials 0.000 description 1
- TVFDJXOCXUVLDH-UHFFFAOYSA-N caesium atom Chemical compound [Cs] TVFDJXOCXUVLDH-UHFFFAOYSA-N 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 239000012876 carrier material Substances 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 229910000420 cerium oxide Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000002734 clay mineral Substances 0.000 description 1
- 238000012790 confirmation Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229910001431 copper ion Inorganic materials 0.000 description 1
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- MWFSXYMZCVAQCC-UHFFFAOYSA-N gadolinium(iii) nitrate Chemical compound [Gd+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O MWFSXYMZCVAQCC-UHFFFAOYSA-N 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical group [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 239000008240 homogeneous mixture Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 229910052809 inorganic oxide Inorganic materials 0.000 description 1
- MVFCKEFYUDZOCX-UHFFFAOYSA-N iron(2+);dinitrate Chemical compound [Fe+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MVFCKEFYUDZOCX-UHFFFAOYSA-N 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 1
- 238000004898 kneading Methods 0.000 description 1
- 238000006138 lithiation reaction Methods 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 238000002796 luminescence method Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- CFYGEIAZMVFFDE-UHFFFAOYSA-N neodymium(3+);trinitrate Chemical compound [Nd+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O CFYGEIAZMVFFDE-UHFFFAOYSA-N 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- UJVRJBAUJYZFIX-UHFFFAOYSA-N nitric acid;oxozirconium Chemical compound [Zr]=O.O[N+]([O-])=O.O[N+]([O-])=O UJVRJBAUJYZFIX-UHFFFAOYSA-N 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 239000000049 pigment Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- TYJJADVDDVDEDZ-UHFFFAOYSA-M potassium hydrogencarbonate Chemical compound [K+].OC([O-])=O TYJJADVDDVDEDZ-UHFFFAOYSA-M 0.000 description 1
- 239000010970 precious metal Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- YZDZYSPAJSPJQJ-UHFFFAOYSA-N samarium(3+);trinitrate Chemical compound [Sm+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O YZDZYSPAJSPJQJ-UHFFFAOYSA-N 0.000 description 1
- 229910052711 selenium Inorganic materials 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- 229910001923 silver oxide Inorganic materials 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000002344 surface layer Substances 0.000 description 1
- YJVUGDIORBKPLC-UHFFFAOYSA-N terbium(3+);trinitrate Chemical compound [Tb+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O YJVUGDIORBKPLC-UHFFFAOYSA-N 0.000 description 1
- 238000010998 test method Methods 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
- 229910052727 yttrium Inorganic materials 0.000 description 1
- VWQVUPCCIRVNHF-UHFFFAOYSA-N yttrium atom Chemical compound [Y] VWQVUPCCIRVNHF-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- 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
- B01D53/9422—Processes characterised by a specific catalyst for removing nitrogen oxides by NOx storage or reduction by cyclic switching between lean and rich exhaust gases (LNT, NSC, NSR)
-
- 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
- B01J23/64—Platinum group metals with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J23/652—Chromium, molybdenum or tungsten
-
- 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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing iron group metals, noble metals or copper
- B01J29/74—Noble metals
- B01J29/7415—Zeolite Beta
-
- 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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/72—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing iron group metals, noble metals or copper
- B01J29/76—Iron group metals or copper
- B01J29/7615—Zeolite Beta
-
- 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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65
- B01J29/78—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups B01J29/08 - B01J29/65 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
- B01J29/7815—Zeolite Beta
-
- B01J35/19—
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/20—Metals or compounds thereof
-
- 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
Definitions
- the present invention nitrogen oxides (mainly consisting N_ ⁇ and N0 2 Prefecture.
- N_ ⁇ _X nitrogen oxides (mainly consisting N_ ⁇ and N0 2 Prefecture.
- the present invention supplies a fuel to a combustion chamber of a diesel engine / gasoline engine in a periodic rich / lean fuel supply process (excurs ion: process), burns the fuel, and brings the generated exhaust gas into contact with a catalyst.
- the present invention relates to a method for catalytic reduction of NOx in exhaust gas and a catalyst therefor.
- Such a method and a catalyst therefor are suitable, for example, for reducing and eliminating harmful nitrogen oxides contained in exhaust gas from automobile engines.
- the present invention is, sulfur oxides (mainly consisting of S 0 2 and S_ ⁇ 3. The following will leave S_ ⁇ _X.)
- S_ ⁇ _X sulfur oxides
- the present invention relates to a method for catalytic reduction of NOx in exhaust gas produced and supplied by combustion without deteriorating the catalyst, and a catalyst therefor.
- the term “excursion” means that the air Z fuel ratio moves from its average value to both along the time axis, or such an operation.
- the term “rich” means that the air / fuel ratio of the fuel in question is smaller than the stoichiometric air / fuel ratio, and the term “lean” means that the air / fuel ratio of the fuel in question is Means that the fuel / fuel ratio is greater than the stoichiometric air / fuel ratio.
- the stoichiometric air / fuel ratio is about 14.5.
- the term “catalyst” means a catalyst or a structure containing the same that operates to remove NOx during rich-lean combustion of fuel.
- “supplying fuel in a periodic rich Z-lean fuel supply process” means that the combustion of fuel is mainly performed in a combustion condition of a diesel engine / gasoline engine under lean conditions (the exhaust gas in the exhaust gas after combustion).
- the oxygen concentration is usually about 5% to 10%.
- the air / fuel ratio is adjusted so that the atmosphere is periodically vibrated alternately between the above-mentioned rich and lean conditions. While supplying, injecting or injecting fuel. Therefore, rich / re —The journey is synonymous with the rich / lean condition. Background art
- N ⁇ x contained in exhaust gas is oxidized and then absorbed into an alkali, or reduced to nitrogen using ammonia, hydrogen, carbon monoxide or hydrocarbon as a reducing agent.
- ammonia, hydrogen, carbon monoxide or hydrocarbon has drawbacks.
- the former method means for treating the generated alkaline wastewater is required to prevent environmental problems.
- the latter method for example, when ammonia is used as a reducing agent, the ammonia reacts with S Ox in the exhaust gas to form salts, and as a result, the catalytic activity decreases at low temperatures. Also, especially when processing NOX from mobile sources such as automobiles, its safety is an issue.
- NOx A storage-reduction system has been proposed as the most promising method.
- fuel is periodically supplied to the combustion chamber in a short time in an amount exceeding the stoichiometric amount.
- Vehicles equipped with lean-burn engines can be driven with very low fuel-air ratios, resulting in lower fuel consumption than vehicles equipped with conventional engines.
- Such a NOx storage-reduction system for a lean-burn engine reduces NOx through two periodic processes at intervals of 1 to 2 minutes.
- the NO on the platinum or rhodium catalyst is oxidized to N_ ⁇ 2, the N 0 2 is as K 2 C_ ⁇ 3 and B a C_ ⁇ 3 Absorbed by an absorbent made of an alkaline compound.
- a rich condition for the second step is formed, and the rich condition is maintained for several seconds. This rich conditions, the absorbed (stored) has been N 0 2 is released from the absorbent, hydrocarbons on a platinum or rhodium catalyst, is to be reduced to nitrogen rather by efficiency carbon monoxide or hydrogen I have.
- a surface catalyst layer (B) (a) at least one selected from platinum, rhodium, palladium and oxides thereof;
- WO 02/22 22 discloses that a catalyst comprising an internal catalyst layer containing a third catalyst component selected from rhodium, palladium, platinum and mixtures thereof exhibits high S Ox durability. It is proposed in 55 specification. Disclosure of the invention
- the present invention provides a method for burning fuel under cyclic rich / lean conditions, in the presence of oxygen, sulfur oxides, or water, and at a wide range of reaction temperatures, and in the exhaust gas produced by this combustion.
- An object of the present invention is to provide a method for catalytic reduction of NOx with high durability without deterioration of the catalyst and a catalyst therefor.
- the present invention is intended to reduce the harmful ammonia during lithiation and degradation in the presence of oxygen, sulfur oxides, or water, especially in the presence of sulfur oxides, which were serious problems of N ⁇ x storage catalysts.
- An object of the present invention is to provide a highly durable catalyst for reducing NOx in a lean process of periodic rich / lean combustion in a wide temperature range without generation.
- Another object of the present invention is to provide a catalyst structure for NOx catalytic reduction in which a catalyst is supported on an inert supporting substrate.
- a method of supplying and burning fuel under periodic rich / lean conditions, contacting generated exhaust gas with a catalyst, and catalytically reducing nitrogen oxides in the exhaust gas According to the law:
- a catalyst component A comprising a mixture of oxides of at least two elements selected from cerium, zirconium, praseodymium, neodymium, terbium, samarium, gadolinium and lanthanum and / or a composite oxide;
- At least one catalyst component C selected from a solid acid supporting at least one metal oxide selected from vanadium, tungsten, molybdenum, copper, iron, cobalt, nickel and manganese.
- a noble metal catalyst component comprising at least one selected from platinum, rhodium, palladium and their oxides
- a method for catalytically reducing nitrogen oxides in exhaust gas comprising: a catalyst component B comprising a carrier; and an internal catalyst layer having a catalyst component B as an internal catalyst component.
- the catalyst used in this method is referred to as a first two-layer catalyst.
- the catalyst component A is It is preferable that the catalyst support a noble metal catalyst component composed of at least one selected from platinum, rhodium, palladium and their oxides.
- the fuel is supplied and burned under a periodic rich lean condition, and the generated exhaust gas is brought into contact with a catalyst to reduce nitrogen oxides in the exhaust gas by catalytic reduction.
- the catalyst is
- a catalyst component A consisting of a mixture of an oxide of at least two elements selected from cerium, zirconium, praseodymium, neodymium, terbium, samarium, gadolinium and lanthanum, and a composite or composite oxide;
- At least one catalyst component C selected from a solid acid supporting at least one metal oxide selected from vanadium, tungsten, molybdenum, copper, iron, cobalt, nickel and manganese.
- a catalyst component comprising a mixture of oxides of at least two elements selected from cerium, zirconium, praseodymium, neodymium, terbium, samarium, gadolinium and lanthanum and / or a composite oxide;
- a noble metal catalyst component comprising at least one selected from platinum, rhodium, palladium and their oxides
- a method for catalytically reducing nitrogen oxides in exhaust gas comprising: a catalyst component B comprising a carrier; and an internal catalyst layer having a catalyst component B as an internal catalyst component.
- the catalyst used in this method is referred to as a second two-layer catalyst.
- At least one of the catalyst component A in the surface catalyst component and the catalyst component A in the internal catalyst component is selected from platinum, rhodium, palladium and oxides thereof. It is preferable that the catalyst support at least one noble metal catalyst component.
- fuel is supplied under cyclic rich / lean conditions.
- the above catalyst is provided as a catalyst for contacting the generated exhaust gas and contacting the generated exhaust gas to catalytically reduce nitrogen oxides in the exhaust gas.
- the fuel is supplied and burned under cyclic rittinolene conditions, the generated exhaust gas is brought into contact with the catalyst structure, and the nitrogen oxides in the exhaust gas are contacted.
- the catalyst structure wherein the catalyst structure is obtained by providing the catalyst on an inert substrate.
- a catalyst structure for supplying and burning fuel under periodic rich / lean conditions, contacting generated exhaust gas, and catalytically reducing nitrogen oxides in the exhaust gas.
- a catalyst structure is provided, wherein the catalyst is provided on an inert substrate.
- FIG. 1 shows the time of the concentration of nitrogen oxides and nitrogen in the gas when the exhaust gas was treated at a reaction temperature of 250 to 400 ° C. using an example of the catalyst according to the present invention. (Rich Z lean time).
- Fig. 2 shows the time of the concentration of nitrogen oxides and nitrogen in the gas when the exhaust gas was treated at a reaction temperature of 250 to 40 O using an example of the catalyst according to the comparative example (rittinolene time).
- the catalytic reduction of nitrogen oxides means that NOx adsorbed on the catalyst during lean is converted to ammonia by a catalytic reaction during rich, and this ammonia is accumulated on the solid acid of the catalyst.
- Ammonia reacts with N ⁇ x in the presence of oxygen during leaning, and NOx is converted to nitrogen, water, carbon monoxide, carbon dioxide, etc. with high efficiency throughout the lean Z-rich process That means.
- N ⁇ x is absorbed on a basic material such as an alkali compound under lean conditions, and the N Ox so absorbed is reduced by a reducing agent such as hydrogen, carbon monoxide, carbon dioxide or the like under rich conditions. Nitrogen formation is only observed under rich conditions as it is reduced to produce nectar. On the other hand, In the method described above, nitrogen is generated only under lean conditions, as shown in FIG. According to the method of the present invention, ammonia produced on the catalyst under rich conditions is adsorbed on the solid acid catalyst component in the catalyst, and the ammonia thus adsorbed on the solid acid catalyst component is thus adsorbed.
- N ⁇ X is purified by a reaction mechanism that is distinctly different from the above-described NOx storage-reduction system in which nitrogen is generated only under rich conditions.
- the first catalyst for catalytically reducing nitrogen oxides in exhaust gas supplies and burns fuel under a periodic rich / lean condition, and makes the generated exhaust gas contact with the exhaust gas.
- a catalyst component A comprising a mixture of oxides of at least two elements selected from cerium, zirconium, praseodymium, neodymium, terbium, samarium, gadolinium and lanthanum and / or a composite oxide;
- a noble metal catalyst component comprising at least one selected from platinum, rhodium, palladium and their oxides
- the catalyst component A is sometimes referred to as an oxygen storage substance, focusing on the fact that it has an oxygen storage function.
- the catalyst component A is 30 to 30 parts by weight based on the weight of all catalyst components. 70% by weight, the catalyst component B is preferably in the range of 20 to 50% by weight, and the catalyst component C is preferably in the range of 10 to 25% by weight. Further, according to the present invention, the catalyst component B preferably comprises 0.5 to 5% by weight of the noble metal catalyst component and 95 to 99.5% by weight of the carrier.
- the catalyst component A is, in one embodiment, as described as component (c), an oxide of at least two elements and / or a composite oxide (solid solution), ie at least It may be at least one selected from a mixture of two elements and a composite oxide (solid solution) of at least these two elements, but the mixture is preferably a homogeneous mixture.
- a composite oxide of the at least two elements is preferably used rather than a mixture of the oxides of the at least two elements, and a binary or ternary composite oxide is particularly preferred. Used.
- the weight ratio of each element in the solid solution to the oxide is as follows: seria Z praseodymium oxide complex oxide, ceria / zirconia complex oxide, ceria / terbium oxide complex oxide, ceria / Samarium oxide composite oxidant, preferably 80
- the oxide-based weight ratio in the solid solution is ceria / gadolinium oxide nozirconia composite oxide, ceria / neodymium oxide zirconia composite oxide, ceria Z zirconia / praseodymium oxide composite. Oxides, selenium / zirconia / lanthanum oxide composite oxide, seria / zirconia Z samarium oxide composite oxide, ceria / zirconia / terbium oxide composite oxide, etc.
- the weight ratio of each element in these composite oxides to the oxide is Ceria, zirconium, terbium oxide, praseodymium oxide, gadolinium oxide, neodymium oxide, samarium oxide, and lanthanum oxide, respectively.
- E_ ⁇ 2, Z r 0 2, T b 0 2, P r 6 O u and shall be calculated as the G a 2 ⁇ 3, N d 2 ⁇ 3, S m 2 0 3 and L a 2 ⁇ 3 I do.
- the catalyst component A in the catalyst according to the present invention can be prepared, for example, by the following method. That is, first, a water-soluble salt of an element constituting the catalyst component, for example, an aqueous solution of nitrate is neutralized or heated and hydrolyzed to form a hydroxyl group, and then the obtained product is oxidized. The firing may be performed at a temperature of 300 to 900 ° C. in a neutral or reducing atmosphere. However, the catalyst component A can also be obtained by calcining a commercially available hydroxide or oxide of the above element as described above.
- the solid acids include acid zeolites such as H—Y zeolite, H—mordenite, H—) 3 zeolite and H—ZSM-5, and titanium oxide, Zirconia, silica-alumina and the like can be used.
- H-mordenite is most preferably used in terms of ammonia adsorption.
- the solid acid supporting the metal oxide is a catalyst in which at least one metal oxide selected from vanadium, tungsten, molybdenum, copper, iron, cobalt, nickel and manganese is supported on the solid acid as described above. It is a component.
- the metal oxide to be supported on the solid acid must be optimally selected according to the reaction temperature when treating the exhaust gas.However, when the reaction temperature is in the range of 200 to 300 ° C, vanadium or copper Oxides are preferably used, while oxides of tungsten, molybdenum, iron, cobalt, nickel or manganese are preferably used in the region where the reaction temperature is 300 ° C. or higher. In addition, by using a mixture of solid acid catalyst components supporting various metal oxides, an effective catalyst can be obtained in a wide temperature range.
- the catalyst component comprising the metal oxide-carrying solid acid can be prepared by a conventionally known metal oxide-carrying method, for example, an impregnation method, an ion exchange method, a kneading method and the like.
- the supported amount of the metal oxide in the solid acid supporting the metal oxide is in the range of 0.1 to 10% by weight based on the total weight of the solid acid and the metal oxide component.
- the supported amount of metal oxide is less than 0.1% by weight, the selective reduction reaction of N ⁇ x by ammonia at the time of lean is insufficient.
- the amount exceeds 10% by weight, the ammonia Oxidation occurs and the NOx reduction rate decreases.
- the catalyst according to the present invention is preferably a two-layer catalyst having a surface catalyst layer and an internal catalyst layer, wherein the surface catalyst layer is exposed so as to directly contact exhaust gas.
- a preferred first two-layer catalyst according to the present invention is
- a catalyst component A comprising a mixture of oxides of at least two elements selected from cerium, zirconium, praseodymium, neodymium, terbium, samarium, gadolinium and lanthanum and / or a composite oxide;
- a noble metal catalyst component comprising at least one selected from platinum, rhodium, palladium and their oxides
- a catalyst component B comprising a carrier and an internal catalyst layer having the internal catalyst component as an internal catalyst component.
- the surface catalyst component of the surface catalyst layer comprises the catalyst component A and the catalyst component C
- the internal catalyst component of the internal catalyst layer comprises the catalyst component B.
- the weight ratio of the surface catalyst component Z and the internal catalyst component is preferably in the range of 1 to 3
- the surface catalyst component of the surface catalyst layer is the catalyst component A 50-90. % By weight and 10 to 50% by weight of the catalyst component C.
- the internal catalyst component of the internal catalyst layer is the catalyst component B.
- the catalyst component B is composed of 0.5 to 5% by weight of the noble metal catalyst component and 95 to 99.5% by weight of the carrier. Is preferred.
- the two-layer catalyst having the surface catalyst layer and the internal catalyst layer as described above has a catalyst structure in which the internal catalyst layer and the surface catalyst layer are laminated in this order on an inert base material. Used as a body.
- a preferred second two-layer catalyst according to the present invention is:
- a catalyst component A comprising a mixture of oxides of at least two elements selected from cerium, zirconium, praseodymium, neodymium, terbium, samarium, gadolinium and lanthanum and / or a composite oxide;
- At least one catalyst component C selected from a solid acid supporting at least one metal oxide selected from vanadium, tungsten, molybdenum, copper, iron, cobalt, nickel and manganese.
- a noble metal catalyst component comprising at least one selected from platinum, rhodium, palladium and their oxides
- the surface catalyst component of the surface catalyst layer is composed of the catalyst component A and the catalyst component C, and the internal catalyst component of the internal catalyst layer is the same as the catalyst component A. It consists of catalyst component B.
- This second two-layer catalyst is different from the first two-layer catalyst in that the internal catalyst component of the internal catalyst layer has the catalyst component B together with the catalyst component A.
- the weight ratio of the surface catalyst component / the internal catalyst component is preferably in the range of 1 to 3, and the surface catalyst component of the surface catalyst layer is
- the catalyst component is preferably composed of 50 to 90% by weight of the catalyst component A and 10 to 50% by weight of the catalyst component C.
- the internal catalyst component of the internal catalyst layer preferably comprises 30 to 90% by weight of the catalyst component A, 0.5 to 5% by weight of the noble metal catalyst component, and 5 to 69.5% by weight of the carrier.
- the second two-layer catalyst having the surface catalyst layer and the inner catalyst layer as described above also preferably has the inner catalyst layer and the surface catalyst layer formed on an inert base material. Is used as a catalyst structure laminated in this order.
- the surface catalyst layer contains at least 75% by weight, preferably at least 75% by weight of a surface catalyst component comprising a catalyst component A and a catalyst component C, It has at least 90% by weight.
- the ratio of the surface catalyst component is less than 75% by weight in the surface catalyst layer, the N Ox adsorption effect of the obtained surface catalyst layer during lean operation and the selective reduction reaction of NO by ammonia become insufficient, and S ⁇ x Durability will also be reduced.
- the internal catalyst layer contains at least 50% by weight, preferably at least 75% by weight of the internal catalyst component comprising (the catalyst component A) and the catalyst component B. Have.
- the ratio of the internal catalyst component is less than 50% by weight in the internal catalyst layer, the N 2 O oxidizing ability during lean and the ammonia generation rate during rich decrease.
- the first catalyst component A of the inner catalyst layer comprises an oxygen storage material, and this oxygen storage material functions as a NOx adsorbent.
- This oxygen storage material The catalyst component A accounts for 30 to 90% by weight of the internal catalyst component in terms of metal oxide.
- the second catalyst component B comprises a noble metal catalyst component and a carrier, and the noble metal catalyst component is preferably supported on the carrier and the catalyst component A. However, the noble metal catalyst component and the catalyst component A May be both supported on a carrier.
- a conventionally known carrier such as alumina, silica, silica-alumina, zeolite, titania and the like is used.
- This support is preferably used in the range of 5 to 69.5% by weight in the internal catalyst component.
- the noble metal catalyst component in the second catalyst component B is contained in the internal catalyst component in a range of 0.5 to 5% by weight in terms of metal. ing. Even if the ratio of the above-mentioned noble metal catalyst component in the internal catalyst component exceeds 5% by weight in terms of metal, the ammonia generation rate at the time of richness does not improve, and conversely, in some cases, it is adsorbed on the solid acid at the time of leaning It promotes oxidation of ammonia and reduces the selectivity of the selective reduction reaction between NOx and ammonia during lean operation.
- the ratio of the noble metal catalyst component in the internal catalyst component is less than 0.5% by weight in terms of metal, ammonia production by the reducing agent decreases.
- the noble metal catalyst component is supported on the carrier and the acid storage material, if the carrier used has ion exchange ability, the degree of dispersion can be increased, so that the noble metal catalyst component is preferably supported by ion exchange.
- the ion exchange capacity of the carrier is limited. Are often supported in a mixed state with a compound.
- the internal catalyst component in the second two-layer catalyst according to the present invention is preferably, for example, first, a noble metal catalyst component supported on a carrier such as alumina or an oxygen storage material by an appropriate means such as an impregnation method or an ion exchange method. After that, calcination is performed at a temperature of 500 to 900 ° C. in an oxidizing or reducing atmosphere to obtain a powder in which a noble metal catalyst component is supported on a carrier or an oxygen storage material. be able to.
- a precious metal catalyst component supported on a carrier such as alumina and an oxygen storage material are prepared as described above, and the internal catalyst component is also powdered by mixing them. Can be obtained as a body.
- the catalyst component ⁇ ⁇ ⁇ ⁇ in the single-layer catalyst and the first two-layer catalyst is a noble metal composed of at least one selected from platinum, rhodium, palladium and their oxides.
- the metal catalyst component is supported.
- at least one of the catalyst component A in the surface catalyst component and the catalyst component A in the internal catalyst component is platinum or rhodium. It is preferable that the catalyst support a noble metal catalyst component composed of at least one selected from palladium, palladium and oxides thereof.
- the catalyst component A supports a noble metal catalyst component composed of at least one selected from platinum, rhodium, palladium and their oxides
- the catalyst component A which is an oxygen storage material
- NOx adsorption is promoted over a wide temperature range, resulting in improved NOx purification over a wide temperature range.
- thermal degradation of the catalyst component A due to NOx adsorption is suppressed, the heat resistance of the catalyst is also improved.
- the catalyst component A mainly serves to adsorb NOx in exhaust gas in the lean process.
- the catalyst component A has both an NO adsorption site and an NO 2 adsorption site.
- N 0 2 adsorption site amount is large.
- the catalyst component B containing the noble metal catalyst component plays a role of highly efficiently reducing NOx adsorbed on the catalyst component A to ammonia in the Ritzche process, and oxidizes NO during the lean period to form NOx P It fulfills the function of increasing the spread rate.
- platinum is most preferably used in terms of ammonia generation efficiency and NO oxidizing power.However, when low-temperature performance is desired for the catalyst, rhodium or Palladium is preferably used. A combination of platinum and at least one selected from rhodium and palladium is also preferably used.
- the catalyst is preferably a two-layer catalyst having a surface catalyst layer and an inner catalyst layer, and such a two-layer catalyst (first and second two-layer catalyst) is preferable.
- a two-layer catalyst first and second two-layer catalyst
- the catalyst of the present invention has an advantage that the catalyst performance does not deteriorate even in the presence of S Ox.
- the ammonia captured by the catalyst component C is not reoxidized by the noble metal catalyst component of the internal catalyst layer in the next lean process, and is effectively used for the selective reduction of N ⁇ x by ammonia on the catalyst component C. Used. According to the catalyst of the present invention, as a result, a high N ⁇ x purification rate can be obtained in the lean / rich process.
- the inner catalyst layer has the catalyst component B as well as the catalyst component A.
- the catalytic component A mainly surface catalyst layer as S 0 2 before being oxidized in the noble metal catalyst component of the inner catalyst layer easily in the gas phase rich during As a result, not only has the advantage of not deteriorating the catalytic performance even in the presence of S Ox, but also is produced by oxidation of N ⁇ on the noble metal catalyst component in the internal catalyst layer. since N 0 2 adsorption ratio is improved, it is possible to obtain a higher N_ ⁇ _X Kiyoshii ⁇ lean / rich stroke.
- the thickness of the surface catalyst layer has a great influence on the NOx reduction ability and the resistance to S ⁇ x poisoning in the catalyst's rich / lean process.
- the optimum thickness of the surface catalyst layer depends on the reaction conditions such as temperature, oxygen concentration, space velocity (SV), etc., but a preferable surface catalyst that can obtain high NOx reduction ability during the rich-noring process
- the layer thickness ranges from 20 m to 80 m. However, usually about 40 im is preferred. Even if the thickness of the surface catalyst layer is set to 8 or more, the performance will not be improved correspondingly, and the diffusion of NOx and reducing agent to the inner catalyst layer will be hindered.
- the thickness of each catalyst layer in convenience the apparent density of the catalyst layer was 1. O gZ c rn 3, calculated from the coating amount of the slurry of base material containing a catalyst component Can be requested.
- the internal catalyst layer has a high ability to oxidize the noble metal component of the internal catalyst component and produces ammonia, and therefore the effect of its thickness on the N ⁇ x reducing ability in the rich catalytic process is as large as the thickness of the surface catalyst layer. Is not large, but usually a range of 10 ⁇ to 50 im is appropriate. Even if the thickness of the inner catalyst layer is more than 50 m, the performance does not improve correspondingly, On the other hand, when the thickness of the inner catalyst layer is smaller than 10 m, the overall NOx reduction ability including the rich / lean process is reduced.
- the catalyst component can be obtained in various forms such as powders and granules. Therefore, the catalyst component can be formed into various shapes such as, for example, a honeycomb, a ring, a sphere, and the like by using any of the well-known methods.
- an appropriate additive for example, a molding aid, a reinforcing material, an inorganic fiber, an organic binder, or the like can be used as necessary.
- the catalyst according to the present invention is a catalyst structure having a catalyst layer (for example, by coating) on a surface of an inert substrate for support having an arbitrary shape, for example, by a wet coat method.
- the inert substrate may be, for example, a clay mineral such as cordierite, or a metal such as stainless steel, preferably a heat-resistant metal such as Fe—Cr—A1.
- the shape may be a honeycomb, an annular shape, a spherical structure, or the like.
- the catalyst components for the surface catalyst layer and the internal catalyst layer can be obtained in various forms such as powders and granules as described above. .
- the internal catalyst layer is formed into various shapes such as a honeycomb, a ring, a sphere, etc. by using such an internal catalyst component by any well-known method.
- catalyst structures of various shapes can be obtained.
- appropriate additives such as a molding aid, a reinforcing material, an inorganic fiber, an organic piner and the like can be used.
- Each of the catalysts according to the present invention is excellent not only in resistance to heat but also in resistance to sulfur oxides, and is capable of reducing NOX in exhaust gas from diesel engines and lean gasoline engines, that is, denitration. It is suitable for use as a catalyst for In the present invention, the catalyst is preferably used in a catalytic reaction under conditions where the combustion atmosphere of the fuel oscillates between the rich condition and the lean condition as described above.
- the period of the catalyst reaction (that is, the time from the rich atmosphere (or lean atmosphere) to the next rich atmosphere (or lean atmosphere)) is preferably 5 to 150 seconds, particularly preferably 30 to 150 seconds. ⁇ 90 seconds.
- the rich lean width ie, the rich time (second) / lean time (second) is generally in the range of 0.5 / 5 to 10 to 150, preferably 2/3 to 5/5. The range is 90.
- the rich condition is usually formed by periodically injecting fuel into the combustion chamber of the engine at an air-fuel ratio of 10 to 14 by weight.
- Typical exhaust gases under rich conditions are several hundred volumes of Ppm NOx, 5-6% by volume of water, 2-3% by volume of carbon monoxide, 2-3% by volume of hydrogen, thousands of volumes by ppm Contains 0 to 0.5% by volume of oxygen.
- the lean condition is usually formed by periodically injecting the fuel into the combustion chamber of the engine at an air / fuel ratio of 20 to 40 by weight.
- Typical exhaust gases under lean conditions are hundreds of ppm of NOx, 5-6% by volume of water, thousands of ppm of carbon monoxide, thousands of ppm of hydrogen, and thousands of ppm of carbon Contains hydrogen and 5-10% by volume oxygen.
- Suitable temperatures for the catalytic reduction of NOx with the catalyst according to the invention are usually such as to have an effective catalytic activity for NOx over a long period of time in a rich process. It is in the range of 150 to 550 ° C, preferably in the range of 200 to 500 ° C. In the above reaction temperature range, the exhaust gas is preferably treated at a space velocity in the range of 5000 to 150,000 h " 1 .
- the exhaust gas containing NOx is brought into contact with the above-described catalyst in a periodic rich / lean process, whereby even in the presence of oxygen, sulfur oxide, or moisture, NOx in exhaust gas can be stably and efficiently catalytically reduced.
- the catalyst according to the present invention can be used in combination with the NOx storage-reduction catalyst used in the NOx storage-reduction system described above, which reduces the NOx stored at the time of leaning, as needed. That is, after the exhaust gas from the engine is treated using the NOx storage-reduction catalyst as a pre-catalyst, it can be treated using the catalyst according to the present invention as a post-catalyst.
- the NOx storage-reduction catalyst stores NOx in exhaust gas at the time of leaning, and reduces N ⁇ ⁇ x to nitrogen by reducing components such as hydrocarbons and carbon monoxide contained in the exhaust gas at a time of richness. When rich, ammonia is also produced as a by-product. At this time, the NOx storage-reduction catalyst has a strong alkalinity, and thus generated ammonia is discharged to the downstream of the catalyst without being adsorbed by the NOx storage-reduction catalyst, which may cause environmental problems.
- the catalyst according to the present invention adsorbs NOx at the time of lean, converts the adsorbed NOx to ammonia at the time of rich, adsorbs the ammonia, and then at the time of lean,
- the monyer reacts with the gaseous N Ox, thus purifying NO with high efficiency by the selective reduction reaction with ammonia. Therefore, the catalyst according to the present invention essentially contains a component that adsorbs ammonia, i.e., a solid acid catalyst, so that the N ⁇ ⁇ x storage-alcohol as used for the N ⁇ x storage of the reduction catalyst is used. Strong alkaline components such as alkaline earth or alkaline metal cannot be used.
- the NOx adsorption rate at a high temperature may decrease, and the NOx purification at a high temperature may not always be sufficient. Therefore, when performing N ⁇ x purification at a high temperature, it may be preferable to use a previously known N ⁇ x storage-reduction catalyst in combination.
- the NOx storage-reduction catalyst for example, alumina is used as a carrier, and an alkali metal such as potassium, sodium, lithium and cesium and an alkali metal such as palladium and calcium are provided on the carrier.
- a catalyst generally called a NOx storage reduction catalyst comprising a noble metal component such as platinum supported together with an earth metal and at least one component selected from rare earth metals such as lanthanum, cerium and yttrium,
- alumina is used as a carrier, and for example, at least one selected from alkali metals and alkaline earth metals, at least one selected from rare earth metals, and at least one selected from noble metals such as platinum are supported on the carrier. And, if necessary, titanium or the like. What is called a medium can be mentioned. Industrial applicability
- NOx in exhaust gas is catalytically reduced with high durability without deterioration of the catalyst even in the presence of oxygen, sulfur oxide or water, and at a wide range of reaction temperatures. be able to.
- N ⁇ x in exhaust gas can be reduced and removed with high durability over a wide temperature range without deteriorating the fuel and producing harmful ammonia when rich.
- cerium nitrate (Ce ( ⁇ 0 3) 3 ⁇ 6 ⁇ 2 0) 103.
- 77 g and praseodymium nitrate (P r ( ⁇ 0 3) 3 ⁇ 6 ⁇ 2 0) 3 5.
- 77 g of ion-exchanged water 1 00 OML
- 0.1 N aqueous ammonia was added to this aqueous solution to neutralize and hydrolyze the cerium salt and praseodymium salt, and then the mixture was aged for 1 hour.
- the product was separated from the resulting slurry by filtration, dried at 120 ° C for 24 hours, and calcined in air at 500 for 3 hours to obtain a ceria / praseodymium oxide composite oxide powder ( An oxide-based weight ratio of 60/40 and a specific surface area of 112 m 2 / g) were obtained.
- Ion-exchanged water 1 00 OML cerium nitrate (C e (Nyu_ ⁇ 3) 3 ⁇ 6 ⁇ 2 0) 34. 59 g and O carboxymethyl zirconium (Z rO (N0 3) 2 ) 84. 45 g lanthanum nitrate (L a ( ⁇ 3 ) 3 ⁇ 6 ⁇ 20 ) 7.97 g was dissolved to prepare an aqueous solution. 0.1 N ammonia water was added to this aqueous solution to neutralize and hydrolyze the cerium salt, oxyzirconium salt and lanthanum salt, and then aged for 1 hour.
- the product was separated from the resulting slurry by filtration, And then calcined in air at 500 ° C for 3 hours to obtain ceria / zirconia Z oxidized lanthanum composite oxide powder (oxide weight ratio 22/73/5, specific surface area 8 Om 2 / g).
- Cerium nitrate in deionized water 100 OmL (C e ( ⁇ 0 3 ) 3 ⁇ 6 ⁇ 2 0) 121. 06 and Okishi zirconium (Z r O (N0 3) 2) 28. 1 2 g and gadolinium nitrate (Gd (.nu.0 3) 3 ⁇ 6 ⁇ 2 0) 7. dissolved and 48 g, to prepare an aqueous solution. 0.1 N aqueous ammonia was added to this aqueous solution to neutralize and hydrolyze the cerium salt, oxyzircombate salt and gadolinium salt, and then aged for 1 hour.
- the product was separated from the resulting slurry by filtration, dried at 120 ° C for 24 hours, and calcined in air at 500 ° C for 3 hours to obtain ceria nozirconia Z gadolinium oxide composite oxide powder ( An oxide-based weight ratio of 72/24/4 and a specific surface area of 198 m 2 / g) were obtained.
- the product was separated from the resulting slurry by filtration, dried at 120 ° C for 24 hours, and calcined in air at 500 ° C for 3 hours to obtain a ceria-zirconia Z neodymium oxide composite oxide powder ( An oxide-based weight ratio of 70/20/10 and a specific surface area of 171 m 2 / g) were obtained.
- the product was separated from the obtained slurry by filtration, dried at 120 ° C for 24 hours, and calcined at 50 ° C for 3 hours in air to obtain ceria / zirconia / acidide / samarium composite oxide powder (Oxide-based weight ratio 72/24 Z4, specific surface area 187 mzog) was obtained.
- Ion-exchanged water was added to 100 OML cerium nitrate (Ce ( ⁇ 0 3) 3 ⁇ 6 ⁇ 2 0) 151. 37 g, an aqueous solution, adding ammonia water 0.1 specified in this neutralization hydrolysis cerium ions Decomposed and aged for 1 hour. The obtained slurry was filtered and dried at 120 ° C. for 24 hours, and then calcined in air at 500 ° C. for 3 hours to obtain ceria powder (specific surface area: 138 m 2 / g). Ion-exchanged water 10 OML to P t (NH 3) 4 ( N0 3) (0% 9. platinum) 2 solution 8.
- Cerium nitrate in deionized water 100 OmL (Ce ( ⁇ 0 3) 3 ⁇ 6 ⁇ 2 0) 34. 59 g and O carboxymethyl zirconium (Z rO (N0 3) 2 ) 84. 45 g lanthanum nitrate (La (N0 3 ) 3 ⁇ 6H 2 ⁇ ) 7.97 g was dissolved to prepare an aqueous solution.
- 0.1 A Moneric water was added to neutralize and hydrolyze the cerium salt, oxyzirconium salt and lanthanum salt, followed by aging for 1 hour. The product was separated from the resulting slurry by filtration, dried at 120 ° C. for 24 hours, and calcined at 500 ° C. for 3 hours in the air to obtain a cerianozirconia Z lanthanum composite oxide.
- a powder (oxide weight ratio 22/73/5, specific surface area 80 V g) was obtained.
- the product was separated from the resulting slurry by filtration, dried at 120 ° C for 24 hours, and calcined in air at 500 ° C for 3 hours to obtain a ceria Z zirconia / praseodymium oxide composite oxide.
- a powder (oxide weight ratio 47/33/22, specific surface area 205 m 2 / g) was obtained.
- Ion-exchanged water 10 OML to P t (NH 3) 4 ( N0 3) (9. 0% of platinum) 2 aqueous solution was added to 8. 40 g, an aqueous solution, ceria powder prepared in Preparation Example 1 to 60 g, and dried at 100 with stirring, and then calcined in air at 500 ° C. for 3 hours to obtain a catalyst powder comprising 1% platinum supported on ceria.
- the thickness of the catalyst layer was calculated by assuming that the apparent density of the catalyst layer was 1.0 g / cm ⁇ and the mechanical contact area of the honeycomb was 250 Om 2 Zg.
- a catalyst comprising 1% platinum and 0.5% rhodium supported on the seria / praseodymium oxide composite oxide powder obtained in Production Example 2 and the iron alumina obtained in Production Example 9 in the same manner as in Example 1.
- a honeycomb catalyst structure having a catalyst layer with a thickness of 6 O / im was obtained using the powder composed of the powder and H-j3-zeolite obtained in Production Example 12.
- Example 2 In the same manner as in Example 1, seria / zirconia / lanthanum oxide composite oxide powder obtained in Production Example 3 and platinum 1% and palladium 0.5% on iron alumina obtained in Production Example 10 and Production Example 14 were used. V 2 ⁇ 5 1% and W0 3 1 0% was obtained with a zirconium oxide powder was supported, thickness 60 An 82-cam catalyst structure having a catalyst layer of m was obtained.
- Example 4 In the same manner as in Example 4, an internal catalyst layer having a thickness of 30 Aim and comprising a catalyst in which 1% of platinum was supported on alumina obtained in Production Example 8 was obtained. Next, 25 g of the ceria / zirconia / neodymium oxide composite oxide powder obtained in Production Example 5 and 5 g of ⁇ -zeolite powder supporting 2.5% of CuO obtained in Production Example 15 were mixed. As a result, a honeycomb catalyst structure having a surface catalyst layer having a thickness of 60 m was obtained.
- Example 5 In the same manner as in Example 5, an internal catalyst layer having a thickness of 30 im and comprising a catalyst in which 1% of platinum was supported on r-alumina obtained in Production Example 8 was obtained. Next, using 25 g of the ceria / terbium oxide composite oxide powder obtained in Production Example 6 and 5 g of the H-mordenite powder obtained in Production Example 11, a surface catalyst layer having a thickness of 60 ⁇ was provided. A honeycomb catalyst structure was obtained. '
- Example 5 In the same manner as in Example 5, an internal catalyst layer having a thickness of 30 m and comprising a catalyst in which 1% of platinum was supported on the iron alumina obtained in Production Example 8 was obtained. Next, 25 g of the cerianozirconia / samarium oxide composite oxide powder obtained in Production Example 8 and 5 g of the H-mordenite powder obtained in Production Example 11 were used. Thus, a honeycomb catalyst structure having a surface catalyst layer having a thickness of 6 was obtained.
- Example 5 In the same manner as in Example 5, an internal catalyst layer having a thickness of 30; m and comprising a catalyst in which 1% of platinum was supported on alumina obtained in Production Example 8 was obtained. Next, using 25 g of the ceria powder obtained in Production Example 1 and 5 g of the H-mordenite powder obtained in Production Example 11, a honeycomb catalyst structure having a surface catalyst layer having a thickness of 60 ⁇ was used. Got.
- Example 4 In the same manner as in Example 4, first, using a catalyst powder obtained by supporting 1% of platinum on 7-alumina Z cell 7 (weight ratio 11) obtained in Production Example 17, a thickness of 30 m Then, using 25 g of the seria powder obtained in Production Example 1 and 5 g of the H-mordenite powder obtained in Production Example 11, a surface catalyst layer having a thickness of 60 im was prepared. The obtained honeycomb catalyst structure was obtained.
- Example 14 In the same manner as in Example 4, using a catalyst powder obtained by supporting 1% of platinum and 0.5% of rhodium on the ferroaluminoceria (weight ratio 1/5) obtained in Production Example 18, Internal touch of thickness 30 ⁇ A medium catalyst layer was prepared. Next, using 25 g of the seria powder obtained in Production Example 1 and 5 g of the H-mordenite powder obtained in Production Example 11, a honeycomb catalyst structure having a surface catalyst layer having a thickness of 60 im was used. Got a body.
- Example 14 Example 14
- Example 4 In the same manner as in Example 4, a catalyst powder comprising 1% of platinum and 0.5% of palladium supported on the iron-alumina Z ceria (weight ratio of 1: 1) obtained in Production Example 19 was used. A honeycomb having a surface catalyst layer having a thickness of 60 m was prepared by using 25 g of the ceria powder obtained in Production Example 1 and 5 g of the H-mordenite powder obtained in Production Example 11. A catalyst structure was obtained.
- Example 4 a catalyst powder obtained by supporting 2% of platinum on a mixture (weight ratio 1/2) of the ceria / zirconia / lanthanum oxide composite oxide obtained in Production Example 20 was obtained. To prepare an internal catalyst layer having a thickness of 30 ⁇ . Then, 25 g of the ceria / zirconia / lanthanum oxide composite oxide powder obtained in Production Example 3 and the H-mordenite powder obtained in Production Example 11 were prepared. A honeycomb catalyst structure having a surface catalyst layer having a thickness of 60 m was obtained using 5 g of the catalyst.
- Catalyst powder comprising 2% platinum supported on a mixture (weight ratio 1Z2) of r-alumina and cerianozirconia Z-praseodymium oxide composite oxide obtained in Production Example 21 in the same manner as in Example 4.
- an internal catalyst layer having a thickness of 30 / m.
- 25 g of the ceria / oxidation praseodymium composite oxide powder obtained in Production Example 2 and the H-mordenite powder 5 obtained in Production Example 11 were prepared.
- Example 16 In the same manner as in Example 16, a catalyst powder comprising 2% platinum supported on a mixture (weight ratio: 12) of the iron alumina obtained in Production Example 21 and ceria-zirconia / oxidized praseodymium composite acid (weight ratio: 12) was used. Then, an internal catalyst layer having a thickness of 15 ⁇ was prepared, and then 5 g of the H-mordenite powder obtained in Production Example 11 was used to obtain a honeycomb catalyst structure having a surface catalyst layer having a thickness of 40 m.
- silica sol was added to 25 g of catalyst powder comprising 1% of platinum and 0.5% of palladium supported on ceria obtained in Production Example 23, and 5 g of H-mordenite powder obtained in Production Example 11.
- the water was mixed to obtain a polish 'coat slurry in the same manner as above. This slurry was coated on the above honeycomb structure to obtain a honeycomb catalyst structure having a surface catalyst layer having a thickness of 60 m and made of the above catalyst.
- an inner catalyst layer having a thickness of 30 was prepared by using catalyst powder obtained by supporting 1% of platinum on the alumina ceria (weight ratio 1/1) obtained in Production Example 17. Then, 25 g of a catalyst powder obtained by supporting 1% of platinum and 0.5% of rhodium on the ceria obtained in Production Example 24 and 5 g of the H-mordenite powder obtained in Production Example 11 were used. Thus, a honeycomb catalyst structure having a surface catalyst layer having a thickness of 60 zm was obtained.
- Ion-exchanged water 10 OML to P t (NH 3) 4 ( N0 3) (9. 0% of platinum) 2 aqueous solution was added to 8. 40 g, an aqueous solution, in which? "60 g of mono-alumina is charged, dried with 10 O: with stirring, and calcined in air at 500 for 3 hours to obtain a catalyst powder comprising 1% of platinum supported on low alumina. Obtained.
- the inner catalyst layer having a thickness of 30 im made of a catalyst in which 1% of platinum is supported on alumina and the ceria / zirconia lanthanum oxide obtained in Production Example 16 were prepared.
- Ion-exchanged water was added to 100 OML cerium nitrate (Ce (Nyu_ ⁇ 3) 3 ⁇ 6 ⁇ 2 0) 151. 37 g, an aqueous solution, adding ammonia water 0.1 specified in this neutralization cerium ions Hydrolyzed and aged for 1 hour. The obtained slurry was filtered, dried at 120 ° C. for 24 hours, and calcined in air at 50 Ot: for 3 hours to obtain a ceria powder (specific surface area: 138 m 2 / g).
- Example 2 in the same manner as in Example 1, an inner catalyst layer having a thickness of 30 im made of a catalyst in which 1% of platinum is supported on the above-mentioned alumina and a thickness of 60 m made of a catalyst in which 1% of rhodium is supported on ceria A honeycomb catalyst structure having a surface catalyst layer was obtained.
- Barium carbonate was prepared from an aqueous solution of caustic palladium and an aqueous solution of sodium carbonate, and 1% of platinum was supported on a mixture (weight ratio: 8/2) of this carbonate (BaC 3 ) and iron alumina.
- the body was prepared.
- ⁇ - alumina poured into aqueous potassium carbonate solution, mixed, dried in air, the product was calcined for 3 hours at 1100 ° C, ⁇ 2 0 ⁇ 12 A 1 2 ⁇ 3 (specific surface area 18m 2 / g) Was prepared.
- the gas containing nitrogen oxide was reduced under the following conditions using each of the catalyst structures according to the above Examples and Comparative Examples.
- the conversion rate (removal rate) from nitrogen oxides to nitrogen was determined by the chemical luminescence method.
- composition of the mixed gas used for the N Ox reduction experiment under the rich condition is as follows.
- the gas under the lean condition was prepared by injecting oxygen into the gas mixture under the rich condition, and its composition is as follows.
- Catalytic reactions were performed with the rich Z-line width ranging from 3 to 30 (seconds / second) to 12/120 (seconds / second), and the performance of each catalyst was examined.
- the catalyst according to the present invention has a high nitrogen oxide removal rate.
- the catalyst according to the comparative example generally has a low nitrogen oxide removal rate.
- Example 15 Furthermore, using the catalyst structures of Example 15 and Comparative Examples 1 and 3, the endurance test was performed for 50 hours under the above-mentioned gas conditions, a rich / nominal width (second / second) of 55/5, and a reaction temperature of 350 ° C. Was done. The results are shown in Table 2. As is evident from Table 2, the catalyst according to the invention has a very high resistance to sulfur oxides as compared to conventional NOx storage-reduction systems.
- the push coat slurry prepared in Comparative Example 3 was evaporated and dried, and then baked at 500 ° C. for 1 hour in air.
- the calcined product has a particle size between 0.25 and 0.5 mm.
- test gas composition under lean conditions is NO 2000 ppm, oxygen 9% by volume, and balance is helium.
- the test gas composition under lean conditions is NO 2000 ppm, oxygen 9% by volume, and balance is helium.
- a line / litch width of 120 seconds / 30 seconds nitrogen and N ⁇ ⁇ x in the treated gas that passed through the catalyst packed bed under rich conditions were analyzed using a quadrupole mass spectrometer (manufactured by Balza Corporation). Omnistar).
- FIG. 1 the result of treating the test gas in the catalyst packed bed using the catalyst according to the present invention is shown in FIG. 1, where the reaction temperature is in the range of 250 to 400 ° C. It is recognized that it has been produced. This means that under rich conditions, the ammonia generated on the catalyst is adsorbed on the solid acid component in the catalyst, and the ammonia thus adsorbed selectively converts N ⁇ x into nitrogen only under lean conditions. In order to reduce to On the other hand, since NOx is adsorbed on the catalyst component A after the end of nitrogen generation, almost no NO is found in the gas that has passed through the catalyst packed bed under most conditions under lean conditions.
Description
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JP2005515381A JP4757027B2 (ja) | 2003-11-11 | 2004-11-08 | 窒素酸化物素酸化物を接触還元するための触媒 |
US10/578,664 US7585477B2 (en) | 2003-11-11 | 2004-11-08 | Catalyst and method for catalytic reduction of nitrogen oxides |
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Cited By (30)
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JP2006314989A (ja) * | 2005-04-11 | 2006-11-24 | Valtion Teknillinen Tutkimuskeskus | 窒素酸化物を接触還元するための触媒及び触媒構造体 |
JP2006326437A (ja) * | 2005-05-24 | 2006-12-07 | Valtion Teknillinen Tutkimuskeskus | 窒素酸化物接触還元用触媒 |
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Also Published As
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JPWO2005044426A1 (ja) | 2007-05-17 |
US20070274889A1 (en) | 2007-11-29 |
JP4757027B2 (ja) | 2011-08-24 |
US7585477B2 (en) | 2009-09-08 |
EP1685891A4 (en) | 2009-03-11 |
EP1685891A1 (en) | 2006-08-02 |
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