WO1998025698A1 - Ammonia oxidation catalyst comprising aluminium oxide, bismuth oxide and manganese oxide - Google Patents

Ammonia oxidation catalyst comprising aluminium oxide, bismuth oxide and manganese oxide Download PDF

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Publication number
WO1998025698A1
WO1998025698A1 PCT/US1997/020830 US9720830W WO9825698A1 WO 1998025698 A1 WO1998025698 A1 WO 1998025698A1 US 9720830 W US9720830 W US 9720830W WO 9825698 A1 WO9825698 A1 WO 9825698A1
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Prior art keywords
oxide
catalyst
ammonia
selectivity towards
nitrous oxide
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PCT/US1997/020830
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French (fr)
Inventor
Vladimir Vasilievich Mokrinskii
Elena Markovna Slavinskaya
Alexander Stepanovich Noskov
Ilya Aleksandrovich Zolotarskii
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Solutia Inc.
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Priority to EP97947521A priority Critical patent/EP0948404A1/en
Priority to CA002274760A priority patent/CA2274760A1/en
Priority to BR9713999-8A priority patent/BR9713999A/en
Priority to JP52667198A priority patent/JP2001505817A/en
Priority to AU52579/98A priority patent/AU744311B2/en
Publication of WO1998025698A1 publication Critical patent/WO1998025698A1/en

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B21/00—Nitrogen; Compounds thereof
    • C01B21/20—Nitrogen oxides; Oxyacids of nitrogen; Salts thereof
    • C01B21/22—Nitrous oxide (N2O)
    • 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
    • B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/32—Manganese, technetium or rhenium
    • B01J23/34—Manganese
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/10—Capture or disposal of greenhouse gases of nitrous oxide (N2O)

Definitions

  • the present invention describes catalysts to be used for nitrous oxide production by ammonia oxidation with molecular oxygen in chemical industry. Along with a high activity, understood as conversion at a definite residence time, catalysts for ammonia oxidation to produce nitrous oxide should also meet the following demands:
  • the selectivity towards NO and NO is 0.9%.
  • the yields of nitrous oxide and NO+NO 2 are 79 and 3.1% respectively.
  • ammonia concentration decreases to 3.02 vol.%, the selectivity towards nitrous oxide falls to 65%. Therefore, beside a low activity in ammonia oxidation by the oxygen excess, the catalyst shows a high selectivity towards nitrogen oxides.
  • Another catalyst for ammonia oxidation consists of the oxides of iron, bismuth and manganese in the following ratio: 79.45% Fe 2 O 3 , 11.53% Bi 2 O 3 , 7.21% MnO 2 [2].
  • the maximum yield of nitrous oxide in the said catalyst is 82%, and it is attained under the following conditions: temperature - 350°C; inlet concentrations: ammonia - 10 vol.%, oxygen - 90 vol%.
  • the selectivity towards nitrogen oxide is 6%.
  • the selectivity towards nitrous oxide and nitrogen oxide is 79% and 1.5% respectively. Therefore, the catalyst does not meet all demands in concern, because it has a low selectivity towards nitrous oxide at a high selectivity towards nitrogen oxide.
  • Catalyst with a composition of 5% MnO 2 , 5% Bi 2 O 3 , 90% Fe 2 O 3 [3] is most close in performance and properties to the catalyst claimed in the present invention. It shows the following results.
  • the maximum nitrous oxide yield is 87%, when reaction mixture containing 10% of ammonia in air (thus in oxygen excess, concentration 18.9 vol.%). If 5 reaction mixture contains 1 ammonia part, 5 air parts, and 5 nitrogen parts, and so it is close to stoichiometry (9.1 vol.% ammonia and 9.55 vol.% oxygen), then the yield of nitrous oxide is 81 %.
  • the residence time for complete conversion is 3.6 s. Therefore, the catalyst has a low activity and not high enough selectivity towards nitrous oxide under conditions, when reaction mixture contains ammonia and oxygen in amounts close to 10 stoichiometry.
  • the present invention aims at providing catalysts that are highly active under conditions, when reaction mixture contains oxygen in amount close or below the stoichiometry one, showing a high selectivity towards nitrous oxide, and a low selectivity towards nitrogen oxide.
  • ⁇ 5 For the purpose the claimed catalysts for the nitrous oxide production by ammonia oxidation have the following composition (mass.%):
  • MnO 2 manganese oxide
  • the catalysts of the said composition are prepared by impregnating alumina with a solution of Mn and Bi nitrates, or by mixing the powders of Mn and Bi oxides with the powder of aluminum hydroxide to be then molded, or depositing the said components on an inert support. At the final stage the catalysts are dried, and calcined at 375-550°C.
  • catalysts show a high activity, when the oxygen content in the reaction mixture is s close or lower the stoichiometry one, and exhibit a high selectivity towards nitrous oxide, and a low selectivity towards nitrogen oxide.
  • ammonia conversion on the said catalysts is 82-99.2%.
  • the selectivity towards nitrous and nitrogen oxides is 82-84.6 and 2.1 - 2.7% respectively.
  • the final product contains 79.6-81.7% of nitrous oxide, 4.1-5.25% of nitrogen oxide, and 0.82-0.84% of oxygen.
  • ammonia conversion on the said s catalysts is 82.5-99.0%.
  • the selectivity towards nitrous and nitrogen oxides is 83-86 and 0.3- 0.35% respectively.
  • After water and ammonia separation the final product contains 82.2- 84.9% of nitrous oxide, 0.6-0.69%) of nitrogen oxide, and 0.75-0.77% of oxygen.
  • the high activity and selectivity of the claimed catalysts in ammonia oxidation to nitrous oxide is provided by its components at the said percent ratios.
  • Catalyst specific surface area also has a positive effect. The tests show that at a stable high activity the catalyst shows the highest selectivity, when its specific surface area ranges within 5-80 m2/g.
  • Example 1 Catalyst with a composition of 13%MnO 2 /l 1 %Bi 2 O 3 /76%Al 2 O 3 is prepared as follows. 100 g of alumina granules are impregnated by incipient wetness with a s solution of Mn and Bi nitrates, are dried in air and then in a drying chamber at 130°C for 2-4 h. Thus obtained product is once again impregnated with a solution of Mn and Bi nitrates, dried in air and in the drying chamber at 130°C for 4 hours. Then the granules were calcined in a furnace at 375-550°C for 2-4 h.
  • reaction mixture composition being 9%NH 3 and 9%O 2 .
  • reaction mixture composition being 9%NH 3 and 9%O 2 .
  • reaction mixture composition being 9%NH 3 and 9%O 2 .
  • reaction mixture composition being 9%NH 3 and 9%O 2 .
  • At 350°C and at a residence time of 0.7 s ammonia conversion is 99.2%.
  • Selectivity towards nitrous oxide and nitrogen oxide is 87 and 2.8% respectively.
  • At 300°C at the same gas composition and at a contact time of 1.6 s ammonia conversion is 99.4%.
  • Selectivity towards nitrous oxide and nitrogen oxide is 88.6 and 0.30% respectively.
  • Ssp is 10 m2/g.
  • Example 2 Catalyst prepared as in example 1 is tested at ammonia to oxygen ratio equal to 1.44 and ammonia concentration equal to 7.3 vol.% in the reaction mixture.
  • nitrous oxide ratio to oxygen 110, while nitrous oxide to nitrogen oxide ratio is 121.
  • the final product (after ammonia and water separation) contains 85.2% of nitrous oxide, 0.7% of nitrogen oxide, and 0.78% of oxygen.
  • Example 3 Catalyst with a composition of 5%MnO 2 /5%Bi 2 O 3 /Fe 2 O 3 is prepared as described in [3] and tested under the following conditions: reaction mixture composition - 0.75%NH 3 , 1.5%O 2 ; residence time - 0.072 s, temperature - 350-300°C. At 350°C ammonia conversion is 73%. Selectivity towards nitrous oxide and nitrogen oxide is 76.9 and 3.9% respectively. At 300°C ammonia conversion is 35%. Selectivity towards nitrous oxide and nitrogen oxide is 68 and 1.4% respectively. Ssp is 4 m2/g.
  • Example 4 Catalyst with a composition of 15%MnO 2 /15%Bi 2 O 3 /70%Al 2 O 3 is prepared as in example 1 and tested as in example 2. At 300°C ammonia conversion is 38%. Selectivity towards nitrous oxide and nitrogen oxide is 79 and 1.4% respectively. Ssp is 11 m2/g.
  • Example 5 Catalyst with a composition of 13%MnO 2 /l 1 %Bi 2 O 3 /76%Al 2 O 3 is prepared as in example 1 and tested as in example 2. At 350°C ammonia conversion is 76%. Selectivity towards nitrous oxide and nitrogen oxide is 76% and 3.8% respectively. At 300°C ammonia conversion is 39%. Selectivity towards nitrous oxide and nitrogen oxide is 83 and 1.3% respectively.
  • Example 6 Catalyst with a composition of 15%MnO 2 /7,5%Bi 2 O 3 /77.5%Al 2 O 3 is prepared as in example 1 and tested as in example 2. At 350°C ammonia conversion is 93.2%. Selectivity towards nitrous oxide and nitrogen oxide is 78.7% and 3.9% respectively. At 300°C ammonia conversion is 58.7%. Selectivity towards nitrous oxide and nitrogen oxide is 80 and 1.2% respectively. Ssp is 11 m2/g.
  • Example 7 Catalyst with a composition of 10%MnO 2 /5%Bi 2 O 3 /85%Al 2 O 3 is prepared as in example 1 and tested as in example 2. At 350°C ammonia conversion is 92.5%. Selectivity towards nitrous oxide and nitrogen oxide is 80% and 3.7% respectively. At 300°C ammonia conversion is 62.4%. Selectivity towards nitrous oxide and nitrogen oxide is 77 and 1.3% respectively. Ssp is 11 m2/g.
  • Example 8 Catalyst with a composition of 16%MnO 2 /16%Bi 2 O 3 /68%Al 2 O 3 is s prepared as in example 1 and tested as in example 2. At 350°C ammonia conversion is 73%. Selectivity towards nitrous oxide and nitrogen oxide is 78.8% and 3.9% respectively. At 300°C ammonia conversion is 37%. Selectivity towards nitrous oxide and nitrogen oxide is 37 and 1.4% respectively. Ssp is 39 m2/g.
  • Example 9 Catalyst with a composition of 5%MnO 2 /4.5%Bi 2 O 3 /90.5%Al 2 O 3 is 0 prepared as follows. 100 g of alumina granules are impregnated by a solution of Mn and Bi nitrates, dried in air and in the drying chamber at 120-130°C for 4 h. The obtained product was calcined in the furnace in air at 375-550°C for 2-4 h. Thus obtained catalyst was tested as in example 2. At 350°C ammonia conversion is 79%. Selectivity towards nitrous oxide and nitrogen oxide is 76% and 3.6% respectively. At 300°C ammonia conversion is 40%. s Selectivity towards nitrous oxide and nitrogen oxide is 80 and 1.3% respectively. Ssp is 5 m2/g.
  • Example 10 Catalyst with a composition of 35%MnO 2 /30%Bi 2 O 3 /35%Al 2 O 3 prepared mixing a mass containing 52 g of Mn oxide and Bi oxide powders and 35 g of aluminum hydroxide powder with 25 cm of water to obtain a moldable paste. Then the paste 0 was molded as cylinder granules 3 mm in diameter, dried at room temperature for 10 h, dried in the chamber at 120°C for 2 h, and calcined in the furnace at 375-550°C for 2-4 h. Thus obtained catalyst was tested as in example 2. At 350°C ammonia conversion is 77%. Selectivity towards nitrous oxide and nitrogen oxide is 78% and 3.1% respectively. At 300°C ammonia conversion is 39%. Selectivity towards nitrous oxide and nitrogen oxide is 74 and 1.1%) respectively. Ssp is 80 m /g. References:

Abstract

Catalyst claimed to be used to produce nitrous oxide by ammonia oxidation with oxygen. The invention aims at providing catalysts exhibiting a high activity, when oxygen content in reaction mixture is close or lower the stoichiometry one, and high selectivity towards nitrous oxide and low selectivity towards nitrogen oxides. The catalyst composition is as follows, mass.%: manganese oxide (referred to MnO2) 5.0-35.0; bismuth oxide 4.5-30.0; aluminium oxide 35.0-90.5; specific surface area is 5-80 m2/g.

Description

AMMONIA OXIDATION CATALYST COMPRISING ALUMINIUM OXIDE, BISMUTH OXIDE AND MANGANESE OXIDE
The present invention describes catalysts to be used for nitrous oxide production by ammonia oxidation with molecular oxygen in chemical industry. Along with a high activity, understood as conversion at a definite residence time, catalysts for ammonia oxidation to produce nitrous oxide should also meet the following demands:
• they should provide a high selectivity towards nitrous oxide and a low selectivity towards nitrogen oxide in the whole temperature range of ammonia oxidation; • they should perform well under conditions, when reaction mixture contains oxygen in stoichiometry amount or below the stoichiometry amount. As a rule, the known catalysts do not comply with all above demands. Thus a bulk manganese-bismuth catalyst [1] containing 5% Bi2O3 and 95% MnO2 has a low activity. At a temperature of 200°C, when the selectivity towards nitrous oxide is maximum, and equals 88.5% at an inlet ammonia concentration of 10.8 vol.% in the oxygen excess, a complete ammonia conversion occurs at a residence time of 5 s. Meanwhile the selectivity towards NO and NO is 0.9%. As the process temperature increases to 300°C, the yields of nitrous oxide and NO+NO2 are 79 and 3.1% respectively. As ammonia concentration decreases to 3.02 vol.%, the selectivity towards nitrous oxide falls to 65%. Therefore, beside a low activity in ammonia oxidation by the oxygen excess, the catalyst shows a high selectivity towards nitrogen oxides.
Another catalyst for ammonia oxidation consists of the oxides of iron, bismuth and manganese in the following ratio: 79.45% Fe2O3, 11.53% Bi2O3, 7.21% MnO2 [2]. The maximum yield of nitrous oxide in the said catalyst is 82%, and it is attained under the following conditions: temperature - 350°C; inlet concentrations: ammonia - 10 vol.%, oxygen - 90 vol%. However, at this temperature the selectivity towards nitrogen oxide is 6%. At 300°C the selectivity towards nitrous oxide and nitrogen oxide is 79% and 1.5% respectively. Therefore, the catalyst does not meet all demands in concern, because it has a low selectivity towards nitrous oxide at a high selectivity towards nitrogen oxide. Catalyst with a composition of 5% MnO2, 5% Bi2O3, 90% Fe2O3 [3] is most close in performance and properties to the catalyst claimed in the present invention. It shows the following results. The maximum nitrous oxide yield is 87%, when reaction mixture containing 10% of ammonia in air (thus in oxygen excess, concentration 18.9 vol.%). If 5 reaction mixture contains 1 ammonia part, 5 air parts, and 5 nitrogen parts, and so it is close to stoichiometry (9.1 vol.% ammonia and 9.55 vol.% oxygen), then the yield of nitrous oxide is 81 %. At 275-300°C the residence time for complete conversion is 3.6 s. Therefore, the catalyst has a low activity and not high enough selectivity towards nitrous oxide under conditions, when reaction mixture contains ammonia and oxygen in amounts close to 10 stoichiometry.
The present invention aims at providing catalysts that are highly active under conditions, when reaction mixture contains oxygen in amount close or below the stoichiometry one, showing a high selectivity towards nitrous oxide, and a low selectivity towards nitrogen oxide. ι5 For the purpose the claimed catalysts for the nitrous oxide production by ammonia oxidation have the following composition (mass.%):
5.0-35.0 - manganese oxide (referred to MnO2)
4.5-30.0 - bismuth oxide (Bi2O3)
90.5-35.0 - aluminum oxide (Al2O3). 0 The catalysts of the said composition are prepared by impregnating alumina with a solution of Mn and Bi nitrates, or by mixing the powders of Mn and Bi oxides with the powder of aluminum hydroxide to be then molded, or depositing the said components on an inert support. At the final stage the catalysts are dried, and calcined at 375-550°C. Thus obtained catalysts show a high activity, when the oxygen content in the reaction mixture is s close or lower the stoichiometry one, and exhibit a high selectivity towards nitrous oxide, and a low selectivity towards nitrogen oxide.
At a temperature of 350°C, and at a residence time of 0.7 sec, ammonia/oxygen ratio being 1.44, and ammonia concentration being 7.3 vol.%, ammonia conversion on the said catalysts is 82-99.2%. The selectivity towards nitrous and nitrogen oxides is 82-84.6 and 2.1 - 2.7% respectively. After water and ammonia separation the final product contains 79.6-81.7% of nitrous oxide, 4.1-5.25% of nitrogen oxide, and 0.82-0.84% of oxygen.
At a temperature of 300°C, and at a residence time of 1.6 sec, ammonia/oxygen ratio being 1.44, and ammonia concentration being 7.3 vol.%, ammonia conversion on the said s catalysts is 82.5-99.0%. The selectivity towards nitrous and nitrogen oxides is 83-86 and 0.3- 0.35% respectively. After water and ammonia separation the final product contains 82.2- 84.9% of nitrous oxide, 0.6-0.69%) of nitrogen oxide, and 0.75-0.77% of oxygen.
The high activity and selectivity of the claimed catalysts in ammonia oxidation to nitrous oxide is provided by its components at the said percent ratios. 0 Catalyst specific surface area also has a positive effect. The tests show that at a stable high activity the catalyst shows the highest selectivity, when its specific surface area ranges within 5-80 m2/g.
Example 1. Catalyst with a composition of 13%MnO2/l 1 %Bi2O3/76%Al2O3 is prepared as follows. 100 g of alumina granules are impregnated by incipient wetness with a s solution of Mn and Bi nitrates, are dried in air and then in a drying chamber at 130°C for 2-4 h. Thus obtained product is once again impregnated with a solution of Mn and Bi nitrates, dried in air and in the drying chamber at 130°C for 4 hours. Then the granules were calcined in a furnace at 375-550°C for 2-4 h. Thus obtained catalyst is tested under reaction conditions similar to those described in [3], reaction mixture composition being 9%NH3 and 9%O2. At 350°C and at a residence time of 0.7 s ammonia conversion is 99.2%. Selectivity towards nitrous oxide and nitrogen oxide is 87 and 2.8% respectively. At 300°C at the same gas composition and at a contact time of 1.6 s ammonia conversion is 99.4%. Selectivity towards nitrous oxide and nitrogen oxide is 88.6 and 0.30% respectively. Ssp is 10 m2/g.
Example 2. Catalyst prepared as in example 1 is tested at ammonia to oxygen ratio equal to 1.44 and ammonia concentration equal to 7.3 vol.% in the reaction mixture.
At 350°C and at a residence time of 0.7 s ammonia conversion is 82%. Selectivity towards nitrous oxide and nitrogen oxide is 84.6 and 2.7% respectively. In the final product nitrous oxide to oxygen ratio is 97.4, nitrous oxide to nitrogen oxide ratio being 15.6. After ammonia and water separation the final product contains 82% of nitrous oxide, 5% of nitrogen oxide, and 0.84% of oxygen.
At 300°C at the same gas composition and at a contact time of 1.6 s ammonia conversion is 82.5%. Selectivity towards nitrous oxide and nitrogen oxide is 86 and 0.35% respectively. In the final product nitrous oxide ratio to oxygen is 110, while nitrous oxide to nitrogen oxide ratio is 121. The final product (after ammonia and water separation) contains 85.2% of nitrous oxide, 0.7% of nitrogen oxide, and 0.78% of oxygen.
Example 3. Catalyst with a composition of 5%MnO2/5%Bi2O3/Fe2O3 is prepared as described in [3] and tested under the following conditions: reaction mixture composition - 0.75%NH3, 1.5%O2; residence time - 0.072 s, temperature - 350-300°C. At 350°C ammonia conversion is 73%. Selectivity towards nitrous oxide and nitrogen oxide is 76.9 and 3.9% respectively. At 300°C ammonia conversion is 35%. Selectivity towards nitrous oxide and nitrogen oxide is 68 and 1.4% respectively. Ssp is 4 m2/g.
Example 4. Catalyst with a composition of 15%MnO2/15%Bi2O3/70%Al2O3 is prepared as in example 1 and tested as in example 2. At 300°C ammonia conversion is 38%. Selectivity towards nitrous oxide and nitrogen oxide is 79 and 1.4% respectively. Ssp is 11 m2/g.
Example 5. Catalyst with a composition of 13%MnO2/l 1 %Bi2O3/76%Al2O3 is prepared as in example 1 and tested as in example 2. At 350°C ammonia conversion is 76%. Selectivity towards nitrous oxide and nitrogen oxide is 76% and 3.8% respectively. At 300°C ammonia conversion is 39%. Selectivity towards nitrous oxide and nitrogen oxide is 83 and 1.3% respectively.
Example 6. Catalyst with a composition of 15%MnO2/7,5%Bi2O3/77.5%Al2O3 is prepared as in example 1 and tested as in example 2. At 350°C ammonia conversion is 93.2%. Selectivity towards nitrous oxide and nitrogen oxide is 78.7% and 3.9% respectively. At 300°C ammonia conversion is 58.7%. Selectivity towards nitrous oxide and nitrogen oxide is 80 and 1.2% respectively. Ssp is 11 m2/g.
Example 7. Catalyst with a composition of 10%MnO2/5%Bi2O3/85%Al2O3 is prepared as in example 1 and tested as in example 2. At 350°C ammonia conversion is 92.5%. Selectivity towards nitrous oxide and nitrogen oxide is 80% and 3.7% respectively. At 300°C ammonia conversion is 62.4%. Selectivity towards nitrous oxide and nitrogen oxide is 77 and 1.3% respectively. Ssp is 11 m2/g.
Example 8. Catalyst with a composition of 16%MnO2/16%Bi2O3/68%Al2O3 is s prepared as in example 1 and tested as in example 2. At 350°C ammonia conversion is 73%. Selectivity towards nitrous oxide and nitrogen oxide is 78.8% and 3.9% respectively. At 300°C ammonia conversion is 37%. Selectivity towards nitrous oxide and nitrogen oxide is 37 and 1.4% respectively. Ssp is 39 m2/g.
Example 9. Catalyst with a composition of 5%MnO2/4.5%Bi2O3/90.5%Al2O3 is 0 prepared as follows. 100 g of alumina granules are impregnated by a solution of Mn and Bi nitrates, dried in air and in the drying chamber at 120-130°C for 4 h. The obtained product was calcined in the furnace in air at 375-550°C for 2-4 h. Thus obtained catalyst was tested as in example 2. At 350°C ammonia conversion is 79%. Selectivity towards nitrous oxide and nitrogen oxide is 76% and 3.6% respectively. At 300°C ammonia conversion is 40%. s Selectivity towards nitrous oxide and nitrogen oxide is 80 and 1.3% respectively. Ssp is 5 m2/g.
Example 10. Catalyst with a composition of 35%MnO2/30%Bi2O3/35%Al2O3 prepared mixing a mass containing 52 g of Mn oxide and Bi oxide powders and 35 g of aluminum hydroxide powder with 25 cm of water to obtain a moldable paste. Then the paste 0 was molded as cylinder granules 3 mm in diameter, dried at room temperature for 10 h, dried in the chamber at 120°C for 2 h, and calcined in the furnace at 375-550°C for 2-4 h. Thus obtained catalyst was tested as in example 2. At 350°C ammonia conversion is 77%. Selectivity towards nitrous oxide and nitrogen oxide is 78% and 3.1% respectively. At 300°C ammonia conversion is 39%. Selectivity towards nitrous oxide and nitrogen oxide is 74 and 1.1%) respectively. Ssp is 80 m /g. References:
1. V.F. Postnikov, L.L. Kuz'min and N.K. Tsal'm,- J.Chem.Ind., 22, 1348 (1937)
2. Zawadzki, Discussions Faraday Soc, 1950, N8, p.140
3. Schlecht, L., and von Nagel, A., Ger. Patent 503200 (1930) Table 1 example content, mass.% conversion, % SN20> SNO'% T°C
MnO2 Bi2O3
13 11 99.2 87 2.8 350
99.4 88.6 0.35 300
13 11 82 84.6 2.7 350
82.5 86 0.35 300
5 5 73 76.9 3.9 350
35 68 1.4 300
15 15 38 79 1.4 300
13 11 76 76 3.8 350
39 83 1.3 300
15 7.5 93.2 78.7 3.9 350
58.7 80 1.2 300
10 5 92.5 80 3.7 350
62.4 77 1.3 300
16 16 73 78.8 3.9 350
37 74.7 1.4 300
5 4.5 79 76 3.6 350
40 80 1.3 300
10 35 30 77 78 3.1 350
39 74 1.1 300

Claims

CLAIMS:
1. A catalyst for production of nitrous oxide, comprising MnO2, Bi2O3, and Al2O3.
2. The catalyst of claim 1, where the catalyst comprises: about 5.0-35.0 % MnO2; about 4.5-30.0% Bi2O3; and about 35.0-90.5% Al2O3.
3. The catalyst of claim 1, where the specific surface area of the catalyst is about 5-80 m2/g.
4. The catalyst of claim 1, where the specific surface area of the catalyst is about 10-40 m2/g.
5. The catalyst of claim 1 , where the catalyst consists essentially of: about 5.0-35.0 % MnO2; about 4.5-30.0% Bi2O3; and about 35.0-90.5% Al2O3.
6. The catalyst of claim 1, where the catalyst comprises: about 13 % MnO2; about 11 % Bi2O3; and about 76 % Al2O3.
7. The catalyst of claim 1, where the catalyst comprises: about 15 % MnO2; about 15 % Bi2O3; and about 70 % Al2O3.
8. The catalyst of claim 1 , where the catalyst comprises: about 15 % MnO2; about 7.5 % Bi2O3; and about 77.5 % Al2O3.
9. The catalyst of claim 1, where the catalyst comprises: about 10 % MnO2; about 5 % Bi2O3; and about 85 % Al2O3.
10. The catalyst of claim 1, where the catalyst comprises: about 16 % MnO2; about 16 % Bi2O3; and about 68 % Al2O3.
11. The catalyst of claim 1 , where the catalyst comprises: about 5 % MnO2; about 4.5 % Bi2O3; and about 90.5 % Al2O3.
12. The catalyst of claim 1, where the catalyst comprises: about 35 % MnO2; about 30 % Bi2O3; and about 35 % Al2O3.
PCT/US1997/020830 1996-12-10 1997-11-12 Ammonia oxidation catalyst comprising aluminium oxide, bismuth oxide and manganese oxide WO1998025698A1 (en)

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EP97947521A EP0948404A1 (en) 1996-12-10 1997-11-12 Ammonia oxidation catalyst comprising aluminium oxide, bismuth oxide and manganese oxide
CA002274760A CA2274760A1 (en) 1996-12-10 1997-11-12 Ammonia oxidation catalyst comprising aluminium oxide, bismuth oxide and manganese oxide
BR9713999-8A BR9713999A (en) 1996-12-10 1997-11-12 Ammonia oxidation catalyst comprising aluminum oxide, bismuth oxide and manganese oxide
JP52667198A JP2001505817A (en) 1996-12-10 1997-11-12 Ammonia oxidation catalyst containing aluminum oxide, bismuth oxide and manganese oxide
AU52579/98A AU744311B2 (en) 1996-12-10 1997-11-12 Ammonia oxidation catalyst comprising aluminium oxide, bismuth oxide and anganese oxide

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RU96123343A RU2102135C1 (en) 1996-12-10 1996-12-10 Catalyst for nitrous oxide synthesis
RU96123343/04 1996-12-10

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US6414197B1 (en) 1997-07-05 2002-07-02 General Electric Company Preparation of phenol and its derivatives
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US7449606B2 (en) 2003-09-25 2008-11-11 Basf Se Method for producing a ketone
US7692045B2 (en) 2004-09-23 2010-04-06 Basf Aktiengesellschaft Method for purifying and concentrating dinitrogen monoxide
US7754172B2 (en) 2005-11-22 2010-07-13 Basf Aktiengesellschaft Method for isolating N2O
US7838705B2 (en) 2003-09-25 2010-11-23 Basf Aktiengesellschaft Process for the preparation of cyclododecanone
WO2011020878A2 (en) 2009-08-21 2011-02-24 Basf Se Method for producing 4-pentenoic acid
WO2012066296A2 (en) 2010-11-19 2012-05-24 Invista Technologies S.A.R. L. Nitrous oxide-containing ionic liquids as chemical reagents
US8404901B2 (en) 2008-04-02 2013-03-26 Basf Se Process for purifying dinitrogen monoxide
US8449655B2 (en) 2006-12-11 2013-05-28 Basf Aktiengesellschaft Process for isolating N2O
US8592632B2 (en) 2008-11-11 2013-11-26 Basf Se Process for preparing cyclic diamines
US8808430B2 (en) 2008-04-02 2014-08-19 Basf Se Process for purifying N2O
DE102014212602A1 (en) 2013-07-02 2015-01-08 Basf Se Process for the preparation of a ketone from an olefin
GB2525721A (en) * 2014-02-27 2015-11-04 Johnson Matthey Plc Exhaust system having N20 catalyst in EGR circuit
WO2024033126A1 (en) 2022-08-11 2024-02-15 Basf Se A process for the explosion-proof storage of nitrous oxide

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4419274A (en) * 1980-12-16 1983-12-06 Pohang Iron & Steel Co., Ltd. Nonmetallic catalyst compositions for oxidation of ammonia and process for making the catalyst
US5212137A (en) * 1990-01-09 1993-05-18 Standard Oil Company Catalyst for the manufacture of acrylonitrile and methacrylonitrile

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4419274A (en) * 1980-12-16 1983-12-06 Pohang Iron & Steel Co., Ltd. Nonmetallic catalyst compositions for oxidation of ammonia and process for making the catalyst
US5212137A (en) * 1990-01-09 1993-05-18 Standard Oil Company Catalyst for the manufacture of acrylonitrile and methacrylonitrile

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
MASSIMILLA L, JOHNSTONE HF: "Reaction Kinetics in fluidized beds", CHEMICAL ENGINEERING SCIENCE, vol. 16, 1961, pages 115 - 112, XP002058297 *
SHEN CY, JOHNSTONE HF: "Gas-solid Contact in FLuidized Beds", A.I.CH.E, vol. 1, no. 3, March 1955 (1955-03-01), pages 349 - 354, XP002058298 *
WERTHER J, HENGER B: "Ermittlung optimaler Betriebseinstellungen für technische Wirbelschichtreaktoren", CHEM. -ING. -TECH, vol. 52, no. 2, 1980, pages 106 - 113, XP002058296 *

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US6414197B1 (en) 1997-07-05 2002-07-02 General Electric Company Preparation of phenol and its derivatives
EP1036761A1 (en) * 1999-03-16 2000-09-20 Phenolchemie GmbH & Co. KG Process for the preparation of nitrous oxide
US6388145B1 (en) 1999-04-05 2002-05-14 General Electric Company Method for the oxidation of benzene and/or toluene to phenol and/or cresols
US7449606B2 (en) 2003-09-25 2008-11-11 Basf Se Method for producing a ketone
US7838705B2 (en) 2003-09-25 2010-11-23 Basf Aktiengesellschaft Process for the preparation of cyclododecanone
WO2006032532A1 (en) 2004-09-23 2006-03-30 Basf Aktiengesellschaft Method for the production of cyclopentanone
US7692045B2 (en) 2004-09-23 2010-04-06 Basf Aktiengesellschaft Method for purifying and concentrating dinitrogen monoxide
US7803971B2 (en) 2004-09-23 2010-09-28 Basf Akiengesellschaft Method for the production of cyclopentanone
US7754172B2 (en) 2005-11-22 2010-07-13 Basf Aktiengesellschaft Method for isolating N2O
US8449655B2 (en) 2006-12-11 2013-05-28 Basf Aktiengesellschaft Process for isolating N2O
US8808430B2 (en) 2008-04-02 2014-08-19 Basf Se Process for purifying N2O
US8404901B2 (en) 2008-04-02 2013-03-26 Basf Se Process for purifying dinitrogen monoxide
US8592632B2 (en) 2008-11-11 2013-11-26 Basf Se Process for preparing cyclic diamines
US8362296B2 (en) 2009-08-21 2013-01-29 Basf Se Process for preparing 4-pentenoic acid
WO2011020878A2 (en) 2009-08-21 2011-02-24 Basf Se Method for producing 4-pentenoic acid
WO2012066296A2 (en) 2010-11-19 2012-05-24 Invista Technologies S.A.R. L. Nitrous oxide-containing ionic liquids as chemical reagents
DE102014212602A1 (en) 2013-07-02 2015-01-08 Basf Se Process for the preparation of a ketone from an olefin
GB2525721A (en) * 2014-02-27 2015-11-04 Johnson Matthey Plc Exhaust system having N20 catalyst in EGR circuit
GB2525721B (en) * 2014-02-27 2016-12-28 Johnson Matthey Plc Exhaust system having N20 catalyst in EGR circuit
US9587591B2 (en) 2014-02-27 2017-03-07 Johnson Matthey Public Limited Company Exhaust system having N2O catalyst in EGR circuit
WO2024033126A1 (en) 2022-08-11 2024-02-15 Basf Se A process for the explosion-proof storage of nitrous oxide

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EP0948404A1 (en) 1999-10-13
CA2274760A1 (en) 1998-06-18
KR20000069398A (en) 2000-11-25
BR9713999A (en) 2000-02-29
RU2102135C1 (en) 1998-01-20

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