Method for oxidizing ammonia and system suitable therefor

Patent metadata

Field	Value
Publication number	US-10414654-B2
Application number	US-201414776422-A
Country	US
Kind code	B2
Filing date	Mar 13, 2014
Priority date	Mar 14, 2013
Publication date	Sep 17, 2019
Grant date	Sep 17, 2019

Abstract

A system suitable for oxidizing ammonia with oxygen in the presence of catalysts is described. The system includes a reactor equipped with at least one supply line for a reactant gas mixture and at least one discharge line for a process gas; a catalyst comprising at least one transition metal oxide that is not an oxide of a platinum metal; and a device for adjusting a molar ratio of oxygen to ammonia of less than or equal to 1.75 mol/mol in the reactant gas mixture by mixing an oxygen-containing gas stream having an O2 content of <20% by volume with a chosen amount of ammonia. The oxygen-containing gas stream is produced by a device for: diluting an air stream with a gas stream comprising less than 20% by volume oxygen; or depleting oxygen from an oxygen-containing gas mixture, preferably from air; or by a combination thereof.

First claim

The invention claimed is:

1. A method for oxidizing ammonia with oxygen in the presence of catalysts comprising at least one transition metal oxide that is not an oxide of a platinum metal, wherein a molar ratio of oxygen to ammonia at the inlet of a reactant gas mixture into a catalyst bed is adjusted to values from 1.25 to 1.75, wherein the outlet temperature of a product gas from the catalyst bed is from 700° C. to 950° C., and wherein the outlet temperature of the product gas from the catalyst bed is adjusted based on a concentration of ammonia of the reactant gas mixture at the inlet of the catalyst bed.

2. The method as claimed in claim 1 , wherein the ratio of the molar amounts of oxygen to ammonia in the reactant gas mixture at the inlet into the catalyst bed is so chosen that it is in the range of from 0.1 mol oxygen/mol ammonia below to 0.4 mol oxygen/mol ammonia above an optimal molar ratio, wherein the optimal molar ratio is the ratio of oxygen to ammonia at the inlet of the reactant gas mixture into the catalyst bed at which a maximum yield of NO x is achieved.

3. The method as claimed in claim 1 , wherein the optimal molar ratio of oxygen to ammonia is determined by carrying out a series of tests under given method conditions using a chosen catalyst in a defined system, at a defined space velocity and flow rate, at a defined outlet or inlet temperature, under a defined pressure and using a defined reaction medium comprising oxygen and a defined amount of ammonia, wherein the concentration of oxygen at the inlet into the catalyst bed is so chosen that the corresponding molar oxygen/ammonia ratio varies between a minimum molar oxygen/ammonia ratio, preferably a minimum molar oxygen/ammonia ratio of 1.25 mol/mol, and a maximum molar oxygen/ammonia ratio, preferably a maximum molar oxygen/ammonia ratio of 1.75 mol/mol, determining a yield of NO x that is achieved in each case, and then determining the molar ratio of oxygen to ammonia that provides the maximum yield of NO x under otherwise constant reaction conditions.

4. The method as claimed in claim 1 , wherein the ratio of the molar amounts of oxygen to ammonia at the inlet of the reactant gas mixture into the catalyst bed is adjusted to values equal to 1.75, and wherein the oxygen content in the product gas at the outlet of the catalyst bed is at least 0.3% by volume.

5. The method as claimed in claim 4 , wherein the ratio of the molar amounts of oxygen to ammonia at the inlet of the reactant gas mixture into the catalyst bed is so chosen that the resulting oxygen content in the product gas at the outlet of the catalyst bed is from 0.3% by volume to 10.0% by volume.

6. The method as claimed in claim 1 , wherein the ammonia concentration at the inlet into an oxidation reactor is from 4 to 15% by volume.

7. The method as claimed in claim 1 , wherein part of the heat of reaction is dissipated, in particular by one of cooling the reactor walls and accommodating integrated cooling devices in the catalyst arrangement.

8. The method as claimed in claim 1 , wherein the inlet temperature of the reactant gas mixture comprising NH 3 and oxygen into the catalyst bed is from 20° C. to 300° C.

9. The method as claimed in claim 1 , wherein at least one of the volume stream of the reactant gas mixture and the volume of catalyst is so adjusted that the resulting space velocity is from 100,000 h −1 to 500,000 h −1 .

10. The method as claimed in claim 1 , wherein the catalyst comprises at least one of (1) doped transition metal oxides that are not oxides of the platinum metals and (2) mixed oxides of such transition metal oxides, wherein the mixed oxides have spinel, delafossite, perovskite or brownmillerite structure.

11. The method as claimed in claim 10 , wherein the mixed oxide has a perovskite structure having the general empirical formula ABO 3±δ , or a brownmillerite structure having the general empirical formula A2B205±o; and
wherein:
δ assumes a value of from 0.01 to 0.5;
A represents mono-, di- or tri-valent cations;
B represents tri-, tetra- or penta-valent cations; and
the ionic radius of A is greater than the ionic radius of B.

12. The method as claimed in claim 11 , wherein the A position of the perovskites or brownmillerites is occupied to the extent of more than 50% by one or more elements selected from the group of the rare earth metals and alkaline earth metals and the B position of the perovskites or brownmillerites is occupied to the extent of more than 50% by one or more elements selected from the group Cr, Mn, Fe, Co, Ni.

13. The method as claimed in claim 1 , wherein the catalyst comprises transition metal oxides that are not oxides of the platinum metals, and optionally other active components and/or co-components, incorporated or embedded in a matrix or comprises transition metal oxides that are not oxides of the platinum metals, and optionally other active components and/or co-components applied to a support.

14. The method as claimed in claim 1 , wherein the catalyst comprises doped transition metal oxides that are not oxides of the platinum metals, and/or mixed oxides of such transition metal oxides, wherein the mixed oxides have spinel, delafossite, or brownmillerite structure.

15. The method as claimed in claim 14 , wherein the mixed oxide having a brownmillerite structure has a general empirical formula A 2 B 2 O 5±δ , wherein δ assumes a value of from 0.01 to 0.5, A represents mono-, di- or tri-valent cations and B represents tri-, tetra- or penta-valent cations, and the ionic radius of A is greater than the ionic radius of B.

16. The method as claimed in claim 12 , wherein the perovskite comprises LaCoO 3±δ .

Assignees

• Thyssenkrupp Ind Solutions Ag

Inventors

• Schwefer Meinhard
• Siefert Rolf
• Ruthardt Klaus
• Cremona Alberto
• Vogna Edoardo

Classifications

• C01P2002/34

  perovskite-type (ABO3) · CPC title

• C01B21/38

  Nitric acid · CPC title

• B01J37/082

  Decomposition and pyrolysis · CPC title

• B01J37/036

  to form a gel or a cogel · CPC title

• B01J37/033

  Using Hydrolysis · CPC title