Process for decomposing ammonia in an off-gas

Abstract: In a process for the catalytic low temperature oxidation of ammonia to nitrogen in an ammonia containing off-gas at a temperature of between 200 o C and 500 o C the improvement comprises, sulphating a catalyst comprising on an inert carrier a metal selected from the group of copper, cobalt, iron, chromium, nickel, manganese and mixtures thereof in the form of their oxides and/or sulphates and a further component selected from the group of platinum metals; contacting the ammonia containing atmosphere with the catalyst, and withdrawing a decomposed gas being rich in nitrogen.

Description: The present invention is directed to a process for decomposing ammonia and more specifically a process for the selective decomposition of ammonia to nitrogen in an ammonia containing off-gas at low temperatures in the presence of a catalyst. Catalytic decomposition of ammonia with oxygen to nitrogen and water proceeds at the following reaction: 4NH 3 + 3O 2 → 2N 2 + 6H 2 O In addition to the above oxidation reaction, ammonia further reacts with oxygen to nitrogen oxides mainly by the reaction: 4NH 3 + 7O 2 → 4NO 2 + 6H 2 O 4NH 3 + 5O 2 → 4NO + 6H 2 O 2NH 3 + 2O 2 → N 2 O + 3H 2 O For reasons of high formation of desired nitrogen, the process depends substantially on the selectivity of a decomposition catalyst for the formation of nitrogen as the main oxidation product rather than the undesired nitrogen oxides. Known catalysts being active in the selective decomposition of ammonia are cobalt or cobalt oxide containing catalysts as described in German Offenlegungsschrift DE-A-2,026,657, and vanadium oxide containing catalysts supported on a carrier of alumina as disclosed in US patent No. 5,139,756. Other known catalysts for the decomposition of ammonia in the lower temperature range contain platinum metals (German Offenlegungsschrift DE-A-2,447,552). We have now found that selectivity and activity of the known ammonia decomposition catalysts are, surprisingly, improved when sulphating the catalysts during or prior to contact with ammonia containing gas. In accordance with the above findings and observations, this invention provides a process for the catalytic low temperature oxidation of ammonia in an ammonia containing gas at a temperature of between 250°C and 500°C wherein the process comprises, sulphating a catalyst comprising on an inert carrier a metal selected from the group of copper, cobalt, iron, chromium, nickel, manganese and mixtures thereof in the form of their oxides and/or sulphides and a further component selected from the group of platinum metals, contacting the ammonia containing gas with the sulphated catalyst; and withdrawing a decomposed gas being rich in nitrogen. In carrying out the process industrially, the catalysts will typically comprise the active catalytic metal in an amount of 1-20% by weight and a platinum metal promotor in an amount of 100-2000 ppm by weight, supported on the carrier. Suitable carriers may be selected from alumina, titania, silica, or mixtures thereof. The catalysts are preferably used in the shape of rings, pellets, tablets and monolithic structured bodies. Convenient procedures for manufacturing the catalysts for use in this invention comprise steps of impregnating the carrier material with an aqueous solution of a salt of the active compounds and then heating to a temperature sufficient to decompose the salt to oxide or sulphide of the metal component. As mentioned before, the activity and the selectivity of the catalysts during decomposition of ammonia is considerably increased, when the catalysts are used in their sulphated form. To maintain the catalysts in the sulphated form, volatile sulphur compounds in an amount of typically 1-4000 ppm are, preferably, added to the ammonia containing gas prior to contact with the catalysts. By the process, an off-gas, having ammonia in a concentration of up to 10.000 ppm by volume, is contacted with the above catalysts usually arranged in a reactor as a fixed bed. At an inlet temperature of between 200°C and 500°C, preferably 230-380°C, ammonia decomposition to nitrogen is nearly complete. Example 1 Preparation of a Co/Pt catalyst supported on a silica carrier. A silica carrier in the form of a ring with an outer diameter of 10 mm was calcined at 600°C in air. The calcined carrier was then impregnated with an aqueous solution of Co(NO 3 ) 2 to a final cobalt concentration of 10% by weight calculated on the total weight of the impregnated carrier. The carrier was dried after impregnation. In a subsequent step, the carrier was further impregnated with platinum from an aqueous solution of H 2 PtCl 6 to a final load of Pt of 670 ppm by weight calculated on the total weight of the impregnated carrier. Finally, the impregnated carrier was dried and calcined at 500°C in air to obtain the active catalyst. Example 2 In a procedure similar to the one of Example 1, a catalyst was prepared having 10% by weight Cu and 670 ppm by weight Pt as the active material on a silica carrier. The calcined carrier was impregnated with an aqueous solution of Cu(NO 3 ) 2 , and, subsequently, with an aqueous solution of H 2 PtCl 6 . The impregnated carrier is then calcined as described in Example 1. Example 3 Preparation of catalyst having Cu, Ni and Pt as active material on a silica carrier. The catalyst was prepared at a procedure similar to the one of Example 2 except for an additional step of impregnating the carrier with an aqueous solution of Ni(NO 3 ) 2 to a final load of Ni of 10% by weight before impregnation with platinum. Example 4 Preparation of a catalyst having Cu, Pd and Pt as active material on a silica carrier. A calcined silica carrier as described above was impregnated with an aqueous solution of Cu(NO 3 ) 2 to a final load of Cu of 10% by weight. The Cu-impregnated carrier was dried and then impregnated with Pd and Pt from an aqueous solution of Pd(NO 3 ) 2 and H 2 PtCl 6 , each to a content of 670 ppm by weight calculated on the total weight of the impregnated carrier. Finally, the impregnated catalyst was activated by calcination at 500°C in air. Example 5 The catalysts, as prepared in Example 1-4, were tested for their activity and selectivity in the decomposition of ammonia to nitrogen. Samples of 0.25 litre were loaded as fixed bed in an adiabatic operated reactor tube. A gas with the composition of 20 vol% O 2 2 vol% H 2 O 1000 ppm NH 3 , and a sulphur dioxide content as specified in the Table below was passed under the conditions specified in the Table through the reactor. Ammonia conversion rates and selectivity for nitrogen obtained with the catalysts under the specified conditions are summarized in the Table. Catalyst concentration Temp °C Inlet Gas Flow NHSV Nm 3 /m 3 /h SO 2 -concentration Inlet ppm NH 3 -concentration N 2 selectivity % Inlet ppm Conv.-outlet % Co/Pt 232 10000 0 1000 94 53 292 10000 200 1000 92 77,9 Cu/Pt 290 10000 0 1000 92 26,1 293 10000 10 1000 98 95,7 293 10000 200 1000 92 97 330 10000 200 1000 99,8 90,9 Cu/Ni/Pt 290 10000 0 1000 95 45,3 306 10000 200 1000 96 98,8 Cu/Pd/Pt 290 10000 0 1000 95 38,9 328 10000 200 1000 99,6 99,1 As obvious from the results, decomposition of ammonia to nitrogen is considerable improved in the presence of small amounts of sulphur dioxide added to the test gas at the reactor inlet. When compared to the known processes operating with non-sulphated catalysts, the presence of sulphur in the gas results in a high selectivity during decomposition of ammonia to nitrogen. Formation of noxious nitrogen oxides, as with the known catalytic ammonia decomposition processes is substantially depressed.

Claims: A process for the catalytic low temperature oxidation of ammonia to nitrogen in an ammonia containing off-gas at a temperature of between 200°C and 500°C wherein the process comprises, sulphating a catalyst comprising on an inert carrier a metal selected from the group of copper, cobalt, iron, chromium, nickel, manganese and mixtures thereof in the form of their oxides and/or sulphides and a further component selected from the group of platinum metals; contacting the ammonia containing off-gas with the catalyst, and withdrawing a decomposed gas being rich in nitrogen. The process of claim 1, wherein the platinum metals comprise platinum and/or palladium. The process of claim 1, wherein the catalyst comprises the metal in an amount of 1-20% by weight calculated as the total weight of the catalyst. The process of claim 1, wherein the catalyst comprises the further component in an amount of 100-2000 ppm by weight calculated on the total weight of the catalyst. The process of claim 1, wherein the carrier is selected from the group of alumina, titania, silica and mixtures thereof. The process of claim 1, wherein the catalyst is in a shape of rings, pellets, tablets or monolithic structured bodies. The process of claim 1, wherein the catalyst is sulphated by adding a volatile sulphur compound to the off-gas. The process of claim 7, wherein the volatile sulphur compound is added in an amount of between 1-4000 ppm by volume to the off-gas.

Inventors: DANNEVANG FLEMMING, DANNEVANG, FLEMMING
Applicants: TOPSOE HALDOR AS, HALDOR TOPSOE A/S
Application year: 1995
Main classification: B01D53
IPC codes: C01B21, B01J23, B01J27, B01D53