Catalyst and process for decomposing carbonyl sulfide and hydrogen cyanide
View Patent ↗A solution of a chromium compound is impregnated into a silica-alumina carrier made of alumina and containing 1 to 5 weight % of silica relative to the weight of the carrier, thereby to obtain a decomposing catalyst carrying 10 to 15 weight % of chromium oxide relative to the weight of the catalyst in terms of Cr 2 O 3 . By contacting mixed gas obtained through partial oxidation of heavy oil and/or coal with the decomposing catalyst, COS and HCN contained in the mixed gas are decomposed/removed. In this case, transition of alumina into boehmite can be suppressed owing to coexistence of silica and chromium oxide, so that COS and HCN can be decomposed by highly active catalytic reactions over a long time.
1. A process for decomposing carbonyl sulfide and hydrogen cyanide contained in a mixed gas obtained by partially oxidizing heavy oil or coal, the mixed gas consisting essentially of hydrogen, carbon monoxide, steam and carbon dioxide and also containing impurities comprising hydrogen sulfide, carbonyl sulfide and hydrogen cyanide, which process comprises:
contacting the mixed gas with a catalyst which comprises:
(a) a carrier made of alumina and containing silica, and
(b) chromium oxide carried by the carrier, thereby converting carbonyl sulfide and carbon dioxide according to the formula:
COS+H 2 O→CO 2 +H 2 S (1)
and converting hydrogen cyanide to ammonia, carbon monoxide and methane according to the following formulae:
HCN+H 2 O→NH 3 +CO (2)
and
HCN+3H 2 →NH 3 +CH 4 (3),
wherein chromium oxide is contained in an amount of 10 to 15 weight % in terms of Cr 2 O 3 relative to the catalyst and the catalyst has a BET specific surface area of 200 m 2 /g or greater,
wherein the mixed gas has a temperature which is higher than a dew point of the mixed gas and is within the range of from 110 to 250° C., and
wherein, in the catalyst, chromium oxide is carried on a surface of the carrier as a complex oxide compound.
2. The process according to claim 1 , which further comprises:
subjecting the mixed gas which has been contacted with the catalyst, to an absorber for removing hydrogen sulfide from the mixed gas.
3. The process according to claim 1 , wherein the mixed gas has a pressure of from atmospheric pressure to 8 MPa and is contacted with the catalyst at a gas hourly space velocity of 900 to 20,000 h −1 .
4. The process according to claim 1 , wherein, in the catalyst, silica is contained in an amount of 1 to 5 weight % relative to the carrier.
5. The process according to claim 1 , wherein the BET specific surface area of the catalyst is 220 to 270 m 2 /g.
6. The process according to claim 1 , wherein the catalyst has an equivalent diameter of 1 mm to 6 mm.
7. The process according to claim 1 , wherein the alumina in the catalyst is γ-type or η-type.