CA1216838A - Catalyst for use in hydrolysis of carbonyl sulfide - Google Patents
Catalyst for use in hydrolysis of carbonyl sulfideInfo
- Publication number
- CA1216838A CA1216838A CA000439837A CA439837A CA1216838A CA 1216838 A CA1216838 A CA 1216838A CA 000439837 A CA000439837 A CA 000439837A CA 439837 A CA439837 A CA 439837A CA 1216838 A CA1216838 A CA 1216838A
- Authority
- CA
- Canada
- Prior art keywords
- catalyst
- group
- hydrolysis
- carbonyl sulfide
- oxides
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Landscapes
- Catalysts (AREA)
Abstract
ABSTRACT
A catalyst which comprises titanium oxide reinforcing material and oxides of one or more metals selected from Group Ia, Group IIa, Group IIb and Group IVb of the periodic table, the weight of said oxides corresponding to at least 0.5 wt.% of the weight of a final catalyst exhibits an excellent activity in hydrolysis of carbonyl sulfide. Said catalytic activity has no possibility of deterio-ration even in the presence of hydrogen sulfide and/or carbon dioxide coexist with feed gas.
A catalyst which comprises titanium oxide reinforcing material and oxides of one or more metals selected from Group Ia, Group IIa, Group IIb and Group IVb of the periodic table, the weight of said oxides corresponding to at least 0.5 wt.% of the weight of a final catalyst exhibits an excellent activity in hydrolysis of carbonyl sulfide. Said catalytic activity has no possibility of deterio-ration even in the presence of hydrogen sulfide and/or carbon dioxide coexist with feed gas.
Description
~2:~683~
A CATALYST FOR USE IN HYDROLYSIS OF CARBONYL SULFIDE
BAC~GROUND OF THE INVENTION
The present invention relstes to a catalyst suitable for convertin~
carbonyl sulfide in ~as into hydrogen sulfide, in the presence of water vapor.
Since sulfur compounds in VQrious ~ases poison catalysts used in chemical processes or corrode the appsratus used, much effort has hitherto been made to remove such sulfur compounds. Generally, it is also necessQry to remove sulfur-compounds from effluent ~ases to reduce air pollution.
Of the sulfur compounds found in gases, H2S and SO2 are relatively easy to remove, and can be removed by dry methods, or wet methods such as alkali solution washin~, amine absorption, and the like. However, as carbonyl sulfide is difficult to remove effectively by wet methods, it is ordinarily converted into hydrogen sulfide according to the hydrolysis reaction noted below:
COS + H20 ~ H2S + C2 An example of convertin~ carbonyl sulfide in a ~as into hydro~en sulfide in the presence of water vapor can be observed when treatin~ the tail gas of the Claus method. In this case, the catalysts used are usually titanium oxide, as carrier, and oxides of transition metals such as iron, cobalt, nickel, molybdenum and the like as active in~redients. We have, found however that these catalysts mentioned above suffer severe deterioration in the presence of hydro~en sulfide. In view of the fact that the hydrolysis of carbonyl sulfide is unavoidably accompanied by the creation of 1' ~. ~7 , hydrogen sulfide, the deteriorstion in activity may be a fatal defect in the catalysts used in the hydrolysis of carbonyl sulfide.
SUMMARY OF THE INVENTION
The object of the present invention is to provide a catalytic composition for use in the hydrolysis of carbonyl sulfide whose activity scarcely deteriorates even in the presence of hydrogen sulfide. This catalyst is prepared by admixing titanium oxide snd reinforcing material with oxides of one or more metals selected from the group consisting of an alkaline metal such as Li, Na, K, Cs or the like, an alkaline earth metal such as Mg, Ca, Ba or the like, Group IIb metals such as Zn, Cd or the like and Group IVb metal such as Sa, Pb or the like in an amount of at least 0.5 wt.% of the final catalyst.
The catalyst comprises mainly titanium oxide and metal oxidets). The COS-hydrolysis activity of this catalyst increases with the amount of metal oxide present, but remains substantially level when the amount of 0.5 wt.~ or more is present. Further amounts of metal oxide shows no marked improvements in COS-hydrolysis activity. In view of this, the preferable amount of metal oxide is more than O.5 wt.~ and a practical upper limit is 10 wt.% from the economical point of view.
BRIEF DESCRIPTION OF THE DRAWINGS
Fig. 1 is a perspective view of a titanium oxide carrier used in Example 2.
Fig. 2 is a graph showing the activities of carbonyl sulfide hydrolysing activity of the catalysts according to the present invention. The conversion is plotted against the active metal contant of the catalyst.
~2~6~}3~3 Fig. 3 which appears on the first sheet of drswings, is B graph which compares the carbonyl sulfide hydroly~is activity of cstalysts according to the present invention with conventional catalysts. The conversion ~ is plotted against hours on stream.
DETAILED DESCRIPTION OF THE INVENTION
Processes for manufacturing the catalysts of the present invention include the following:
a) A process which comprises mixing a titQnic acid or titanate and reinforcing material with salts or oxides of active metals selected from said alkaline metals, alkaline earth metals, Group IIB metals and Group IVb metals, forming this mixture into the required shape and dimensions and thereafter calcining the same, b) A process which comprises impregn~ting a carrier, made of a titanium oxide and reinforcing material and formed as required, with an active metal salt solution and thereafter calcining the same; and c) A process which comprises impregnating titanium oxide powder with an active metal salt solution, thereafter admixing the same with reinforcin&
material, forming as required, and then calcining.
The reinforcing material used herein comprises one or more materials selected from silica, alumina, clay and aluminosilicate. To keep the sctivity of this catalyst high, the amount of reinforcing material used should be limited to at most 30 wt.~ of the molding.
The catalysts according to the present invention may be manufactured, however, by any other process although that mentioned above is normally used in the preparation of such formed catslysts.
.. ~, .
~2:~6~3~
The hydrolysis of carbonyl sulfide using the catalyst according to the present invention is carried out at a temperature of 200 C or more. When a high temperature of 400 C or more is employed, however, the rate of reaction does not increase much. Therefore, it is preferable that the cntalyst according to the present invention be used at Q temperature range of 200 to The catalysts of the present invention are extremely effective for converting the carbonyl sulfide in gas into hydrogen sulfide by hydrGlysis, and their activity scarcely deteriorates in the presence of hydrogen sulfide, carbon dioxide and other compounds in the reaction system. Therefore, the catalysts of the present invention may be utilized in the treatment of not only the tail gas of the Claus method but also various carbonyl sulfide-containing exhaust gases, and are also effective for the hydrolysis of carbonyl sulfide contained in the gases with which reducing gases coexist, such as those resulting from coal gasification, petroleum cracking and the like. In view of the fact that the gases obtained by coal gasification normally contain dust in an amount of about several to ten-grams~Nm , it is preferable when treating these gases, that the catalysts have a shape capable of protecting the catalyst from abrasion and catalyst bed logging; for instance, a honeycomb shape or a shape as shown Fig. 1, is preferred.
Example 1 A 5 mm~ spherical titanium oxide carrier (TiO2 93 wt.%, SiO2 4 wt.%
and A~ 23 3 wt.~) was placed in a vessel equipped with a vacuum system and an impregnating liquid supply system, and decompressed for 20 minutes through said vacuum system. Next, a predetermined amount of impregnating liquid was sprayed 1 ~216838 on the titanium oxide carrier through said imPregnating li~uid supply system and was left standing for one night. Thereafter, the carrier was taken out therefrom, dried in a rotary dryer at 120C for 1 hour, and therea~ter calcined at 500C for 3 hours.
Thus, there was obtained as shown in Table 1.
Table 1 Active Active metal .
Name of metal contents (as Remarks *
Catalyst species oxide) wt.~
_ _ -A-l Ba 0.1 barium acetate
A CATALYST FOR USE IN HYDROLYSIS OF CARBONYL SULFIDE
BAC~GROUND OF THE INVENTION
The present invention relstes to a catalyst suitable for convertin~
carbonyl sulfide in ~as into hydrogen sulfide, in the presence of water vapor.
Since sulfur compounds in VQrious ~ases poison catalysts used in chemical processes or corrode the appsratus used, much effort has hitherto been made to remove such sulfur compounds. Generally, it is also necessQry to remove sulfur-compounds from effluent ~ases to reduce air pollution.
Of the sulfur compounds found in gases, H2S and SO2 are relatively easy to remove, and can be removed by dry methods, or wet methods such as alkali solution washin~, amine absorption, and the like. However, as carbonyl sulfide is difficult to remove effectively by wet methods, it is ordinarily converted into hydrogen sulfide according to the hydrolysis reaction noted below:
COS + H20 ~ H2S + C2 An example of convertin~ carbonyl sulfide in a ~as into hydro~en sulfide in the presence of water vapor can be observed when treatin~ the tail gas of the Claus method. In this case, the catalysts used are usually titanium oxide, as carrier, and oxides of transition metals such as iron, cobalt, nickel, molybdenum and the like as active in~redients. We have, found however that these catalysts mentioned above suffer severe deterioration in the presence of hydro~en sulfide. In view of the fact that the hydrolysis of carbonyl sulfide is unavoidably accompanied by the creation of 1' ~. ~7 , hydrogen sulfide, the deteriorstion in activity may be a fatal defect in the catalysts used in the hydrolysis of carbonyl sulfide.
SUMMARY OF THE INVENTION
The object of the present invention is to provide a catalytic composition for use in the hydrolysis of carbonyl sulfide whose activity scarcely deteriorates even in the presence of hydrogen sulfide. This catalyst is prepared by admixing titanium oxide snd reinforcing material with oxides of one or more metals selected from the group consisting of an alkaline metal such as Li, Na, K, Cs or the like, an alkaline earth metal such as Mg, Ca, Ba or the like, Group IIb metals such as Zn, Cd or the like and Group IVb metal such as Sa, Pb or the like in an amount of at least 0.5 wt.% of the final catalyst.
The catalyst comprises mainly titanium oxide and metal oxidets). The COS-hydrolysis activity of this catalyst increases with the amount of metal oxide present, but remains substantially level when the amount of 0.5 wt.~ or more is present. Further amounts of metal oxide shows no marked improvements in COS-hydrolysis activity. In view of this, the preferable amount of metal oxide is more than O.5 wt.~ and a practical upper limit is 10 wt.% from the economical point of view.
BRIEF DESCRIPTION OF THE DRAWINGS
Fig. 1 is a perspective view of a titanium oxide carrier used in Example 2.
Fig. 2 is a graph showing the activities of carbonyl sulfide hydrolysing activity of the catalysts according to the present invention. The conversion is plotted against the active metal contant of the catalyst.
~2~6~}3~3 Fig. 3 which appears on the first sheet of drswings, is B graph which compares the carbonyl sulfide hydroly~is activity of cstalysts according to the present invention with conventional catalysts. The conversion ~ is plotted against hours on stream.
DETAILED DESCRIPTION OF THE INVENTION
Processes for manufacturing the catalysts of the present invention include the following:
a) A process which comprises mixing a titQnic acid or titanate and reinforcing material with salts or oxides of active metals selected from said alkaline metals, alkaline earth metals, Group IIB metals and Group IVb metals, forming this mixture into the required shape and dimensions and thereafter calcining the same, b) A process which comprises impregn~ting a carrier, made of a titanium oxide and reinforcing material and formed as required, with an active metal salt solution and thereafter calcining the same; and c) A process which comprises impregnating titanium oxide powder with an active metal salt solution, thereafter admixing the same with reinforcin&
material, forming as required, and then calcining.
The reinforcing material used herein comprises one or more materials selected from silica, alumina, clay and aluminosilicate. To keep the sctivity of this catalyst high, the amount of reinforcing material used should be limited to at most 30 wt.~ of the molding.
The catalysts according to the present invention may be manufactured, however, by any other process although that mentioned above is normally used in the preparation of such formed catslysts.
.. ~, .
~2:~6~3~
The hydrolysis of carbonyl sulfide using the catalyst according to the present invention is carried out at a temperature of 200 C or more. When a high temperature of 400 C or more is employed, however, the rate of reaction does not increase much. Therefore, it is preferable that the cntalyst according to the present invention be used at Q temperature range of 200 to The catalysts of the present invention are extremely effective for converting the carbonyl sulfide in gas into hydrogen sulfide by hydrGlysis, and their activity scarcely deteriorates in the presence of hydrogen sulfide, carbon dioxide and other compounds in the reaction system. Therefore, the catalysts of the present invention may be utilized in the treatment of not only the tail gas of the Claus method but also various carbonyl sulfide-containing exhaust gases, and are also effective for the hydrolysis of carbonyl sulfide contained in the gases with which reducing gases coexist, such as those resulting from coal gasification, petroleum cracking and the like. In view of the fact that the gases obtained by coal gasification normally contain dust in an amount of about several to ten-grams~Nm , it is preferable when treating these gases, that the catalysts have a shape capable of protecting the catalyst from abrasion and catalyst bed logging; for instance, a honeycomb shape or a shape as shown Fig. 1, is preferred.
Example 1 A 5 mm~ spherical titanium oxide carrier (TiO2 93 wt.%, SiO2 4 wt.%
and A~ 23 3 wt.~) was placed in a vessel equipped with a vacuum system and an impregnating liquid supply system, and decompressed for 20 minutes through said vacuum system. Next, a predetermined amount of impregnating liquid was sprayed 1 ~216838 on the titanium oxide carrier through said imPregnating li~uid supply system and was left standing for one night. Thereafter, the carrier was taken out therefrom, dried in a rotary dryer at 120C for 1 hour, and therea~ter calcined at 500C for 3 hours.
Thus, there was obtained as shown in Table 1.
Table 1 Active Active metal .
Name of metal contents (as Remarks *
Catalyst species oxide) wt.~
_ _ -A-l Ba 0.1 barium acetate
2 Ba 0.5 ditto
3 Ba 1 ditto
4 Ba 4 ditto Ba 10 ditto 6 Ba 15 ditto G Ca 1 calcium acetate F Mg 0.5 magnesium nitrate H Zn 4 zinc acetate I Cd 1 B Li 4 lithium hydroxide C Na 3 sodium hydroxide IC Ba/Zn 2.5/2.5 barium acetate/zinc acetate L Ba/Pb 2.5/2 barium acetate/lead acetate M Zn/Pb 1.5/1.5 zinc acetate/lead acetate D K 3 potassium hydroxide E Cs 4 cesium nitrate ___ Sn 2 tin nitrate * denotes precursor of active metal species ~ ~216838 ¦Example 2 l A titanium oxide lattice-shaped carrier (monolith: TiO2 195 wt.%, SiO2 3 wt.~ and AQ2O3 2 wt.%) as shown in Fig. 1 (wherein, ¦d = 8.4 mm, t = 1.4 mm and W = 30.8 mm) was dipped into an aqueous ¦solution obtained by dissolving a predetermined amount of ¦precursory compound of an active metal species in 400 cc of ¦distilled water, and was left standing at room temperature (17C) ¦for 1 hour. Thereafter, the carrier was taken out of the aqueous ¦solution, and was dried for 12 hours while passing air through ¦ the lattice openin~ of the carrier. This carrier was then calcined at 500C for 3 hours. Thus, there was obtained a catalyst as shown in Table II.
Table II
Name of Active metal Contents (as oxlde) 1 ~.. t Experiment 1 A glass-made reactor (50 mm inside diameter and 400 mm length) was charged with a predetermined amount of Catalyst A-l, and the gas having a composition (COS 73 ppm, H2S 800 ppm, H2O 3%, N2 96.9~) was passed through the same. The initial COS hydrolysis activity of catalyst A-l was measured under the conditions of SV 7000 hr 1 and reaction temperature 350C.
~ 3a Following the same procedure, the titanium oxide carrier used in Example 1 and Catalysts A-2 to M were evaluated with reference to the initial COS hy~rolysis activity, and the -thus obtained results are as shown in Fig. 2.
Experiment 2 he reactor used in Experiment 1 was charged with a catalyst after the gaps between the inner wall of said reactor and the outside of a lattice-shaped catalyst had been filled up with ceramic fiber and sea sand. This catalyst was evaluated with reference to the COS hydrolysis activity at a reaction temperature of 400~C in accordance with the same procedure as Experiment 1.
Catalysts N to S were subjected to this evaluation.p~ocedure.
The obtained results are as shown in Table III.
Table III
..,..
Name of Shape Active metal COS conversion rate catalyst species (~) .. . _ ._ .... _ N lattice-shaped Mg (1) 71.1 O ditto Ca (1) 78.3 P ditto Ba (1) 82.0 Q ditto Zn (1) 88.5 R ditto Pb tl) 82.8 S ditto Ba/Zn(l/l) 90.2 Note) The numbers in round brackets denote the amounts of active metal species contained (wt.% as oxide) Experiment 3 For examining the effect of the components admixed with the COS-containing ~as on the COS hydrolysis, Catalyst T which comprise admixing a lattice-shaped titanium oxide carrier with 4 wt.~ of barium as oxide was placed in a reactor as in Example 2 ~ 15138 ¦and subjected to the same test procedure as Experiment 1 at a reaction -temperature of 400~C. The obtained results are as shown ~ . r~
~16~3 o ~,0 ~ 00 CO 1~ OD 1 O O Q O O O O O
.~ o o o o u~ ~ ~
-- N ~~ ~ ~ O ~ CO
Z ~ ~ ~ ~ ~o cr~ ~ OD
N o~I I ~ I ~ ~) ~ ~) C~ o', I I
_ _ ~ O ~ o\o I I I O O O O O
Q ~ ~
E~ 0~ o\ ~
. O ~ ~ 00 I I I I I I O
'Z ~ I ~ O
Ei o o o o o o O O I O O O O
~<~1 . co a) co oc~ oo OD
U~ ~
C~ ~ I~
_~ ~_ _.
X ~ O ~
_ ~Z
~ ~Z16~3~
From comparison of Experiments Nos. 1 to 3 of Table IV, -the activity of the catalyst of the present invention is shown barely influenced by the presence of hydrogen sulfide and carbon dioxide.
Likewise, from Experiment Nos. 4 and 5, it is found that the catalyst of the present invention can exhibit a superior activity even when reducing gases (CO and H2) and CO2 coexist. In this connection, it is to be noted that the raw gas used in Experiment No. 5 is of substantially the same composition as the gas obtained by the gasification of coal. The latter gas sometimes contains HCQ, NH3 and the like, but as is evident from comparison of Experiment Nos. 6 to 8, the catalyst of the present invention is entirely free from the influence of HCQ and NH
Experiment 4 Catalysts enumerated in Table V were obtained by repeating the exactly same procedure as Example 1.
Table V
Name of Active metal species (as oxide) wt.%
There catalysts were placed respectively in the same reactor as Example 1 and fed with the undermentioned gas of Composition [I] for hydrolysis under the conditions of reaction temperature 400C and SV 12900 hr 1. After 2 hours, the gas fed to the reactor was changed to the one undermentioned [II] for followup study of the changes in COS conversion with reaction time.
12~i838 The obtained results are shown in Fig. 3. In Fig. 3, it is to be noted that only in the case of Cntalyst Z, was the supply of gases reversed, namely, the gas of Composition (II) was first supplied, and then the gas of Composition ~I).
Table VI
Gas Composition [I] [II] .
COS 73 ppm 73 ppm 2 _ 800 ppm 2 3 % 3 %
N2 96.9 % 96.9 %
As shown in Fig. 3, the conversion rate of the catalysts of the present invention, A-4, B and H, lowered oniy about 1 to 5% even when the gas is admixed with H2S. In contrast, Control Catalysts Y and Z are influenced markedly by the presence of H2S, showing a 50 to 80% reduction in its activity.
Table II
Name of Active metal Contents (as oxlde) 1 ~.. t Experiment 1 A glass-made reactor (50 mm inside diameter and 400 mm length) was charged with a predetermined amount of Catalyst A-l, and the gas having a composition (COS 73 ppm, H2S 800 ppm, H2O 3%, N2 96.9~) was passed through the same. The initial COS hydrolysis activity of catalyst A-l was measured under the conditions of SV 7000 hr 1 and reaction temperature 350C.
~ 3a Following the same procedure, the titanium oxide carrier used in Example 1 and Catalysts A-2 to M were evaluated with reference to the initial COS hy~rolysis activity, and the -thus obtained results are as shown in Fig. 2.
Experiment 2 he reactor used in Experiment 1 was charged with a catalyst after the gaps between the inner wall of said reactor and the outside of a lattice-shaped catalyst had been filled up with ceramic fiber and sea sand. This catalyst was evaluated with reference to the COS hydrolysis activity at a reaction temperature of 400~C in accordance with the same procedure as Experiment 1.
Catalysts N to S were subjected to this evaluation.p~ocedure.
The obtained results are as shown in Table III.
Table III
..,..
Name of Shape Active metal COS conversion rate catalyst species (~) .. . _ ._ .... _ N lattice-shaped Mg (1) 71.1 O ditto Ca (1) 78.3 P ditto Ba (1) 82.0 Q ditto Zn (1) 88.5 R ditto Pb tl) 82.8 S ditto Ba/Zn(l/l) 90.2 Note) The numbers in round brackets denote the amounts of active metal species contained (wt.% as oxide) Experiment 3 For examining the effect of the components admixed with the COS-containing ~as on the COS hydrolysis, Catalyst T which comprise admixing a lattice-shaped titanium oxide carrier with 4 wt.~ of barium as oxide was placed in a reactor as in Example 2 ~ 15138 ¦and subjected to the same test procedure as Experiment 1 at a reaction -temperature of 400~C. The obtained results are as shown ~ . r~
~16~3 o ~,0 ~ 00 CO 1~ OD 1 O O Q O O O O O
.~ o o o o u~ ~ ~
-- N ~~ ~ ~ O ~ CO
Z ~ ~ ~ ~ ~o cr~ ~ OD
N o~I I ~ I ~ ~) ~ ~) C~ o', I I
_ _ ~ O ~ o\o I I I O O O O O
Q ~ ~
E~ 0~ o\ ~
. O ~ ~ 00 I I I I I I O
'Z ~ I ~ O
Ei o o o o o o O O I O O O O
~<~1 . co a) co oc~ oo OD
U~ ~
C~ ~ I~
_~ ~_ _.
X ~ O ~
_ ~Z
~ ~Z16~3~
From comparison of Experiments Nos. 1 to 3 of Table IV, -the activity of the catalyst of the present invention is shown barely influenced by the presence of hydrogen sulfide and carbon dioxide.
Likewise, from Experiment Nos. 4 and 5, it is found that the catalyst of the present invention can exhibit a superior activity even when reducing gases (CO and H2) and CO2 coexist. In this connection, it is to be noted that the raw gas used in Experiment No. 5 is of substantially the same composition as the gas obtained by the gasification of coal. The latter gas sometimes contains HCQ, NH3 and the like, but as is evident from comparison of Experiment Nos. 6 to 8, the catalyst of the present invention is entirely free from the influence of HCQ and NH
Experiment 4 Catalysts enumerated in Table V were obtained by repeating the exactly same procedure as Example 1.
Table V
Name of Active metal species (as oxide) wt.%
There catalysts were placed respectively in the same reactor as Example 1 and fed with the undermentioned gas of Composition [I] for hydrolysis under the conditions of reaction temperature 400C and SV 12900 hr 1. After 2 hours, the gas fed to the reactor was changed to the one undermentioned [II] for followup study of the changes in COS conversion with reaction time.
12~i838 The obtained results are shown in Fig. 3. In Fig. 3, it is to be noted that only in the case of Cntalyst Z, was the supply of gases reversed, namely, the gas of Composition (II) was first supplied, and then the gas of Composition ~I).
Table VI
Gas Composition [I] [II] .
COS 73 ppm 73 ppm 2 _ 800 ppm 2 3 % 3 %
N2 96.9 % 96.9 %
As shown in Fig. 3, the conversion rate of the catalysts of the present invention, A-4, B and H, lowered oniy about 1 to 5% even when the gas is admixed with H2S. In contrast, Control Catalysts Y and Z are influenced markedly by the presence of H2S, showing a 50 to 80% reduction in its activity.
Claims (6)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A catalyst composition for use in the hydrolysis of carbonyl sulfide to convert same into hydrogen sulfide, which consists essentially of a catalyst carrier made of titanium oxide and not more than 30 wt.% of a reinforcing material selected from the group consisting of silica, alumina, clay and aluminosilicates, said catalyst carrier having deposited on it from about 0.5 to about 10 wt.% of at least one oxide of a metal of Group IA or Group IIA of the Periodic chart of the Elements.
2. A catalyst composition for use in the hydrolysis of carbonyl sulfide to convert same into hydrogen sulfide, which consists essentially of a catalyst carrier made of titanium oxide and not more than 30 wt.% of a reinforcing material selected from the group consisting of silica, alumina, clay and aluminosilicates, said catalyst carrier having deposited on it from about 0.5 to about 10 wt.% of a mixture of oxides of two metals selected from the group consisting of (1) barium and zinc, (2) barium and lead and (3) zinc and lead.
3. A catalyst according to Claim 1 wherein said metal is lithium, sodium, potassium or cesium.
4. A catalyst according to Claim 1 wherein said metal is magnesium, calcium or barium.
5. A catalyst according to Claim 1 in which said oxide is lithium or sodium oxide.
6. A catalyst according to Claim 2 in which said mixture of oxides consists of a mixture of oxides of barium and zinc.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000439837A CA1216838A (en) | 1983-10-25 | 1983-10-27 | Catalyst for use in hydrolysis of carbonyl sulfide |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US06/545,406 US4511668A (en) | 1983-10-25 | 1983-10-25 | Catalyst for use in hydrolysis of carbonyl sulfide |
| CA000439837A CA1216838A (en) | 1983-10-25 | 1983-10-27 | Catalyst for use in hydrolysis of carbonyl sulfide |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1216838A true CA1216838A (en) | 1987-01-20 |
Family
ID=25670191
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000439837A Expired CA1216838A (en) | 1983-10-25 | 1983-10-27 | Catalyst for use in hydrolysis of carbonyl sulfide |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA1216838A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5511270A (en) * | 1994-10-26 | 1996-04-30 | Eliachar; Eliahu | Hair brush |
| CN111589450A (en) * | 2019-02-21 | 2020-08-28 | 中国石油天然气股份有限公司 | Carbonyl sulfide hydrolysis catalyst and preparation method thereof |
| CN114196448A (en) * | 2022-02-16 | 2022-03-18 | 北京中航天业科技有限公司 | Full-flow dry type blast furnace gas fine desulfurization system and method |
-
1983
- 1983-10-27 CA CA000439837A patent/CA1216838A/en not_active Expired
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5511270A (en) * | 1994-10-26 | 1996-04-30 | Eliachar; Eliahu | Hair brush |
| CN111589450A (en) * | 2019-02-21 | 2020-08-28 | 中国石油天然气股份有限公司 | Carbonyl sulfide hydrolysis catalyst and preparation method thereof |
| CN111589450B (en) * | 2019-02-21 | 2022-12-02 | 中国石油天然气股份有限公司 | Carbonyl sulfide hydrolysis catalyst and preparation method thereof |
| CN114196448A (en) * | 2022-02-16 | 2022-03-18 | 北京中航天业科技有限公司 | Full-flow dry type blast furnace gas fine desulfurization system and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4511668A (en) | Catalyst for use in hydrolysis of carbonyl sulfide | |
| US4174373A (en) | Process for removing sulfur oxides and nitrogen oxides from flue gases | |
| US3725531A (en) | Catalytic conversion of organic sulfur components of industrial off-gases | |
| US4427576A (en) | Catalyst for oxidation of hydrogen sulfide and/or organosulfur compounds to SO2 and process for preparing the catalyst | |
| US4191115A (en) | Carbonaceous fuel combustion with improved desulfurization | |
| NO167849B (en) | Catalyst for Nitrogen Reduction in Combustion Gases. | |
| CA2784700C (en) | Deactivation-resistant catalyst for selective catalytic reduction of nox | |
| US4138469A (en) | Process for catalytically treating exhaust gas containing NOx in the presence of ammonia gas | |
| US4141959A (en) | Process for removing nitrogen oxides from combustion flue gas | |
| CA2033215C (en) | Purification of sulphide-containing gases | |
| US4091076A (en) | Method of removing sulfur emissions from a fluidized-bed combustion process | |
| KR950009707B1 (en) | Catalyst and process for treating sulphur compounds containing gases | |
| CA1216838A (en) | Catalyst for use in hydrolysis of carbonyl sulfide | |
| CA2153748C (en) | Alumina-based catalyst for the treatment of gases containing sulphur compounds, use of these catalysts for the treatment and processes for treatment of the said gases | |
| GB2143225A (en) | Catalytic claus process for the oxidation of hydrogen sulphide to elemental sulphur and/or sulphur dioxide | |
| JPS6311053B2 (en) | ||
| JP4959927B2 (en) | Method for removing sulfur-containing compounds by direct oxidation | |
| US3981971A (en) | Process for reducing nitrogen oxides | |
| KR100272680B1 (en) | Catalysts suitable for removing sulfur compounds from industrial gases, methods for their preparation and their use | |
| CA1171846A (en) | Activated alumina claus catalyst and method | |
| US4244937A (en) | Sulfur dioxide oxidation catalyst and process | |
| US6019953A (en) | Process for gas incineration | |
| DK162596B (en) | PROCEDURE FOR THE PREPARATION OF Elemental Sulfur | |
| JPH01258746A (en) | Catalytic filter and production thereof | |
| CA2087265C (en) | Catalyst and process for removal of sulphur compounds and oxides from fluid streams |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |