Method of producing catalyst for oxidation purification of acid gas containing hydrogen sulfide

专利摘要:
This invention relates to catalytic chemistry, in particular to the preparation of a catalyst (QD) for the oxidation of an acid gas containing hydrogen sulphide, natural gas or gas from a refinery. The preparation of QDs, which allows purification of gas with a hydrogen sulfide content of 12 vol.% At 850 ° C and having a longer service life, is carried out using active alumina, partially or fully hydrothermally treated, and the addition of an additive as a carrier. Preparation of CT involves the formation of a carrier - active alumina, subjected to hydrothermal treatment, partially (by 30 wt.%) Or completely; nponHTky carrier catalytically active phase selected from oxides of at least one of the following metals: Ge, Cu, Ag, W, Co, Ni, Bi, Cg, Cd. In addition, at one of the above stages, 2-4% by weight of QD are additionally introduced to at least one of the rare earth metal oxides, barium, zirconium, silicon. It is better to prepare the carrier from active alumina by agglomerating the active powdered alumina of a poorly crystallized and / or amorphous structure, followed by hydrothermal treatment, or by conducting a hydrothermal treatment first. The molding of the carrier is carried out by mixing the active and alumina subjected and not subjected to hydrothermal treatment by the method of extrusion (oil drops). The content of the catalytically active phase is preferably 5-10% by weight. Test CT in the oxidation of the gas of the following composition, vol.%: 12.0; 0 6.0; WITH 45.0; 7.0; Nj the rest at 850 ° C and a space velocity of 900 initially shows a sulfur yield of 58%, and after 100 hours of QT operation, a decrease to 5 2-55% (against 34% in the known case). 4 hp ff, 2 tab. § SL
公开号:SU1322969A3
申请号:SU843699151
申请日:1984-01-27
公开日:1987-07-07
发明作者:Дюпен Тьерри
申请人:Рон-Пуленк Спесьялитэ Шимик (Фирма)；
IPC主号:

专利说明:

I 1
The invention relates to a method for producing a catalyst by oxidizing a molten gas containing hydrogen or natural gas or gas from a refinery plant.
The aim of the invention is to obtain a catalyst allowing the gas to be purified.
with a hydrogen sulphide content of 12% by volume at 850 C n with an increased — service life due to the use of active alumina subjected to hydrothermal treatment, partially or completely, as a carrier and due to cc (for one of the compounds of the preparation of of the amount specified in F.


Example (comparative). As the initial t-linozem, an activated glannous of poorly crystallized and / or amorphous structure is used, obtained by the rapid dehydration of hydrargillite in a stream of hot gases with an inlet temperature of approximately 800 ° C and a contact time of approximately 0.5 s.
After grinding, this powder is agglomerated in the form of balls with the aid of rotating the drum. Powder and water are simultaneously introduced into the rotating drum with this chain. The images of the balls are continuously selected by the method of ejection due to centrifugal force.
After drying with PO C, the balls are calcined in air at 800 ° C. Thus, a support is obtained from active alumina without hydrothermal treatment.
100 g of alumina balls are impregnated with 45 cm of iron nitrate (IT) solution containing 5 g of iron. Catalyst obtained; after drying and calcined 1P1 at 800 ° C, it contains 5% by weight of the catalytically active phase in the form of iron oxide (HI), alumina is the rest. Kata properties
The lysator is as follows: specific surface area (R1) 105 m; bulk density (refinery) 0.79; total pore volume (SOP) 0.45; The alumina carrier used in this example was not subjected to hydrothermal treatment, and no compounds selected from oxides of rare earth metals, alkaline earth metals were introduced into it.
0
five
0
five
Q zirconia, silica or their precursors.
PRI mme R 2. Aluminum hydroxide balls are thermally processed as follows: 4 kg of aluminum hydroxide balls are treated in the vapor phase at 195 ° C for 3 hours. The medium in which they are treated is formed by a mixture of acetic acid containing 10 g per 100 g , and nitric acid containing 7 g per 100 g of ACO ,. Nitric acid can dissolve about 2.5% by weight of aluminum hydroxide beads. Acetic acid carries an anion adatate, which combines with aluminum ions in solution to form compounds in which the atomic ratio of CH COO / A1 is below 3. Thus, the treated balls are thermoactivated in an oven at 900 ° C for 1 hour. Then 100 g of alumina balls,
Some impregnate 97 cm of a solution of ferrous nitrate containing 5 g of iron, lanthanum nitrate containing 1 g of lanthanum, and neodymium nitrate containing I g of neodymium.
After scrubbing and calcining in air at 800 ° C, the catalyst has the following composition, in wt.%: 5; La ,, 0, 1; Nd /), 1; 93
The catalyst has the following properties: UP 103 refinery
0.46 g / cm; SOP 0.97 cm / g. 5 All the alumina contained in the used active alumina carrier was subjected to hydrothermal treatment.
0
five
0
EXAMPLE 3 A carrier was prepared, consisting of balls of active alumina, subjected and not subjected to hydrothermal treatment.
The first source of alumina is a sol of ultrafine alumina obtained by the method of oil droplets, i.e. the aluminum hydroxide sol is subjected to hydrothermal treatment: 50 g of slightly crystallizing active hydroxide are introduced into an autoclave containing 1 l of an aqueous solution of an equimolar mixture of nitric acid and ammonium nitrate, having a pH of 1.15, while
N0, the molar ratio -tg --- will be
5Al-z i
equal to 0.3. The contents of the autoclave are mixed. It is then heated.
ABOUT
within 24 hours at 150 ° C. An aluminum hydroxide suspension is obtained, containing ultrathin boron in plate form, having a conversion degree of about 50%.
The specific surface of the substance obtained after drying the suspension in a drying chamber at 11 ° C for 3 hours is 200. In this case, it is aluminum hydroxide with a poorly crystalline structure and / or an amorphous structure after hydrothermal treatment.
The second active alumina, used as spheroidal particles, is not subjected to hydrothermal treatment.
These two sources of alumina are mixed with water and the pH is adjusted to 6. The weight ratio o6 oirx of the sources of alumina is 30% for the first and 70% for the second, based on.
After dehydration, drying and calcination, balls are obtained, which are processed as follows.
100 g of alumina beads are used, which are impregnated with 97 cm of an alcohol solution of ethyl silicate containing 2 g of SiO, then after
-ABOUT
drying and calcination at 500 ° C carried out the impregnation of 97 cm of copper nitrate solution containing 2 g of copper with a solution of silver nitrate containing 2 g of silver. After drying and calcination at 800 ° C, the catalyst has the following composition, wt%: SiO 2; CuO 2; Ap, 0 3; 93
The properties of the catalyst obtained are the following: PN 137 PNZ 0.47 SOP 0.97.
30% of the alumina constituting the active alumina carrier is hydrothermally treated.
EXAMPLE 4 Ultrathin alumina 2 is used, which is obtained by hydrothermal processing of powdered active alumina of poorly crystallized and / or amorphous structure.
Conditions of hydrothermal treatment are identical to those specified in example 3.
100 g of the obtained alumina is stirred in the presence of water. To the resulting paste was added 10 g of fine iron oxide powder. The extrudate mixture thus obtained is dried and calcined at 600 ° C. Then the catalyst mass is impregnated with a barium nitrate solution containing 2.5 g barium. After
drying and calcining at 800 ° C. The catalyst has the following composition, in May,% BaO 2.5; 10.0; 87.5.
The catalyst has the following characteristics: UE 119; Oil Refinery 0.65 g / cm; SOP 0.61 cm / g.
 The entire amount of alumina constituting the used activated alumina carrier was subjected to hydrothermal treatment.
Example5. 100 g of alumina balls used in Example 2 are impregnated with one 98 cm of a solution of zirconium oxychloride containing 4.0% by weight of zirconia. After drying and calcining at 800 ° C, the resulting product is passed through 98 cm of a solution of chromic acid containing 5 g of chromium. After suppi and calcination at 800 ° C, a catalyst of the following composition was obtained; wt.%: Zr024,0; Cr, 0c 5.0; 91.0.
The properties of the catalyst are as follows: UP 99; Refinery 0.47 g / cm; SOP 0.98 cm / g.
All the alumina constituting the active alumina carrier used was subjected to a hydrothermal treatment.
EXAMPLE 6 A series of catalysts is prepared, starting from a carrier of active alumina described in Example 2 and containing 2.2% lanthanum oxide, introduced by impregnation with a solution of lanthanum nitrate, drying and calcining at 700 s.
These catalysts are obtained by impregnation with a solution, containing precursors of the active phase. The composition and properties of the catalysts obtained after drying and calcining in air at 800 ° C; in table.1.
PRI me R 7. In the laboratory reactor serves the gas of the following composition,%: HjS 1., 0; 0 6.0; C (45.0; P., 0; 7.0; N ,, 30.0.
Solution temperature at isotherm
In operation, it is 850 ° C, and the gas velocity is such that the ground speed per foot 7JHN conditions is 900 hours.
Catalysts are compared by measuring the activity of hydrogen sulfide conversion in relation to the output from the catalytic reactor after 8 hours and, after 100 hours of operation, and determining the yield of the sulfur produced.
The results are shown in table 2.

权利要求:
Claims (5)
[1]
1. A method for producing a catalyst for purification by oxidation of an acid gas containing hydrogen sulfide, comprising molding a support containing alumina and impregnating the support with a catalytically active phase selected from oxides of at least one of the following metals: iron, copper, silver, tungsten, cobalt, nickel, bismuth, chromium, cadmium, characterized in that, in order to obtain a catalyst that allows
purify the gas with a hydrogen sulfide content of 12 vol.% at 850 ° C and with a long service life, active alumina is used as carrier, subjected to hydrothermal treatment partially with 30 wt.% or completely, and in one of the above stages 2- 4% by weight of the catalyst, at least one compound selected from the group consisting of rare earth oxides, barium oxide, zirconia, silica.
ten
5 5
20
25
[2]
2. The method according to claim 1, characterized by the fact that the carrier of active alumina is prepared by agglomerating the active powdered alumina of poorly crystallized and / or amorphous structure, followed by hydrothermal treatment.
[3]
3. Method POP.1, characterized in that the active powdered alumina of a poorly crystallized and / or amorphous structure is first subjected to hydrothermal treatment, and then a carrier is formed.
[4]
4. A method according to claim 3, characterized in that the molding is carried out by mixing the active alumina subjected to hydrothermal treatment with the active alumina, is not subjected to hydrothermal processing, and the molding is carried out by extrusion or by the method of oil droplets.
[5]
5. Method pop. 1, differing ayu sch and with the fact that the content of the catalytically active phase is 5-10 wt.%.
Table 1
9
01
95
96
103
0.47
0.46 0.46 0.47
0.46
95
96
96
94
96
1 editor G. Volkov
Compiled by V.Teplov Kova Tehred L. Serdyukova
Order 2881/58 Circulation 510 Subscription
VNIIPI USSR State Committee
for inventions and discoveries 113035, Moscow, Zh-35, Raushsk nab., 4/5
Production and printing company, Uzhgorod, Projecto st., 4
Table 2
Proofreader L. Pilipenko

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法律状态:

优先权:

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申请号 | 申请日 | 专利标题

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FR8301426A|FR2540006B1|1983-01-31|1983-01-31|HYDROGEN SULPHIDE OXIDATION CATALYST|

---