SU552017A3 - The method of obtaining elemental sulfur - Google Patents

Description

Sashysh temperature jumps n contributes to the smooth flow of the rcaktski.

The amount of sulfur introduced is 0.05-3 mol%, preferably 0.1-1.S MOin.%.

The process is carried out in any of the well-known catalysts that are suitable for the reduction of sulfur dioxide, such as bauxite, alkoxydia, biconcrash, calcium sulphide, vanadium oxide, alumina or their mixtures. Ilptt this catalyst in the type of sharpened 6.35 19, 05 mm. Continued 1; gsos; p-koshaktak10,1 - 7 seconds, tf "preferably 0.25 -t. 3.5 seconds. When l is less than 0.1 seconds, the degree of aversion {w is the indicator, while the duration of contact is more than 7 seconds, and it provides 1 scale of property.

Reduced sulfur dioxide can be pure or in the form of exhaust gases with the content of SO) from 1 to 100%.

The molar ratio between the sulfur dioxide reagents / reducing gas should be 1.33 - 6.5: 1, depending on the reducing gas used. For example, when using butane, the ratio of sulfur dioxide to butane is 4.5–6.5: 1, and when it is used, methane is 133–2: 1. The maximum number of asholues & hydrocarbon-gas gases is escaped into ashhuns.

In the production of suction gas, there are traces of bladder cancer and sulfur dioxide, which are two

And only an orsh reactor for reconditioned, installed in front of the Yushus re-enforcer, the servicemen at the hospital, npeepweBWti {jS n {"(7T" TByiniien) in the product gas in a major amount of operational | due to reyushi OvSOj. -:

Productive. gases, in the "| c1 (rd) ne zone of recovery; the capacitor for sulfur is passed through - then aociynaiOT 9 .o & klaus is the best converter. At the same time, a part of the prod uct gas may be put on recirculation to feed it into.

initial reaction mixture.

Examples 1-3. A series of experiments in which a gas containing SO with different concentrations interacts with methane in the presence of a catalyst was carried out, which was

calcium aluxate on a carrier - oyuk alyuiints. The results obtained are given in table. 1-2. The amount of sulfur introduced into the reduction zone in examples 1-3 is 1 mol% in terms of Sg, h1p corresponds to the

mixtures of elemental sulfur found in forms 52.8bI58.

Table 1

odable SOz

CH4

Era in terms of Si 5b

S8

Lzot

Product SOi

CH4

HI o COS

WITH CSi H, S

H, CO, Sulfur

 The temperature at the entrance to the reactor in all examples is 537 ° the temperature at the outlet of the reactor in example 1-953 °; in example 2-663 °; in example 3 - 1064 °

9.16

57.93

30.16 4.66

8.28 13.73

3.73

3.73 0.02 0.02

0.03 0.03

3.77 68.75 7.19

2.66 0.0067

53.43

1.32 17.52 0.386 0.039, 397 3.302 0.003

1,486 0,020 0,001, 001 5,431 5,220 11,337 3,545

1,772

0,084 26,326 8,131 4,588 1,374 19.00 4.383

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Claims (2)

o o o o o o o o o rf i7 Example 1 Supplement of an actor in actor is a coventryr gas & a gas gas containing sulfur dioxide in the amount of 87.5 and 12.5% of water to which the methane ratio is obtained for the molar ratio of the oxygen ratio sulfur t methane equal to 1.93: 1. In example 3, the concentration of dioxide dioxide in the feed gas is 10 mol% and molar. the ratio between sulfur dioxide and methane is 1.97: 1. As follows from the data presented in these tables, the initial reduction reaction in Examples 1 to 2 is natanat at 537 ° C and the reaction is completed with an actual residence time in the equipment of 0.55 n 2.5 s, respectively, which is determined mainly by but full use of methane. & In the example, the reaction proceeds smoothly to completion within 0.55 seconds and the distribution of product gas is a composition that corresponds to thermodynamic equilibrium at a temperature at the outlet of the reactor equal to 953 ° C. It has been established that a slight improvement in the use of methane, i.e. a decrease in residual carbon monoxide and hydrogen, can be achieved by introducing part of the unheated reagents, i.e. sulfur dioxide and methane, into the intermediate zone in the catalyst bed. This lowers the temperature at the outlet of the reactor and shifts the equilibrium state towards the lower end of the growth of carbon monoxide and hydrogen. Example 2 is similar to Example 1, except that the gas containing sulfur dioxide has a sulfur dioxide concentration of about 10 mol%, & the actual residence time in the apparatus for the full utilization of methane is 2.5 seconds. The composition of the product gas is qualitative, since the concentrations of carbon disulfide, 1L carbonyl sulphide, hydrogen and carbon monoxide are negligible. Example 3 is given in order to show the benefits arising from the introduction of sulfur into the reduction zone. The composition of the feed gas is the same as in Example 1. The temperature at the inlet to the reactor is raised to 750 ° C. Without the addition of sulfur, an ITO temperature at the entrance to the p @ 8K1Or will be increased to this level fom yr, so that the reaction can reach a high reaction rate. The jersey of three 732 ° C, the reaction proceeds very much during the first 0.5 seconds, only 0.18 mol of methane is required, and after approximately 0.8 seconds of duration, when the temperature of the gas is 827 ° C, the reaction reaches completion almost instantaneously, which indicates that the reaction’s extreme harshness, naturally) increases the temperature in the reactor and is 242 ° C, i.e. from 827 to 1064 ° C for 0.5 sec. In that case, if sulfur is converted and gas is used, concentrations of sulfur dioxide in concentrations, for example, sulfur dioxide contents of about 1-16 mol%, the reduction reaction proceeds more smoothly than when using more concentrated gases, but it is required that Initiation was 787 - 815 ° C. Claim 1. The method of obtaining elemental sulfur by reducing or sulfur dioxide by hydrocarbon gas, such as methane, at elevated temperatures in the presence of a catalyst, characterized in that After initiation and stabilization of the process, vaporized elemental sulfur in an amount of 0.05 -3 mol% in terms of Si2 is introduced into the reaction zone. The method according to claim 1, characterized in that the process is carried out at 454 - 1316 ° C. 3. A method according to claim 1, characterized in that the ratio between sulfur dioxide and hydrocarbon gas is 1.35 - 6.5: 1, preferably 1.33 - 2.0: 1. 4. A method according to claim 1, characterized in that a portion of the feed mixture is supplied to the medium catalyst bed. Sources of information taken into account in the examination; 1. US patent number 2270427, class. 23-260, 1938 2. US patent N 3199955, cl. 23-226, 1963