JPS63501562A - Method for removing sulfur compounds contained in residual gas - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

[Detailed description of the invention] A method for removing sulfur compounds contained in residual gas The present invention is particularly applicable to the CLAUS sulfur process. A method for removing sulfur compounds contained in residual gas discharged from the field. Concerning the law. In this method, the sulfur compounds are recovered in the form of sulfur.

For partial oxidation treatment of acidic gas containing H and S, known as the CLAUS method. Therefore, the residual gas emitted from a sulfur factory that manufactures sulfur is approximately 0.2 to 2 volumes. % of sulfur compounds and vaporous and/or cellular sulfur. The size of these sulfur compounds A portion consists of H2S, and the rest consists of SO, CS2, and COS.

Such residual gases typically comply with standards imposed by air pollution laws. The total sulfur compound content is kept as low as possible so that it can be released into the atmosphere after incineration while protecting At the same time, these sulfur compounds are treated in sulfur factories to provide acidity. It will be processed for recovery in this form.

Developed by the applicant to treat residual gas from CLAUS sulfur plants The known method is to cool the residual gas to a temperature below 160° C. Sulfur is formed by the reaction of H2S and 802 in contact with a catalyst, and the sulfur-containing C The LAUS catalyst is periodically scavenged with non-oxidizing working gas at a temperature of 200°C to 500°C. The sulfur retained on the catalyst is evaporated, thereby regenerating the catalyst, and this regeneration is then performed. by cooling the fresh catalyst to the temperature necessary to bring it into new contact with the residual gas. Become. The catalyst is operated at a sufficiently low temperature so that the sulfur generated is retained in the catalyst. function. Further, the catalyst cooling treatment is carried out using an inert gas at a temperature of less than 160°C. The cooling gas contains at least the amount of water vapor at the end of its use.

Standards imposed by laws regarding air pollution caused by sulfur compounds are becoming increasingly strict. Therefore, in order to address these criteria, the applicant has made improvements to the aforementioned method.

The present invention relates to this improvement. This improved method eliminates the presence of residual gas in In addition, the sulfur organic compounds not recovered by the above-mentioned known methods can be sufficiently recovered. and the sulfur yield of the reaction of H2S and S02 by contact with CLAUS catalyst. Improve.

As a result, the overall recovery rate of sulfur compounds contained in the residual gas is improved and the associated Consequently, the total concentration of sulfur products discharged into the atmosphere will be further reduced.

It is an object of the present invention to remove residual gases such as those from CLAUS sulfur plants. A more complete method for removing sulfur compounds contained in This is associated with the recovered amount, and is derived from residual gas and contains H2S and 502 below 160℃ The gas stream is contacted with a CLAUS catalyst to form sulfur by reaction with H2S and SO□. The catalyst is heated at a sufficiently low temperature so that the sulfur generated is retained in the catalyst. functioning at a temperature of 100% and then emitting purified residual gas with an extremely low content of sulfur compounds, The sulfur-retaining CLAUS catalyst was heated to a non-oxidizing gas at a temperature of 200°C to 500’C. The sulfur retained on the catalyst is evaporated by periodic scavenging with a and then convert the regenerated catalyst into H,S using an inert gas at a temperature below 160°C. and from cooling to the temperature required for new contact with the S02-containing gas. and the cooling gas contains water vapor at least during the final stages of its use. is preferred, and the gas to be brought into contact with the CLAUS catalyst is discharged from a sulfur plant. Hydrogenation of residual gas to unify the sulfur compounds contained in it into H and S forms and hydrolysis, and then the gaseous emissions resulting from said treatment. is cooled to a moisture content of approximately 10% by volume and adjusted to this low moisture gas output. Add 1lfi oxygen-containing gas and oxidize it with H2S at a temperature higher than 150℃. in contact with a catalyst to produce a controlled oxidation of H2S and to reduce H2S and SO to approximately 2: generating a gas stream containing elemental sulfur in a molar ratio of 1, with the proviso that said molar ratio is By continuously adjusting the flow rate of free oxygen-containing gas added to the low-moisture gaseous effluent. The gas stream resulting from the oxidation reaction is then cooled to 160°. temperature below C, so that most of the sulfur contained in this gas is separated by condensation. The present invention provides a method characterized in that: It's there.

The operation of subjecting the residual gas to a combination of hydrogenation and hydrolysis usually requires the presence of a catalyst. During this operation, S02, CS2, CO contained in the residual gas Sulfur compounds such as S and vaporous and/or cellular sulfur are converted to H2S.

This conversion is carried out under the action of S02 and, in the case of vaporous and/or cellular sulfur, hydrogen. In the case of CO3 and C82, hydrolysis occurs due to the action of water vapor present in the residual gas. Implemented by solution. A combined hydrogenation and hydrolysis process in the presence of a catalyst. The temperature can reach about 140°C to 550°C, preferably about 200°C to 400°C. Perform at temperature. The hydrogen necessary for the hydrogenation reaction is extracted from the hydrogen already contained in the residual gas. or if the residual gas contains e.g. CO and H2O. May be generated in situ in the hydrogenation and hydrolysis zone by reaction with H2O. H2 and hydrogen may be added to the residual gas from an external hydrogen source, or from an external hydrogen source. One advantageous method of supplying CO and CO is by using fuel gas bars that operate at substoichiometric levels. the combustion gas produced by the burner to the residual gas. use The amount of hydrogen is S contained in the residual gas subjected to hydrogenation/hydrolysis treatment and can be hydrogenated. Nearly complete removal of sulfur compounds or products such as Ox, vaporous and/or cellular sulfur It is necessary to make it sufficient to convert it into H and S. used in actual operation The amount of hydrogen required for the conversion of the hydrogenatable sulfur products present in the residual gas to H2S The amount can be increased from 1 to 6 times the stoichiometric amount.

Residual gas combined? 5 Sufficient amount of water required for hydrolysis of COS and CS2 If it does not contain steam, the necessary The required amount of water vapor can be added to the residual gas.

Catalysts that can be used for hydrogenation/hydrolysis include Group Va and Group Va of the Periodic Table of Elements. Metals of group Ha and group Vll, such as cobalt, molybdenum, chromium, and vana. Compounds of metals such as dium, thorium, nickel, tungsten, and uranium Examples include those containing. The above compounds include silica, alumina, silica/alumina It may or may not be placed on a support of the type. placed on alumina Hydrodesulfurization catalysts based on cobalt oxide and molybdenum oxide can Particularly effective in hydrolysis treatment. In this hydrogenation/hydrolysis process, the gaseous reaction medium The contact time with the catalyst can be varied within a fairly wide range. This contact time is normal advantageously 0.5 to 8 seconds, more particularly 1 to 5 seconds under pressure and temperature conditions of Ru.

Gaseous emissions resulting from subjecting the residual gas to a combined hydrogenation/hydrolysis treatment are optional. techniques known in the art, e.g. by indirect heat exchange with cooler fluids and/or water spraying. Cooling to bring the temperature low enough that most of the water contained in it condenses and becomes water-containing. A reduced moisture content of 10% by volume is allowed to form in the open gaseous discharge.

The low-moisture gaseous effluent thus obtained is then used to cause oxidation of H2S. Reheat to a temperature compatible with the required temperature. This heat treatment is particularly effective due to condensation. carried out by indirect heat exchange with the hot gaseous effluent which is cooled to separate the water. obtain. The required amount of free oxygen-containing gas is then added to this effluent. This addition operation contacting said low-moisture gaseous effluent with an oxidation catalyst operating at a temperature higher than 150°C; or preferably before this contacting treatment.

The free oxygen-containing gas used to oxidize the H2S contained in the gaseous effluent is usually However, pure oxygen, air with a high oxygen content, or inert gases other than nitrogen and oxygen It is also possible to use mixtures of in various proportions. Free oxygen-containing gases are as described above. <, containing H, S and S02 in a H2S:S02 molar ratio equal to a molar ratio of about 2:1 ) H2S is partially oxidized to form a gas stream containing to some extent the elemental sulfur. The amount of oxygen used is adjusted to provide the minimum amount of oxygen needed to It will be done.

The amount of free oxygen-containing gas can be adjusted by any known method, e.g. by controlling the gas flow resulting from oxidation. The values of the H2S:SO□ molar ratio were measured and calculated based on the results of these measurements. The flow rate of the free oxygen-containing gas used for oxidation is changed depending on the required amount. This is carried out in such a way that the H2S:S02 molar ratio is maintained at a value of 2:1. .

The contact time between the gaseous reaction medium and the oxidation catalyst is between 0.5 and 1 at normal pressure and temperature conditions. It can be set to 0 seconds.

The oxidation catalyst is CLAUS oxidation of H2S with a stoichiometric amount of oxygen, i.e. the following reaction formula: %formula% One can choose among a variety of catalysts that can promote oxidation according to.

This reaction combines H2S and SO□ in addition to the sulfur element in a ratio of H,S:S approximately equal to 2:1. A gas stream containing 0.02 molar ratio is generated.

In particular, the oxidation catalyst that can be used in the process of the invention is advantageously selected from the group: It is possible.

1) At least one metal selected from among Fe, Ni, Co, Cu, and Zn A catalyst comprising a combination of various compounds and a support made of silica and/or alumina.

French Patent No. 7,531,769 dated October 17, 1975 (Publication No. 2, 3 No. 27,960).

II) Catalysts based on titanium oxide, especially titanium oxide and alkaline earth metals In combination with sulfates, e.g. calcium sulfate. Dated March 13, 1981 Disclosed in French Patent No. 81.05029 (Publication No. 2.501532).

III) Fe, Cu, Cd, Zn, Cr, Mo, 'A, Co, at least one compound of a metal selected from Ni and Bi, and optionally Therefore, at least one compound of noble metals such as Pd, PL, Ir and Rh catalyst in combination with a support consisting of silica and/or titanium oxide. Said support may optionally contain small amounts of alumina. French Patent No. 811 dated August 19, 1981 Disclosed in No. 5900 (Publication No. 2,511,663).

IV) At least one compound of metals selected from the group listed in III) materials and especially thermally stabilized by at least one rare earth oxide A catalyst formed in combination with a support made of modified alumina. German Patent Publication No. 3. Disclosed in No. 403,328.

The oxidation catalyst advantageously comprises a type II catalyst and a type II, III or IV catalyst. The advantage of continued use of Fuchsei is that the gas flow resulting from oxidation no longer contains oxygen. You can choose not to include it.

This is necessary to avoid deactivation of the CLAUS catalyst in later stages of processing. Ru.

CLAUS stoichiometric picture TenoH2Scl') The oxidation reaction takes place at a temperature of 150°C to 1000°C. The oxidation catalyst is selected from among catalysts that exhibit sufficient thermal stability at the holding temperature. do. For example, type I) catalysts can be used up to about 400°C, and type TI) catalysts up to about 500°C, type III) up to about 700°C, type IV ) can be used up to about 1000°C.

The gas stream resulting from the oxidation process contains vaporous sulfur and also contains H2S and SO□. In a molar ratio equal to about 2:1. This gas stream is transferred to a condenser such as a sulfur condenser. cooling to a value below 160°C, so that the Allow most of the sulfur to be separated by condensation and then contact the CLAUS catalyst let This catalyst has a structure in which sulfur produced by the reaction between I(2S and 302) is deposited on it. Works at temperatures low enough to be deposited. This temperature is advantageously between about 120°C and 14°C. It is 0°C.

The refining residual gas that results from contact with the CLAUS catalyst is typically vented to the atmosphere. Convert any sulfur compounds that may still be present in very small amounts to SO□ before It is subjected to thermal incineration or catalytic incineration in order to convert it.

The sulfur-containing CLAtlS catalyst is heated at 2 to evaporate the sulfur retained on the catalyst. Periodically regenerated by scavenging with non-oxidizing working gas at temperatures between 00°C and 500°C The regenerated catalyst is exposed to the necessary temperature for new contact with the gas stream resulting from oxidation. Cool to ℃. This cooling is carried out using an inert gas at a temperature below 160°C. The cooling gas advantageously retains at least the amount of water vapor in the final stage of the catalyst cooling process. Ru.

The scavenging gases used to regenerate the sulfur-containing CLAUS catalyst are methane, nitrogen, and CO. 2, or a mixture of these gases, or a refining residual gas to be incinerated. or a portion of the residual gas to be treated. This scavenging gas Reducing gaseous compounds such as H2, CO and especially H2S are at least regenerated. during the final stage of the process, i.e. after most of the sulfur deposited on the catalyst has evaporated. , for example 0.5 to 25% by volume.

Contacting the gas stream resulting from the oxidation process with the CLAIJS catalyst typically involves multiple steps. carried out in a catalytic conversion zone. These zones must be played by at least one zone. / functions in the cooling stage and the rest is used to function in the CLAUS reaction stage .

Alternatively, more than one zone is used for the CLΔUS reaction, and at least one operation with one zone used for the regeneration stage and at least one zone used for cooling. Can also be done.

CLAUS catalyst reacts between H2S and SO□, i.e. reaction 2 below: H2S+5O2 -〉3/x　SX+2120ku- Any catalyst that can promote sulfur formation by.

For example, the CLA[IS catalyst may be bauxite, alumina, silica, natural or is a synthetic zeolite, a catalyst of the type I) mentioned above, or a mixture of these substances or can be composed of combinations.

The regeneration gas preferably passes sequentially from the heating zone through the regeneration zone and the cooling zone. In this cooling zone, most of the sulfur contained in the gas is separated by condensation, It then circulates in a closed circuit back to the heating zone. This regeneration gas is of course open circuit. It may be circulated like this.

The gas used to cool the regenerated catalyst is used to regenerate the sulfur-containing catalyst. It is the same type of gas, that is, it is a nearly inert gas. Regeneration gas and cooling gas circuit may be independent of each other. A regeneration gas circuit as described above connects the cooling zone outlet and the regeneration gas circuit. It may have a branch connecting the inlet/inlet of the live zone bypassing the heating zone. this This allows the regeneration gas to be used as a cooling gas without passing through the heating zone. It becomes possible to use

As previously mentioned, the cooling gas is more specific during at least the final stages of the regenerated catalyst cooling process. Quantitatively, when the temperature of the regenerated catalyst during cooling becomes lower than about 250℃, it will contain water vapor. obtain. However, this regeneration gas may contain water vapor from the beginning of the regeneration catalyst cooling process. cold The amount of water vapor that the cooling gas may contain can vary quite widely, e.g. from 1 to 50% by volume. could be.

In order to explain the method of the present invention described above in more detail, non-limiting examples are provided below. List.

1 round box 60.4% by volume of H2S, 36.3% by volume of CO2, 3.2% by volume of water, Emitted from a sulfur plant that performs partial oxidation of acid gases containing 0.1% by volume of hydrocarbons. The remaining gas was treated.

The treated residual gas had the following composition expressed in mole %.

H2S: 0.80 SO□: 0.40 S+ (steam): 0.08 CO□: 16.65 1 (20: 29.80 CO: 0.52 COS: 0.02 cs2: o, os This treatment was carried out using an apparatus consisting of the following members.

- A burner that burns fuel gas with air, which guides the residual gas to be treated. a burner having a substoichiometric inlet and an outlet; Inlet and outlet separated from each other by a fixed bed of monohydrogenation and hydrolysis catalysts hydrogenation and hydration, the inlet of which is connected to the outlet of said burner through a pipe a cracking reactor, - a first exchange circuit of an indirect heat exchanger, a low pressure steam generation heat exchanger and an air Air cooler (a&ror&frig&rant) and an outlet for liquid at the bottom and an outlet at the top. A cooling assembly comprising in series a water spray column with an outlet for a gas, said The inlet of the first exchange circuit is connected to the outlet of the hydrogenation and hydrolysis reactor via a pipe. assembly, - Inlet and outlet separated from each other by a fixed bed of catalyst that oxidizes 82S to sulfur. a catalytic oxidation reactor having an opening, one opening for heat exchange of the cooling assembly; connected to the upper outlet of said water spray column by an inlet pipe through a second exchange circuit of the vessel. On the other hand, a pipe extends beyond the outlet, and a sulfur condenser is disposed on this pipe, and a sulfur condenser is arranged on the pipe. The tube includes an air inlet located downstream of the heat exchanger and a variable flow I valve, the valve being Controlled by a regulator that adjusts the molar ratio H,S:SO2 at the outlet of the oxidation reactor catalytic oxidation reactor, such as one placed in parallel with each other and each with a fixed bed of CLAtlS catalysts. A catalytic converter train consisting of two catalytic converters with separate inlets and outlets.

These two converters are connected via clock-switched valves, one to the reaction stage. the inlet is connected to the outlet of a sulfur condenser connected to the catalytic oxidation reactor; One outlet is connected to the incinerator inlet and the other is placed in the regeneration/cooling stage. i.e. first placed in the regeneration circuit and then placed in the cooling circuit. It operates alternately. Note that non-oxidizing scavenging gas is supplied to the regeneration circuit via the converter. Provide means for circulating the sulfur from the heater to the sulfur condenser and back to the heater. and the cooling circuit circulates a low temperature inert gas through a converter disposed in the circuit. arranged to form a ring.

The catalysts used in the combined hydrogenation and hydrolysis process are cobalt oxide and molybdenum oxide. The ball was made of alumina impregnated with liveden and had a diameter of about 5 mm. This ball is The specific surface area is 250 m2/g, and the surface area is 1.75% based on the weight of the catalyst. It contained rut and 8% molybdenum.

The catalyst for the oxidation of H2S to sulfur was stabilized with 10 wt% calcium sulfate. A layer of 4I diameter extrudates made of titanium oxide and activated aluminum impregnated with iron sulfate. (The iron content in the catalyst (5% by weight).

CLAUS catalyst is made of alumina beads with a specific surface area of 260 m”/g and a diameter of 4 to 61 mm. It was composed of

The residual gas injected into the burner at a flow rate of 233 mol/h is approximately A temperature of 350° C. was reached and at this temperature it entered the hydrogenation/hydrolysis reactor. this In the reactor, virtually complete conversion of S02, S, C82 and CO5 to H2S takes place. The gaseous effluent discharged from this reactor has a temperature of about 380°C and contains no sulfur. It contained substantially no H7SL as a yellow-containing compound. This gaseous exhaust cools through the heat exchanger of the cooling assembly, the steam generation exchanger, and the air cooler to approximately 80°C. It was cooled and at this temperature entered the water spray column of the assembly.

Cooled air at about 35°C containing about 4.6% water vapor by volume flows from the top of the column. Body excreta leaked out.

This cooled effluent is reheated in the heat exchanger of the cooling assembly and then Air was added at 7.61 moles/hour through a port provided for the purpose. the resulting mixture The material entered the catalytic oxidation reactor at a temperature of 200°C. Gas passing through the oxidation reactor The contact time of the base with the stabilized titanium oxide layer and the iron sulfate impregnated alumina layer is approximately They were 3 seconds and 1.5 seconds. The conversion rate of 112S in the oxidation reactor is about 72%. The gas stream exiting the reactor has a temperature of about 295°C and 1) 2s and Contains SO2 at a molar ratio of H2S:SO approximately equal to 2:1, and the extent to which It also contained an amount of elemental sulfur.

The gas stream is cooled to 130°C in a sulfur condenser connected to the oxidation reactor; Most of the sulfur contained in the gas stream was separated by Ti condensation. This gas flow is was injected into the catalytic converter functioning in the CLAIIS reaction stage. Outlet of said converter from a temperature of about 135°C and a total of 800 volumes Rp,p,m.

A purified residual gas was discharged containing sulfur products equal to .

The sulfur-containing catalyst contained in the converter is sequentially placed in a regeneration stage and a cooling stage. The scavenging gas used to regenerate the medium is made up of a portion of the purified residual gas, and is used in the regeneration circuit. After heating to 300-350℃ in a reheater, the regeneration stage was carried out at a flow rate of 260ONm'/hour. introduced into the converter. The sulfur-containing scavenging gas discharged from the converter in the regeneration stage is then Flows into the sulfur condenser of the regeneration circuit, and most of the sulfur contained in the gas is condensed. There it is cooled to about 130°C so that it can be separated and then returned to the reheater for regeneration. Reused. The scavenging gas discharged from the converter during the regeneration stage contains substantially sulfur. Once the residual gas is no longer present, it is treated in a sulfur unit that discharges the residual gas to be treated. A portion of the acid gas was injected into this scavenging gas to reduce the H2S concentration of the scavenging gas to about 10 % by volume, and the scavenging treatment of the catalyst with H2S-containing gas is sufficient to reactivate the catalyst. It was carried out over a period of time.

The regenerated catalyst is then removed by passing a gas stream at about 130°C through a converter containing the regenerated catalyst. The catalyst was cooled to about 130°C. This cooling gas is the purified residue that has been cooled to the appropriate temperature. A portion of the gas was passed through the cooling circuit at a flow rate of 2100 Nm'/hr.

The water content of this cooling gas was approximately 5% by volume.

The catalytic converter is operated for 30 hours during the purification stage, i.e. the reaction stage, and 30 hours during the regeneration/cooling stage. However, for 10 hours of this time, it was operated alternately for cooling.

The duration of the final stage of regeneration, carried out in the presence of H2S, was 2 hours.

A sulfur factory that uses this residual gas treatment method to treat residual gas emissions can It showed a total sulfur yield of 99.70%.

International Survey 1111 Cattle ), NNEX To THE INTEE+ATICNAL 5EARCHRE PORτ 0 NINTERNATIONAL APPLICATION CATZON No. ? CT/YRa610O36S (sA i4917)

Claims (17)

[Claims] 1. Sulfur in residual gases, especially those from CLAUS sulfur plants. This is a method for removing compounds while recovering them in the form of sulfur, in which H derived from residual gas is removed. A gas stream containing 2S and SO2 at a temperature below 160° C. is contacted with the CLAUS catalyst. sulfur is formed by the reaction of H2S and SO2, provided that the catalyst is It works at a temperature low enough so that the sulfur is retained on this catalyst, and then the sulfur compounds The CLAUS catalyst discharges refined residual gas containing extremely small amounts of sulfur and retains sulfur. The medium is periodically scavenged with a non-oxidizing working gas at a temperature of 200°C to 500°C onto the catalyst. The retained sulfur is evaporated, thus regenerating the catalyst, and then below 160°C. This regenerated catalyst is reconstituted with a H2S and SO2 containing gas using an inert gas at a temperature of The process consists of cooling to the temperature necessary to bring the catalyst into contact with the CLAUS catalyst. The residual gas discharged from the sulfur factory is converted into H It is subjected to a combination of hydrogenation and hydrolysis in order to unify it into the 2S form, and then this by cooling the gaseous effluent resulting from the treatment of the gas to reduce its moisture content to a value of less than about 10% by volume. A controlled amount of free oxygen-containing gas is added to this low moisture gaseous effluent and it is heated to 150°C. Contact with H2S oxidation catalyst at higher temperature to controllably oxidize H2S and SO2 in a H2S:SO2 molar ratio approximately equal to 2:1, and also contains elemental sulfur. generating a gas stream containing a certain amount, provided that said molar ratio is in addition to said low moisture gaseous exhaust; by continuously adjusting the flow rate of free oxygen-containing gas, and finally Cooling the gas stream resulting from the oxidation treatment to a temperature below 160°C; to ensure that most of the sulfur contained in this gas stream is separated by condensation. A method characterized in that the method is formed by: 2. The combined hydrogenation and hydrolysis treatment is carried out at a temperature of about 140°C to 550°C, preferably Claim 1, characterized in that the method is carried out at a temperature of preferably about 200°C to 400°C. The method described in. 3. The H2S oxidation catalyst is made of a metal selected from Fe, Ni, Co, Cu and Zn. Combination of at least one compound and a support made of alumina and/or silica The method according to claim 1 or 2, characterized in that it is obtained by combing. 4. H2S oxidation catalyst is based on titanium oxide, especially titanium oxide and alkaline earth characterized by being formed in combination with metal sulfates, e.g. calcium sulfate The method according to claim 1 or 2. 5. H2S oxidation catalyst is Fe, Cu, Cd, Zn, Cr, Mo, W, Co, Ni and at least one compound of metal selected from Bi and Bi, and optionally P. d, a compound of at least one noble metal such as Pt, Ir and Rh, and silica. and/or a combination with a support made of titanium oxide, and the support is optional. 3. The method according to claim 1 or 2, characterized in that the method may contain a small amount of alumina. . 6. H2S oxidation catalyst is Fe, Cu, Cd, Zn, Cr, Mo, W, Co, Ni and at least one compound of metal selected from Bi and Bi, and optionally P. d, Pt, Ir and Rh, and especially a small amount. Activated alumina thermally stabilized by a small amount of at least one rare earth oxide Claim 1 characterized in that it is formed by a combination with a support consisting of is the method described in 2. 7. The H2S oxidation catalyst is a layer of the catalyst according to any one of claims 4 to 6, and and a layer of the catalyst according to claim 3 following the claim 3. The method described in Box 1 or 2. 8. The temperature of H2S oxidation by contact with the oxidation catalyst is approximately 150°C to 400°C. The method according to claim 3 or 7, characterized in that: 9. The temperature of H2S oxidation by contact with the oxidation catalyst is approximately 150°C to 500°C. The method according to claim 4, characterized in that: 10. The temperature of H2S oxidation by contact with an oxidation catalyst is about 150°C to 700°C. The method according to claim 5, characterized in that: 11. The temperature of H2S oxidation by contact with an oxidation catalyst is about 150°C to 1000°C. The method according to claim 6, characterized in that: 12. CLAUS catalysts are characterized in that they function at temperatures of approximately 120°C to 140°C. 12. The method according to any one of claims 1 to 11. 13. The scavenging gas used for regeneration is a reducing gas selected from H2, CO and H2S. The active compound is removed during at least the final stage of regeneration, i.e. most of the sulfur deposited on the catalyst. According to any one of claims 1 to 12, the content is contained after the component has evaporated. the method of. 14. The concentration of reducing compounds contained in the scavenging gas used for regeneration is 0.5 to 2. 14. A method according to claim 13, characterized in that it is 5% by volume. 15. The gas that cools the regenerated CLAUS catalyst is used at least at the end of the catalyst cooling process. Claims 1 to 14, characterized in that water vapor is included during the step. the method of. 16. The amount of water vapor contained in the cooling gas is 1 to 50% by volume. The method according to claim 15. 17. CLAUS catalysts include alumina, bauxite, silica, natural or synthetic enzymes. At least a metal selected from olite, Fe, Ni, Co, Cu and Zn. Composed of a combination of one type of compound and a support made of alumina and/or silica or a mixture of these substances. 16. The method according to any one of et al.