WO2018166937A1

WO2018166937A1 - Method and device for the preparation of a hydrogen sulphide-containing gas stream

Info

Publication number: WO2018166937A1
Application number: PCT/EP2018/056003
Authority: WO
Inventors: Stefan Hauke; Ralph Joh; Hans Wolfgang Nickelfeld; Rüdiger Schneider; Michael Schüler; Hatice Gülsah Sönmez
Original assignee: Siemens Aktiengesellschaft
Priority date: 2017-03-14
Filing date: 2018-03-12
Publication date: 2018-09-20

Abstract

The invention relates to a method for the preparation of a hydrogen sulphide-containing gas stream (3), in particular a stream of natural gas, wherein a gas stream (3) containing hydrogen sulphide (2) is fed to an absorber (7), in which the hydrogen sulphide (2) is absorbed in a washing medium (9) and reacts by means of a catalyst (13) to elemental sulphur (14), wherein the catalyst (13) is reduced during the reaction of the absorbed hydrogen sulphide (2). According to the invention, the washing medium (15) charged with elemental sulphur (14) and the reduced catalyst (17) is fed to a regeneration stage (37), in which the reduced catalyst (17) is regenerated by reaction with an oxygen-containing gas (49), a static mixer (43) being used for the regeneration of the catalyst (17) in the regeneration stage (37). The invention further relates to a device (1) comprising a regeneration stage (37) that is designed with a static mixer (43) for the preparation of a gas stream (3).

Description

description

Process and device for the treatment of a hydrogen sulphide-containing gas stream

The invention relates to a process for the treatment of a hydrogen sulfide-containing gas stream, in particular a natural gas stream. Furthermore, the invention relates to a device for the treatment of a hydrogen sulfide-containing gas flow.

Natural gas is a fossil fuel with a relatively low emission of carbon dioxide (C0 ₂ ) and a comparatively low emission of other waste products during combustion. His contribution as one of the most important

Energy resources of the world are rising steadily. Against the background of raw material shortages, constantly rising energy requirements and environmental protection reasons, the treatment and utilization of natural gas is thus a promising option for the efficient and low-emission generation of energy.

However, the direct use of natural gas is only possible to a limited extent. Due to the acidic components such as in particular hydrogen sulfide (H ₂ S) raw natural gas can not be used directly in a gas turbine, for pipeline transport or in a combined heat and power plant (CHP). Therefore, natural gas streams with a high content of hydrogen sulphide are often flared unused. In this respect, there is a major challenge in the treatment of acid gases, especially in the separation of hydrogen sulfide.

For the separation of hydrogen sulfide from natural gas industrially different methods are used. One process, which is characterized by low complexity and low investment costs, is the so-called direct oxidation. In the direct oxidation, an H ₂ S-containing gas stream in an absorber with a liquid washing medium in Contact containing a catalyst or a catalytically active component. The hydrogen sulfide is absorbed in the wash medium and oxidized by the catalyst to elemental sulfur. The reduced catalyst is oxidatively regenerated in a further process step under the influence of atmospheric oxygen.

To regenerate the catalyst, countercurrent bubble columns (oxidizers) are generally used as contact devices. To increase the partial pressure drop (increase in tractive force) and to increase the specific mass transfer area (for example by foaming or the gas fraction in the bubble column), for example, gassing stirrers, perforated plates, sintered metal internals or other gassing systems such as membrane aerators, nozzles (for example Venturi nozzles) or gassing rings are used.

The use of such bubble columns, however, involves some problems. In the catalyst regeneration, the mass transfer of the oxygen into the liquid phase (washing medium) is the limiting step of the process, since a sufficient rate of ascent of the gas bubbles in the bubble column must be ensured. For this, the gas bubbles must reach a minimum size. If the gas bubbles are too small, entrainment of gas from the bubble column into the absorber may occur, resulting in undesirable introduction of air constituents into the natural gas in the absorber. Such a gas input can lead, for example, to the formation of explosive mixtures. In return, however, as the bubble size increases, the effective mass transfer area decreases, as a result of which mass transfer decreases.

In order for a functioning bubble regime to develop in a bubble column, the gas load must not be too high, since otherwise the gas bubbles coalesce and even then the necessary mass transfer surface for catalyst regeneration is not reached. Therefore, bubble columns must be designed with a comparatively large diameter, which leads to a high space requirement and high investment costs. For the use of sour natural gas as part of the local energy supply, however, it is necessary that the plants used here (for example, for offshore applications) take up little space. Also, the weight of liquid hold-up at this point makes operation of direct oxidation processes with bubble columns as contact devices for catalyst regeneration unfavorable. In addition, bubble columns during operation are sensitive to the change in the surface tension, which influences the foaming behavior in the respective bubble columns. The alkaline washing media commonly used for the treatment of natural gas show such an increased foaming tendency. Although suitable measures can prevent the discharge of foam from a bubble column, the type and stability of the foam are often not uniform. The process is correspondingly difficult to control.

The invention is therefore based on the object to provide a way for efficient and cost-effective treatment of a hydrogen sulfide-containing gas stream and in particular a natural gas stream.

This object is achieved by the features of claims 1 and 10. Advantageous embodiments of the invention are set forth in the dependent claims and the description below.

In the process according to the invention, a hydrogen sulfide-containing gas is used for the treatment of a hydrogen sulfide-containing gas stream and in particular of a natural gas stream

Gas stream fed to an absorber in which the sulfur - hydrogen is absorbed in a washing medium and reacts by means of a catalyst to elemental sulfur, wherein the catalyst is reduced in the reaction of the absorbed hydrogen sulfide. That with elemental sulfur and The washing medium loaded in the reduced catalyst is then fed to a regeneration stage in which the reduced catalyst is regenerated by reaction with an oxygen-containing gas. According to the invention, a static mixer is used for the regeneration of the catalyst in the regeneration stage.

Through the use of a static mixer as a contact apparatus of the necessary for the regeneration of the catalyst while recovering the regenerated washing medium intensive contact between the two phases, ie the oxygen-containing gas and the liquid is ensured. In this case, a static mixer, in contrast to the previously used bubble columns in terms of the ratios of the gas and liquid flows are operated much more flexible, since, for example, different bubble regimes play no role. Due to the intensive mixing of the two phases results in a very efficient mass transfer, so that even comparatively short residence times of the two phases in the static are sufficient to ensure the regeneration of the catalyst.

For the purposes of the present invention, a static mixer is understood to mean a mixer which comprises non-movable, flow-influencing mixing elements. The mixing is thus achieved solely by the flow movement of the phases or reactants to be mixed. For this purpose, the mixing elements influencing the flow, for example by means of screws, lamellas or even lattices, expediently are arranged one behind the other in a corresponding tube.

The loaded washing medium and the oxygen-containing gas flow through the static mixer, preferably in cocurrent. In this context, a laden washing medium in the sense of the present invention is understood as meaning a washing medium which (in precipitated form) reduces the catalyst and elemental sulfur reduced in the formation of the sulfur. holds. The mixing elements divide the flowing through the tube stream from the loaded washing medium and the oxygen-containing gas, twist the resulting partial flows and lead them together again. The mixing elements in a static mixer thus ensure a constant renewal of the

Phase interfaces, which speeds up the mass transfer. As a result, the necessary residence time of the two phases in the static mixer can be considerably reduced and, compared to a bubble column, the liquid holdup can also be significantly reduced.

Furthermore, because of the fluids flowing through the static mixer in direct current, the relative velocity of gas and liquid can be neglected relative to one another, so that substantially higher gas and liquid loads can be realized. Moreover, unlike a bubble column, it does not matter if the static mixer is placed upright or lying down. A more flexible setup plan and a considerable space saving compared to a conventional bubble column are the result.

The surface tension of the washing medium, which is responsible for undesirable foaming, has only a small influence on the process performance in the case of a static mixer. The process can be operated more stable, since unlike the bubble column there is no danger that unwanted liquid with the air flow from the regeneration stage will be discharged (effervescence). The previously reduced catalyst contained in the loaded wash medium is reformed during the passage of the static mixer by the reaction with the oxygen-containing gas. The oxygen-containing gas is expediently flowed into the regeneration stage or into the static mixer for this purpose. Under an oxygen-containing gas in the context of the present invention is basically understood to mean any gas whose oxygen content is high enough to rebuild the catalytic active components. As sour Substance-containing gas can be used for example ambient air, oxygen-enriched air or pure oxygen. When the laden washing medium comes into contact with the gas, the oxygen contained in the gas passes from the gas phase into the liquid phase, ie into the washing medium. The oxygen-containing gas depleted of oxygen. In the liquid phase, the oxidation of the catalyst previously reduced in sulfur formation takes place; the catalyst is regenerated or recovered. The washing medium containing the regenerated catalyst is then again available for the separation of hydrogen sulfide and its subsequent oxidation available.

After oxidation, a multiphase mixture of regenerated wash medium, oxygen-depleted gas, and contained solids leaves the membrane contactor. The multiphase mixture is preferably fed to a separation stage in which the two phases are separated from one another. The separation of gas and liquid in this separation stage, for example, a gas-liquid separator, is not critical, since the phases here in the DC (on) flow. The oxygen-depleted gas is expediently released into the environment. The regenerated washing medium is expediently fed to the absorber starting from the separating stage and is used there for the reprocessing of a gas stream flowing into the absorber. Advantageously, the catalyst used is a metal salt. In principle, all metal salts of which the metal ions can be present in several oxidation states are suitable here. Preferably, the salts of the metals iron, manganese or copper are used. The oxidation of the Schweielwasser- substance to elemental sulfur thus takes place with simultaneous reduction of the metal ion. The sulfur precipitates as a solid and the metal ions remain dissolved in the wash medium. In particular, a washing medium is used which contains the catalyst, ie the respective metal salt.

In principle, the laden washing medium flowing out of the absorber can be fed directly from the absorber to the regeneration stage in order to regenerate the reduced catalyst there. However, in the absorption of hydrogen sulphide, methane (CH ₄ ) also dissolves in the washing medium, which during the regeneration of the washing medium (within the regeneration stage) can reach the gas used for this purpose which leaves the regeneration stage again. However, this must be avoided for safety reasons.

Accordingly, it is particularly preferred within the scope of the invention for the loaded washing medium to be depressurized before it is fed to the regeneration stage. By a relaxation of the loaded washing medium before its regeneration of the catalyst, a prescribed unwanted enrichment of natural gas components such as methane (CH ₄ ) is prevented in the washing medium. The natural gas components absorbed in the washing medium are desorbed from the washing medium and preferably separated before entering the regeneration stage. In an expedient embodiment, the separated methane or the methane-containing partial stream is again compressed and the emerging from the absorber, purified from H ₂ S.

Gas stream (sweet gas) supplied. Alternatively preferably, the methane can be supplied to a further use. The essentially methane-free washing medium after the expansion is then fed to the regeneration stage as described above.

Conveniently, at least part of the precipitated in the oxidation of the hydrogen sulfide elemental

Sulfur separated from the wash medium. In this case, so much sulfur is preferably removed that the concentration of the precipitated sulfur in the loaded washing medium after separation is in a range between 1% and 10%. From- Depending on the structural nature of the device components used for carrying out the method, the separation of the precipitated sulfur at various points is possible.

In an advantageous embodiment, the separation of the elemental sulfur takes place by the removal of a partial flow of the washing medium before it enters the regeneration stage. In this case, the partial flow can take place, for example, either before the expansion of the laden washing medium flowing out of the absorber or else afterwards. Preference is given to a removal of the partial flow of the expanded washing medium. The sulfur contained in the partial flow is expediently separated therefrom. The separation is preferably carried out by means of customary separation units, for example by means of a hydrocyclone or by means of filtration units. The sulfur itself is expediently sent for further utilization. The sulfur-purified partial stream of the washing medium can then be recycled at various points in the process. In a preferred embodiment of the invention, the part-stream purified by sulfur is fed to the expansion stage. Alternatively preferably, the partial flow is metered into the washing medium supplied to the regeneration stage and flows together with it into the regeneration stage. Depending on the process, direct dosing into the regeneration stage may also be advantageous. As the washing medium, an amino acid salt solution is preferably used. An aqueous amino acid salt solution is useful here. The use of mixtures of different amino acid salts as a washing medium is also possible. The inventive device for processing a

Hydrogen sulfide-containing gas stream, in particular a natural gas stream, comprises an absorber for the absorption of

Hydrogen sulphide by means of a washing medium and for closing oxidation of the absorbed hydrogen sulfide to elemental sulfur with reduction of a catalyst used for this purpose, as well as a fluidically coupled with the absorber regeneration stage for regeneration of the reduced catalyst by means of an oxygen-containing gas, wherein the regeneration stage is designed for regeneration of the catalyst with a static mixer.

In the absorber, the hydrogen sulfide is absorbed by absorption in the washing medium from a gas stream. The washing medium used here is preferably an amino acid salt solution. The absorbed within the absorber in the washing medium hydrogen sulfide reacts within the absorber by means of a catalyst to elemental sulfur and is thereby reduced itself. The catalyst used is preferably a metal salt which is contained in the washing medium.

For regeneration or recovery of the catalyst, the laden washing medium is supplied to the fluidically coupled with the absorber regeneration stage. Trained with a static mixer regeneration stage is connected downstream of the absorber in the flow direction of the loaded washing medium. To supply the loaded washing medium to the regeneration stage, the absorber expediently comprises a discharge line, which is fluidically coupled to a supply line of the regeneration stage. In this way, the loaded washing medium, starting from the absorber, can flow into the regeneration stage where the previously reduced catalyst is regenerated as part of the sulfur precipitation.

The loaded wash medium flows with an oxygen-containing gas in cocurrent through the regeneration stage. For supplying the oxygen-containing gas, the regeneration stage is expediently connected to a corresponding supply line. The reduced catalyst in the absorber is then recovered in the regeneration stage by oxidation by means of the oxygen-containing gas. Conveniently, the regeneration stage downstream of a separation stage fluidically. The separation stage is used to separate the emerging from the regeneration stage or the static mixer two-phase mixture of regenerated wash medium (low Schweielanteil, regenerated catalyst) and oxygen depleted or depleted gas. For supplying the two-phase mixture to the separation stage, the regeneration stage is connected to a discharge line, which is fluidically coupled to a supply line of the separation stage. The separation stage is the regeneration stage thus downstream in the flow direction of the two-phase mixture.

After separation of the two-phase mixture, the depleted of oxygen gas is released in an expedient embodiment in the environment. For this purpose, the separation stage is suitably connected to a discharge line, via which the depleted gas is removed from the process. Alternatively, it is preferably possible to supply the oxygen-reduced gas to the gas turbine. In this case, the discharge line of the separation stage is expediently coupled to a supply line of a gas turbine.

The regenerated washing medium is returned to the absorber starting from the separation stage and used there for the renewed absorption of hydrogen sulphide and for its oxidation to elemental sulfur. For this purpose, the separation stage is expediently coupled fluidically with the absorber. In other words, the absorber of the separation stage is downstream in terms of flow in the flow direction of the regenerated washing medium. For this purpose, a discharge line of the separation stage is fluidically coupled to a supply line of the absorber. In a further preferred embodiment, an expansion stage, a so-called flash stage, is fluidically connected between the absorber and the regeneration stage. In the expansion stage, the effluent from the absorber is discharged. mende washing medium containing the precipitated sulfur and the reduced catalyst, relaxed. During expansion, natural gas components contained in the scrubbing medium, in particular methane, are desorbed, thus preventing their undesired enrichment in the scrubbing medium.

The expansion stage is expediently connected in the discharge line of the absorber and downstream of the absorber in the flow direction of the loaded washing medium flow. After the expansion, the substantially methane-free washing medium is withdrawn via a discharge line connected to the expansion stage and fed to the regeneration stage. Preferably, the expansion stage is connected to a removal line for removal of at least a partial flow of the washing medium. So part of the oxidation of the

Hydrogen sulfide precipitated elemental sulfur are separated from the wash medium. The preferred concentration of the precipitated sulfur remaining in the washing medium after separation is in a range between 1% and 10%.

Alternatively preferably, a removal line for removing a partial flow of the loaded washing medium may also be connected elsewhere. Thus, one of the discharge line of the absorber (before the relaxation) or the supply line of Regegenerationsstufe (after the relaxation) connected discharge line is possible. The separation of the sulfur is preferably carried out in a flow direction of the

Partial flow of the extraction line fluidly connected separation unit. The use of a hydrocyclone or a filtration unit is expedient here. The separated sulfur itself is expediently sent for further utilization.

The sulfur-purified partial stream of the washing medium is preferably fed to the expansion stage. For this purpose, Preferably, a return line of the separation unit fluidly coupled to a supply line of the expansion stage. Alternatively or additionally preferred is a

Return line of the separation unit fluidly coupled to a supply line of the regeneration stage, so that the part of the washing medium purified by sulfur is metered to the washing medium supplied to the regeneration stage and is fed together with this (as a combined main stream) of the regeneration stage.

A further preferred embodiment is the direct fluidic coupling of the return line of the separation unit with the regeneration stage. For this purpose, it is expedient if the return line of the separation unit is fluidically coupled to a separate supply line of the regeneration stage. The sulfur-purified partial stream of the washing medium is fed to the regeneration stage in this case separately from the main stream. Further advantageous embodiments of the device will become apparent from the dependent claims directed to the method. In this case, the advantages named for the method and its further developments can be transferred analogously to the device.

Embodiments of the invention will be explained in more detail with reference to a drawing. Showing:

1 shows a schematic representation of a device for processing a gas stream with a static mixer, as well

2 in a three-dimensional schematic representation of the static mixer according to FIG. 1

Corresponding parts (and sizes) are always provided with the same reference numerals in all figures. In FIG 1, a device 1 is shown, which is used for the treatment of a hydrogen sulfide 2 containing gas stream 3. The gas stream 3, in this case a natural gas stream, is fed via a feed line 5 to an absorber 7. In the absorber 7 is an aqueous amino acid salt solution as the washing medium 9. The gas stream 3 is contacted in countercurrent with the washing medium 9, wherein the hydrogen sulfide 2 contained in the gas stream 3 is absorbed in the washing medium 9. The purified in this way of hydrogen sulfide 2 gas stream 10 is withdrawn via a discharge line 11 from the absorber 7 and can then be fed to a further use.

The hydrogen sulfide 2 absorbed in the washing medium 9 is oxidized by a catalyst 13 contained in the washing medium 9, in the present case a Fe (III) salt, to elemental sulfur 14, which precipitates in the washing medium 9. The catalyst 13 is reduced in this case, the metal ions (Fe (II) ions) remain in solution. The loaded washing medium 15, which now contains the reduced catalyst 17 and elemental sulfur 14, is now supplied to the absorber 7 fluidically downstream expansion stage 21 (flash stage). For this purpose, a discharge line 23 of the absorber 7 is fluidically coupled to a feed line 25 of the expansion stage 21

Within the expansion stage 21, the loaded washing medium 15 is expanded and desorbed in this contained natural gas components such as in particular contained methane. The

Desorbed natural gas components escape via one of the expansion stage 21 connected to the discharge line 27 from the process. In addition, a partial flow 29 of the loaded

Wash medium 15 removed from the expansion stage 21 via one of these connected extraction line 31. This reduces the concentration of precipitated sulfur 14 in the loaded wash medium 15 to a concentration of about 5%. The withdrawn from the washing medium 15 partial stream 29 is supplied via the withdrawal line 31 designed as a hydrocyclone separation unit 33, in which the sulfur 14 is separated from the washing medium 15. The separated from the partial flow 29 sulfur 14 itself is fed to a further utilization 35. The scrubbing medium 15 purified by sulfur 14 is supplied to the expansion stage 21 in the present case. For this purpose, a return line 36 of the separation unit 33 is fluidically coupled to a supply line 38 of the expansion stage 21. Alternatively or additionally (depending on the process conditions), it is possible to meter the sulfur-purified partial stream 29 of the washing medium 15 to the regeneration stage 21 supplied washing medium 15 or via a separate line directly to the regeneration stage 21.

To recover the catalyst 17, the loaded washing medium 15, starting from the expansion stage 21, is supplied to one of these regeneration stages 37 downstream of the latter in the direction of flow of the loaded washing medium 15. For this purpose, a discharge line 39 of the expansion stage 21 is fluidically coupled to a supply line 41 of the regeneration stage 37. The regeneration stage 37 is formed with a static mixer 43, which comprises in a tube 45 static mixing elements 47 arranged one behind the other. A detailed description of the static mixer 43 can be seen in FIG.

In addition to the loaded washing medium 15, an oxygen-containing gas 49, in the present case atmospheric oxygen, flows over one

Feed line 50 in the regeneration stage 37 a. The laden washing medium 15 and the oxygen-containing gas 49 flow through the regeneration stage 37, that is to say the static mixer 43 in the same direction, ie in the same direction. Upon contact of the loaded washing medium 15 with the oxygen-containing gas 49 of the previously reduced catalyst 17 is regenerated by the oxidation of Fe (II) ions to Fe (III) - ions. The catalyst 13 recovered in this way is then available for the renewed oxidation of hydrogen sulfide 2 available.

After the oxidation of the catalyst 17 leaves a mixture 51 of regenerated washing medium 9 and oxygen depleted gas 53, the regeneration stage 37. To separate the mixture 51 in its two phases 9, 53, the mixture 51 of the regeneration stage 37 fluidically downstream separation stage 55 is supplied. For this purpose, the regeneration stage 37, a discharge line 57 is connected, which is fluidically coupled to a feed line 59 of the separation stage 55.

After the separation of the gas 53 from the two-phase mixture 51, the latter is discharged into the environment via a discharge line 61 connected to the separation stage 55. Alternatively, it is possible to supply the oxygen-depleted gas 53 to a further utilization. The regenerated washing medium 9 is supplied to the absorber 7 starting from the separation stage 55. For this purpose, a discharge line 63 of the separation stage 55 is fluidly coupled to a supply line 65 of the absorber 7. Within the absorber 9, the regenerated washing medium 9 is then used again for the treatment of a gas stream 3 fed to the absorber 7.

2, the static mixer 43 used in the device 1 according to FIG. 1 is shown. The static mixer 43 comprises a plurality of static, flow-influencing mixing elements 47 arranged in the tube 45. When the loaded washing medium 15 and the oxygen-containing gas 49 (starting from the expansion stage 21 or the absorber 7) via the corresponding supply lines 41, 50 in the static mixer 43 and this flow through the DC, the mixing is achieved solely by the flow movement of the two phases 15, 49. Thanks to the static mixing elements 47, a continuous renewal of the phase interface between the two phases 15, 49 is ensured, so that the necessary mass transfer between them and thus the desired Oxidation and thus regeneration of the catalyst 17 is ensured with only a short residence time within the static mixer 43.

The regeneration stage 37 leaving mixture 51 is, as already described for FIG 1, the separation stage 55 and the regenerated washing medium 9 separated there from the oxygen-depleted gas 53. The regenerated washing medium 9 is returned to the absorber 7.

The invention will be particularly apparent from the embodiments described above, but is not limited to these embodiments. Rather, other embodiments of the invention may be derived from the claims and the foregoing description.

Claims

claims

1. A process for the treatment of a hydrogen sulphide-containing gas stream (3), in particular a natural gas stream, wherein a gas stream (3) containing hydrogen sulphide (2) is fed to an absorber (7) in which the hydrogen sulphide (2) is mixed in a washing medium (9). and reacts by means of a catalyst (13) to give elemental sulfur (14), the catalyst (13) being reduced in the reaction of the absorbed hydrogen sulphide (2), with elemental sulfur (14) and the reduced catalyst (13). 17) is supplied to a regeneration stage (37) in which the reduced catalyst (17) is regenerated by reaction with an oxygen-containing gas (49), and for regeneration of the catalyst (17) in the regeneration stage (17). 37) a static mixer (43) is used.

2. The method of claim 1, wherein the loaded Waschmedi- um (15) and the oxygen-containing gas (49) flow through the static mixer (43) in cocurrent.

3. The method of claim 1 or 2, wherein a mixture (51) of regenerated washing medium (9) and deoxygenated gas (53) after the regeneration of the catalyst (17) is fed to a separation stage (55).

4. The method according to any one of the preceding claims, wherein the regenerated washing medium (9), starting from the separation stage (55) is supplied to the absorber (7).

5. The method according to any one of the preceding claims, wherein as catalyst (13) a metal salt is used.

6. The method according to any one of the preceding claims, wherein a washing medium (9) is used which contains the catalyst (13).

7. The method according to any one of the preceding claims, wherein the loaded washing medium (15) before the supply to the regeneration stage (37) is relaxed.

8. The method according to any one of the preceding claims, wherein at least a partial stream (29) of the elemental sulfur (14) from the loaded washing medium (15) is separated.

9. The method according to any one of the preceding claims, wherein as the washing medium (9) an amino acid salt solution is used.

10. Device (1) for the treatment of a hydrogen sulfide-containing gas stream (3), in particular a natural gas stream comprising an absorber (7) for the absorption of

Hydrogen sulfide (2) by means of a washing medium (9) and for subsequent oxidation of the absorbed hydrogen sulfide (2) to elemental sulfur (14) with reduction of a catalyst used for this purpose (13), as well as a flow technologically coupled with the absorber (7) regeneration stage ( 37) for the regeneration of the reduced catalyst (17) by means of an oxygen-containing gas (49), wherein the regeneration stage (37) for the regeneration of the catalyst (17) with a static mixer (43) is formed.

11. Device (1) according to claim 10, wherein the absorber (7) comprises a discharge line (23), which is fluidically coupled to a supply line (41) of the regeneration stage (37).

12. Device (1) according to claim 10 or 11, wherein the regeneration stage (37) is connected to a feed line (50) for supplying the oxygen-containing gas (49).

13. Device (1) according to any one of claims 9 to 12, wherein the regeneration stage (37) is a separation stage (55) fluidly connected downstream.

14. Device (1) according to claim 13, wherein the separation stage (55) is fluidically coupled to the absorber (7).

15. Device (1) according to one of claims 10 to 14, wherein an expansion stage (21) is fluidically connected between the absorber (7) and the regeneration stage (37).

16. Device (1) according to claim 15, wherein the expansion stage (21) is connected to a removal line (31) for removing at least a partial flow (29) of the loaded washing medium (15).