Process to produce liquid sulphur from a stream containing hydrogen sulfide and related installation

Abstract

The process comprises: - feeding the hydrogen sulfide containing stream (12) in an enclosure (20) comprising a packing bed (30) containing a catalyst; - reacting, in the packing bed (30), hydrogen sulfide from the hydrogen sulfide containing stream (12) with sulfur dioxide to form liquid Sulphur (14) and a lean gas (16); - removing the liquid Sulphur (14) at a first outlet (26) of the enclosure (20) and removing the lean gas (16) at a second outlet (28) of the enclosure (20) - rotating the packing bed (30) around a rotation axis (A-A') in the enclosure (20) to evacuate the liquid Sulphur (14) and the lean gas (16) from the packing bed (30).

Description

[0001] Process to produce liquid Sulphur from a stream containing hydrogen sulfide and related installation

[0002] The present invention concerns a process to produce liquid Sulphur from a hydrogen sulfide containing stream, comprising the following steps:

[0003] - feeding the hydrogen sulfide containing stream in an enclosure comprising a packing bed containing a catalyst ;

[0004] - reacting, in the packing bed, hydrogen sulfide from the hydrogen sulfide containing stream with sulfur dioxide to form liquid Sulphur and a lean gas ; removing the liquid Sulphur at a first outlet of the enclosure and removing the lean gas at a second outlet of the enclosure.

[0005] This process is carried out to treat a gas stream containing hydrogen sulfide, in order to recover a lean gas, having a lesser content of hydrogen sulfide than the gas stream containing hydrogen sulfide, and liquid Sulphur.

[0006] The process is applicable to all gases, but is particularly adapted to treat feeds arising from a hydrocarbon production field comprising oil and gas producing wells. The treatment of gas streams containing hydrogen sulfide is necessary in many hydrocarbon production fields, due to the occurrence of hydrogen sulfide in crude oil and gas extracted from the reservoirs.

[0007] The process is also adapted to refineries or more generally, to industrial plants to treat acid gases produced during industrial operations, such as natural gas production, biogas production, syngas production or field gas production.

[0008] Traditionally Sulphur has been produced using the so-called “Claus process”, where hydrogen sulfide and sulfur dioxide react within a fixed catalyst bed in gas phase and produce Sulphur in gas phase at high temperatures.

[0009] However, at high temperatures, the conventional Claus process is limited in its conversion due to the reaction equilibrium being reached.

[0010] Higher conversion can be achieved at lower temperatures. Nevertheless, when a Claus reactor is operated below Sulfur dew point (120 °C -150 °C), liquid Sulfur physically stay on the catalyst, temporarily deactivating the catalyst.

[0011] To overcome this problem, sub dew point Claus reactors are installed in parallel, with one operating and one in regeneration. When the catalyst of one reactor is saturated with liquid Sulfur, the reacting gas is diverted to a spare reactor. The catalyst in the deactivated reactor is then regenerated by sending hot process gas to 300°C - 350 °C to desorb the Sulfur. The recovered stream is sent to a condenser to recover the liquid Sulfur. Such processes are efficient, but require a large number of equipment, since at least two parallel reactors must be provided and operated, to allow high conversion, as well as high throughput. This increases the capital expenditures. The catalyst regeneration must be carried out quite frequently, which also increases the operational expenditures.

[0012] One aim of the invention is to provide a process which produces liquid Sulphur from a hydrogen sulfide containing stream, with very high conversion and with reduced capital and operational expenditures.

[0013] To this aim, the process according to the invention is a process of the above type, characterized by rotating the packing bed around a rotation axis in the enclosure to evacuate the liquid Sulphur and the lean gas from the packing bed.

[0014] The process according to the invention may comprise one or more of the following feature(s), taken solely, or according to any technical feasible combination :

[0015] - it comprises : o feeding the hydrogen sulfide containing stream at an inner surface of the packing bed located around the rotation axis ; o circulating the hydrogen sulfide and the sulfur dioxide away from the rotation axis and o peripherally evacuating the lean gas and the liquid Sulphur produced in the rotating packing bed out of the rotating packing bed.

[0016] - it comprises separating the mixture of lean gas and liquid Sulphur at a separation space located in the enclosure at the outer periphery of the rotating packing bed ;

[0017] - it comprises axially feeding the hydrogen sulfide containing stream along the rotation axis, and preventing the hydrogen sulfide containing stream from mixing with the lean gas and the liquid Sulphur via a rotary seal ;

[0018] - the temperature of the rotating packing bed is lower than 150°C and comprised between 110°C and 130°C ;

[0019] - it comprises the following preliminary steps: o providing an acid gas feed containing hydrogen sulfide; o mixing the acid gas feed with an oxygen containing gas feed, in particular with air ; o producing sulfur dioxide in at least one stage upstream of the enclosure, the hydrogen sulfide containing gas also comprising sulfur dioxide produced in the at least one stage upstream of the enclosure. - the at least one stage upstream of the enclosure comprises a Claus thermal stage having a furnace and a condenser, the process comprising extracting a liquid Sulphur feed from the condenser ;

[0020] - the at least one stage upstream of the enclosure comprises at least a Claus catalyst stage, located downstream of the Claus thermal stage, the Claus catalyst stage comprising a static catalyst bed reactor, the process comprising extracting the hydrogen sulfide containing gas from an outlet of the static catalyst bed reactor ;

[0021] - it comprises feeding, between the outlet of the static catalyst bed reactor and the inlet of the enclosure, a stream containing oxygen ;

[0022] - the at least one stage upstream of the enclosure comprises a Claus direct oxidation reactor, the Claus direct oxidation reactor receiving the acid gas feed containing hydrogen sulfide or receiving a stream produced in a Claus catalyst stage, the hydrogen sulfide containing gas being recovered at an outlet of the Claus direct oxidation reactor ;

[0023] - it comprises a tail gas treating unit comprising an amine absorber downstream of the enclosure, the process comprising passing the lean gas preferably after hydrogenation and quenching in the amine absorber to produce an off gas.

[0024] The invention also concerns an installation for producing Sulphur from a stream containing hydrogen sulfide, the installation comprising: an enclosure defining an inlet to introduce a hydrogen sulfide containing stream, the enclosure comprising a packing bed containing a catalyst, the catalyst being configured to react hydrogen sulfide from the hydrogen sulfide containing stream with sulfur dioxide to form liquid Sulphur and a lean gas ;

[0025] - the enclosure defining a first outlet to remove the liquid Sulphur from the enclosure and a second outlet to remove the lean gas from the enclosure ; characterized in that the packing bed is configured to be driven in rotation around a rotation axis in the enclosure to evacuate the liquid Sulphur from the packing bed.

[0026] The installation according to the invention may comprise one or more of the following feature(s), taken solely or according to any technical combination :

[0027] - the rotary packing bed comprises an upper guiding plate and a lower guiding plate configured to guide the mixture of hydrogen sulfide and sulfur dioxide radially away from the rotation axis to evacuate the liquid Sulfur and the lean gas peripherally out of rotary packing bed ;

[0028] - it comprises at least one stage upstream of the enclosure producing sulfur dioxide, an acid gas feed line emerging in the at least one stage upstream of the enclosure, the acid gas containing hydrogen sulfide, and a mixer to mix the acid gas feed with an oxygen containing gas feed, in particular with air, the hydrogen sulfide containing gas containing sulfur dioxide produced in the at least one stage upstream of the enclosure ;

[0029] - the at least one stage upstream of the enclosure comprises a Claus thermal stage having a furnace and a condenser, the condenser having an outlet to extract a liquid Sulphur feed from the condenser ;

[0030] - the at least one stage upstream of the enclosure comprises at least a Claus catalyst stage downstream of the Claus thermal stage, the Claus catalyst stage comprising a static catalyst bed reactor, the static catalyst bed reactor having an outlet to extract the hydrogen sulfide containing gas, the outlet to extract the hydrogen sulfide containing gas being connected to the enclosure, the at least one stage upstream of the enclosure optionally comprising a tap feeding a stream containing oxygen in the hydrogen sulfide containing gas, the tap being located between the outlet of the static catalyst bed reactor and the inlet of the enclosure ;

[0031] - the rotary packing bed comprises a cooler to control the operating temperature of the reaction.

[0032] The invention will be better understood, based on the following description, given solely as an example, and made in reference to the following drawings, in which:

[0033] - [Fig. 1] figure 1 is a view schematically illustrating a rotating bed used in an installation for carrying out the process according to the invention;

[0034] - [Fig. 2] figure 2 is an example of an installation in which the rotating bed of figure 1 is used with a Claus thermal stage and at least a Claus catalyst stage;

[0035] - [Fig. 3] figure 3 is a functional scheme of a variant of the installation of figure 2

[0036] - [Fig. 4] figure 4 is an installation in which the rotating bed of figure 1 is used in an installation downstream of a hot mode SmartSulf™ reactor, in replacement of a cold mode reactor;

[0037] - [Fig. 5] figure 5 is a functional scheme of a variant of the installation of figure 4.

[0038] A first rotary packing bed reactor 10 according to the invention is depicted in figure 1. The rotary packing bed reactor 10 is implemented in an installation, in which at least a hydrogen sulfide containing stream 12 has to be treated to produce liquid Sulphur 14 and a lean gas 16, having a lesser content in hydrogen sulfide than the hydrogen sulfide containing stream 12.

[0039] Several examples of installations in which the rotary packing bed reactor 10 is implemented are disclosed in figures 2 to 6. The hydrogen sulfide containing stream 12 is advantageously a mixture containing hydrogen sulfide and sulfur dioxide. The rotary packing bed reactor 10 is intended for reacting hydrogen sulfide with sulfur dioxide in order to produce the liquid Sulphur 14, and the lean gas 16.

[0040] The chemical reaction which is carried out in the reactor 10 is generally called “Claus Reaction” and can be summarized as:

[0041] 2 H2S + SO2<-> 3 / x Sx + 2 H2O (a)

[0042] The reaction is carried out in the rotary packing bed reactor 10 below the dew point of Sulfur, at a temperature that is lower than 150°C, and generally comprised between 110°C and 130°C. At such a temperature, the Sulphur that is produced in the above- mentioned reaction is in the liquid phase.

[0043] The pressure in the rotary packing bed reactor 10 is generally comprised between 1.02 bara and 2 bara.

[0044] The content in hydrogen sulfide in the hydrogen sulfide containing stream 12 is for example comprised between 0.5 mol % and 4 mol %, preferably between 0.5 mol % and 1.5 mol %.

[0045] The content of sulphur oxide in the hydrogen sulfide containing stream 12 is for example comprised between 0.25 mol % and 2 mol %, preferably between 0.25 mol % and 0.75 mol %.

[0046] As seen in figure 1 , the rotary packing bed reactor 10 comprises an enclosure 20 defining an internal volume 22, an introduction inlet 24 for the hydrogen sulfide containing stream 12, emerging in the internal volume 22, a liquid sulphur outlet 26 and a lean gas outlet 28, the outlets 26, 28 emerging from the internal volume 22.

[0047] According to the invention, the rotary packing bed reactor 10 further comprises a rotary packing bed 30, mounted rotatable around a rotation axis A-A’, and a driving shaft 32 to rotate the rotary packing bed 30 around axis A-A’. The rotary packing bed reactor 10 also comprises a rotary seal 34 for separating the hydrogen sulfide containing stream 12 from the lean gas 16 produced in the rotary packing bed 30.

[0048] In this example, the enclosure 20 defines a tight inner internal volume 22, which only opens at the inlet 24 and at the outlets 26, 28.

[0049] The enclosure 20 here comprises a lower bowl 36, and an upper wall 38, closing the lower bowl 36.

[0050] The inlet 24 comprises an inlet tube 40, inserted in the internal volume 22. The inlet tube 40 extends parallel to the rotation axis A-A’, preferentially concentrically with the rotation axis A-A’. The inlet tube 40 defines a plurality of side passages 42, for feeding the hydrogen sulfide containing stream 12 to the inner volume 22.

[0051] In this example, the liquid Sulphur outlet 26 is located at the bottom of the enclosure 20, apart from the axis A-A’. It emerges downwardly, to let the liquid Sulphur 14 flow under the effect of gravity.

[0052] The lean gas outlet 28 is located at the top of the enclosure 20, preferably in the upper wall 38. It is located apart from the rotation axis A-A’ to let the lean gas 16 spontaneously rise out of the internal volume 22.

[0053] The rotary catalyst packing bed 30 comprises an annular porous frame 44 receiving the catalyst. It advantageously comprises a lower guiding plate 46 and an upper guiding plate 48, the annular porous frame 44 being sandwiched between the guiding plates 46, 48.

[0054] The annular porous frame 44 comprises a catalyst support, which defines passages for circulation of gas and liquids, and an active catalyst deposited on the support.

[0055] The support is for example a metallic or polymeric structure with catalyst deposit or a 3D-printed structuralized filler The catalyst is a catalyst suitable to run a Claus reaction, also referred to as a “Claus catalyst”.

[0056] It comprises for example at least one catalyst among titanium dioxide (TiOg), alumina (AI2O3), cobalt molybdenum, nickel molybdenum and / or iron .

[0057] The lower guiding plate 46 and the upper guiding plate 48 tightly seal the annular porous frame 44 of the rotary packing bed 30, respectively downwardly and upwardly.

[0058] The annular porous frame 44 defines an inner annular introduction surface 50 for the hydrogen sulfide containing stream 12, which opens towards and around axis A-A’, facing the side passages 42 of the inlet tube 40 .

[0059] The annular porous frame 44 further defines an outer annular peripheral surface 52, which opens away from axis A-A’, facing a peripheral separation space 54 defined between the rotary catalyst packing bed 30 and a side wall of the enclosure 20.

[0060] In this example, the rotary shaft 32 is mounted below the lower guiding plate 46. It is configured to drive the rotary packing bed 30 in rotation around the rotation axis A-A’, for example at a speed greater than 100 rpm or an acceleration factor greater than 10 compared to gravity.

[0061] The rotary seal 34 is mounted above the rotary packing bed, circumferentially around the axis A-A’. It comprises at least a static part protruding from the upper wall 38 towards the rotary packing bed 30 and at least one rotating part which protrudes from the upper guiding plate 48 towards the upper wall 38.

[0062] The rotary seal 34 tightly separates an inner space 60, located around the axis A- A’ in which the hydrogen sulfide containing stream 12 emerges, and an outer space 62, connected to the peripheral annular space 54, through which the lean gas 16 exits.

[0063] The operation of the rotary packing bed reactor 10 according to the invention will now be described, in an installation producing a hydrogen sulfide containing stream 12.

[0064] In the installation, the hydrogen sulfide containing stream 12 is continuously fed to the rotary packing bed reactor 10.

[0065] The hydrogen sulfide containing stream 12 circulates in the inlet tube 40 and enters the rotary packing bed reactor 10 through the side passages 42.

[0066] The rotary packing bed 30 is driven in rotation around the axis A-A’, at a speed greater than 100 rpm, as defined above. The temperature in the rotary packing bed 30 is below the dew point of Sulfur,

[0067] The hydrogen sulfide containing stream 12 then enters the annular porous frame 44 through the inner annular peripheral surface 50. The mixture of hydrogen sulfide and sulfur dioxide contained in stream 12 radially flows through the annular porous frame 44, away from the rotation axis A-A’, between the lower guiding plate 46 and the upper guiding plate 48 and contacts the catalyst.

[0068] The hydrogen sulfide reacts with the sulfur dioxide on the catalyst to produce liquid Sulphur 14 and lean gas 16.

[0069] Thanks to the rotation of the rotary packing bed 30, the lean gas 16 and the liquid Sulphur 14 are expelled out of the annular porous frame 44 in the separation space 54 by centripetal effect, through the annular outer peripheral surface 52.

[0070] In the separation space 54, the liquid Sulphur 14 settles by gravity, and flows down to the liquid Sulphur outlet 26, where it is removed from the rotary packing bed reactor 10.

[0071] The lean gas 16 rises in the separation space 54, and is recovered at the lean gas outlet 28 to be further treated.

[0072] The lean gas 16 is prevented from contacting the hydrogen sulfide containing stream 12, thanks to the annular rotary seal 34 located above the rotary packing bed 30.

[0073] The lean gas 16 recovered at the lean gas outlet 28 has a content depleted in hydrogen sulfide, as compared to the hydrogen sulfide containing stream 12.

[0074] For example, more than 99% and, preferably equal or above 99.5% of the sulfur contained in stream 12 is recovered in liquid sulfur 14. Thanks to the continuous removal of liquid Sulphur 14 out of the annular porous frame 44 containing the catalyst, liquid Sulphur 14 produced in the rotary packing bed 30 does not significantly deposit or accumulate on the catalyst, and is continuously removed from the catalyst. This allows the catalyst to remain active

[0075] The reaction can therefore be carried out at temperatures below the dew point of Sulphur, which leads to significantly improved reaction yields.

[0076] The reaction can furthermore be carried out in a continuous manner, and does not require a frequent regeneration of the catalyst contained in the annular porous frame 44, contrary to traditional cold bed absorption processes or conventional Claus processes.

[0077] The rotary packing bed reactor 10 according to the invention is therefore very efficient to continuously treat a hydrogen sulfide containing stream 12, to remove at least part of the Sulphur contained in it, and to produce a lean gas 16 with a decreased hydrogen sulfide content.

[0078] The process including the rotary packing bed reactor 10 according to the invention limits the number of pieces of equipment, leading to lower capital expenditures. It can be continuously operated, which decreases operational expenditures.

[0079] Furthermore, the high speed of rotation of the rotary packing bed 30 allows an efficient Sulphur degassing, with an improved yield.

[0080] The rotary packing bed reactor 10 can be implemented in several types of installations in which a hydrogen sulfide containing stream 12 is generated.

[0081] In the example of figure 2, the rotary packing bed reactor 10 is integrated in a downstream stage of a conventional Claus installation 100.

[0082] The conventional Claus installation 100 comprises in a known manner, a Claus thermal stage 102, and at least one Claus catalyst stage 104.

[0083] The Claus thermal stage 102 comprises a furnace 106, a condenser 108, configured to treat the outlet of the furnace 106.

[0084] The furnace 106 is configured to receive a feed stream 112 comprising hydrogen sulfide, potentially a fuel stream 110, and an air stream 114, which thermally reacts in the furnace 106 according to the following reaction:

[0085] 2 H2S + 3 O22 SO2+ 2 H2O (b1)

[0086] 2 H2S + SO23 S + 2 H2O (b2)

[0087] These reaction produces Sulphur and sulfur dioxide.

[0088] The products 115, including reaction products such as Sulphur and sulfur dioxide and unreacted hydrogen sulfide are evacuated at an outlet of the furnace 106 to be conveyed to the condenser 108.

[0089] In the condenser, liquid Sulphur 116 is evacuated at a lower outlet 118. Fumes 120 containing hydrogen sulfide are evacuated at an upper outlet 122.

[0090] Each Claus catalyst stage 104 comprises a reheater 124, a catalytic reactor 126, and a condenser 128.

[0091] The fumes 120 are reheated in the heater 124, to be introduced in the catalytic reactor 126.

[0092] In the catalyst reactor 126, the stream is put in contact with a catalyst such as Alumina or Titanium based catalyst to form gaseous Sulphur and a flue gas containing hydrogen sulfide according to the following reaction :

[0093] 2 H2S + SO23 S + 2 H2O (C)

[0094] The temperature in the catalytic reactor 126 is higher than the Sulfur dew point.

[0095] The reaction products are conveyed to the condenser 128, to be separated into a liquid Sulphur stream 130, which is recovered at an outlet 132 of the condenser 128, and into the hydrogen sulfide containing stream 12, which is introduced in the continuously running rotary packing bed reactor 10 according to the invention.

[0096] In the example of figure 2, the rotary packing bed reactor 10 according to the invention replaces a traditional tail gas treatment unit (TGTU) normally provided downstream of the Claus catalyst stage(s) 104.

[0097] The rotary packing bed reactor 10 continuously treats the hydrogen sulfide containing stream 12 arising from the catalyst stage 104, without having to use a hydrogenation reactor, a quench tower, and an amine bed.

[0098] As compared to a conventional three stages Claus installation, which usually has a Sulphur recovery from about 94% to 97%, the replacement of one stage of Claus catalyst reactor by a rotary packing bed reactor 10 according to the invention, improves the recovery to 99 % and reduces the number of equipment, including heat transfer apparatus from five to two. The capital expenditures are therefore reduced. In addition, removing heat transfer equipment also decreases the operational expenditures.

[0099] In a variant shown in figure 3, an air flow 140 is introduced in the hydrogen sulfide containing stream 12, between the outlet of the Claus catalyst stage 104 and the inlet 24 for introducing the hydrogen sulfide containing stream 12 in the rotary packing bed reactor 10.

[0100] The hydrogen sulfide containing stream 12, mixed with the air flow, allows a direct oxydation of the hydrogen sulfide directly in the rotary packing bed reactor 10, (referred to as “Super Claus” process for example).

[0101] This process is particularly efficient to obtain recoveries above 99%, in particular from 99.0% to 99.5%. The process is run in a continuous manner. The centrifugal effect of the rotating packed bed 10 allows to prevent sulfur deposit and subsequent operational downtime.

[0102] Another installation 160 including a rotary packing bed reactor 10 according to the invention is shown in figure 4. This installation 160 is for example a modified “SmartSulf™” installation.

[0103] A feed 110 containing hydrogen sulfide is mixed with a flow of air 114, and is at least partially condensed in a first reheater 162.

[0104] The feed 110 is then introduced into a Claus catalyst reactor 164 whose operating temperature is above the dew point of sulphur. The Claus catalyst reactor 164 is a continuous reactor in which part of the feed 110 is converted into sulfur dioxide, in the presence of a controlled amount of air. In addition, the Claus catalyst reactor 164 produces gaseous Sulphur.

[0105] The Claus catalyst reactor 164 is filled with a catalyst, such as titanium dioxide (TiOg), alumina (AI2O3),. Boiling feed water 166 is fed to the Claus catalyst reactor 164, and is converted into steam 168 by contactless heat exchange in the Claus catalyst reactor 164 for example by passing through a coil provided in the Claus catalyst reactor 164.

[0106] The reaction products 170 are collected at the bottom of the Claus catalyst reactor 164 and are sent to a condenser 172.

[0107] Liquid Sulfur 174 is collected at the bottom of the condenser 172, and a hydrogen sulfide containing stream 12 is collected at the top of the condenser 172 to be continuously introduced in the rotary packing bed reactor 10.

[0108] A steam stream 176 is also collected in the condenser 172.

[0109] The rotary packing bed reactor 10 replaces the cold stage of a traditional “Smart Sulf™” oxidation reactor.

[0110] Contrary to the traditional “Smart Sulf™” oxidation reactor, in which the hot stage and the cold stage operate discontinuously to allow regeneration of the catalyst in the cold stage, the installation 160 comprising a rotary packing bed reactor 10 is configured to operate in continuously, and does not need frequent regeneration cycles. In the installation 160, Sulphur recovery does not periodically decrease as in the traditional “SmartSulf™” oxidation reactor when a change of bed from the hot bed to the cold bed is carried out.

[0111] Moreover, thermal stress in the catalyst and the associate equipments is limited due to a reduction of cyclic changes in temperature. The Sulphur recovery is improved and the operating costs are reduced. Moreover, the equipment needed to implement the Claus process is simpler and less expensive, diminishing the capital expenses and increasing the unit uptime

[0112] Integrating the rotary packing bed reactor 10 downstream of a hot stage “SmartSulf™” reactor also improves the Sulphur recovery up to 99.5%.

[0113] Generally, the installation 160 is particularly adapted for small capacity hydrogen sulfide treatment, and does not require additional tail gas treatment unit (TGTU).

[0114] For larger capacities, the installation 200 shown in figure 5 may be used. The installation 200 comprises a Claus thermal stage 102, and at least a Claus catalyst stage 104. It comprises, downstream of the Claus catalyst stage 104, an installation 160 as shown in figure 4 comprising a hot stage Claus catalyst reactor 164 and condenser 172, and a rotary packing bed reactor 10 according to the invention.

[0115] Such an installation 200 allows a high throughput with Sulphur recovery up to 99.5%.

Claims

REVENDICATIONS1. Process for producing Sulphur from a stream (12) containing hydrogen sulfide, the process comprising the following steps :- feeding the hydrogen sulfide containing stream (12) in an enclosure (20) comprising a packing bed (30) containing a catalyst ;- reacting, in the packing bed (30), hydrogen sulfide from the hydrogen sulfide containing stream (12) with sulfur dioxide to form liquid Sulphur (14) and a lean gas (16);- removing the liquid Sulphur (14) at a first outlet (26) of the enclosure (20) and removing the lean gas (16) at a second outlet (28) of the enclosure (20) characterized by:- rotating the packing bed (30) around a rotation axis (A-A’) in the enclosure (20) to evacuate the liquid Sulphur (14) and the lean gas (16) from the packing bed (30).

2. Process according to claim 1 , comprising :- feeding the hydrogen sulfide containing stream (12) at an inner surface (50) of the packing bed (30) located around the rotation axis (A-A’);- circulating the hydrogen sulfide and the sulfur dioxide away from the rotation axis (A-A’) and- peripherally evacuating the lean gas (16) and the liquid Sulphur (14) produced in the rotating packing bed (30) out of the rotating packing bed (30).

3. Process according to any one of the preceding claims, comprising separating the mixture of lean gas (16) and liquid Sulphur (14) at a separation space (54) located in the enclosure (20) at the outer periphery of the rotating packing bed (30).

4. Process according to any one of the preceding claims, comprising axially feeding the hydrogen sulfide containing stream (12) along the rotation axis (A-A’), and preventing the hydrogen sulfide containing stream (12) from mixing with the lean gas (16) and the liquid Sulphur (14) via a rotary seal (34).

5. Process according to any one of the preceding claims, wherein the temperature of the rotating packing bed (30) is lower than 150°C and comprised between 110°C and 130°C.

6. Process according to any one of the preceding claims comprising the following preliminary steps:- providing an acid gas feed (110) containing hydrogen sulfide;- mixing the acid gas feed (110) with an oxygen containing gas feed, in particular with air ;- producing sulfur dioxide in at least one stage upstream of the enclosure (20), the hydrogen sulfide containing gas (12) also comprising sulfur dioxide produced in the at least one stage upstream of the enclosure (20).

7. Process according to claim 6, wherein the at least one stage upstream of the enclosure (20) comprises a Claus thermal stage (102) having a furnace (106) and a condenser (108), the process comprising extracting a liquid Sulphur feed (116) from the condenser (108).

8. Process according to claim 7, wherein the at least one stage upstream of the enclosure (20) comprises at least a Claus catalyst stage (104), located downstream of the Claus thermal stage (102), the Claus catalyst stage (104) comprising a static catalyst bed reactor (126), the process comprising extracting the hydrogen sulfide containing gas (12) from an outlet of the static catalyst bed reactor (126).

9. Process according to claim 8, wherein comprising feeding, between the outlet of the static catalyst bed reactor (126) and the inlet of the enclosure (20), a stream (140) containing oxygen.

10. Process according to any one of claims 6 to 9, wherein the at least one stage upstream of the enclosure (20) comprises a Claus direct oxidation reactor (164), the Claus direct oxidation reactor (164) receiving the acid gas feed (110) containing hydrogen sulfide or receiving a stream produced in a Claus catalyst stage (104), the hydrogen sulfide containing gas (12) being recovered at an outlet of the Claus direct oxidation reactor (164).

11. Process according to any one of claims 6 to 10, comprising a tail gas treating unit comprising an amine absorber downstream of the enclosure (20), the process comprising passing the lean gas (16) preferably after hydrogenation and quenching in the amine absorber to produce an off gas.

12. Installation for producing Sulphur from a stream (12) containing hydrogen sulfide, the installation comprising:- an enclosure (20) defining an inlet (24) to introduce a hydrogen sulfide containing stream (12), the enclosure comprising a packing bed (30) containing a catalyst, the catalyst being configured to react hydrogen sulfide from the hydrogen sulfide containing stream (12) with sulfur dioxide to form liquid Sulphur (14) and a lean gas (16) ; the enclosure (20) defining a first outlet (26) to remove the liquid Sulphur (14) from the enclosure (20) and a second outlet (28) to remove the lean gas (16) from the enclosure (20); characterized in that the packing bed (30) is configured to be driven in rotation around a rotation axis (A-A') in the enclosure (20) to evacuate the liquid Sulphur (14) from the packing bed (30).

13. Installation according to claim 12, wherein the rotary packing bed (30) comprises an upper guiding plate (48) and a lower guiding plate (50) configured to guide the mixture of hydrogen sulfide and sulfur dioxide radially away from the rotation axis (A-A’) to evacuate the liquid Sulfur (14) and the lean gas (16) peripherally out of rotary packing bed (30).

14. Installation according to any one of claims 12 or 13, comprising at least one stage upstream of the enclosure (20) producing sulfur dioxide, an acid gas feed line (110) emerging in the at least one stage upstream of the enclosure (20), the acid gas containing hydrogen sulfide, and a mixer to mix the acid gas feed (110) with an oxygen containing gas feed, in particular with air, the hydrogen sulfide containing gas (12) containing sulfur dioxide produced in the at least one stage upstream of the enclosure (20).

15. Installation according to claim 14, wherein the at least one stage upstream of the enclosure (20) comprises a Claus thermal stage (102) having a furnace (106) and a condenser (108), the condenser (108) having an outlet to extract a liquid Sulphur feed (116) from the condenser (108).

16. Installation according to claim 15, wherein the at least one stage upstream of the enclosure (20) comprises at least a Claus catalyst stage (104)downstream of the Claus thermal stage (102), the Claus catalyst stage (104) comprising a static catalyst bed reactor (126), the static catalyst bed reactor (126) having an outlet to extract the hydrogen sulfide containing gas (12), the outlet to extract the hydrogen sulfide containing gas (12) being connected to the enclosure (20), the at least one stage upstream of the enclosure (20) optionally comprising a tap feeding a stream (140) containing oxygen in the hydrogen sulfide containing gas (12), the tap being located between the outlet of the static catalyst bed reactor (126) and the inlet of the enclosure (20).

17. Installation according to any one of claims 14 to 16, wherein the rotary packing bed (30) comprises a cooler to control the operating temperature of the reaction.

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