Hydrogenation tail gas oxidation adsorption device and process for sulfur recovery device

Abstract

The invention discloses a sulfur recovery device hydrogenation tail gas oxidation adsorption device and process, and the sulfur recovery device hydrogenation tail gas oxidation adsorption device comprises a sulfur recovery device tail gas treatment unit hydrogenation reactor, a quench tower, an absorption tower, a regeneration tower and an incinerator which are connected in sequence, the gas outlet end of the incinerator is connected with two oxidation catalytic reactors which are arranged in parallel, and the outlets of the two oxidation catalytic reactors are respectively connected with the hydrogenation reactor and the purified flue gas outlet through pipelines; the oxidation catalytic reactor is also connected with a reducing gas source; incinerator tail gas is introduced into one oxidation catalytic reactor to be in an oxidation adsorption state; and reducing gas is introduced into the other oxidation catalytic reactor to be in a reduction regeneration state. According to the oxidation adsorption device and technology, the concentration of sulfur dioxide discharged by a hydrogenation tail gas incinerator of a sulfur recovery device can be smaller than 30 mg / m < 3 > and is far lower than the current strictest limit value of 100 mg / m < 3 >.

Description

Technical Field

[0001] The present invention relates to the technical field of sulfur recovery, and in particular, to a hydrogenation tail gas oxidation adsorption device and process for a sulfur recovery device. Background Art

[0002] Sulfur dioxide is the main sulfur-containing compound emitted during the processing of fossil fuels such as crude oil, natural gas, and coal. Improving the sulfur recovery rate can significantly reduce environmental pollution. With the rapid development of the economic society, environmental pollution has become a restricting factor.

[0003] In recent years, China has also paid attention to the impact of environmental pollution. Improving the utilization efficiency of renewable resources and reducing pollutant emissions are the common needs of the whole society. Therefore, more stringent restrictions have been imposed on the sulfur dioxide emission concentration. These include GB31570-2015 "Emission Standards for Pollutants from Petroleum Refining Industry", GB31571-2015 "Emission Standards for Pollutants from Petrochemical Industry", GB39728-2020 "Emission Standards for Air Pollutants from Onshore Oil and Gas Extraction Industry", etc. For refineries, in general areas, the sulfur recovery device is required to have a SO2 emission concentration of less than 400 mg / m 3 , and in some sensitive areas, less than 100 mg / m 3 . For natural gas purification plants, those with a treatment scale greater than 200 t / d are required to have an emission concentration of less than 400 mg / m 3 , and those with a treatment scale less than or equal to 200 t / d are required to have a SO2 emission concentration of less than 800 mg / m 3 . For environmentally sensitive areas, even lower sulfur dioxide emission requirements are proposed, with a sulfur dioxide emission concentration of less than 50 mg / m 3 .

[0004] Currently, through measures such as process upgrading and transformation and catalyst replacement in the original domestic sulfur recovery devices, the up-to-standard emission of sulfur dioxide during the normal operation of the sulfur recovery devices has been achieved. For example, large sulfur recovery devices use reduction absorption types (such as SCOT, SSR, HCR) to achieve a SO2 emission concentration of less than or equal to 400 mg / m 3 standard requirements, and a supporting caustic scrubbing process is used to achieve a tail gas sulfur dioxide emission of less than 100 mg / m 3 emission requirements. Medium and small-scale sulfur recovery devices use oxidation absorption types (such as Cansolv) tail gas treatment processes to meet the standard requirements of a sulfur dioxide emission concentration of less than 100 mg / m 3 standard requirements. Some sulfur recovery devices with low latent sulfur content directly use a caustic scrubbing process to treat the Claus tail gas of the sulfur recovery device.

[0005] The above method can meet the sulfur dioxide emission limit requirements of existing standards, but it has a long process flow, many devices, complex operations, requires the addition of chemicals such as ammonia and sodium hydroxide during the production process, and also produces secondary pollutants such as high-salt wastewater and waste residues. Therefore, there is no sulfur dioxide removal process with a short process flow, simple operation, and an emission concentration less than 30mg / m 3 for the following sulfur dioxide.

[0006] In addition, the existing technologies have at least the following problems:

[0007] (1) For the process of reducing and absorbing tail gas, the sulfur dioxide concentration in the flue gas can only be reduced to below 400mg / m 3 limit value, and it is difficult to further reduce the emission concentration; the process flow is long, there are many devices, not only a hydrogenation hydrolysis catalyst needs to be supported, but also a highly efficient selective desulfurization solvent under normal pressure needs to be supported; ammonia water or 30% sodium hydroxide needs to be added during the production process to adjust the pH of the quench tower, and acidic wastewater is generated during the production process; sulfur blockage is likely to occur in the quench tower due to incomplete hydrogenation; side reactions during the hydrogenation hydrolysis reaction process generate secondary pollutants such as sulfur, methanethiol, and ethanethiol due to the decrease in the inlet temperature of the hydrogenation reactor, increasing the sulfur dioxide emission concentration in the flue gas.

[0008] (2) For the alkali liquor washing method, 30% sodium hydroxide solution is used as the absorbent to absorb sulfur dioxide, and the alkali liquor consumption for absorbing a unit of sulfur dioxide is large; waste solids such as alkali residues are generated during the production process; high-salt wastewater is generated during the production process; an evaporation crystallization device needs to be supported, and the purity of the generated sulfates and sulfites is difficult to meet the industrial standard requirements.

[0009] (3) If the sulfur recovery device of the low-temperature Claus process is equipped with an oxidation absorption method device, ① the process flow is relatively long and there are many cold heat exchange devices; ② high requirements are imposed on the equipment materials, and the materials of some devices require above alloy steel; ③ concentrated sulfuric acid storage tanks and sodium hydroxide solution storage tanks need to be set in the production device area for pH adjustment during the production process, otherwise the sulfur dioxide absorption effect will be affected; ④ high-salt wastewater is generated, and the existing sewage treatment scale and methods cannot handle it.

[0010] Therefore, for the above existing process technical problems of sulfur dioxide removal for sulfur recovery devices, only the alkali liquor washing method currently meets the sulfur dioxide emission concentration less than 50mg / m 3 , but it is also impossible to further reduce the sulfur dioxide emission concentration. And many problems are exposed in the actual application of this method, such as an increase in the system pressure difference, pipeline blockage caused by alkali residue crystallization, and the inability of the sewage treatment plant to handle a large amount of high-salt wastewater, etc.

[0011] In view of this, the present application is specifically proposed. Summary of the Invention

[0012] To solve the above problems, the object of the present invention is to provide a hydrogenation tail gas oxidation adsorption device and process for a sulfur recovery device. Compared with the existing alkali liquor washing method for the reduction absorption process, the process is shorter, the equipment is less, no chemicals are added, no waste water is discharged, and no alkali residue is generated. It can achieve a sulfur dioxide concentration in the tail gas of the hydrogenation tail gas incinerator of less than 30 mg / m 3 , greatly reducing the emission of sulfur-containing pollutants and realizing the recycling of sulfur resources at the same time.

[0013] The present invention is realized through the following technical solutions:

[0014] In the first aspect, the present invention provides a hydrogenation tail gas oxidation adsorption device for a sulfur recovery device, including a hydrogenation reactor, a quench tower, an absorption tower, a regeneration tower and an incinerator which are sequentially connected in the tail gas treatment unit of the sulfur recovery device. The top of the absorption tower is connected to the intake end of the incinerator,

[0015] The outlet end of the incinerator is connected with two parallel oxidation catalytic reactors. The outlets of the two oxidation catalytic reactors are respectively connected to the hydrogenation reactor and the purified flue gas discharge port through pipelines;

[0016] The oxidation catalytic reactor is also connected with a reducing gas source;

[0017] One oxidation catalytic reactor is in an oxidation adsorption state with the incinerator tail gas introduced, and is used to adsorb sulfur dioxide in the incinerator tail gas;

[0018] The other oxidation catalytic reactor is in a reduction regeneration state with reducing gas introduced, and is used to reduce and regenerate the adsorbed sulfur dioxide and return it to the hydrogenation reactor in the tail gas treatment unit of the sulfur recovery device.

[0019] In a specific embodiment, the oxidation catalytic reactor is filled with an oxidation catalytic adsorbent, and the oxidation catalytic adsorbent includes aluminum hydroxide, a porous adsorbent material and various metal salts.

[0020] In a specific embodiment, the reaction temperature of the oxidation catalytic reactor is 300 - 600 °C, preferably 400 - 550 °C.

[0021] In a specific embodiment, the volumetric space velocity of the oxidation catalytic reactor is 100 - 2000 h -1 , preferably 500 - 1500 h -1 .

[0022] In a specific embodiment, the oxidation catalytic reactor is a vertical fixed-bed reactor, and the gas flow direction is from top to bottom.

[0023] In a specific embodiment, the gas flow rate in the reactor in the oxidation adsorption state is 5 to 20 times, preferably 10 to 15 times, that in the reactor in the reduction regeneration state.

[0024] In a specific embodiment, the reducing gas source is hydrogen, carbon monoxide or hydrogen sulfide, preferably hydrogen sulfide.

[0025] In a specific embodiment, the ratio of sulfur dioxide, hydrogen sulfide and sulfur vapor in the sulfur-containing compounds generated during reduction regeneration is 7:2:1.

[0026] In a specific embodiment, sulfur dioxide concentration detection devices are provided at the outlets of both oxidation catalytic reactors.

[0027] In a second aspect, the present invention also provides a hydrogenation tail gas oxidation adsorption process for a sulfur recovery device, based on the above oxidation adsorption device, including the following steps:

[0028] (1) The tail gas treated by the incinerator in the tail gas treatment unit of the sulfur recovery device is introduced into the reactor containing the oxidation catalytic adsorbent, and sulfur dioxide generated by the incinerator is removed by the oxidation adsorption method;

[0029] (2) After the reactor reacts for a certain period of time, a reducing gas is introduced into the reactor containing the oxidation catalytic adsorbent, and sulfur dioxide is regenerated by the reducing gas and returned to the hydrogenation reactor in the tail gas treatment unit of the sulfur recovery device;

[0030] (3) The hydrogenation reactor hydrogenates sulfur dioxide into hydrogen sulfide, and then the amine liquid in the absorption tower absorbs hydrogen sulfide;

[0031] (4) The amine liquid after absorbing hydrogen sulfide is introduced into the regeneration tower to regenerate high-concentration hydrogen sulfide and return it to the combustion furnace of the sulfur recovery device.

[0032] The oxidation adsorption device described in the present invention is connected between the incinerator and the chimney, and hydrogen sulfide, carbonyl sulfide and carbon disulfide that are not completely treated and recovered by the reduction absorption tail gas treatment device of the sulfur recovery device are all burned and converted into sulfur dioxide through the incinerator. The sulfur dioxide concentration is about 400 mg / m 3 , and then the gas containing sulfur dioxide is directly introduced into the vertical fixed-bed oxidation catalytic reactor of the present invention, and is converted and adsorbed under the catalytic action of the loaded oxidation catalytic adsorbent. The chemical reaction formula is: MxO + SO2 + 1 / 2O2 → MxSO4. The sulfur dioxide concentration of the purified flue gas coming out of the reactor is less than 30 mg / m 3 , which is much lower than the current strictest national emission limit of 100 mg / m 3 and can be directly discharged into the atmosphere through the chimney.

[0033] After running for a certain period of time, the sulfur dioxide concentration data detected by the on-line sulfur dioxide detection device set at the outlet of the reactor is close to 30 mg / m 3 When it reaches, the tail gas of the incinerator is switched to another reactor for oxidative adsorption, while reducing gas is introduced into this reactor for reduction and regeneration. The chemical reaction formula is: MxSO4 + H2S → MxO + SO2 + H2O. The sulfur dioxide-containing gas regenerated by reduction is returned to the hydrogenation reactor of the tail gas treatment unit. The hydrogenation catalyst is used to hydrogenate sulfur dioxide into hydrogen sulfide, and then the amine solution in the tail gas treatment unit is used to absorb hydrogen sulfide, achieving deep emission reduction of sulfur dioxide from the incinerator. The hydrogen sulfide acidic gas regenerated from the amine solution in the tail gas treatment unit is returned to the combustion furnace of the sulfur recovery unit for treatment, realizing the recovery and utilization of sulfur resources.

[0034] Compared with the prior art, the present invention has the following advantages and beneficial effects:

[0035] 1. The hydrogenation tail gas oxidative adsorption device and process for a sulfur recovery unit provided in the embodiment of the present invention can achieve that the sulfur dioxide concentration discharged from the incinerator of the hydrogenation tail gas of the sulfur recovery unit is less than 30 mg / m 3 , far lower than the current strictest limit of 100 mg / m 3 ;

[0036] 2. The hydrogenation tail gas oxidative adsorption device and process for a sulfur recovery unit provided in the embodiment of the present invention can be directly connected between the incinerator and the chimney of all existing supporting reduction absorption tail gas treatment devices. The raw material gas of the system comes from the existing incinerator, and the purified flue gas can be directly discharged to the chimney, while the reducing gas is supplied by the existing reduction gas system in the factory, and the modification workload is small;

[0037] 3. The hydrogenation tail gas oxidative adsorption device and process for a sulfur recovery unit provided in the embodiment of the present invention have a short process flow, few equipment, no heat exchange equipment, small floor area, low investment cost, do not require the addition of chemicals during the production process, and do not discharge waste water or waste residue, which is more environmentally friendly;

[0038] 4. The hydrogenation tail gas oxidative adsorption device and process for a sulfur recovery unit provided in the embodiment of the present invention have a small amount of sulfur dioxide regeneration gas. The regenerated sulfur dioxide is returned to the hydrogenation reactor for treatment, and has little impact on the entire sulfur recovery unit;

[0039] 5. The hydrogenation tail gas oxidative adsorption device and process for a sulfur recovery unit provided in the embodiment of the present invention use an oxidation catalytic adsorbent that can be regenerated to restore its oxidative adsorption performance and be recycled. Description of the Drawings

[0040] To more clearly illustrate the technical solutions of the exemplary embodiments of the present invention, the accompanying drawings required for the embodiments will be briefly introduced below. It should be understood that the following drawings only show certain embodiments of the present invention and should not be regarded as limiting the scope. For those of ordinary skill in the art, without creative efforts, other related drawings can also be obtained based on these drawings.

[0041] Figure 1 The structure diagram of the oxidation adsorption device provided in Embodiment 1 of the present invention, where both R1 and R2 are oxidation catalytic reactors. Detailed implementation manners

[0042] To make the objectives, technical solutions, and advantages of the present invention clearer and more understandable, the present invention will be further described in detail below in conjunction with the embodiments. The illustrative embodiments and descriptions of the present invention are only used to explain the present invention and are not intended to limit the present invention.

[0043] In the following description, a large number of specific details are set forth in order to provide a thorough understanding of the present invention. However, it is obvious to those of ordinary skill in the art that the present invention does not have to be implemented with these specific details. In other embodiments, well-known structures, circuits, materials, or methods are not specifically described to avoid obscuring the present invention.

[0044] Throughout the specification, the reference to "one embodiment", "embodiment", "one example", or "example" means that the specific features, structures, or characteristics described in connection with the embodiment or example are included in at least one embodiment of the present invention. Therefore, the phrases "one embodiment", "embodiment", "one example", or "example" appearing throughout the specification do not necessarily all refer to the same embodiment or example. In addition, the specific features, structures, or characteristics can be combined in any appropriate combination and / or sub-combination in one or more embodiments or examples. The term "and / or" used here includes any and all combinations of one or more of the related listed items.

[0045] In the description of the present invention, the orientation or positional relationship indicated by terms such as "front", "rear", "left", "right", "upper", "lower", "vertical", "horizontal", "high", "low", "inner", "outer", etc. is only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the protection scope of the present invention.

[0046] Embodiment 1

[0047] As Figure 1As shown in the figure, a hydrogenation tail gas oxidation adsorption device for a sulfur recovery device provided by an embodiment of the present invention. The present invention provides a hydrogenation tail gas oxidation adsorption device for a sulfur recovery device, including a hydrogenation reactor, a quench tower, an absorption tower, a regeneration tower, and an incinerator that are connected in sequence. The top of the absorption tower is connected to the intake end of the incinerator. It is characterized in that

[0048] The outlet end of the incinerator is connected to two oxidation catalytic reactors arranged in parallel. The outlets of the two oxidation catalytic reactors are respectively connected to the hydrogenation reactor and the purified flue gas discharge outlet through pipelines;

[0049] The oxidation catalytic reactor is also connected to a reducing gas source;

[0050] In one oxidation catalytic reactor, the incinerator tail gas is introduced and in an oxidation adsorption state, which is used to adsorb sulfur dioxide in the incinerator tail gas;

[0051] In the other oxidation catalytic reactor, reducing gas is introduced and in a reduction regeneration state, which is used to reduce and regenerate the adsorbed sulfur dioxide and return it to the hydrogenation reactor of the sulfur recovery device tail gas treatment unit.

[0052] In a specific embodiment, the oxidation catalytic reactor is filled with an oxidation catalytic adsorbent, and the oxidation catalytic adsorbent includes aluminum hydroxide, a porous adsorbent material, and various metal salts.

[0053] In a specific embodiment, the reaction temperature of the oxidation catalytic reactor is 300 - 600 °C, preferably 400 - 550 °C.

[0054] In a specific embodiment, the volumetric space velocity of the oxidation catalytic reactor is 100 - 2000 h -1 , preferably 500 - 1500 h -1 .

[0055] In a specific embodiment, the oxidation catalytic reactor is a vertical fixed-bed reactor, and the gas flow direction is from top to bottom.

[0056] In a specific embodiment, the gas flow rate in the reactor in the oxidation adsorption state is 5 - 20 times, preferably 10 - 15 times, that in the reactor in the reduction regeneration state.

[0057] In a specific embodiment, the reducing gas source uses hydrogen, carbon monoxide, or hydrogen sulfide, preferably hydrogen sulfide.

[0058] In a specific embodiment, the ratio of sulfur dioxide, hydrogen sulfide, and sulfur vapor in the sulfur-containing compounds generated by reduction regeneration is 7:2:1.

[0059] In a specific embodiment, sulfur dioxide concentration detection devices are provided at the outlets of both oxidation catalytic reactors.

[0060] The oxidation adsorption device of the invention is connected between the incinerator and the chimney. The hydrogen sulfide, carbonyl sulfide, and carbon disulfide that are not completely treated and recovered by the reduction absorption tail gas treatment device of the sulfur recovery device are completely burned and converted into sulfur dioxide through the incinerator. The sulfur dioxide concentration is about 400 mg / m 3 , and then the gas containing sulfur dioxide is directly introduced into the vertical fixed-bed oxidation catalytic reactor of the present invention, where it is converted and adsorbed under the catalytic action of the loaded oxidation catalytic adsorbent. The chemical reaction formula is: MxO + SO2 + 1 / 2O2 → MxSO4. The sulfur dioxide concentration in the purified flue gas coming out of the reactor is less than 30 mg / m 3 , which is much lower than the current strictest national emission limit of 100 mg / m 3 and can be directly discharged into the atmosphere through the chimney.

[0061] After operating for a certain period of time, when the sulfur dioxide concentration data detected by the on-line sulfur dioxide detection device provided at the outlet of the reactor is close to 30 mg / m 3 , the incinerator tail gas is switched to another reactor for oxidation adsorption, and a reducing gas is introduced into this reactor for reduction and regeneration. The chemical reaction formula is: MxSO4 + H2S → MxO + SO2 + H2O. The sulfur dioxide-containing gas regenerated by reduction is returned to the hydrogenation reactor of the tail gas treatment unit. The hydrogenation catalyst is used to hydrogenate sulfur dioxide into hydrogen sulfide, and then the amine liquid in the tail gas treatment unit is used to absorb hydrogen sulfide, achieving deep emission reduction of sulfur dioxide from the incinerator. The hydrogen sulfide acidic gas regenerated from the amine liquid in the tail gas treatment unit is returned to the combustion furnace of the sulfur recovery device for treatment, realizing the recycling of sulfur resources.

[0062] Example 2

[0063] A hydrogenation tail gas oxidation adsorption process for a sulfur recovery device provided by an embodiment of the present invention, based on the oxidation adsorption device described in the embodiment, includes the following steps:

[0064] (1) The tail gas treated by the incinerator of the sulfur recovery device tail gas treatment unit is introduced into a reactor containing an oxidation catalytic adsorbent, and sulfur dioxide generated by the incinerator is removed by the oxidation adsorption method;

[0065] (2) After the reactor has reacted for a certain period of time, a reducing gas is introduced into the reactor containing the oxidation catalytic adsorbent to regenerate sulfur dioxide and return it to the hydrogenation reactor of the sulfur recovery device tail gas treatment unit;

[0066] (3) The hydrogenation reactor hydrogenates sulfur dioxide into hydrogen sulfide, and then the amine liquid in the absorption tower is used to absorb hydrogen sulfide;

[0067] (4) The amine solution after absorbing hydrogen sulfide is introduced into the regeneration tower for reproduction, and high-concentration hydrogen sulfide is generated and returned to the combustion furnace of the sulfur recovery unit.

[0068] Example 3

[0069] A hydrogenation tail gas oxidation adsorption process for a sulfur recovery unit provided by an embodiment of the present invention is specifically as follows:

[0070] (1) When the tail gas treatment device of the sulfur recovery unit is in operation, the gas containing a small amount of hydrogen sulfide of about 150 ppm, carbonyl sulfide of about 40 ppm, and carbon disulfide of about 20 ppm at the top of the absorber is introduced into the incinerator, and a certain proportion of fuel gas and air is added, and the sulfides are all converted into sulfur dioxide;

[0071] (2) The sulfur dioxide containing 350 mg / m 3 entering the oxidation catalytic reactor R1 undergoes a chemical adsorption reaction under the action of the oxidation catalytic adsorbent, and the sulfur dioxide content in the purified flue gas coming out of the oxidation catalytic reactor R1 is 25 mg / m 3 , and it is directly discharged to the chimney and into the atmosphere;

[0072] (3) When the oxidation catalytic reactor R1 has undergone chemical adsorption for a certain time and the sulfur dioxide concentration detection device detects that the sulfur dioxide content reaches 25 mg / m 3 , through the pneumatic switching valve, the flue gas discharged from the incinerator is switched to the oxidation catalytic reactor R2 for oxidation catalytic adsorption;

[0073] (4) Heated reducing gas is introduced into the oxidation catalytic reactor R1 for regeneration. The flow rate of the reducing gas is 10% of the flue gas flow rate, and the concentration of the reducing gas is 15%. After operating for a period of time, the sulfates generated by chemical adsorption are completely reduced to sulfur dioxide and hydrogen sulfide;

[0074] (5) The regenerated gas discharged from the oxidation catalytic reactor R2 is returned to the inlet of the hydrogenation reactor. In the hydrogenation reactor, sulfur dioxide is converted into hydrogen sulfide under the action of the hydrogenation catalyst, and then the hydrogen sulfide is absorbed by the amine solution in the absorber, achieving the reduction of sulfur dioxide emissions from the incinerator.

[0075] The above specific implementation manners further elaborate on the purpose, technical solution, and beneficial effects of the present invention. It should be understood that the above is only the specific implementation manner of the present invention and is not used to limit the protection scope of the present invention. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A hydrogenation tail gas oxidation adsorption device for a sulfur recovery unit, comprising a hydrogenation reactor, a quench tower, an absorption tower, a regeneration tower and an incinerator which are connected in sequence in the tail gas treatment unit of the sulfur recovery unit. The top of the absorption tower is connected to the intake end of the incinerator. It is characterized in that, The outlet end of the incinerator is connected to two parallel oxidation catalytic reactors. The outlets of the two oxidation catalytic reactors are respectively connected to the hydrogenation reactor and the purified flue gas discharge outlet through pipelines; the oxidation catalytic reactor is also connected to a reducing gas source; One oxidation catalytic reactor is in an oxidation adsorption state with incinerator tail gas introduced, for adsorbing sulfur dioxide in the incinerator tail gas; The other oxidation catalytic reactor is in a reduction regeneration state with reducing gas introduced, for reducing and regenerating the adsorbed sulfur dioxide and returning it to the hydrogenation reactor in the tail gas treatment unit of the sulfur recovery unit.

2. The hydrogenation tail gas oxidation adsorption device of the sulfur recovery device according to claim 1, wherein The oxidation catalytic reactor is filled with an oxidation catalytic adsorbent, and the oxidation catalytic adsorbent includes aluminum hydroxide, a porous adsorption material and various metal salts.

3. The hydrogenation tail gas oxidation adsorption device of a sulfur recovery device according to claim 1, wherein, The reaction temperature of the oxidation catalytic reactor is 300 - 600 °C.

4. The hydrogenation tail gas oxidation adsorption device of a sulfur recovery device according to claim 1, characterized in that, The volumetric space velocity of the oxidation catalytic reactor is 100 to 2000 h -1 .

5. A hydrogenation tail gas oxidation adsorption device for a sulfur recovery device according to claim 1, characterized in that, The oxidation catalytic reactor is a vertical fixed bed reactor, and the gas flow direction is from top to bottom.

6. The hydrogenation tail gas oxidation adsorption device of a sulfur recovery device according to claim 1, wherein, The gas flow rate in the reactor in the oxidation adsorption state is 5 - 20 times that in the reactor in the reduction regeneration state.

7. A hydrogenation tail gas oxidation adsorption device for a sulfur recovery device according to claim 1, characterized in that, The reducing gas source uses hydrogen, carbon monoxide or hydrogen sulfide.

8. A hydrogenation tail gas oxidation adsorption device for a sulfur recovery device according to claim 1, characterized in that, In the sulfur-containing compounds generated by reduction regeneration, the ratio of sulfur dioxide, hydrogen sulfide to sulfur vapor is 7:2:

1.

9. A hydrogenation tail gas oxidation adsorption device for a sulfur recovery device according to claim 1, characterized in that, Sulfur dioxide concentration detection devices are provided at the outlets of both oxidation catalytic reactors.

10. A hydrogenation tail gas oxidation adsorption process for a sulfur recovery unit, characterized in that, Based on the oxidation adsorption device according to any one of claims 1 - 9, the following steps are included: (1) Introduce the tail gas treated by the incinerator in the tail gas treatment unit of the sulfur recovery unit into the reactor containing the oxidation catalytic adsorbent, and use the oxidation adsorption method to remove sulfur dioxide generated by the incinerator; (2) After the reactor reacts for a certain period of time, introduce reducing gas into the reactor containing the oxidation catalytic adsorbent, and use the reducing gas to regenerate sulfur dioxide and return it to the hydrogenation reactor in the tail gas treatment unit of the sulfur recovery unit; (3) The hydrogenation reactor hydrogenates to convert sulfur dioxide into hydrogen sulfide, and then uses the amine solution in the absorption tower to absorb hydrogen sulfide; (4) The amine solution after absorbing hydrogen sulfide is introduced into the regeneration tower to reproduce high-concentration hydrogen sulfide and return it to the combustion furnace of the sulfur recovery unit.

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