Sulfur-containing gas treatment process

Abstract

The invention relates to the technical field of acid gas treatment, in particular to a sulfur-containing gas treatment process. Comprising the following steps that S1, incineration treatment is conducted, specifically, sulfur-containing gas is divided into two parts, one part exchanges heat with flue gas of an incineration unit, the other part serves as a cold source to cool a regenerated adsorbent, and the two parts of sulfur-containing gas are mixed and then enter the incineration unit to be combusted to generate flue gas containing sulfur dioxide; sulfur dioxide-containing flue gas passes through a waste heat boiler and a heat exchanger to recover heat; s2, adsorption treatment: performing adsorption sulfur dioxide removal treatment on the sulfur dioxide-containing flue gas by using an adsorbent in an adsorption unit to obtain purified gas; s3, carrying out regeneration treatment; and S4, utilizing the regenerated adsorbent and recovering sulfur resources. The method can be used for simultaneously treating various sulfides and fully recycling sulfur resources, is simple in process operation and high in adaptability, can be widely applied to treatment of sulfur-containing gases in various fields, and effectively reduces the content of SO2 in flue gas.

Description

Technical Field

[0001] The invention relates to the technical field of acid gas treatment, and in particular to a sulfur-containing gas treatment process. Background Art

[0002] As we all know, in recent years, with the improvement of people's environmental awareness, my country's environmental protection laws and regulations have become increasingly stringent. In 2015, my country issued a new pollutant emission standard, "Petroleum Refining Industry Pollutant Emission Standard (GB31570-2015)", which stipulates that the special emission limit of SO2 from process heating furnace flue gas is 50mg / Nm 3 The emission limit of catalytic cracking catalyst regeneration flue gas is 100mg / Nm 3 The SO2 special emission concentration limit of the flue gas from the sulfur recovery unit is 100 mg / Nm 3 The following; and sulfur tail gas SO2 emissions are also one of the important indicators in the total pollutant verification and accounting of the Ministry of Environmental Protection. It can be seen that my country's requirements for flue gas SO2 emissions are becoming increasingly stringent. Flue gas SO2 emissions have become a major bottleneck in the development of various industries.

[0003] At present, flue gas desulfurization technologies at home and abroad are mainly divided into two major categories. The first is wet desulfurization, that is, using a certain liquid absorbent to treat the exhaust gas; such as a flue gas wet desulfurization process disclosed in a Chinese invention patent (publication (announcement) number: CN100411715C), in which a hydrated absorbent mixed liquid is sprayed down from a spray device at the top of a desulfurization tower; the flue gas enters the middle of the desulfurization tower, and contacts the hydrated absorbent in reverse in the multi-layer wire mesh area in the desulfurization tower, so that SO2 and the like in the flue gas are transferred to the liquid phase; air is introduced into the upper layer of the hydrated absorbent in the circulation tank of the hydrated absorbent at the bottom of the desulfurization tower, so that the absorbed SO2 is oxidized to form granular gypsum; an appropriate amount of the well-mixed hydrated absorbent mixed liquid at the bottom of the circulation tank is drawn out, and the larger granular gypsum therein is separated to maintain the solid concentration of the hydrated absorbent and its absorption capacity for SO2. It can maintain a high desulfurization efficiency and enhance the system operation stability, greatly reducing the desulfurization project cost and the desulfurization system operation cost. The equipment is not easy to clog and is suitable for the needs of industrial production.

[0004] The second is dry desulfurization, which uses powdered or granular adsorbents or absorbents to remove SO2 from flue gas. For example, a coke oven flue gas dry desulfurization process disclosed in a Chinese invention patent (authorization announcement number CN111773915B) uses a fluidized bed and a moving bed to couple multiple adsorptions of SO2 for efficient removal. The process specifically includes the following steps: (1) the flue gas to be treated enters the fluidized bed, and the powdered adsorbent is sprayed into the fluidized bed, and the powdered adsorbent is used to perform preliminary adsorption of SO2 in a fluidized state; (2) the flue gas treated in the fluidized bed enters the moving bed, and the granular adsorbent is transported to the moving bed, and the granular adsorbent in the moving bed is used to continue to adsorb SO2 in the flue gas; (3) the granular adsorbent on the moving bed is used to filter and intercept the dust and powdered adsorbent carried in the flue gas, and the powdered adsorbent adhered to the granular adsorbent is used to adsorb SO2 in the flue gas; (4) the flue gas treated in the moving bed enters the bag filter, and the bag filter is used to remove dust from the flue gas. Compared with the prior art, the present invention can significantly improve the flue gas dry desulfurization efficiency and the utilization rate of the desulfurizer.

[0005] At present, flue gas desulfurization in my country is basically based on imported technologies, which are mainly wet methods. The most representative and fastest-growing wet desulfurization technology is the alkaline washing desulfurization, such as the LABSORBTM technology of DuPontTM BELCO. If the wet desulfurization technology of flue gas post-alkaline washing is adopted, 50mg / Nm 3 The following are lower emissions, but this type of process produces new secondary pollutants - sodium sulfate-containing wastewater. This type of wastewater cannot be discharged directly, and the investment in the reprocessing process is huge. Summary of the invention

[0006] In view of the deficiencies in the prior art, the present invention provides a sulfur-containing gas treatment process that can simultaneously treat multiple sulfides and fully recover sulfur resources. The process operation is simple, the adaptability is strong, and the process can be widely used in the treatment of sulfur-containing gases in various fields, and can effectively reduce the SO2 content in flue gas.

[0007] To achieve the above object, the present invention provides the following technical solutions: A sulfur-containing gas treatment process comprises the following steps: S1. Incineration treatment: The sulfur-containing gas is divided into two parts, one part is used for heat exchange with the flue gas of the incineration unit, and the other part is used as a cold source to cool the regenerated adsorbent. The two parts of sulfur-containing gas are mixed and then enter the incineration unit for combustion to obtain sulfur dioxide-containing flue gas; S2. Adsorption treatment: The adsorption unit uses an adsorbent to adsorb and remove sulfur dioxide from the sulfur dioxide-containing flue gas to obtain purified gas; S3, regeneration treatment: the regeneration unit performs thermal regeneration treatment on the adsorbent to be regenerated obtained after the adsorption and desulfurization treatment to obtain the regenerated adsorbent and the regeneration gas containing sulfur dioxide; S4. Utilization of regenerated adsorbent and recovery of sulfur resources: the regenerated adsorbent is circulated back to the adsorption unit to continue to remove sulfur dioxide; the regenerated gas containing sulfur dioxide enters the sulfur recovery unit to recover sulfur or is used to produce sulfuric acid.

[0008] Preferably, in step S4, the flue gas from the incineration unit is used as the regeneration gas source. The regeneration gas source carries the regeneration gas containing a relatively high concentration of sulfur dioxide generated during the regeneration process, which is dedusted by a dust collector and then sent to a sulfur recovery device by a regeneration fan to further recover sulfur resources or be used to produce sulfuric acid.

[0009] Preferably, the incineration unit comprises an incinerator, a waste heat boiler and a heat exchanger connected in sequence; In step S1, the sulfur-containing gas is heated to 110-150°C by the heat exchanger with the flue gas and then enters the incinerator. The sulfur dioxide-containing flue gas generated by the incinerator is cooled to 240-280°C by the waste heat boiler and then enters the heat exchanger to exchange heat with the sulfur-containing gas. The flue gas is further cooled to 140-180°C and then enters the adsorption unit.

[0010] Preferably, the adsorption unit in step S2 comprises a mobile adsorption bed, which is provided with a storage layer, an adsorption layer and a discharge layer in sequence from bottom to top, an isolation baffle is provided between the storage layer and the adsorption layer, and an isolation baffle is also provided between the discharge layer and the adsorption layer; The sulfur dioxide-containing flue gas from the incineration unit enters from the gas inlet at the bottom of the adsorption layer. The flue gas entering the adsorption layer moves from bottom to top and contacts with the adsorbent for adsorption and desulfurization. The adsorption temperature is 150-190℃ and the flue gas space velocity is 400-1000h -1 , SO2 contained in the flue gas is removed, and purified gas is obtained at the outlet of the adsorption layer; During the process of adsorption and removal of sulfur dioxide, the purification effect is monitored by an online flue gas analyzer. When the SO2 content in the purified gas is stable and there is no obvious upward trend, it indicates that the adsorption can continue; when the SO2 content in the purified gas gradually increases and the upward trend is obvious, it indicates that the adsorbent needs to be regenerated. At this time, the isolation baffle between the adsorption layer and the unloading layer is opened, and the adsorbent to be regenerated is unloaded to the unloading layer. At the same time, the isolation baffle between the storage layer and the adsorption layer is opened, and fresh adsorbent is added to the adsorption layer to continue to adsorb and remove sulfur dioxide.

[0011] Preferably, in step S3, the regeneration unit comprises a regenerator, a regeneration layer is provided at the top of the regenerator, a cooling layer is provided at the bottom of the regenerator, and a heating mechanism is provided in the regeneration layer; After the adsorbent to be regenerated produced by the adsorption unit is sent to the regeneration layer, the heating mechanism heats and regenerates the adsorbent to be regenerated. The regeneration temperature is 380-400℃ and the air velocity is 500-1000h -1 ; In step S4, the regenerated adsorbent is unloaded from the regeneration layer into the cooling layer and cooled under the action of part of the sulfur-containing gas. The regenerated adsorbent is cooled to 50-80°C. The cooled regenerated adsorbent is dedusted by a dust collector and then enters the adsorption unit for recycling.

[0012] Preferably, the sulfur-containing gas refers to a gas containing one or more sulfides such as hydrogen sulfide, sulfur dioxide, elemental sulfur, COS, mercaptans, sulfides, disulfides, etc. produced in the fields of natural gas purification, refining and coal chemical industry. In addition to sulfides, its components also include CO2, N2, H2O, NH3 and hydrocarbons.

[0013] Preferably, the total sulfur content of the sulfur-containing gas is 0-2000ppm; further, the total sulfur content is preferably 0-1000ppm. To ensure the desulfurization effect, it is recommended to use nitrogen to appropriately dilute the sulfur-containing gas with a sulfur content higher than 2000ppm before treatment.

[0014] Preferably, the incineration tail gas includes water vapor, O2, SO2, N2, CO2 and CO; Preferably, the adsorbent is selected from at least one of activated carbon, activated coke, metal oxide and molecular sieve; further, activated carbon is preferred.

[0015] Preferably, the metal oxide includes but is not limited to copper oxide, iron oxide or zinc oxide, etc.; further, copper oxide is preferred.

[0016] Preferably, the molecular sieve includes but is not limited to X-type molecular sieve, Y-type molecular sieve or NaY molecular sieve; further, including but not limited to the above molecular sieves, preferably NaY molecular sieve.

[0017] Preferably, the initial sulfur capacity of the adsorbent is 100-250 g sulfur / 1000 g adsorbent.

[0018] Preferably, the content of SO2 in the purified gas obtained by the mobile adsorption bed for desulfurization is ≤10mg / m 3 ; further, preferably ≤5mg / m 3 .

[0019] Compared with the prior art, the present invention provides a sulfur-containing gas treatment process, which has the following beneficial effects: (1) Use a mobile adsorption bed to adsorb SO2 from flue gas and reduce the SO2 emission concentration in flue gas to less than 10 mg / m 3 , achieving near-zero emissions.

[0020] (2) It can be used to treat tail gas containing various sulfides, promote the treatment of sulfur-containing waste gas in various industries, and solve the development bottlenecks in the fields of refining, natural gas chemical industry and coal chemical industry.

[0021] (3) A closed-loop circulation of sulfur is achieved during operation. The regenerated gas containing sulfur dioxide produced after the adsorbent is regenerated can be returned to the sulfur recovery unit to continue to recover sulfur resources or be used to produce sulfuric acid.

[0022] (4) Utilizing the waste heat generated inside the device can effectively reduce the overall energy consumption of the system.

[0023] (5) Using incinerator flue gas as the regeneration gas source effectively saves nitrogen consumption.

[0024] (6) The process is simple, with few equipments, easy operation and control, low investment and no secondary pollution. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] Figure 1 It is a schematic diagram of the process flow of the present invention.

[0026] Markings in the accompanying drawings: 1. Incineration unit 11, sulfur-containing gas 12, incinerator 13, waste heat boiler 14, heat exchanger; 2. Adsorption unit 21, mobile adsorption bed 211, storage layer 212, adsorption layer 213, unloading layer 22, chimney 23, first hoist 24, first dust collector; 3. Regeneration unit 31, regenerator 311, regeneration layer 312, cooling layer 32, second dust collector 33, regeneration fan 34, regeneration gas 35, second elevator 36, regeneration gas source. DETAILED DESCRIPTION

[0027] The following will be combined with the drawings in the embodiments of the present invention to clearly and completely describe the technical solutions in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0028] See also Figure 1 A sulfur-containing gas treatment process of the present invention comprises the following steps: S1. Incineration treatment: The sulfur-containing gas 11 is divided into two parts, one part is used for heat exchange with the flue gas generated by the incinerator 12 of the incineration unit 1, and the other part is used as a cold source to cool the regenerated adsorbent. The two parts of the sulfur-containing gas 11 are mixed and enter the furnace of the incinerator 12 to mix with the fuel gas and air to undergo a thermal reaction to obtain sulfur dioxide-containing flue gas; the sulfur dioxide-containing flue gas recovers heat through a waste heat boiler 13 and a heat exchanger 14.

[0029] The sulfur-containing gas 11 is heat-exchanged with the flue gas generated by the incinerator 12 to 110-150°C through the heat exchanger 14 and then enters the incinerator 12. The furnace temperature in the incinerator 12 is 600-750°C. Thermal incineration is carried out under the action of fuel gas and air. The generated sulfur dioxide-containing flue gas is cooled to 240-280°C by the waste heat boiler 13, enters the heat exchanger 14 to exchange heat with the sulfur-containing gas 11, and is further cooled to 140-180°C before entering the adsorption unit 2.

[0030] S2. Adsorption treatment: In adsorption unit 2, the sulfur dioxide-containing flue gas is subjected to adsorption and desulfurization treatment using an adsorbent to obtain purified gas.

[0031] The adsorption unit 2 includes an adsorption bed 21, a chimney 22 and a first elevator 23. The adsorption bed 21 is provided with a discharge layer 213, an adsorption layer 212 and a storage layer 211 from bottom to top. An isolation baffle is provided between the storage layer 211 and the adsorption layer 212, and an isolation baffle is also provided between the adsorption layer 212 and the discharge layer 213. The chimney 22 is connected to the upper part of the adsorption layer 212, and the first elevator 23 is connected between the discharge layer 213 and the regeneration unit 3.

[0032] The sulfur-containing flue gas after cooling enters the bottom gas inlet of the adsorption layer 212 of the mobile adsorption bed 21. The flue gas entering the adsorption layer 212 moves from bottom to top and contacts with the adsorbent to undergo adsorption and desulfurization treatment. The adsorption temperature is 150-190°C and the air velocity of the flue gas is 400-1000h -1 , SO2 contained in the flue gas is removed, and purified flue gas is obtained at the outlet of the adsorption layer 212; the purified gas is discharged through the chimney 22.

[0033] During the process of adsorption and removal of sulfur dioxide, the purification effect is monitored by an online flue gas analyzer. When the SO2 content in the purified gas is stable and there is no obvious upward trend, it indicates that the adsorption can continue; when the SO2 content in the purified gas gradually increases and the upward trend is obvious, it indicates that the adsorbent needs to be regenerated. At this time, the isolation baffle between the adsorption layer 212 and the unloading layer 213 is opened, and the adsorbent to be regenerated is unloaded to the unloading layer 213. At the same time, the isolation baffle between the storage layer 211 and the adsorption layer 212 is opened, and fresh adsorbent is added to the adsorption layer 212 to continue to adsorb and remove sulfur dioxide.

[0034] The adsorbent to be regenerated in the unloading layer 213 is lifted by the first lifting machine 23 to the regeneration unit 3 for regeneration treatment.

[0035] S3, regeneration treatment: the regeneration unit 3 regenerates the adsorbent to be regenerated. The regeneration unit 3 comprises a regenerator 31, a regeneration layer 311 is arranged on the upper part of the regenerator 31, a cooling layer 312 is arranged on the lower part of the regenerator 31, and an electric ceramic furnace is arranged in the regeneration layer 311.

[0036] The adsorbent to be regenerated is sent to the regeneration layer 311 of the regenerator 31 by the first elevator 23. The adsorbent to be regenerated is subjected to thermal regeneration treatment by an electric ceramic furnace after the adsorption and desulfurization treatment to obtain a regenerated adsorbent and a regeneration gas containing sulfur dioxide 34. The regeneration temperature is 380-400°C and the air velocity is 500-1000h -1 .

[0037] S4. Utilization of regenerated adsorbent and recovery of sulfur resources: the regenerated adsorbent is circulated back to the adsorption unit 2 to adsorb sulfur dioxide; the regenerated gas 34 containing sulfur dioxide enters the sulfur recovery unit to recover sulfur or is used to produce sulfuric acid; the flue gas of the incineration unit 1 is used as the regeneration gas source 36, and the regeneration gas source 36 carries the regeneration gas 34 containing a relatively high concentration of sulfur dioxide generated during the regeneration process, and after dust removal by the second dust collector 32, it is sent to the sulfur recovery device by the regeneration fan 33 to further recover sulfur resources or be used to produce sulfuric acid.

[0038] The regenerated adsorbent after high-temperature regeneration is discharged from the regeneration layer 311 into the cooling layer 312, and is cooled to 50-80°C under the action of part of the sulfur-containing gas 11. The part of the sulfur-containing gas 11 after absorbing heat returns to the incinerator 12 of the incineration unit 1 for thermal incineration reaction.

[0039] The cooled regenerated adsorbent is sent to the first dust collector 24 through the second elevator 35 for dust removal and then enters the storage layer 211 of the mobile adsorption bed 21 for recycling.

[0040] Specifically, sulfur-containing gas 11 refers to gas containing one or more sulfides such as hydrogen sulfide, sulfur dioxide, elemental sulfur, COS, mercaptan, sulfide, disulfide, etc. produced in the fields of natural gas purification, refining and coal chemical industry. Its components include CO2, N2, H2O, NH3 and hydrocarbons in addition to sulfides. In sulfur-containing gas 11, the total sulfur content is 0-2000ppm; further, the total sulfur content is preferably 0-1000ppm. In order to ensure the desulfurization effect, it is recommended to use nitrogen to appropriately dilute the sulfur-containing gas 11 with a sulfur content higher than 2000ppm before processing. Incineration tail gas includes water vapor, O2, SO2, N2, CO2 and CO.

[0041] The adsorbent of the adsorption unit 2 is selected from at least one of activated carbon, activated coke, metal oxides and molecular sieves; further, activated carbon is preferred.

[0042] The above-mentioned metal oxide includes one of copper oxide, iron oxide or zinc oxide, preferably copper oxide. The above-mentioned molecular sieve includes but is not limited to X-type molecular sieve, Y-type molecular sieve or NaY molecular sieve, preferably NaY molecular sieve.

[0043] The present invention will be further described below in conjunction with specific embodiments.

[0044] Embodiment 1: The process of the present invention is used to treat sulfur-containing gas (H2S 200ppm, CO2 5v%, H2O 5v%, COS 86ppm, hydrocarbons 1v%, and the rest is nitrogen) produced by a sulfur unit of a refinery, and the steps are as follows: (1) Thermal incineration unit 1 treatment: A portion of the sulfur-containing gas 11 is heat-exchanged with the flue gas generated by the incinerator 12 to 135°C through the heat exchanger 14 and then enters the incinerator 12 (furnace temperature 650°C) for thermal incineration under the action of fuel gas and air. The generated sulfur dioxide-containing flue gas is cooled to 250°C by the waste heat boiler 13 and then enters the heat exchanger 14 for heat exchange with the sulfur-containing gas 11. It is further cooled to 155°C and then enters the adsorption unit 2.

[0045] (2) Adsorption unit 2 treatment The sulfur-containing flue gas after cooling enters the adsorption layer 212 of the adsorption bed 21 through the bottom gas inlet. The flue gas entering the adsorption layer 212 moves from bottom to top and contacts with the adsorbent (activated carbon adsorbent with an initial sulfur capacity of 160g sulfur / 1000g) to undergo adsorption and desulfurization treatment (adsorption temperature is 160°C, flue gas space velocity is 500h -1 ), the SO2 contained in the flue gas is removed, and purified flue gas is obtained at the outlet of the adsorption layer 212; the purified gas is discharged through the chimney 22.

[0046] During the process of adsorption and removal of sulfur dioxide, the purification effect is monitored by an online flue gas analyzer. When the SO2 content in the purified gas is stable and there is no obvious upward trend, it indicates that the adsorption can continue; when the SO2 content in the purified gas gradually increases and the upward trend is obvious, it indicates that the adsorbent needs to be regenerated. At this time, the isolation baffle between the adsorption layer 212 and the unloading layer 213 is opened, and the adsorbent to be regenerated is unloaded to the unloading layer 213. At the same time, the isolation baffle between the storage layer 211 and the adsorption layer 212 is opened, and fresh adsorbent is added to the adsorption layer 212 to continue to adsorb and remove sulfur dioxide.

[0047] The cooled regenerated adsorbent is sent to the first dust collector 24 through the second elevator 35 for dust removal and then enters the storage layer 211 of the mobile adsorption bed 21 for recycling.

[0048] (3) Regeneration unit 3 processing: After the adsorbent to be regenerated is sent to the regeneration layer 311 of the regenerator 31 by the first elevator 23, the adsorbent to be regenerated is heated and regenerated by the electric ceramic furnace (regeneration temperature 380°C, air velocity 800h -1 ), the flue gas of the incinerator 12 is used as the regeneration gas source 36 to carry the regeneration gas 34 containing a relatively high concentration of sulfur dioxide generated during the regeneration process. The regeneration gas 34 is dedusted by the second dust collector 32 and then sent to the sulfur recovery device by the regeneration fan 33 to further recover sulfur resources.

[0049] The regenerated adsorbent after high-temperature regeneration is discharged from the regeneration layer 311 into the cooling layer 312, and is cooled (cooled to 60°C) under the action of part of the sulfur-containing gas 11. The part of the sulfur-containing gas 11 that has absorbed heat returns to the incineration unit 1 for thermal incineration reaction.

[0050] The cooled regenerated adsorbent is sent to the storage layer 211 of the moving adsorption bed 21 through the second elevator 35 for recycling.

[0051] From system startup to 80h of operation, the SO2 concentration in the purified gas was 0mg / m 3 ; After the system was operated for 126 hours, the SO2 concentration in the purified gas reached 3.5 mg / m 3 At this time, the adsorbent in the adsorption layer 212 of the adsorption unit 2 is unloaded into the unloading layer 213 to prepare for regeneration. At the same time, the adsorbent in the storage layer 211 enters the adsorption layer 212 to continue to play an adsorption role, and the SO2 concentration of the flue gas of the device drops to 0mg / m 3 The adsorbent in the discharge layer 213 is sent to the regenerator 31 for regeneration, and the regenerated adsorbent is continuously sent to the storage layer 211 of the adsorption unit 2 for standby use. During the entire operation cycle of the device, the SO2 emission is always kept low (the content of SO2 in the purified gas is less than 5mg / m 3 ).

[0052] Embodiment 2: like Figure 1 As shown, the process of the present invention is used to treat sulfur-containing gas 11 (H2S 235ppm, CO2 2v%, H2O 5v%, COS 121ppm, hydrocarbons 2v%, and the rest is nitrogen) produced by a natural gas purification plant, and the steps are as follows: (1) Thermal incineration unit 1 treatment: The sulfur-containing gas 11 is heat-exchanged with the flue gas generated by the incinerator 12 to 140°C through the heat exchanger 14 and then enters the incinerator 12 (furnace temperature 660°C) for thermal incineration under the action of fuel gas and air. The generated sulfur dioxide-containing flue gas is cooled to 260°C by the waste heat boiler 13 and then enters the heat exchanger 14 for heat exchange with the sulfur-containing gas 11. It is further cooled to 160°C and then enters the adsorption unit 2.

[0053] (2) Adsorption unit 2 treatment: The sulfur-containing flue gas after cooling enters the adsorption layer 212 of the adsorption bed 21 through the bottom gas inlet. The flue gas entering the adsorption layer 212 moves from bottom to top and contacts with the adsorbent (activated carbon adsorbent with an initial sulfur capacity of 180g sulfur / 1000g) to undergo adsorption and desulfurization treatment (adsorption temperature is 165°C, flue gas space velocity is 600h -1 ), the SO2 contained in the flue gas is removed, and purified flue gas is obtained at the outlet of the adsorption layer 212; the purified gas is discharged through the chimney 22.

[0054] During the process of adsorption and removal of sulfur dioxide, the purification effect is monitored by an online flue gas analyzer. When the SO2 content in the purified gas is stable and there is no obvious upward trend, it indicates that the adsorption can continue; when the SO2 content in the purified gas gradually increases and the upward trend is obvious, it indicates that the adsorbent needs to be regenerated. At this time, the isolation baffle between the adsorption layer 212 and the unloading layer 213 is opened, and the adsorbent to be regenerated is unloaded to the unloading layer 213. At the same time, the isolation baffle between the storage layer 211 and the adsorption layer 212 is opened, and fresh adsorbent is added to the adsorption layer 212 to continue to adsorb and remove sulfur dioxide.

[0055] The cooled regenerated adsorbent is sent to the first dust collector 24 through the second elevator 35 for dust removal and then enters the storage layer 211 of the mobile adsorption bed 21 for recycling.

[0056] (3) Regeneration unit 3 processing: After the adsorbent to be regenerated is sent to the regeneration layer 311 of the regenerator 31 by the first elevator 23, the adsorbent to be regenerated is heated and regenerated by the electric ceramic furnace (regeneration temperature 385°C, air velocity 600h -1 ), the flue gas from the incinerator 12 is used as the regeneration gas source 36 to carry the regeneration gas 34 containing a relatively high concentration of sulfur dioxide generated during the regeneration process, which is then dedusted by the second dust collector 32 and sent to the sulfur recovery device by the regeneration fan 33 to further recover sulfur resources.

[0057] The regenerated adsorbent after high-temperature regeneration is discharged from the regeneration layer 311 into the cooling layer 312, and is cooled (cooled to 55°C) under the action of part of the sulfur-containing gas 11. The part of the sulfur-containing gas 11 that has absorbed heat returns to the incineration unit 1 for thermal incineration reaction.

[0058] The cooled regenerated adsorbent is sent to the storage layer 211 of the moving adsorption bed 21 through the second elevator 35 for recycling.

[0059] From system startup to 92h of operation, the SO2 concentration in the purified gas was 0mg / m 3 ; After the system was operated for 148 hours, the SO2 concentration in the purified gas reached 2.9 mg / m 3At this time, the adsorbent in the adsorption layer 212 of the adsorption unit 2 is unloaded into the unloading layer 213 to prepare for regeneration. At the same time, the adsorbent in the storage layer 211 enters the adsorption layer 212 to continue to play an adsorption role, and the SO2 concentration of the flue gas of the device drops to 0mg / m 3 The adsorbent in the discharge layer 213 is sent to the regenerator 31 for regeneration, and the regenerated adsorbent is continuously sent to the storage layer 211 of the adsorption unit 2 for standby use. During the entire operation cycle of the device, the SO2 emission is always kept low (the content of SO2 in the purified gas is less than 5mg / m 3 ).

[0060] Embodiment 3: like Figure 1 As shown, the process of the present invention is used to treat sulfur-containing gas 11 (H2S 3000ppm, CO2 15v%, H2O 6v%, COS 252ppm, hydrocarbons 1v%, and the rest is nitrogen) generated by a coal chemical enterprise. Since the sulfur content of the gas is high, it needs to be diluted and treated. Nitrogen is used to dilute the gas. After dilution, the H2S concentration is 1230ppm. The treatment steps are as follows: (1) Incineration unit 1 treatment: The sulfur-containing gas 11 is heat-exchanged with the flue gas generated by the incinerator 12 to 150°C through the heat exchanger 14 and then enters the incinerator 12 (furnace temperature 700°C) for thermal incineration under the action of fuel gas and air. The generated sulfur dioxide-containing flue gas is cooled to 270°C by the waste heat boiler 13, enters the heat exchanger 14 for heat exchange with the sulfur-containing gas 11, and is further cooled to 165°C before entering the adsorption unit 22.

[0061] (2) Adsorption unit 2 treatment: The sulfur-containing flue gas after cooling enters the adsorption layer 212 of the adsorption bed 21 through the bottom gas inlet. The flue gas entering the adsorption layer 212 moves from bottom to top and contacts with the adsorbent (activated carbon adsorbent with an initial sulfur capacity of 200g sulfur / 1000g) to undergo adsorption and desulfurization treatment (the adsorption temperature is 170°C and the flue gas space velocity is 400h -1 ), the SO2 contained in the flue gas is removed, and purified flue gas is obtained at the outlet of the adsorption layer 212; the purified gas is discharged through the chimney 22.

[0062] During the process of adsorption and removal of sulfur dioxide, the purification effect is monitored by an online flue gas analyzer. When the SO2 content in the purified gas is stable and there is no obvious upward trend, it indicates that the adsorption can continue; when the SO2 content in the purified gas gradually increases and the upward trend is obvious, it indicates that the adsorbent needs to be regenerated. At this time, the isolation baffle between the adsorption layer 212 and the unloading layer 213 is opened, and the adsorbent to be regenerated is unloaded to the unloading layer 213. At the same time, the isolation baffle between the storage layer 211 and the adsorption layer 212 is opened, and fresh adsorbent is added to the adsorption layer 212 to continue to adsorb and remove sulfur dioxide.

[0063] The cooled regenerated adsorbent is sent to the first dust collector 24 through the second elevator 35 for dust removal and then enters the storage layer 211 of the mobile adsorption bed 21 for recycling.

[0064] (3) Regeneration unit 3 processing: After the adsorbent to be regenerated is sent to the regeneration layer 311 of the regenerator 31 by the first elevator 23, the adsorbent to be regenerated is heated and regenerated by the electric ceramic furnace (regeneration temperature 390°C, air velocity 500h -1） The regeneration gas 34 containing a relatively high concentration of sulfur dioxide generated during the regeneration process is dedusted by the second dust collector 32 and then sent to the sulfur recovery device by the regeneration fan 33 to further recover sulfur resources.

[0065] The regenerated adsorbent after high-temperature regeneration is discharged from the regeneration layer 311 into the cooling layer 312, and is cooled (cooled to 50°C) under the action of part of the sulfur-containing gas 11. The part of the sulfur-containing gas 11 that has absorbed heat returns to the incineration unit 1 for thermal incineration reaction.

[0066] The cooled regenerated adsorbent is sent to the storage layer 211 of the moving adsorption bed 21 through the second elevator 35 for recycling.

[0067] From system startup to 68h of operation, the SO2 concentration in the purified gas was 0mg / m 3 ; After the system was operated for 88 hours, the SO2 concentration in the purified gas reached 5mg / m 3 At this time, the adsorbent in the adsorption layer 212 of the adsorption unit 2 is unloaded into the unloading layer 213 to prepare for regeneration. At the same time, the adsorbent in the storage layer 211 enters the adsorption layer 212 to continue to play an adsorption role, and the SO2 concentration of the flue gas of the device drops to 0mg / m 3 The adsorbent in the discharge layer 213 is sent to the regenerator 31 for regeneration, and the regenerated adsorbent is continuously sent to the storage layer 211 of the adsorption unit 2 for standby use. During the entire operation cycle of the device, the SO2 emission is always kept low (the content of SO2 in the purified gas is less than 5mg / m 3 ).

[0068] Embodiment 4: like Figure 1 As shown, the process of the present invention is used to treat sulfur-containing tail gas (H2S 152ppm, COS 65ppm, mercaptan 212ppm) of a chemical enterprise, and the steps are as follows: (1) Incineration unit 1 treatment: The sulfur-containing gas 11 is heat-exchanged with the flue gas generated by the incinerator 12 to 145°C through the heat exchanger 14 and then enters the incinerator 12 (furnace temperature 680°C) for thermal incineration under the action of fuel gas and air. The generated sulfur dioxide-containing flue gas is cooled to 265°C by the waste heat boiler 13, enters the heat exchanger 14 for heat exchange with the sulfur-containing gas 11, and is further cooled to 150°C before entering the adsorption unit 22.

[0069] (2) Adsorption unit 2 treatment: The sulfur-containing flue gas after cooling enters the adsorption layer 212 of the adsorption bed 21 through the bottom gas inlet. The flue gas entering the adsorption layer 212 moves from bottom to top and contacts with the adsorbent (activated carbon adsorbent with an initial sulfur capacity of 170g sulfur / 1000g) to undergo adsorption and desulfurization treatment (the adsorption temperature is 160°C and the flue gas space velocity is 800h -1 ), the SO2 contained in the flue gas is removed, and purified flue gas is obtained at the outlet of the adsorption layer 212; the purified gas is discharged through the chimney 22.

[0070] During the process of adsorption and removal of sulfur dioxide, the purification effect is monitored by an online flue gas analyzer. When the SO2 content in the purified gas is stable and there is no obvious upward trend, it indicates that the adsorption can continue; when the SO2 content in the purified gas gradually increases and the upward trend is obvious, it indicates that the adsorbent needs to be regenerated. At this time, the isolation baffle between the adsorption layer 212 and the unloading layer 213 is opened, and the adsorbent to be regenerated is unloaded to the unloading layer 213. At the same time, the isolation baffle between the storage layer 211 and the adsorption layer 212 is opened, and fresh adsorbent is added to the adsorption layer 212 to continue to adsorb and remove sulfur dioxide.

[0071] The cooled regenerated adsorbent is sent to the first dust collector 24 through the second elevator 35 for dust removal and then enters the storage layer 211 of the mobile adsorption bed 21 for recycling.

[0072] (3) Regeneration unit 3 processing: After the adsorbent to be regenerated is sent to the regeneration layer 311 of the regenerator 31 by the first elevator 23, the adsorbent to be regenerated is heated and regenerated by the electric ceramic furnace (regeneration temperature 380°C, air velocity 800h -1 ), the regeneration gas 34 containing a relatively high concentration of sulfur dioxide generated during the regeneration process is dedusted by the second dust collector 32 and then sent to the sulfur recovery device by the regeneration fan 33 to further recover sulfur resources.

[0073] The regenerated adsorbent after high-temperature regeneration is discharged from the regeneration layer 311 into the cooling layer 312, and is cooled (cooled to 65°C) under the action of part of the sulfur-containing gas 11. The part of the sulfur-containing gas 11 that has absorbed heat returns to the incineration unit 1 for thermal incineration reaction.

[0074] The cooled regenerated adsorbent is sent to the storage layer 211 of the moving adsorption bed 21 through the second elevator 35 for recycling.

[0075] From system startup to 87h of operation, the SO2 concentration in the purified gas was 0mg / m 3 ; After the system was operated for 138 hours, the SO2 concentration in the purified gas reached 4.6 mg / m 3 At this time, the adsorbent in the adsorption layer 212 of the adsorption unit 2 is unloaded into the unloading layer 213 to prepare for regeneration. At the same time, the adsorbent in the storage layer 211 enters the adsorption layer 212 to continue to play an adsorption role, and the SO2 concentration of the flue gas of the device drops to 0mg / m 3 The adsorbent in the discharge layer 213 is sent to the regenerator 31 for regeneration, and the regenerated adsorbent is continuously sent to the storage layer 211 of the adsorption unit 2 for standby use. During the entire operation cycle of the device, the SO2 emission is always kept low (the content of SO2 in the purified gas is less than 5mg / m 3 ).

[0076] Embodiment 5: like Figure 1 As shown, the process of the present invention is used to treat sulfur-containing gas 11 (H2S 85ppm, COS 156ppm, mercaptan 218ppm, disulfide 106ppm) generated by a certain refinery, and the steps are as follows: (1) Incineration unit 1 treatment: The sulfur-containing gas 11 is heat-exchanged with the flue gas generated by the incinerator 12 to 125°C through the heat exchanger 14 and then enters the incinerator 12 (furnace temperature 635°C) for thermal incineration under the action of fuel gas and air. The generated sulfur dioxide-containing flue gas is cooled to 245°C by the waste heat boiler 13 and then enters the heat exchanger 14 for heat exchange with the sulfur-containing gas 11. It is further cooled to 140°C and then enters the adsorption unit 22.

[0077] (2) Adsorption unit 2 treatment: The sulfur-containing flue gas after cooling enters the adsorption layer 212 of the adsorption bed 21 through the bottom gas inlet. The flue gas entering the adsorption layer 212 moves from bottom to top and contacts with the adsorbent (activated carbon adsorbent with an initial sulfur capacity of 125g sulfur / 1000g) to undergo adsorption and desulfurization treatment (adsorption temperature is 150°C, flue gas space velocity is 1000h -1 ), the SO2 contained in the flue gas is removed, and purified flue gas is obtained at the outlet of the adsorption layer 212; the purified gas is discharged through the chimney 22.

[0078] During the process of adsorption and removal of sulfur dioxide, the purification effect is monitored by an online flue gas analyzer. When the SO2 content in the purified gas is stable and there is no obvious upward trend, it indicates that the adsorption can continue; when the SO2 content in the purified gas gradually increases and the upward trend is obvious, it indicates that the adsorbent needs to be regenerated. At this time, the isolation baffle between the adsorption layer 212 and the unloading layer 213 is opened, and the adsorbent to be regenerated is unloaded to the unloading layer 213. At the same time, the isolation baffle between the storage layer 211 and the adsorption layer 212 is opened, and fresh adsorbent is added to the adsorption layer 212 to continue to adsorb and remove sulfur dioxide.

[0079] The cooled regenerated adsorbent is sent to the first dust collector 24 through the second elevator 35 for dust removal and then enters the storage layer 211 of the mobile adsorption bed 21 for recycling.

[0080] (3) Regeneration unit 3 processing: After the adsorbent to be regenerated is sent to the regeneration layer 311 of the regenerator 31 by the first elevator 23, the adsorbent to be regenerated is heated and regenerated by the electric ceramic furnace (regeneration temperature 390°C, air velocity 1000h -1 ), the regeneration gas 34 containing a relatively high concentration of sulfur dioxide generated during the regeneration process is dedusted by the second dust collector 32 and then sent to the sulfur recovery device by the regeneration fan 33 to further recover sulfur resources.

[0081] The regenerated adsorbent after high-temperature regeneration is discharged from the regeneration layer 311 into the cooling layer 312, and is cooled (cooled to 80°C) under the action of part of the sulfur-containing gas 11. The part of the sulfur-containing gas 11 that has absorbed heat returns to the incineration unit 1 for thermal incineration reaction.

[0082] The cooled regenerated adsorbent is sent to the storage layer 211 of the moving adsorption bed 21 through the second elevator 35 for recycling.

[0083] From system startup to 62h of operation, the SO2 concentration in the purified gas was 0mg / m 3 ; After the system was in operation for 83 hours, the SO2 concentration in the purified gas reached 6.8 mg / m 3 At this time, the adsorbent in the adsorption layer 212 of the adsorption unit 2 is unloaded into the unloading layer 213 to prepare for regeneration. At the same time, the adsorbent in the storage layer 211 enters the adsorption layer 212 to continue to play an adsorption role, and the SO2 concentration of the flue gas of the device drops to 0mg / m 3 The adsorbent in the discharge layer 213 is sent to the regenerator 31 for regeneration, and after regeneration, the adsorbent is continuously sent to the storage layer 211 of the adsorption unit 2 for standby use. During the entire operation cycle of the device, the SO2 emission is always kept low (the content of SO2 in the purified gas is less than 10mg / m 3 ).

[0084] Embodiment 6: like Figure 1As shown, the process of the present invention is used to treat sulfur-containing gas 11 (H2S 213ppm, COS 103ppm, mercaptan 56ppm, sulfide 86ppm) produced by a natural gas purification enterprise, and the steps are as follows: (1) Incineration unit 1 treatment: The sulfur-containing gas 11 is heat-exchanged with the flue gas generated by the incinerator 12 to 150°C through the heat exchanger 14 and then enters the incinerator 12 (furnace temperature 750°C) for thermal incineration under the action of fuel gas and air. The generated sulfur dioxide-containing flue gas is cooled to 280°C by the waste heat boiler 13, enters the heat exchanger 14 for heat exchange with the sulfur-containing gas 11, and is further cooled to 180°C before entering the adsorption unit 22.

[0085] (2) Adsorption unit 2 treatment: The sulfur-containing flue gas after cooling enters the adsorption layer 212 of the adsorption bed 21 through the bottom gas inlet. The flue gas entering the adsorption layer 212 moves from bottom to top and contacts with the adsorbent (activated carbon adsorbent with an initial sulfur capacity of 150g sulfur / 1000g) to undergo adsorption and desulfurization treatment (the adsorption temperature is 190°C and the flue gas space velocity is 1000h -1 ), the SO2 contained in the flue gas is removed, and purified flue gas is obtained at the outlet of the adsorption layer 212; the purified gas is discharged through the chimney 22.

[0086] During the process of adsorption and removal of sulfur dioxide, the purification effect is monitored by an online flue gas analyzer. When the SO2 content in the purified gas is stable and there is no obvious upward trend, it indicates that the adsorption can continue; when the SO2 content in the purified gas gradually increases and the upward trend is obvious, it indicates that the adsorbent needs to be regenerated. At this time, the isolation baffle between the adsorption layer 212 and the unloading layer 213 is opened, and the adsorbent to be regenerated is unloaded to the unloading layer 213. At the same time, the isolation baffle between the storage layer 211 and the adsorption layer 212 is opened, and fresh adsorbent is added to the adsorption layer 212 to continue to adsorb and remove sulfur dioxide.

[0087] The cooled regenerated adsorbent is sent to the first dust collector 24 through the second elevator 35 for dust removal and then enters the storage layer 211 of the mobile adsorption bed 21 for recycling.

[0088] (3) Regeneration unit 3 processing: After the adsorbent to be regenerated is sent to the regeneration layer 311 of the regenerator 31 by the first elevator 23, the adsorbent to be regenerated is heated and regenerated by the electric ceramic furnace (regeneration temperature 400°C, air velocity 1000h -1 ), the regeneration gas 34 containing a relatively high concentration of sulfur dioxide generated during the regeneration process is dedusted by the second dust collector 32 and then sent to the sulfur recovery device by the regeneration fan 33 to further recover sulfur resources.

[0089] The regenerated adsorbent after high-temperature regeneration is discharged from the regeneration layer 311 into the cooling layer 312, and is cooled (cooled to 80°C) under the action of part of the sulfur-containing gas 11. The part of the sulfur-containing gas 11 that has absorbed heat returns to the incineration unit 1 for thermal incineration reaction.

[0090] The cooled regenerated adsorbent is sent to the storage layer 211 of the moving adsorption bed 21 through the second elevator 35 for recycling.

[0091] From system startup to 77h of operation, the SO2 concentration in the purified gas was 0mg / m 3 ; After the system was in operation for 98 hours, the SO2 concentration in the purified gas reached 8.2 mg / m 3 At this time, the adsorbent in the adsorption layer 212 of the adsorption unit 2 is unloaded into the unloading layer 213 to prepare for regeneration. At the same time, the adsorbent in the storage layer 211 enters the adsorption layer 212 to continue to play an adsorption role, and the SO2 concentration of the flue gas of the device drops to 0mg / m 3 The adsorbent in the discharge layer 213 is sent to the regenerator 31 for regeneration, and after regeneration, the adsorbent is continuously sent to the storage layer 211 of the adsorption unit 2 for standby use. During the entire operation cycle of the device, the SO2 emission is always kept low (the content of SO2 in the purified gas is less than 10mg / m 3 ).

[0092] Comparative Example 1 The adsorption unit 2 in the system of Example 1 is replaced by an alkali washing tower. The sulfur-containing gas 11 enters the incinerator 12 for incineration treatment (temperature 680°C; air velocity 800h -1 ), producing incineration exhaust gas containing sulfur dioxide (the content of SO2 is 418mg / m 3 ).

[0093] The above-mentioned sulfur dioxide-containing incineration tail gas is transported to the alkali washing tower (using NaOH solution with a concentration of 10wt%), and SO2 is removed under the absorption of alkali solution (absorption temperature is 35°C and pressure is 0.1MPa), and the purified gas is discharged from the chimney 22 after leaving the alkali washing tower. The SO2 content in the purified gas is 12mg / m 3 .

[0094] The system will suffer from severe corrosion during long-term operation, causing the device to be unable to operate normally. In addition, the generated salty wastewater is difficult to treat and requires huge investment in reprocessing.

[0095] Comparative Example 2 A natural gas purification plant produces sulfur-containing gas 11 (H2S 216ppm, COS 75ppm). The gas is directly discharged after being burned in an incinerator 12. The SO2 content in the flue gas is as high as 386mg / m 3 .

[0096] Comparative Example 3 The sulfur-containing gas 11 (H2S 3156ppm, COS 101ppm) produced by a coal chemical enterprise cannot be directly incinerated and discharged due to its high concentration. At the same time, the concentration of hydrogen sulfide is low, and it cannot be treated by conventional sulfur recovery processes. Later, the selective oxidation process was used for treatment. However, because the sulfur-containing gas 11 also contains a high content of COS, COS removal treatment is required first. The device process is complicated, the operation is difficult, and the investment is huge.

[0097] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present application, rather than to limit it. Although the present application has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or replace some or all of the technical features therein with equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present application.

Claims

1. A sulfur-containing gas treatment process, characterized in that: The following steps are involved: S1. Incineration treatment: The sulfur-containing gas is divided into two parts, one part is used for heat exchange with the flue gas of the incineration unit, and the other part is used as a cold source to cool the regenerated adsorbent. The two parts of sulfur-containing gas are mixed and then enter the incineration unit for combustion to obtain sulfur dioxide-containing flue gas; S2. Adsorption treatment: The adsorption unit uses an adsorbent to adsorb and remove sulfur dioxide from the sulfur dioxide-containing flue gas to obtain purified gas; S3, regeneration treatment: the regeneration unit performs thermal regeneration treatment on the adsorbent to be regenerated obtained after the adsorption and desulfurization treatment to obtain the regenerated adsorbent and the regeneration gas containing sulfur dioxide; S4. Utilization of regenerated adsorbent and recovery of sulfur resources: the regenerated adsorbent is circulated back to the adsorption unit to continue to remove sulfur dioxide; the regenerated gas containing sulfur dioxide enters the sulfur recovery unit to recover sulfur or is used to produce sulfuric acid.

2. A sulfur-containing gas treatment process according to claim 1, characterized in that: In step S4, the flue gas from the incineration unit is used as the regeneration gas source. The regeneration gas source carries the regeneration gas containing a relatively high concentration of sulfur dioxide generated during the regeneration process. After dust removal by the dust collector, it is sent to the sulfur recovery device by the regeneration fan to further recover sulfur resources or be used for the production of sulfuric acid.

3. A sulfur-containing gas treatment process according to claim 1, characterized in that: The incineration unit comprises an incinerator, a waste heat boiler and a heat exchanger connected in sequence; In step S1, the sulfur-containing gas is heated to 110-150°C by the heat exchanger with the flue gas and then enters the incinerator. The sulfur dioxide-containing flue gas generated by the incinerator is cooled to 240-280°C by the waste heat boiler and then enters the heat exchanger to exchange heat with the sulfur-containing gas. The flue gas is further cooled to 140-180°C and then enters the adsorption unit.

4. A sulfur-containing gas treatment process according to claim 1, characterized in that: The adsorption unit in step S2 includes a mobile adsorption bed, which is provided with a discharge layer, an adsorption layer and a storage layer from bottom to top, an isolation baffle is provided between the storage layer and the adsorption layer, and an isolation baffle is also provided between the discharge layer and the adsorption layer; The sulfur dioxide-containing flue gas from the incineration unit enters from the gas inlet at the bottom of the adsorption layer. The flue gas entering the adsorption layer moves from bottom to top and contacts with the adsorbent for adsorption and desulfurization. The adsorption temperature is 150-190℃ and the flue gas space velocity is 400-1000h -1 , SO2 contained in the flue gas is removed, and purified gas is obtained at the outlet of the adsorption layer; During the process of adsorption and removal of sulfur dioxide, the purification effect is monitored by an online flue gas analyzer. When the SO2 content in the purified gas is stable and there is no obvious upward trend, it indicates that the adsorption can continue; when the SO2 content in the purified gas gradually increases and the upward trend is obvious, it indicates that the adsorbent needs to be regenerated. At this time, the isolation baffle between the adsorption layer and the unloading layer is opened, and the adsorbent to be regenerated is unloaded to the unloading layer. At the same time, the isolation baffle between the storage layer and the adsorption layer is opened, and fresh adsorbent is added to the adsorption layer to continue to adsorb and remove sulfur dioxide.

5. A sulfur-containing gas treatment process according to claim 1, characterized in that: In step S3, the regeneration unit includes a regenerator, a regeneration layer is provided at the upper part of the regenerator, a cooling layer is provided at the lower part of the regenerator, and a heating mechanism is provided in the regeneration layer; After the adsorbent to be regenerated produced by the adsorption unit is sent to the regeneration layer, the heating mechanism heats and regenerates the adsorbent to be regenerated. The regeneration temperature is 380-400℃ and the air velocity is 500-1000h -1 ; In step S4, the regenerated adsorbent is unloaded from the regeneration layer into the cooling layer and cooled under the action of part of the sulfur-containing gas. The regenerated adsorbent is cooled to 50-80°C. The cooled regenerated adsorbent is dedusted by a dust collector and then enters the adsorption unit for recycling.

6. A sulfur-containing gas treatment process according to claim 1, characterized in that: The adsorbent is selected from at least one of activated carbon, activated coke, metal oxides and molecular sieves.

7. A sulfur-containing gas treatment process according to claim 6, characterized in that: The metal oxide includes at least one of copper oxide, iron oxide or zinc oxide.

8. A sulfur-containing gas treatment process according to claim 6, characterized in that: The molecular sieve includes but is not limited to X-type molecular sieve, Y-type molecular sieve or NaY molecular sieve.

9. A sulfur-containing gas treatment process according to claim 1, characterized in that: The initial sulfur capacity of the adsorbent is 100-250 g sulfur / 1000 g adsorbent.

10. A sulfur-containing gas treatment process according to claim 1, characterized in that: The content of SO2 in the purified gas in step S2 is ≤10mg / m 3 .

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