A method for deep removal of sulfides from fuel gas

Abstract

The application provides a method for deeply removing sulfides from fuel gas, comprising the following steps: (1) removing hydrogen sulfide gas by an organic alcohol amine absorbent; (2) contacting and reacting the fuel gas after removal of hydrogen sulfide gas with an oxidizing solvent to remove methyl mercaptan, dimethyl sulfide and residual hydrogen sulfide, the oxidizing solvent comprising 1-10% of an organic alcohol amine, 0.5-20% of an organic solvent, 2-38% of an oxidizing agent, 0.2-1% of an inorganic salt, and the balance of water, the organic solvent being at least one selected from the group consisting of tributyl phosphate, dimethylformamide, N-methyl pyrrolidone and polyethylene glycol dimethyl ether; the oxidizing agent being at least one selected from the group consisting of sodium hypochlorite, sodium chlorate, potassium hypochlorite, potassium chlorate, hydrogen peroxide and potassium permanganate; the inorganic salt being sodium carbonate and / or potassium carbonate; (3) adsorbing the fuel gas after removal of hydrogen sulfide, methyl mercaptan and dimethyl sulfide by an adsorbent to remove carbonyl sulfur and carbon disulfide.

Description

Technical Field

[0001] This invention belongs to the field of fuel desulfurization technology, specifically relating to a method for deep removal of sulfides from fuel gas. Background Technology

[0002] During crude oil processing, including atmospheric and vacuum distillation, catalytic cracking, catalytic reforming, hydrocracking, and delayed coking, a large amount of gaseous hydrocarbons, known as refinery gas, are produced as byproducts. This refinery gas undergoes gas separation to remove hydrocarbons below C2 concentrations, and after desulfurization with alkanolamines, most of it is used as fuel gas for heating furnaces. The sulfur content of this fuel gas is generally between 20 and 100 mg / m³. 3 It contains hydrogen sulfide as the main sulfur-containing substance, and small amounts of organic sulfides such as methanethiol, dimethyl sulfide, and carbonyl sulfide.

[0003] When fuel gas burns in the furnace, sulfides oxidize to form SO2. Some of the SO2 further oxidizes to SO3, which reacts with water vapor to form sulfuric acid vapor. When the flue gas temperature drops to the sulfuric acid dew point, the sulfuric acid vapor condenses on the metal surfaces of the furnace body and the furnace air preheater, causing sulfuric acid dew point corrosion. To avoid corrosion, the design value for the furnace exhaust gas temperature must be at least 15°C above the flue gas acid dew point temperature. Therefore, the exhaust gas temperature of furnaces in refineries is generally controlled between 120 and 160°C, and the thermal efficiency of the furnaces is 91% to 93%.

[0004] Currently, the fuel gas used in the heating furnace is treated with MDEA (methodized amine desulfurization). MDEA desulfurization uses a conventional gravity absorption tower. The MDEA absorbent and sulfur-containing dry gas undergo counter-current mass transfer within the tower. Sulfides (mainly hydrogen sulfide) are absorbed, forming a rich absorbent solution. The desulfurized gas is discharged from the top of the tower and used as fuel gas for the heating furnace. The rich absorbent solution is heated in a desorption tower to desorb acidic gases. These acidic gases enter a sulfur recovery unit to produce sulfur products, while the lean absorbent solution is recycled back to the absorption tower for reuse. MDEA desulfurization primarily absorbs and removes hydrogen sulfide gas. It has high selectivity for hydrogen sulfide gas, but its absorption effect on other sulfur-containing compounds such as mercaptans, thioethers, and carbonyl sulfides is generally weak. Furthermore, the sulfur content in the gas after MDEA desulfurization is still between 20 and 100 mg / m³. 3 This approach cannot meet the requirements for improving the quality and efficiency of heating furnaces. The desulfurization of amines using conventional gravity absorption towers has limited mass transfer efficiency and requires a large footprint, tall towers, numerous auxiliary equipment, high energy consumption, and complex process flow and operation.

[0005] Hypergravity technology is a novel chemical process intensification technology that has emerged in recent years. Under hypergravity conditions, liquids are sheared and torn into micron- to nanometer-scale liquid films, filaments, and droplets by a high-speed rotating packed bed, forming a huge interphase contact area. Simultaneously, the phase interface renewal rate is extremely fast, which can significantly improve gas-liquid mass transfer efficiency by 1 to 3 orders of magnitude. Therefore, it can drastically reduce the footprint of the equipment while increasing its production efficiency and capacity. Hypergravity equipment significantly reduces the footprint, tower height, and liquid holdup, thus reducing equipment investment and operating costs. Furthermore, hypergravity equipment features rapid start-up, simple operation, and strong adaptability, and has already been successfully applied in flue gas, tail gas, and waste gas treatment. Applying hypergravity technology to deep desulfurization processes for fuel gas shows great promise.

[0006] CN 110982566 A discloses a process for removing organic sulfur from natural gas. This process uses a catalytic adsorption type organic sulfur desulfurizer to catalytically hydrolyze or catalytically thermally decompose organic sulfur into hydrogen sulfide. The hydrogen sulfide then reacts with the active component in the catalytic adsorption type organic sulfur desulfurizer to form metal sulfides, which are then removed. However, the catalytic adsorption reaction is carried out at high temperatures, requiring heat exchange and pressurization, making the process relatively complex. Furthermore, it is difficult to guarantee the catalyst's shock resistance and long-term operational activity.

[0007] CN 104548926 A discloses an organic sulfur removal process. In this process, an organic sulfur hydrogenation catalyst is used to treat carbonyl sulfur-containing gas in a hydrogen atmosphere to convert the carbonyl sulfur into hydrogen sulfide. The hydrogen sulfide is then removed under the action of a desulfurizing agent, thereby achieving high-efficiency removal of sulfides. The catalytic hydrogenation reaction is carried out under high temperature and high pressure, and is specifically targeted at the removal of carbonyl sulfur gas.

[0008] CN 207987130 U discloses a system for associated gas desulfurization and mercaptan removal, including an acid gas absorption tower, an oxidation reactor, a bag filter, and an organic sulfur conversion tower. In the acid gas absorption tower, hydrogen sulfide in the gas is catalytically oxidized to generate elemental sulfur. The gas, after hydrogen sulfide removal, passes through a gas-liquid separator and is heated before entering the non-hydrogenated catalytic conversion tower for organic sulfur (thiols). The thiols are converted back to hydrogen sulfide and then returned to the acid gas absorption tower for further treatment. The sulfur solution generated in the acid gas absorption tower enters the oxidation reactor to restore the catalyst's reactivity (Fe2+). 2+ After oxidation, the sulfur is returned to the acid gas absorption tower, where it is filtered out in a bag filter to remove the sulfur product from the sulfur slurry from the oxidation reactor. This process uses a conventional absorption tower, which has low mass transfer efficiency; the conversion of organic thiols under high temperature and catalytic conditions results in high energy consumption; and the process flow is complex, making it difficult to guarantee the catalyst's shock resistance and long-term operational activity.

[0009] The methods for removing organic sulfur compounds from gases described in the prior art all involve catalytic reactions under high temperature and high pressure to generate inorganic sulfur, followed by treatment of the inorganic sulfur. The processes are relatively complex, the catalyst's shock resistance and activity are difficult to guarantee, and the mass transfer effect of conventional absorption towers needs to be improved. Summary of the Invention

[0010] The purpose of this invention is to provide a method for deep removal of sulfides from fuel gas.

[0011] To achieve the above objectives, the present invention provides a method for deep removal of sulfides from fuel gas, comprising the following steps:

[0012] (1) Remove hydrogen sulfide gas using an organic alcohol amine absorbent;

[0013] (2) The fuel gas after hydrogen sulfide removal is reacted with an oxidizing solvent to remove methanethiol, dimethyl sulfide and residual hydrogen sulfide. The oxidizing solvent includes 1%~10% organic alcohol amine, 0.5%~20% organic solvent, 2%~38% oxidant, 0.2%~1% inorganic salt, and the balance is water. The organic solvent is selected from at least one of dimethylformamide, N-methylpyrrolidone and polyethylene glycol dimethyl ether; the oxidant is selected from at least one of sodium chlorate, potassium chlorate and hydrogen peroxide; and the inorganic salt is sodium carbonate and / or potassium carbonate.

[0014] (3) The fuel gas after removing hydrogen sulfide, methanethiol and dimethyl sulfide is adsorbed with an adsorbent to remove carbonyl sulfide and carbon disulfide.

[0015] In the method for deep removal of sulfides from fuel gas described in this invention, the polyethylene glycol dimethyl ether mentioned in step (2) is a polyethylene glycol dimethyl ether with a carbon chain length of 3 to 8.

[0016] The method for deep removal of sulfides from fuel gas according to the present invention, wherein the organic alcohol amine absorbent in step (1) is an aqueous solution of N-methyldiethanolamine (MDEA) and a sterically hindered amine, wherein the sterically hindered amine is at least one of isobutanolamine (AMP), tert-butylaminoethoxyethanol (TBEE), and 2-(tert-butylaminoethyl)ethyl ether, the mass ratio of N-methyldiethanolamine (MDEA) to the sterically hindered amine is 1.15~2.5:1, and the mass fraction of the organic alcohol amine absorbent is 16~80%.

[0017] The method for deep removal of sulfides from fuel gas according to the present invention, wherein the organic alcohol amine in step (2) is at least one of N-methyldiethanolamine MDEA, isobutanolamine AMP, monoethanolamine MEA, diethanolamine DEA and diisopropanolamine DIPA.

[0018] The method for deep removal of sulfides from fuel gas according to the present invention, wherein the adsorbent in step (3) is Cu 2+Zn 2+ Ag + It is a molecular sieve-based fine desulfurization adsorbent with active components.

[0019] The method for deep removal of sulfides from fuel gas described in this invention is carried out in a hypergravity reactor in both steps (1) and (2).

[0020] The method for deep removal of sulfides from fuel gas described in this invention uses a structured stainless steel wire mesh packing or a stainless steel corrugated plate packing as the rotating packing in the centrifugal reactor, preferably a structured stainless steel wire mesh packing, with a specific surface area of ​​900–1200 m². 2 / m 3 Preferably 1000-1200 m 2 / m 3 .

[0021] The method for deep removal of sulfides from fuel gas according to the present invention, wherein the reaction conditions of the hypergravity reactor in step (1) are: hypergravity factor 20-150, operating pressure 0.1-0.8 MPa, temperature at room temperature, and liquid-to-gas ratio 2.0-50.0 L / m³. 3 The residence time of the gas in the packing layer is 0.02 to 2.0 s.

[0022] The method for deep removal of sulfides from fuel gas according to the present invention, in step (2), has the following reaction conditions in the hypergravity reactor: hypergravity factor 30–150, operating pressure 0.1–0.6 MPa, temperature at room temperature, and liquid-to-gas ratio 2.0–50.0 L / m³. 3 The residence time of the gas in the packing layer is 0.05 to 2.0 seconds.

[0023] The method for deep removal of sulfides from fuel gas according to the present invention includes step (3) in a fixed-bed reactor with a bed height of 100 mm, ceramic balls filling both ends of the bed, an adsorption temperature of room temperature, a pressure of 0.1–0.6 MPa, and a space velocity of 0.5–1.5 h⁻¹. -1 .

[0024] Beneficial effects of this invention:

[0025] The organic solvent in the oxidizing solvent promotes the mutual dissolution of other components and increases the solubility of organic sulfide components in the oxidizing solvent, which greatly improves the absorption and dissolution effect of organic sulfides. The oxidant can directly oxidize the low concentration of organic sulfide molecules (methanethiol and dimethyl sulfide) absorbed and dissolved in the oxidizing solvent into stable sulfonates. The inorganic salt provides an alkaline environment, increases the internal turbulence of the fluid, increases the mass transfer driving force, and thus improves the purification efficiency.

[0026] Organic alcohol amine absorbents and oxidizing solvents are composed of organic alcohol amines, organic solvents, oxidants, inorganic salts, and water. They are widely available, inexpensive, non-toxic, harmless, simple to prepare, and safe to transport and store. Organic alcohol amine absorbents exhibit high selectivity and large absorption capacity for acidic gases (H2S), and low co-absorption rate for CO2. The high-gravity absorption process offers high mass transfer efficiency, requires a small equipment footprint, necessitates small amounts of absorbent or oxidizing solvent, simplifies operation, reduces energy consumption, and demonstrates strong shock resistance.

[0027] This process is simple and highly targeted, thoroughly removing sulfides from refinery fuel gas and reducing the total sulfur content to 1 mg / m³. 3 This reduces the exhaust gas temperature of the heating furnace, improves the thermal efficiency of the heating furnace, and significantly reduces the liquid circulation volume and energy consumption. Attached Figure Description

[0028] Figure 1 This is a schematic diagram of the process flow for deep removal of sulfides from fuel gas according to the present invention. Detailed Implementation

[0029] The present invention will now be described in detail through embodiments. It should be noted that the following embodiments are only for further illustration of the present invention and should not be construed as limiting the scope of protection of the present invention. Those skilled in the art can make some non-essential improvements and adjustments to the present invention based on the above description.

[0030] like Figure 1 As shown, the process for deep removal of sulfides from fuel gas according to the present invention involves the fuel gas first passing through a hypergravity reactor where an organic alcohol amine absorbent absorbs and removes hydrogen sulfide gas. The fuel gas enters the outer cavity of the hypergravity reactor through gas inlet 1, passes through the rotating packed bed under pressure, enters the inner cavity, and exits from the central gas outlet pipe, ultimately exiting from gas outlet 1. The organic alcohol amine absorbent enters through the axial absorbent inlet in the middle of the hypergravity reactor, is evenly distributed by a liquid distributor, and is sprayed onto the hypergravity rotating packed bed. Under the centrifugal force generated by high-speed rotation, it flows radially outward, falls after hitting the stationary outer cavity wall, and is discharged from the absorbent outlet at the bottom to the absorbent storage tank. The absorbent is continuously circulated by a pump. The fuel gas and the organic alcohol amine absorbent are in counter-current contact in the hypergravity rotating packed bed, completing mass transfer; that is, H2S gas in the fuel gas is absorbed into the absorbent, completing the purification and removal of H2S from the fuel gas.

[0031] The rich absorbent solution is sent to the absorbent regeneration unit, and the regenerated lean absorbent solution is returned to the absorbent storage tank for recycling. The regenerated H2S gas is sent to the sulfur recovery unit for further recovery and utilization of sulfur resources. A certain proportion of fresh absorbent is added as needed to ensure that the circulating absorbent has a stable absorption capacity and absorption effect, enabling the unit to operate continuously for long periods.

[0032] After hydrogen sulfide removal, the fuel gas undergoes further oxidation in a hypergravity reactor. This oxidation process removes small amounts of methanethiol, dimethyl sulfide, and other gases by converting them into sulfonates, while simultaneously ensuring that any remaining unabsorbed H2S is absorbed again. The H2S-removed fuel gas exiting gas outlet 1 enters the outer cavity of the hypergravity reactor through gas inlet 2. Under pressure, it passes through the rotating packing and enters the inner cavity, exiting through the central gas outlet pipe and finally exiting through gas outlet 2. The oxidizing solvent enters through the axial oxidizing solvent inlet in the middle of the hypergravity reactor, is evenly distributed by a liquid distributor, and then sprayed onto the hypergravity rotating packing bed. Under the centrifugal force generated by the high-speed rotation, it flows radially outward, falls upon contact with the stationary outer cavity wall, and is discharged from the bottom oxidizing solvent outlet to the oxidizing solvent storage tank. The oxidizing solvent is continuously circulated and reused by a pump. After H2S removal, the fuel gas and the oxidizing solvent come into counter-current contact in a centrifugal rotating packed bed to complete the oxidation mass transfer. That is, small amounts of gases such as methanethiol and dimethyl sulfide in the fuel gas are oxidized into sulfonates and removed.

[0033] A certain proportion of fresh solvent is added to the oxidation solvent storage tank as needed to ensure that the circulating oxidation solvent has stable oxidation performance and to achieve continuous long-term operation of the unit.

[0034] After hydrogen sulfide, methanethiol, and dimethyl sulfide are removed from the fuel gas, the remaining carbonyl sulfide, carbon disulfide, and other organic sulfides are removed in the adsorption unit through highly efficient adsorption materials.

[0035] Example 1

[0036] For processing fuel gas from a refinery, the total sulfur content at the inlet is 60-80 g / m³. A supergravity absorption method is used. The supergravity device is packed with stainless steel wire mesh with a specific surface area of ​​1200 m² / m³, a supergravity factor of 120, an operating pressure of 0.5 MPa, ambient temperature, a liquid-to-gas ratio of 40 L / m³, and a gas residence time of 0.24 s. The absorbent is a 50% (w / w) aqueous solution of organic alcohol amines, including N-methyldiethanolamine and 2-(tert-butylamine ethyl) ether in a (w / w) ratio of 1.15:1. The process employs hypergravity oxidation. The hypergravity apparatus uses stainless steel wire mesh as packing material, with a specific surface area of ​​1200 m² / m³, a hypergravity factor of 120, an operating pressure of 0.5 MPa, ambient temperature, a liquid-to-gas ratio of 40 L / m³, and a gas residence time of 0.24 s. The oxidation solvents include 2% monoethanolamine, 2% diisopropanolamine (DIPA), 15% dimethylformamide, 10% potassium chlorate, 0.2% potassium carbonate, and water as the balance. A fixed-bed adsorption bed with a height of 100 mm is used, with approximately 10 mm high, Φ3 mm ceramic balls at both ends. The adsorbent is Ag. +The active component is a molecular sieve-based desulfurization adsorbent. The adsorption process is as follows: adsorption temperature at room temperature, pressure at 0.5 MPa, and space velocity at 1.2 h⁻¹. -1 .

[0037] After the device is running stably, gas samples are taken from the gas inlet according to standard HJ 732-2014, and the total sulfur content is found to be below 1 mg / m³ by the total sulfur analyzer.

[0038] Example 2

[0039] For processing fuel gas from a refinery, the total sulfur content at the inlet is 80-100 g / m³. A supergravity absorption method is used. The supergravity device is filled with stainless steel wire mesh with a specific surface area of ​​1000 m² / m³, a supergravity factor of 30, an operating pressure of 0.1 MPa, ambient temperature, a liquid-to-gas ratio of 10 L / m³, and a gas residence time of 1.44 s. The absorbent is a 60% (w / w) aqueous solution of organic alcohol amines, including N-methyldiethanolamine and isobutanolamine AMP in a (w / w) ratio of 2.5:1. The process employs hypergravity oxidation. The hypergravity apparatus uses stainless steel wire mesh as packing material, with a specific surface area of ​​1000 m² / m³, a hypergravity factor of 100, an operating pressure of 0.1 MPa, ambient temperature, a liquid-to-gas ratio of 40 L / m³, and a gas residence time of 1.44 s. The oxidation solvents include 8% isobutanolamine (AMP), 2% diisopropanolamine (DIPA), 12% N-methylpyrrolidone, 10% sodium chlorate, 0.8% sodium carbonate, and water as the balance. A fixed-bed adsorption bed with a height of 100 mm is used, with approximately 10 mm high, Φ3 mm ceramic spheres at both ends. The adsorbent is Cu. 2+ The active component is a molecular sieve-based desulfurization adsorbent. The adsorption process is as follows: adsorption temperature at room temperature, pressure at 0.1 MPa, and space velocity at 1.0 h⁻¹. -1 .

[0040] After the device is running stably, gas samples are taken from the gas inlet according to standard HJ 732-2014, and the total sulfur content is found to be below 1 mg / m³ by the total sulfur analyzer.

[0041] Example 3

[0042] For processing fuel gas from a refinery, the total sulfur content at the inlet is 60-80 g / m³. A supergravity absorption method is used. The supergravity device is packed with stainless steel wire mesh with a specific surface area of ​​1000 m² / m³, a supergravity factor of 100, an operating pressure of 0.1 MPa, ambient temperature, a liquid-to-gas ratio of 25 L / m³, and a gas residence time of 0.72 s. The absorbent is a 26% (w / w) aqueous solution of organic alcohol amines, including N-methyldiethanolamine and isobutanolamine AMP in a 1.5:1 (w / w) ratio. The process employs hypergravity oxidation. The hypergravity device uses stainless steel wire mesh as packing material, with a specific surface area of ​​1000 m² / m³, a hypergravity factor of 80, an operating pressure of 0.1 MPa, ambient temperature, a liquid-to-gas ratio of 25 L / m³, and a gas residence time of 0.72 s. The oxidation solvent consists of the following mass ratio: N-methyldiethanolamine (MDEA) 2%, diisopropanolamine (DIPA) 6%, N-methylpyrrolidone 12%, hydrogen peroxide 30%, sodium carbonate 0.8%, and water as the balance. A fixed-bed adsorption bed with a height of 100 mm is used, with approximately 10 mm high, Φ3 mm ceramic spheres at both ends. The adsorbent is Cu... 2+ The active component is a molecular sieve-based desulfurization adsorbent. The adsorption process is as follows: adsorption temperature at room temperature, pressure at 0.1 MPa, and space velocity at 0.8 h⁻¹. -1 .

[0043] After the device is running stably, gas samples are taken from the gas inlet according to standard HJ 732-2014, and the total sulfur content is found to be below 1 mg / m³ by the total sulfur analyzer.

[0044] Comparative Example 1

[0045] For treating fuel gas from a refinery, with a total sulfur content of 60-80 g / m³ at the inlet, a centrifugal absorption system was employed. The centrifugal device used stainless steel wire mesh as packing material, with a specific surface area of ​​1200 m² / m³, a centrifugal factor of 120, an operating pressure of 0.1 MPa, ambient temperature, a liquid-to-gas ratio of 40 L / m³, and a gas residence time of 0.24 s. The absorbent was a 68% (w / w) aqueous solution of organic alcoholic amines, comprising N-methyldiethanolamine and 2-(tert-butylamine ethyl) ether in a 1.15:1 (w / w) ratio. The adsorbent was Ag... + The active component is a molecular sieve-based desulfurization adsorbent. The adsorption process is as follows: adsorption temperature at room temperature, pressure at 0.5 MPa, and space velocity at 1.2 h⁻¹. -1 .

[0046] After the device was running stably, a gas sample was taken from the gas inlet according to standard HJ 732-2014, and the total sulfur content was measured to be 32.1 mg / m³ by the total sulfur analyzer.

[0047] Of course, the present invention may have other various embodiments. Without departing from the spirit and essence of the present invention, those skilled in the art can make various corresponding changes and modifications according to the present invention, but these corresponding changes and modifications should all fall within the protection scope of the claims of the present invention.

Claims

1. A method for deep removal of sulfides from fuel gas, characterized in that, Includes the following steps: (1) Remove hydrogen sulfide gas using an organic alcohol amine absorbent; (2) The fuel gas after hydrogen sulfide removal is reacted with an oxidizing solvent to remove methanethiol, dimethyl sulfide and residual hydrogen sulfide. The oxidizing solvent includes 1%~10% organic alcohol amine, 0.5%~20% organic solvent, 2%~38% oxidant, 0.2%~1% inorganic salt, and the balance is water. The organic solvent is selected from at least one of dimethylformamide, N-methylpyrrolidone and polyethylene glycol dimethyl ether; the oxidant is selected from at least one of sodium chlorate, potassium chlorate and hydrogen peroxide; and the inorganic salt is sodium carbonate and / or potassium carbonate. (3) The fuel gas after removing hydrogen sulfide, methanethiol and dimethyl sulfide is adsorbed with an adsorbent to remove carbonyl sulfide and carbon disulfide.

2. The method for deep removal of sulfides from fuel gas according to claim 1, characterized in that, The polyethylene glycol dimethyl ether mentioned in step (2) is a polyethylene glycol dimethyl ether with a carbon chain length of 3 to 8.

3. The method for deep removal of sulfides from fuel gas according to claim 1, characterized in that, The organic alcohol amine absorbent mentioned in step (1) is an aqueous solution of N-methyldiethanolamine (MDEA) and a sterically hindered amine, wherein the sterically hindered amine is at least one of isobutanolamine (AMP), tert-butylaminoethoxyethanol (TBEE), and 2-(tert-butylaminoethyl)ethyl ether, the mass ratio of N-methyldiethanolamine (MDEA) to the sterically hindered amine is 1.15 to 2.5:1, and the mass fraction of the organic alcohol amine absorbent is 16 to 80%.

4. The method for deep removal of sulfides from fuel gas according to claim 1, characterized in that, The organic alcohol amine mentioned in step (2) is at least one of N-methyldiethanolamine (MDEA), isobutanolamine (AMP), monoethanolamine (MEA), diethanolamine (DEA), and diisopropanolamine (DIPA).

5. The method for deep removal of sulfides from fuel gas according to claim 1, characterized in that, The adsorbent mentioned in step (3) is Cu 2+ Zn 2+ Ag + It is a molecular sieve-based fine desulfurization adsorbent with active components.

6. The method for deep removal of sulfides from fuel gas according to claim 1, characterized in that, Both steps (1) and (2) are carried out in a hypergravity reactor.

7. The method for deep removal of sulfides from fuel gas according to claim 6, characterized in that, The rotating packing in the high gravity reactor is either structured stainless steel wire mesh packing or stainless steel corrugated plate packing, with a specific surface area of ​​900–1200 m². 2 / m 3 .

8. The method for deep removal of sulfides from fuel gas according to claim 6, characterized in that, The rotating packing in the supergravity reactor is a structured stainless steel wire mesh packing.

9. The method for deep removal of sulfides from fuel gas according to claim 7, characterized in that, The specific surface area of ​​the rotating packing material in the centrifugal reactor is 1000–1200 m². 2 / m 3 .

10. The method for deep removal of sulfides from fuel gas according to claim 6, characterized in that, The reaction conditions in the hypergravity reactor in step (1) are: hypergravity factor 20–150, operating pressure 0.1–0.8 MPa, temperature at room temperature, and liquid-to-gas ratio 2.0–50.0 L / m³. 3 The residence time of the gas in the packing layer is 0.02 to 2.0 s.

11. The method for deep removal of sulfides from fuel gas according to claim 6, characterized in that, The reaction conditions in the hypergravity reactor in step (2) are: hypergravity factor 30–150, operating pressure 0.1–0.6 MPa, temperature at room temperature, and liquid-to-gas ratio 2.0–50.0 L / m³. 3 The residence time of the gas in the packing layer is 0.05 to 2.0 seconds.

12. The method for deep removal of sulfides from fuel gas according to claim 1, characterized in that, Step (3) is carried out in a fixed-bed reactor with a bed height of 100 mm. Both ends of the bed are filled with ceramic balls. The adsorption temperature is room temperature, the pressure is 0.1–0.6 MPa, and the space velocity is 0.5–1.5 h⁻¹. -1 .

Images