System device and method for deeply removing and regenerating hydrogen sulfide in sulfur-containing tail gas

Abstract

The invention discloses a system device and method for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas. The system device comprises a supergravity absorption device, a first gas-liquid separator, a lean amine liquid cooler, a rich amine liquid delivery pump, a lean and rich liquid heat exchanger, a rich amine liquid preheater, a multi-stage supergravity regeneration device, a condenser, a second gas-liquid separator, a reboiler and a lean amine liquid delivery pump. According to the system device disclosed by the invention, the transfer process between the gas and the absorbent is enhanced by adopting the supergravity equipment, so that the deep removal of hydrogen sulfide in the low-pressure sulfur-containing gas can be realized, and the problem of unstable operation caused by compression in a conventional method is avoided; after the sulfur-containing tail gas is treated, the content of hydrogen sulfide in the gas is less than or equal to 15mg / m < 3 >.

Description

Technical Field

[0001] The present invention belongs to the technical field of sulfur-containing tail gas treatment, and in particular relates to a system device and method for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas. Background Art

[0002] The petrochemical industry produces a large amount of low-pressure gases, such as top gas from atmospheric and vacuum units, atmospheric top gas, reduced top gas, gasholder recovery gas, and Claus unit tail gas. Because these gases contain hydrogen sulfide, direct discharge or incineration before discharge will cause environmental pollution, necessitating desulfurization treatment.

[0003] The industry typically uses the alcoholamine process to remove hydrogen sulfide from gases. Typically, the gas is first compressed to approximately 1.0 MPa and then absorbed in an absorption tower. The rich amine solution, which has absorbed the hydrogen sulfide, is then fed to a regeneration tower. The hydrogen sulfide desorbed from the rich amine solution is then fed to a Claus unit for sulfur production. The regenerated lean amine solution then returns to the absorption tower, completing the cycle. However, the exhaust gas composition is complex, and condensate or other impurities may form during the compression process, potentially causing compressor malfunction and impacting stable production operations. Summary of the Invention

[0004] The first technical problem to be solved by the present invention is to provide a system for deep removal and regeneration of hydrogen sulfide from sulfur-containing tail gas. The system uses supergravity equipment to enhance the transfer process between gas and absorbent, which can achieve deep removal of hydrogen sulfide from low-pressure sulfur-containing gas, avoiding the operational instability caused by compression in conventional methods. The hydrogen sulfide content in the gas after sulfur-containing tail gas treatment is ≤15mg / m 3 .

[0005] The second technical problem to be solved by the present invention is to provide a method for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas using the above-mentioned system device.

[0006] In order to solve the above-mentioned first technical problem, the technical solution adopted by the present invention is as follows:

[0007] A system for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas, comprising a supergravity absorption device, a first gas-liquid separator, a lean amine liquid cooler, a rich amine liquid delivery pump, a lean-rich liquid heat exchanger, a rich amine liquid preheater, a multi-stage supergravity regeneration device, a condenser, a second gas-liquid separator, a reboiler, and a lean amine liquid delivery pump;

[0008] The gas inlet of the supergravity absorption device is connected to the sulfur-containing tail gas through a pipeline; the gas outlet of the supergravity absorption device is connected to the first gas-liquid separator through a pipeline; the liquid outlet at the bottom of the first gas-liquid separator is connected to the supergravity absorption device through a pipeline;

[0009] The liquid outlet of the high-gravity absorption device is connected to the rich amine liquid delivery pump, the lean-rich liquid heat exchanger, and the rich amine liquid preheater in sequence through a pipeline, and then connected to the liquid inlet of the multi-stage high-gravity regeneration device;

[0010] The liquid outlet at the bottom of the multi-stage high gravity regeneration device is connected to the liquid inlet of the reboiler through a pipeline, and the liquid outlet of the reboiler is connected to the inlet of the lean amine liquid delivery pump through a pipeline;

[0011] The outlet of the lean amine liquid delivery pump is connected to two branch pipes, the first branch pipe is connected in sequence to the lean-rich liquid heat exchanger, the lean amine liquid cooler and the liquid inlet of the supergravity absorption device; the second branch pipe directly flows back to the multi-stage supergravity regeneration device;

[0012] The gas outlet of the multi-stage supergravity regeneration device is connected to the condenser and the second gas-liquid separator in sequence through a pipeline; the liquid outlet of the second gas-liquid separator is connected to the reboiler.

[0013] Preferably, the supergravity absorption device includes but is not limited to a rotating packed bed, a stator-rotor reactor and a baffled device that enhances mass transfer between gas and liquid by rotation; the filler of the supergravity absorption device is one of stainless steel wire mesh filler, structured silicon carbide filler, and surface hydrophilic and hydrophobic combination filler.

[0014] Preferably, the supergravity absorption device has a certain liquid storage capacity, and is an integrated combination of supergravity equipment and a rich amine liquid storage tank; for example, the residence time of the rich amine liquid in the supergravity absorption device is 1-10 minutes.

[0015] Preferably, the multi-stage rotor of the multi-stage high-gravity regeneration device has 2-4 layers; a liquid distributor is provided at the inner edge of each stage of the rotor, and a gas inlet is provided on the outer shell at the outer edge of the lowest stage of the rotor. Partition plates are provided between the multi-stage rotors, and the multi-stage rotors form a series of gas phase flow channels; the filler of the multi-stage high-gravity regeneration device is one of stainless steel wire mesh filler, structured silicon carbide filler, and surface hydrophilic and hydrophobic combination filler.

[0016] In order to solve the above second technical problem, the technical solution adopted by the present invention is as follows:

[0017] A method for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas using the above system device comprises the following steps:

[0018] 1) The hydrogen sulfide-containing tail gas is transported to the gas inlet of the supergravity absorption device, where it is countercurrently contacted with the lean amine liquid from the multi-stage supergravity regeneration device and reacts. The hydrogen sulfide in the gas is absorbed into the liquid phase. The tail gas after the reaction is discharged through the gas outlet of the supergravity absorption device and then transported to the first gas-liquid separator; the gas separated by the first gas-liquid separator enters the tail gas incinerator for incineration and then discharged into the atmosphere. The liquid separated by the first gas-liquid separator flows back to the supergravity absorption device through the liquid outlet;

[0019] 2) The lean amine liquid from the multi-stage high-gravity regeneration device absorbs hydrogen sulfide in the high-gravity absorption device to form rich amine liquid. The rich amine liquid is delivered to the rich amine liquid delivery pump through the liquid outlet at the bottom of the high-gravity absorption device, and then heat-exchanged in the lean-rich liquid heat exchanger and heated in the rich amine liquid heater before being delivered to the multi-stage high-gravity regeneration device;

[0020] 3) The rich amine liquid entering the multi-stage high gravity regeneration device is countercurrently contacted with the steam from the reboiler in the packing area and the cavity area. The hydrogen sulfide in the rich amine liquid is desorbed and enters the condenser along with the steam through the gas outlet of the multi-stage high gravity regeneration device to recover part of the heat. The amine liquid is then transported to the second gas-liquid separator, where the steam and hydrogen sulfide are separated. The obtained hydrogen sulfide gas is transported to the Claus unit for sulfur production. The liquid condensed in the second gas-liquid separator is refluxed to the reboiler.

[0021] 4) The liquid in the multi-stage super gravity regeneration device is transported to the reboiler from the bottom liquid outlet. After the regenerated lean amine liquid passes through the lean amine liquid delivery pump, a portion of it returns to the multi-stage super gravity regeneration device through the second branch pipe to further improve the desorption rate of the absorption liquid. The remaining lean amine liquid is transported to the lean-rich amine liquid heat exchanger and the lean amine liquid cooler through the first branch pipe and then enters the super gravity absorption device to complete the entire cycle operation.

[0022] Preferably, in step 1), the operating temperature of the high gravity absorption device is 30-50°C, the high gravity level is 50-200, and the gas-liquid volume flow ratio is 20-100:1.

[0023] Preferably, in step 3), the operating temperature of the multi-stage hypergravity regeneration device is 110-130°C, and the hypergravity level is 50-200.

[0024] Any range described in the present invention includes the end value and any numerical value between the end values ​​and any sub-range formed by the end value or any numerical value between the end values.

[0025] Unless otherwise specified, all raw materials in the present invention can be purchased commercially, and the equipment used in the present invention can adopt conventional equipment in the relevant field or refer to the existing technology in the relevant field.

[0026] Compared with the prior art, the present invention has the following beneficial effects:

[0027] 1) The present invention can achieve deep removal of hydrogen sulfide in low-pressure sulfur-containing gas by using supergravity equipment, avoiding the operational instability problem caused by compression in conventional methods; the hydrogen sulfide content in the sulfur-containing tail gas after treatment of the present invention is ≤15mg / m 3 ;

[0028] 2) The present invention utilizes a multi-layer rotor high-gravity device for the regeneration process of rich amine liquid. Combined with the circulation of lean amine liquid in the reboiler and the multi-stage high-gravity regeneration device, deep regeneration of rich amine liquid can be achieved, providing a good guarantee for deep purification of hydrogen sulfide in sulfur-containing tail gas under low-pressure conditions.

[0029] 3) The present invention uses a supergravity device for the deep removal of hydrogen sulfide from sulfur-containing tail gas and the regeneration process of rich amine liquid. Compared with the traditional hydrogen sulfide removal and rich amine liquid regeneration process based on gas compression and reabsorption with tower equipment as the core, the hydrogen sulfide absorption process and the rich amine liquid regeneration process have significantly reduced equipment investment and floor space, and can also significantly reduce operating energy consumption, thus having good industrial application value. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] The specific embodiments of the present invention will be further described in detail below with reference to the accompanying drawings.

[0031] Figure 1 The figure is a schematic structural diagram of a system device for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas according to the present invention. DETAILED DESCRIPTION

[0032] In order to explain the present invention more clearly, the present invention is further described below in conjunction with preferred embodiments. Those skilled in the art should understand that the following specific description is illustrative rather than restrictive and should not be used to limit the scope of protection of the present invention.

[0033] See also Figure 1 As shown, as one aspect of the present invention, a system device for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas of the present invention comprises: a supergravity absorption device 1, a first gas-liquid separator 2, a lean amine liquid cooler 3, a rich amine liquid delivery pump 4, a lean and rich liquid heat exchanger 5, a rich amine liquid preheater 6, a multi-stage supergravity regeneration device 7, a condenser 8, a second gas-liquid separator 9, a reboiler 10, and a lean amine liquid delivery pump 11;

[0034] The gas inlet of the supergravity absorption device 1 is connected to the sulfur-containing tail gas 100 through a pipeline;

[0035] The gas outlet of the high-gravity absorption device 1 is connected to the first gas-liquid separator 2 through a pipeline; the first gas-liquid separator in the present invention is used to separate the tail gas treated by the high-gravity absorption device from a small amount of mixed absorption liquid;

[0036] The liquid outlet at the bottom of the first gas-liquid separator 2 is connected to the supergravity absorption device 1 through a pipeline for circulation and reflux; the gas outlet at the top of the first gas-liquid separator 2 can be connected to an external incinerator 20, which is used to incinerate the tail gas after the supergravity absorption device 1 absorbs hydrogen sulfide and then discharge it into the atmosphere, thereby reducing the emission of toxic and harmful gases;

[0037] The liquid outlet of the high-gravity absorption device 1 is connected to the rich amine liquid delivery pump 4, the lean-rich liquid heat exchanger 5, and the rich amine liquid preheater 6 in sequence through a pipeline, and then connected to the liquid inlet of the multi-stage high-gravity regeneration device 7; the lean-rich liquid heat exchanger 5 is used to cool the lean amine liquid with the rich amine liquid and to heat the rich amine liquid with the lean amine liquid; the rich amine liquid preheater 6 is used to preheat the rich amine liquid so that it can reach the regeneration temperature as soon as possible when entering the multi-stage high-gravity regeneration device 7;

[0038] The liquid outlet at the bottom of the multi-stage supergravity regeneration device 7 is connected to the liquid inlet of the reboiler 10 through a pipeline, and the liquid outlet of the reboiler 10 is connected to the inlet of the lean amine liquid delivery pump 11 through a pipeline;

[0039] The outlet of the lean amine liquid delivery pump 11 is connected to two branch pipes. The first branch pipe is connected in sequence to the lean-rich liquid heat exchanger 5, the lean amine liquid cooler 3 and the liquid inlet of the supergravity absorption device 1; the second branch pipe directly flows back to the multi-stage supergravity regeneration device 7, completing the cycle of sulfur-containing tail gas absorption and regeneration process;

[0040] The gas outlet of the multi-stage high-gravity regeneration device 7 is connected to the condenser 8 and the second gas-liquid separator 9 in sequence through a pipeline; the liquid outlet of the second gas-liquid separator 9 is connected to the reboiler 10; the gas outlet of the second gas-liquid separator 9 can be externally connected to a Claus device for preparing sulfur; the function of the second gas-liquid separator 9 is to separate the gas generated by the multi-stage high-gravity regeneration device and the entrained liquid.

[0041] According to certain embodiments of the present invention, the supergravity absorption device 1 includes but is not limited to a rotating packed bed, a stator-rotor reactor and a baffled flow device that enhances mass transfer between gas and liquid by rotation; the filler of the supergravity absorption device is one of stainless steel wire mesh filler, structured silicon carbide filler, and surface hydrophilic and hydrophobic combination filler.

[0042] According to certain embodiments of the present invention, the supergravity absorption device 1 has a certain liquid storage capacity and is an integrated integration of supergravity equipment and a rich amine liquid storage tank; for example, the residence time of the rich amine liquid in the supergravity absorption device is 1-10 minutes.

[0043] According to certain embodiments of the present invention, the multi-stage rotor of the multi-stage supergravity regeneration device 7 has 2-4 layers; a liquid distributor is provided at the inner edge of each stage of the rotor, and a gas inlet is provided on the outer shell at the outer edge of the lowest stage of the rotor. Partition plates are provided between the multi-stage rotors, and the multi-stage rotors form a series of gas flow channels; the filler of the multi-stage supergravity regeneration device 7 is one of stainless steel wire mesh filler, structured silicon carbide filler, and surface hydrophilic and hydrophobic combination filler.

[0044] As another aspect of the present invention, a method for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas using the above-mentioned system device comprises the following steps:

[0045] 1) The hydrogen sulfide-containing tail gas with a pressure of less than 0.1 MPa is transported to the gas inlet of the supergravity absorption device 1, and is countercurrently contacted with the lean amine liquid from the multi-stage supergravity regeneration device 7 to react, and the hydrogen sulfide in the gas is absorbed into the liquid phase. The tail gas after the reaction is discharged through the gas outlet of the supergravity absorption device 1 and then transported to the first gas-liquid separator 2; the gas separated by the first gas-liquid separator 2 enters the tail gas incinerator for incineration and then discharged into the atmosphere, and the liquid separated by the first gas-liquid separator 2 is refluxed to the supergravity absorption device 1 through the liquid outlet; the lean amine liquid in the present invention can be selected from MDEA solution, composite amine absorbent solution with MDEA as the main absorbent, etc.; the hydrogen sulfide-containing tail gas in the present invention can be Claus hydrogenation tail gas, vacuum tower overhead gas and other sulfur-containing tail gases;

[0046] 2) The lean amine liquid from the multi-stage high gravity regeneration device 7 absorbs hydrogen sulfide in the high gravity absorption device 1 to form a rich amine liquid. The rich amine liquid is delivered to the rich amine liquid delivery pump 4 through the liquid outlet at the bottom of the high gravity absorption device 1, and then passes through the lean-rich liquid heat exchanger 5 and the rich amine heater 6 for heating before being delivered to the multi-stage high gravity regeneration device 7;

[0047] 3) The rich amine liquid entering the multi-stage high gravity regeneration device 7 is countercurrently contacted with the steam from the reboiler 10 in the packing area and the cavity area. The hydrogen sulfide in the rich amine liquid is desorbed and enters the condenser 8 along with the steam through the gas outlet of the multi-stage high gravity regeneration device 7 to recover part of the heat. The amine liquid is then transported to the second gas-liquid separator 9. The steam and hydrogen sulfide are separated in the second gas-liquid separator 9. The obtained hydrogen sulfide gas is transported to the Claus device 90 for sulfur production. The liquid condensed in the second gas-liquid separator 9 is refluxed to the reboiler 10.

[0048] 4) The liquid in the multi-stage super gravity regeneration device 7 is transported from the bottom liquid outlet to the reboiler 10. After the regenerated lean amine liquid passes through the lean amine liquid delivery pump 11, a portion of it returns to the multi-stage super gravity regeneration device 7 through the second branch pipe to further improve the desorption rate of the absorption liquid. The remaining lean amine liquid is transported to the lean-rich amine liquid heat exchanger 5 and the lean amine liquid cooler 3 through the first branch pipe and then enters the super gravity absorption device 1, completing the entire cycle operation.

[0049] According to certain embodiments of the present invention, in step 1), the operating temperature of the hypergravity absorption device is 30-50°C, the hypergravity level is 50-200, and the gas-liquid volume flow ratio is 20-100:1.

[0050] According to certain embodiments of the present invention, in step 3), the operating temperature of the multi-stage hypergravity regeneration device is 110-130° C., and the hypergravity level is 50-200° C.

[0051] The hypergravity level can be calculated using the following formula:

[0052]

[0053] Where N is the rotor speed, unit is r·min -1 ; r is the average value of the inner and outer diameters of the rotor, in meters; g is the acceleration due to gravity, which is 9.8 m·s -2 .

[0054] Example 1

[0055] See also Figure 1As shown, a method for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas using the system device of the present invention is specifically performed as follows: during the absorption process, hydrogen sulfide-containing gas enters the supergravity absorption device through the gas inlet, and under the action of pressure, the gas enters the packing area from the outer edge of the rotor, and the lean amine liquid from the multi-stage supergravity regeneration device is introduced into the center of the supergravity absorption device rotor, and after passing through the liquid distributor, it is evenly distributed on the inner edge of the rotor and enters the packing area and then flows to the outer edge of the rotor, where it contacts and reacts with the gas in the packing area and the cavity area outside the rotor in countercurrent; the rich amine liquid that has absorbed hydrogen sulfide passes through the rich amine liquid delivery pump 4, the lean-rich liquid heat exchanger 5 and the rich amine liquid preheater 6 in sequence. Then it enters the liquid inlet of the multi-stage super gravity regeneration device 7, and contacts with the steam from the reboiler 10 in the packing area of ​​each rotor and the outer cavity area of ​​the rotor in countercurrent. The hydrogen sulfide in the rich amine liquid is desorbed and leaves the multi-stage super gravity regeneration device 7 with the steam and enters the condenser 6 and the gas-liquid separator 9, where the steam and hydrogen sulfide are separated to obtain hydrogen sulfide gas and sent to the Claus device to make sulfur. The condensed liquid returns to the reboiler 10; the liquid leaving the multi-stage super gravity regeneration device 7 enters the reboiler 10, and the regenerated lean amine liquid passes through the lean amine liquid delivery pump 11, the lean-rich liquid heat exchanger 5 and the lean amine liquid cooler 3, and then enters the super gravity absorption device 1, completing the entire cycle operation.

[0056] The parameter conditions of the system device of the present invention are as follows:

[0057] The raw gas is a medium hydrogen sulfide gas with a content of 1.5% (V), and the absorption liquid is a 30% MDEA aqueous solution;

[0058] The operating temperature of the hypergravity absorption device is 40°C, and the hypergravity level during the absorption process is 90;

[0059] The gas-liquid volume flow ratio during the absorption process is 50:1, and the filler used in the supergravity absorption device is a surface hydrophilic-hydrophobic composite filler;

[0060] The temperature of the multi-stage high gravity regeneration device is 125 ° C, the volume ratio of the circulating lean amine liquid to the produced lean amine liquid is 2:1, the rotor of the multi-stage high gravity regeneration device is 3 layers, the high gravity level of the multi-stage high gravity is 70, and the filler used is stainless steel wire mesh filler. The hydrogen sulfide content in the lean amine liquid after regeneration is 0.08g / kg; the hydrogen sulfide content in the treated gas is 9mg / m 3 .

[0061] Implementation Column 2

[0062] As described in Example 1, other conditions remain unchanged, the volume ratio of the circulating lean amine liquid to the produced lean amine liquid is 0.5:1, the hydrogen sulfide content in the lean amine liquid after regeneration is 0.20g / kg; the hydrogen sulfide content in the treated gas is 14mg / m 3 .

[0063] Example 3

[0064] As described in Example 1, other conditions remain unchanged, the rotor of the high gravity regeneration device is 4 layers, and the hydrogen sulfide content in the lean amine liquid after regeneration is 0.06g / kg. The hydrogen sulfide content in the treated gas is 4mg / m 3 .

[0065] Example 4

[0066] As described in Example 1, other conditions remain unchanged, the hypergravity level during the absorption process is 200, and the hydrogen sulfide content in the treated gas is 7 mg / m 3 .

[0067] Example 5

[0068] As shown in Example 1, other conditions remain unchanged, the gas-liquid volume flow ratio of the absorption process is 40:1, and the hydrogen sulfide content in the treated gas is 7 mg / m 3 .

[0069] Example 6

[0070] As shown in Example 1, other conditions remain unchanged, the gas-liquid volume flow ratio of the absorption process is 100:1, and the hydrogen sulfide content in the treated gas is 15 mg / m 3 .

[0071] Comparative Example 1

[0072] As shown in Example 1, other conditions remain unchanged, the gas-liquid volume flow ratio of the absorption process is 120:1, and the hydrogen sulfide content in the treated gas is 45 mg / m 3 .

[0073] Since the gas-liquid ratio is higher than that in Example 1, the amount of hydrogen sulfide required to be absorbed per unit volume of absorbent increases, resulting in the concentration of hydrogen sulfide in the treated tail gas significantly exceeding that in Example 1.

[0074] Comparative Example 2

[0075] As shown in Example 1, other conditions remain unchanged, the hypergravity level of the absorption process is 30, and the hydrogen sulfide content in the treated gas is 180 mg / m 3 .

[0076] Since the hypergravity level is lower than that in Example 1, the mass transfer effect between gas and liquid becomes poor, so the hydrogen sulfide concentration in the tail gas after treatment is significantly higher than that in Example 1.

[0077] Comparative Example 3

[0078] As shown in Example 1, other conditions remain unchanged, the hypergravity level of the absorption process is 300, and the hydrogen sulfide content in the treated gas is 6 mg / m 3 .

[0079] The hydrogen sulfide content in the tail gas after absorption is slightly lower than that in Example 1, but the energy consumption of the absorption equipment is significantly higher than that in Example 1.

[0080] Comparative Example 4

[0081] As shown in Example 1, other conditions remain unchanged, the hypergravity level during the regeneration process is 40, and the hydrogen sulfide content in the lean amine liquid after regeneration is 0.35 g / kg. The hydrogen sulfide content in the treated gas is 25 mg / m 3 .

[0082] Since the hypergravity level during the regeneration process is significantly lower than that in Example 1, the mass and heat transfer effects during the regeneration process are poor, and the hydrogen sulfide content in the lean amine liquid after regeneration is high, thereby affecting the absorption effect.

[0083] Comparative Example 5

[0084] As shown in Example 1, other conditions remain unchanged, the lean liquid is not circulated during the regeneration process, and the hydrogen sulfide content in the lean amine liquid after regeneration is 0.60g / kg. The hydrogen sulfide content in the treated gas is 48mg / m 3 .

[0085] Since the lean liquid is not circulated during the regeneration process, the regeneration depth is insufficient and the residual hydrogen sulfide content in the lean liquid is high, thus affecting the effect of the absorption process.

[0086] Obviously, the above embodiments of the present invention are merely examples for the purpose of clearly illustrating the present invention and are not intended to limit the embodiments of the present invention. Those skilled in the art will appreciate that other variations or modifications based on the above description are possible. It is not possible to enumerate all embodiments here. Any obvious variations or modifications arising from the technical solution of the present invention remain within the scope of protection of the present invention.

Claims

1. A system for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas, characterized in that: It includes a super gravity absorption device, a first gas-liquid separator, a lean amine liquid cooler, a rich amine liquid delivery pump, a lean and rich liquid heat exchanger, a rich amine liquid preheater, a multi-stage super gravity regeneration device, a condenser, a second gas-liquid separator, a reboiler, and a lean amine liquid delivery pump; The gas inlet of the supergravity absorption device is connected to the sulfur-containing tail gas through a pipeline; the gas outlet of the supergravity absorption device is connected to the first gas-liquid separator through a pipeline; the liquid outlet at the bottom of the first gas-liquid separator is connected to the supergravity absorption device through a pipeline; The liquid outlet of the high-gravity absorption device is connected to the rich amine liquid delivery pump, the lean-rich liquid heat exchanger, and the rich amine liquid preheater in sequence through a pipeline, and then connected to the liquid inlet of the multi-stage high-gravity regeneration device; The liquid outlet at the bottom of the multi-stage high gravity regeneration device is connected to the liquid inlet of the reboiler through a pipeline, and the liquid outlet of the reboiler is connected to the inlet of the lean amine liquid delivery pump through a pipeline; The outlet of the lean amine liquid delivery pump is connected to two branch pipes, the first branch pipe is connected in sequence to the lean-rich liquid heat exchanger, the lean amine liquid cooler and the liquid inlet of the supergravity absorption device; the second branch pipe directly flows back to the multi-stage supergravity regeneration device; The gas outlet of the multi-stage supergravity regeneration device is connected to the condenser and the second gas-liquid separator in sequence through a pipeline; the liquid outlet of the second gas-liquid separator is connected to the reboiler.

2. The system device for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas according to claim 1, characterized in that: The high-gravity absorption device includes but is not limited to a rotating packed bed, a stator-rotor reactor and a baffled device that strengthens the mass transfer between gas and liquid by rotation; the filler of the high-gravity absorption device is one of stainless steel wire mesh filler, structured silicon carbide filler and surface hydrophilic-hydrophobic combined filler.

3. The system device for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas according to claim 1, characterized in that: The supergravity absorption device has liquid storage capacity and is an integrated combination of supergravity equipment and a rich amine liquid storage tank.

4. The system for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas according to claim 1, characterized in that: The residence time of the rich amine solution in the supergravity absorption device is 1-10 minutes.

5. The system for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas according to claim 1, characterized in that: The multi-stage rotor of the multi-stage high-gravity regeneration device has 2-4 layers; a liquid distributor is provided at the inner edge of each stage rotor, and a gas inlet is provided on the outer shell at the outer edge of the lowest stage rotor; partition plates are provided between the multi-stage rotors, and the multi-stage rotors form a series of gas phase flow channels; the filler of the multi-stage high-gravity regeneration device is one of stainless steel wire mesh filler, structured silicon carbide filler, and surface hydrophilic and hydrophobic combined filler.

6. A method for deep removal and regeneration of hydrogen sulfide in sulfur-containing tail gas using the system device according to any one of claims 1 to 5, characterized in that: The steps include: 1) The hydrogen sulfide-containing tail gas is transported to the gas inlet of the supergravity absorption device, where it is countercurrently contacted with the lean amine liquid from the multi-stage supergravity regeneration device and reacts. The hydrogen sulfide in the gas is absorbed into the liquid phase. The tail gas after the reaction is discharged through the gas outlet of the supergravity absorption device and then transported to the first gas-liquid separator; the gas separated by the first gas-liquid separator enters the tail gas incinerator for incineration and then discharged into the atmosphere. The liquid separated by the first gas-liquid separator flows back to the supergravity absorption device through the liquid outlet; 2) The lean amine liquid from the multi-stage high-gravity regeneration device absorbs hydrogen sulfide in the high-gravity absorption device to form rich amine liquid. The rich amine liquid is delivered to the rich amine liquid delivery pump through the liquid outlet at the bottom of the high-gravity absorption device, and then heat-exchanged in the lean-rich liquid heat exchanger and heated in the rich amine liquid heater before being delivered to the multi-stage high-gravity regeneration device; 3) The rich amine liquid entering the multi-stage high gravity regeneration device is countercurrently contacted with the steam from the reboiler in the packing area and the cavity area. The hydrogen sulfide in the rich amine liquid is desorbed and enters the condenser along with the steam through the gas outlet of the multi-stage high gravity regeneration device to recover part of the heat. The amine liquid is then transported to the second gas-liquid separator, where the steam and hydrogen sulfide are separated. The obtained hydrogen sulfide gas is transported to the Claus unit for sulfur production. The liquid condensed in the second gas-liquid separator is refluxed to the reboiler. 4) The liquid in the multi-stage super gravity regeneration device is transported to the reboiler from the bottom liquid outlet. After the regenerated lean amine liquid passes through the lean amine liquid delivery pump, a portion of it returns to the multi-stage super gravity regeneration device through the second branch pipe to further improve the desorption rate of the absorption liquid. The remaining lean amine liquid is transported to the lean-rich amine liquid heat exchanger and the lean amine liquid cooler through the first branch pipe and then enters the super gravity absorption device to complete the entire cycle operation.

7. The method for deep removal and regeneration of hydrogen sulfide according to claim 6, characterized in that: In step 1), the operating temperature of the supergravity absorption device is 30-50°C.

8. The method for deep removal and regeneration of hydrogen sulfide according to claim 6, wherein: In step 1), the hypergravity level of the hypergravity absorption device is 50-200, and the gas-liquid volume flow ratio is 20-100:

1.

9. The method for deep removal and regeneration of hydrogen sulfide according to claim 6, wherein: In step 3), the operating temperature of the multi-stage high gravity regeneration device is 110-130°C.

10. The method for deep removal and regeneration of hydrogen sulfide according to claim 6, characterized in that: In step 3), the hypergravity level of the multi-stage hypergravity regeneration device is 50-200.

Images