Sulfur recovery unit

Abstract

This invention provides a sulfur recovery device. The sulfur recovery device includes a reaction section having a first reaction chamber and a first inlet, a second inlet, and a product outlet communicating with the first reaction chamber; a feeding section including a first air inlet pipe configured to introduce hydrogen sulfide gas into the first reaction chamber via the first inlet; an air inlet section for supplying air to the second inlet; a sulfur collection section including a receiving structure and a first collection pipe communicating with the product outlet; and an air distribution ratio adjustment section including a controller and a temperature detection component. The temperature detection component is disposed on the first air inlet pipe and is controlled by the controller, which is also controlled by the air inlet section to control the air flow rate supplied by the air inlet section to the second inlet. The technical solution of this invention solves the problem in existing sulfur recovery devices that affect the air distribution ratio adjustment.

Description

Technical Field

[0001] This invention relates to the field of sulfur recovery technology, and more specifically, to a sulfur recovery device. Background Technology

[0002] Coal-based methanol production refers to the process of producing methanol from coal through a series of chemical reactions. The basic flow of the coal-based methanol process includes the following main steps: Step 1, gasification: In this process, coal reacts with oxygen and water under high pressure to generate syngas. The main components of syngas include CO, H2, CO2, H2O, and small amounts of CH4, H2S, etc. The equation for the gasification reaction is: C + H2O = CO + H2; Step 2, conversion: In the conversion process, CO reacts with water vapor to generate more H2. The equation for the conversion reaction is: CO + H2O(g) = CO2 + H2 (exothermic reaction); Step 3, low-temperature methanol washing and purification: This is used to remove CO2, H2S, and other impurities from the gas phase; Step 4, methanol synthesis and refining: The purified syngas is compressed by a gas compressor and enters the methanol reactor. Under certain pressure and with the action of a catalyst, crude methanol is generated. After passing through a separator, the crude methanol then passes through a methanol refiner to obtain refined methanol product.

[0003] During the purification process, the generated H2S is sent to a sulfur recovery unit to generate sulfur, ensuring that the SO2 content in the tail gas meets the standards. Sulfur recovery utilizes Claus sulfur recovery technology to treat acidic gases containing H2S. Claus sulfur recovery technology is a chemical process used to treat acidic gases containing hydrogen sulfide (H2S) and convert them into elemental sulfur. Claus sulfur recovery technology is implemented through a Claus oxidizer. Inside the Claus oxidizer, one-third of the H2S is oxidized to SO2 by air. The SO2 then reacts with the unconverted H2S to produce sulfur. The reaction equations are as follows: 2H2S + 3O2 = 2SO2 + 2H2O; 2H2S + SO2 = 2H2O + 3S. The air ratio refers to the ratio of the amount of acidic gas entering the Claus oxidizer to the amount of air entering the Claus oxidizer. Generally, the H2S / SO2 ratio after the reaction is controlled by adjusting the air ratio, thereby improving the sulfur conversion rate.

[0004] The air distribution ratio is generally adjusted using an online analyzer. However, the online analyzer in a sulfur recovery unit passes through the Claus oxidation furnace, reactor, and condenser, thus exhibiting a certain degree of lag. Existing technologies have made improvements to address this lag. For example, CN204022473U discloses an H2S / SO2 ratio control system for a sulfur recovery unit. This method effectively controls the H2S / SO2 ratio, improving the stability of the ratio and reducing the sulfur content in the sulfur production tail gas. This reduces the load on the subsequent tail gas hydrogenation treatment section, ultimately lowering the sulfur content in the exhaust gas and achieving significant economic and social benefits. CN109824017A discloses a sulfur recovery unit and method based on automatic adjustment of Claus air distribution. This method changes the traditional independent dual-loop control process of main and auxiliary air. When the auxiliary air overshoots, the main air flow rate is adjusted to control the air distribution system, ensuring that the H2S to SO2 ratio at the Claus process reactor outlet approaches the ideal reaction ratio while simultaneously bringing the auxiliary air flow rate back to a reasonable range. CN109850852A discloses a Claus air distribution control system based on a sulfur recovery device. This method first changes the location of the online H2S / SO2 analyzer from the outlet of the Claus secondary reactor to the outlet of the Claus primary reactor, reducing the lag time of detection feedback. It uses the H2S content in the process gas to control the air distribution, mitigating the oscillation problem caused by unstable proportional control. Although patent CN109850852A changes the location of the online analyzer for detecting H2S / SO2 gas content from the outlet of the Claus secondary reactor to the outlet of the Claus primary reactor, reducing the lag time of detection feedback, it still cannot completely solve the problem of detection feedback lag. CN113264508B discloses a sulfur recovery method and apparatus. This method simultaneously incorporates an acid gas component analyzer and a ratio analyzer. When the acid gas composition changes, the concentration of the air-oxygen mixture in the first delivery pipeline is adjusted in a timely manner via a first regulating valve, and the concentration of the mixture in the second delivery pipeline is adjusted in a timely manner via a second regulating valve, ensuring that the sulfur recovery device maintains optimal air distribution operation, thereby improving the sulfur recovery rate. CN116358298A discloses an industrial control system for a sulfur recovery device. This method includes a main fan control system, an acid gas control system, an air-gas ratio control system, and an online feedback control system. By comprehensively utilizing a first flow detection component, an acid gas flow detection component, a second flow detection component, and an online gas analyzer to collect information on the air entering and leaving the sulfur recovery device, fuel gas, and acidic gases generated in the reaction, measurement errors can be effectively reduced, and the total sulfur recovery rate of the Claus sulfur recovery device can be improved.

[0005] However, when the temperature of the acid gas (H2S) is too high, it will carry the methanol from the upstream low-temperature methanol washing unit into the Claus oxidizer. In this way, the methanol will consume oxygen in the Claus oxidizer, thereby reducing the oxygen content in the Claus oxidizer. This will not only reduce the sulfur content generated in the Claus oxidizer, but also affect the adjustment of the air distribution ratio. Summary of the Invention

[0006] The main objective of this invention is to provide a sulfur recovery device to solve the problem that existing sulfur recovery devices can affect the adjustment of the air distribution ratio.

[0007] To achieve the above objectives, the present invention provides a sulfur recovery device, comprising a reaction section having a first reaction chamber and a first inlet, a second inlet, and a product outlet connected to the first reaction chamber; a feeding section including a first air inlet pipe configured to introduce hydrogen sulfide gas into the first reaction chamber via the first inlet; an air inlet section for supplying air to the second inlet; a sulfur collection section including a receiving structure and a first collection pipe connected to the receiving structure and the product outlet; and an air distribution ratio adjustment section including a controller and a temperature detection component disposed on the first air inlet pipe and controlled by the controller, which is controlled by the air inlet section to control the air flow rate supplied by the air inlet section to the second inlet.

[0008] Furthermore, the air intake section includes: a second air intake pipe, the air intake end of which is used to introduce external air, and the air outlet end of which is connected to a second inlet; a hydrodynamic component, which is disposed on the second air intake pipe; a regulating valve assembly, which is disposed on the second air intake pipe, and a controller is connected to the regulating valve assembly and / or the hydrodynamic component for control.

[0009] Furthermore, the regulating valve assembly includes a first regulating valve and a second regulating valve, wherein the flow regulation range of the first regulating valve is greater than the flow regulation range of the second regulating valve; or, the air intake section further includes a filter, which is disposed at the air intake end of the second air intake pipe and is used to filter the outside air.

[0010] Furthermore, the feeding section also includes: a feeding pipeline configured to allow the passage of the mixed material; a gas-liquid separation structure having a first separation chamber and a feeding port, a first liquid outlet and a first gas outlet communicating with the first separation chamber, the first gas outlet communicating with a first air inlet pipeline and the feeding port communicating with the feeding pipeline.

[0011] Furthermore, the reaction section also has a combustion chamber and a third inlet and a fourth inlet communicating with the combustion chamber. The combustion chamber and the first reaction chamber are spaced apart, and the combustion chamber is located on at least one side of the first reaction chamber. The sulfur recovery device also includes: a third air inlet pipe, one end of which is connected to a second air inlet pipe and the other end of which is connected to a third inlet; and a fourth air inlet pipe, one end of which is used to introduce fuel gas and the other end of which is connected to a fourth inlet.

[0012] Furthermore, the reaction section includes: a reaction body having a first inlet, a second inlet, and a first outlet; a first conveying pipeline having a first end connected to the first outlet and a second end having a product outlet; and a first heat exchanger located on the outer periphery of the first conveying pipeline for cooling the mixture in the first conveying pipeline.

[0013] Furthermore, the sulfur recovery device also includes: a first pipeline, the second end of which is provided with a gas outlet, and one end of the first pipeline is connected to the gas outlet; a first reactor, having a second reaction chamber and a fifth inlet and a second outlet connected to the second reaction chamber, the fifth inlet being connected to the other end of the first pipeline; a second pipeline, including a first main pipe and a first branch pipe and a second branch pipe both connected to the first main pipe, the first main pipe being connected to the second outlet, the first branch pipe being connected to the receiving structure, and the second branch pipe being used to discharge gas; and a second heat exchanger, located on the outer periphery of the first main pipe, the second heat exchanger being used to cool the mixture in the first main pipe.

[0014] Furthermore, the sulfur recovery device also includes a second liquid inlet pipe and a second gas outlet pipe. The second heat exchanger has a second heat exchange chamber. One end of the second liquid inlet pipe is connected to the low-pressure boiler, and the other end of the second liquid inlet pipe is connected to the second heat exchange chamber. One end of the second gas outlet pipe is connected to the second heat exchange chamber, and the other end of the second gas outlet pipe is used to discharge steam.

[0015] Furthermore, the sulfur recovery device also includes: a second reactor having a third reaction chamber and a sixth inlet and a third outlet connected to the third reaction chamber, the sixth inlet being connected to a second branch pipe; a third conveying pipeline including a second main pipe and a third branch pipe and a fourth branch pipe both connected to the second main pipe, the second main pipe being connected to a third outlet, the third branch pipe being connected to a receiving structure, and the fourth branch pipe being used to discharge gas; a third heat exchanger located on the outer periphery of the second branch pipe, the third heat exchanger being used to heat the gas in the second branch pipe; and a fourth heat exchanger located on the outer periphery of the second main pipe, the fourth heat exchanger being used to cool the mixture.

[0016] Furthermore, the sulfur recovery device also includes a third liquid inlet pipe and a third gas outlet pipe, a fourth heat exchanger having a third heat exchange chamber, one end of the third liquid inlet pipe being connected to a low-pressure boiler, the other end of the third liquid inlet pipe being connected to the third heat exchange chamber, one end of the third gas outlet pipe being connected to the third heat exchange chamber, and the other end of the third gas outlet pipe being used to discharge steam; or, the sulfur recovery device also includes: an analysis unit, installed on the fourth branch pipe, the analysis unit being used to detect the gas content, and a controller being connected to the analysis unit for control; or, the sulfur recovery device also includes: a sulfur separation unit, installed on the fourth branch pipe, the sulfur separation unit having a second liquid outlet; a fourth collection pipe, one end of the fourth collection pipe being connected to a receiving structure, the other end of the fourth collection pipe being connected to the second liquid outlet, the sulfur separation unit being used to separate the liquid sulfur in the fourth branch pipe from the fourth branch pipe and allow it to enter the receiving structure through the fourth collection pipe.

[0017] Applying the technical solution of this invention, hydrogen sulfide gas is introduced into the first reaction chamber through the first inlet via the first inlet pipe, while air enters the first reaction chamber through the second inlet. The hydrogen sulfide gas and air react within the first reaction chamber. By installing a temperature detection component on the first inlet pipe, when the temperature of the hydrogen sulfide gas in the first inlet pipe increases, the temperature detection component transmits a signal to the controller. The controller can immediately respond to the temperature change of the hydrogen sulfide gas and adjust the air flow rate entering the second inlet in a timely manner. This avoids methanol being carried into the first reaction chamber due to the increased temperature of the hydrogen sulfide gas, thus preventing methanol from consuming air in the first reaction chamber. This not only avoids the problem of decreased sulfur production in the first reaction chamber but also prevents the hydrogen sulfide gas-air ratio from deviating from the optimal setting. This invention, through the correlation control of temperature and air flow rate, precisely compensates for the change in the air-air ratio caused by methanol consuming oxygen, ensuring that the reaction in the first reaction chamber proceeds under optimal conditions and improving the sulfur conversion rate. Attached Figure Description

[0018] The accompanying drawings, which form part of this application, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an undue limitation of the invention. In the drawings:

[0019] Figure 1 A schematic diagram of an embodiment of the sulfur recovery device of the present invention is shown;

[0020] Figure 2 It shows Figure 1 A curve showing the relationship between the acid gas temperature and air consumption in a sulfur recovery unit.

[0021] The above figures include the following reference numerals:

[0022] 100. Reaction section; 200. Inlet section; 10. Main reaction body; 11. Regeneration tower; 12. Tail gas incineration section; 13. Receiving structure; 14. Sulfur granulator; 15. First inlet pipe; 16. Seventh inlet pipe; 17. Sixth inlet pipe; 18. Fourth inlet pipe; 20. First reactor; 21. Second inlet pipe; 22. First heat exchanger; 23. Second heat exchanger; 24. Fourth heat exchanger; 25. Third heat exchanger; 26. Fourth collection pipe; 27. Second branch pipe; 28. Fifth pipe; 29. ​​Return pipe; 30. Second reactor; 31. First liquid inlet pipe; 32. Second liquid inlet pipe; 3 3. First collection pipeline; 34. First branch pipe; 35. Third branch pipe; 36. Fifth air inlet pipeline; 37. Third liquid inlet pipeline; 38. Third air inlet pipeline; 40. Gas-liquid separation structure; 41. Second pipeline; 42. Feed pipeline; 43. Fourth branch pipe; 44. Central pipe; 45. First pipeline; 46. First gas outlet pipeline; 47. First main pipeline; 48. Second gas outlet pipeline; 49. Second main pipeline; 50. Analysis section; 51. First liquid outlet pipeline; 52. Third gas outlet pipeline; 53. Third pipeline; 55. Fourth pipeline; 60. Fluid dynamic components; 70. Filter; 80. Sulfur separation section; 90. Absorption tower. Detailed Implementation

[0023] It should be noted that, unless otherwise specified, the embodiments and features described in this application can be combined with each other. The present invention will now be described in detail with reference to the accompanying drawings and embodiments.

[0024] like Figure 1 As shown, an embodiment of the present invention provides a sulfur recovery device. The sulfur recovery device includes a reaction section 100 having a first reaction chamber and a first inlet, a second inlet, and a product outlet communicating with the first reaction chamber; a feeding section including a first air inlet pipe 15 configured to introduce hydrogen sulfide gas into the first reaction chamber through the first inlet; an air inlet section 200 for supplying air to the second inlet; a sulfur collection section including a receiving structure 13 and a first collection pipe 33 for communicating the receiving structure 13 with the product outlet; and an air distribution ratio adjustment section including a controller and a temperature detection component. The temperature detection component is disposed on the first air inlet pipe 15 and is controlled by the controller. The controller is controlled by the air inlet section 200 to control the air flow rate introduced by the air inlet section 200 to the second inlet.

[0025] In the above technical solution, hydrogen sulfide gas is introduced into the first reaction chamber through the first inlet of the first inlet pipe 15, and air enters the first reaction chamber through the second inlet. The hydrogen sulfide gas and air react within the first reaction chamber. By installing a temperature detection component on the first inlet pipe 15, when the temperature of the hydrogen sulfide gas in the first inlet pipe 15 increases, the temperature detection component transmits a signal to the controller. The controller can immediately respond to the temperature change of the hydrogen sulfide gas and adjust the air flow rate entering the second inlet of the inlet section 200 in a timely manner. This avoids methanol being carried into the first reaction chamber due to the increased temperature of the hydrogen sulfide gas, thus preventing methanol from consuming air in the first reaction chamber. This not only avoids the problem of decreased sulfur production in the first reaction chamber but also prevents the hydrogen sulfide gas-air ratio from deviating from the optimal setting. This invention, through the correlation control of temperature and air flow rate, accurately compensates for the change in the air-air ratio caused by methanol consuming oxygen, ensuring that the reaction in the first reaction chamber proceeds under optimal conditions and improving the sulfur conversion rate.

[0026] Furthermore, in embodiments of the present invention, the combination of the temperature detection component and the air ratio adjustment unit provides greater flexibility in the operation of the sulfur recovery device. Technicians can observe the temperature of the hydrogen sulfide gas and make timely adjustments to the airflow entering the first reaction chamber, reducing the lag in reliance on the analysis unit 50 and enhancing the predictability and controllability of the sulfur recovery device.

[0027] Specifically, in the embodiments of the present invention, the reaction occurring in the first reaction chamber is a Claus reaction, which includes two stages: oxygen in the air entering the first reaction chamber reacts with 1 / 3 of the H2S to generate SO2, and SO2 then reacts with unconverted H2S to produce sulfur. The reaction equations are as follows: 2H2S + 3O2 = 2SO2 + 2H2O; 2H2S + SO2 = 2H2O + 3S. The generated sulfur enters the receiving structure 13 through the product outlet via the first collection pipe 33. The receiving structure 13 is a sulfur aeration tank. The sulfur recovery device also includes a sulfur granulator 14. After aeration in the receiving structure 13, the sulfur enters the sulfur granulator 14. The sulfur granulator 14 is a device for converting liquid sulfur into solid granules. The specific structures of the sulfur aeration tank and the sulfur granulator 14 can be referred to in the prior art, and will not be described in detail here.

[0028] Specifically, in the embodiments of the present invention, the temperature detection component is a temperature sensor.

[0029] like Figure 1As shown, in an embodiment of the present invention, the air intake 200 includes a second air intake pipe 21, the air intake end of the second air intake pipe 21 is used to introduce external air, and the air outlet end of the second air intake pipe 21 is connected to a second inlet; a fluid dynamic component 60 is disposed on the second air intake pipe 21; a regulating valve assembly is disposed on the second air intake pipe 21, and a controller is controlled to be connected to the regulating valve assembly and / or the fluid dynamic component 60.

[0030] In the above technical solution, when the temperature of the hydrogen sulfide gas in the first intake pipe 15 increases, the temperature detection component transmits a signal to the controller. The controller can adjust the air flow rate into the first reaction chamber by adjusting the rotation speed of the fluid power component 60 and / or the opening of the regulating valve assembly. In this way, on the one hand, it can prevent the high-temperature hydrogen sulfide gas from carrying methanol into the first reaction chamber, thereby preventing methanol from consuming air in the first reaction chamber and improving the sulfur yield. On the other hand, it can also compensate for the imbalance of the air distribution ratio caused by temperature changes, reduce control lag, and improve the reaction efficiency in the first reaction chamber.

[0031] Preferably, in an embodiment of the present invention, the hydrodynamic component 60 is a fan.

[0032] In one embodiment, the hydrodynamic component may also be a piston pump, a compressor, or a diaphragm pump.

[0033] Specifically, in the embodiments of the present invention, when the temperature of hydrogen sulfide gas rises and causes methanol in the first reaction chamber to consume oxygen, the air flow rate entering the first reaction chamber is adjusted in a timely manner to ensure the optimal conduct of the sulfur generation reaction, thereby reducing energy consumption and improving energy utilization efficiency.

[0034] like Figure 1 As shown, in an embodiment of the present invention, the regulating valve assembly includes a first regulating valve and a second regulating valve, wherein the flow regulation range of the first regulating valve is greater than the flow regulation range of the second regulating valve.

[0035] In the above technical solution, by setting a first regulating valve and a second regulating valve, dynamic control can be achieved from large-scale adjustment to fine-tuning of the air flow entering the first reaction chamber. By using regulating valves with different adjustment ranges in combination, the best balance point can be found between large-scale adjustment and small-scale adjustment, avoiding the control instability that may occur when a single regulating valve is adjusted significantly, thereby avoiding the phenomenon of affecting the sulfur yield.

[0036] Specifically, in the embodiments of the present invention, since the first regulating valve has a large flow rate regulation range, it is suitable for handling a large range of air flow rate changes and can quickly respond to changes in air demand caused by large temperature fluctuations of hydrogen sulfide gas; the second regulating valve has a smaller flow rate regulation range and is more suitable for fine adjustment. Through the synergistic effect of the first regulating valve and the second regulating valve, the regulating valve assembly can achieve more precise air flow rate control.

[0037] Specifically, in an embodiment of the present invention, the second intake pipe 21 includes a first intake branch pipe and a second intake branch pipe. A first regulating valve is disposed on the first intake branch pipe, and a second regulating valve is disposed on the second intake branch pipe. The first regulating valve is a main process air regulating valve, and the second regulating valve is a secondary process air regulating valve. The flow rate regulation range of the first regulating valve is 0-4000 m³ / s. 3 / h, the adjustment range of the second regulating valve is 0-800m 3 / h.

[0038] like Figure 1 As shown in the embodiment of the present invention, the air intake 200 further includes a filter 70, which is disposed at the air intake end of the second air intake pipe 21 and is used to filter the outside air.

[0039] In the above technical solution, by setting up a filter 70, the filter 70 can filter the external air entering the second air inlet pipe 21 of the sulfur recovery device, effectively removing dust, particulate matter and other impurities in the external air, preventing these impurities from entering the first reaction chamber, thereby reducing interference with the sulfur generation process.

[0040] like Figure 1 As shown, in an embodiment of the present invention, the feeding section further includes a feeding pipe 42, which is configured to allow the passage of a mixture; the gas-liquid separation structure 40 has a first separation chamber and a feeding port, a first liquid outlet and a first gas outlet communicating with the first separation chamber, the first gas outlet communicating with the first air inlet pipe 15, and the feeding port communicating with the feeding pipe 42.

[0041] In the above technical solution, the mixed material enters the gas-liquid separation structure 40 through the feed pipe 42. The first separation chamber can separate the mixed material introduced through the feed pipe 42. The separated gas enters the first reaction chamber through the first gas outlet and the first gas inlet pipe 15 so as to react with the oxygen in the first reaction chamber to generate sulfur.

[0042] Specifically, in the embodiments of the present invention, the gas phase of the mixture is an acidic gas, the main components of which are H2S, N2 and CO2, and the liquid phase of the mixture is mainly methanol. The gas-liquid separation structure 40 is a gas-liquid separation tank, which can separate liquid methanol from the mixture so that H2S in the acidic gas can react with oxygen in the first reaction chamber to generate sulfur.

[0043] like Figure 1 As shown, in an embodiment of the present invention, the reaction section further includes a combustion chamber and a third inlet and a fourth inlet communicating with the combustion chamber. The combustion chamber and the first reaction chamber are spaced apart, and the combustion chamber is located on at least one side of the first reaction chamber. The temperature-controlled sulfur recovery device further includes a third air inlet pipe 38, one end of which is connected to the second air inlet pipe 21, and the other end of which is connected to the third inlet; and a fourth air inlet pipe 18, one end of which is used to introduce fuel gas, and the other end of which is connected to the fourth inlet.

[0044] In the above technical solution, external air enters the combustion chamber through the third inlet via the second intake pipe 21 and the third intake pipe 38, while fuel gas enters the combustion chamber through the fourth inlet via the fourth intake pipe 18. The external air and fuel gas are burned in the combustion chamber, which can increase the reaction temperature in the first reaction chamber and thus increase the yield of sulfur.

[0045] Specifically, in embodiments of the present invention, the fuel gas includes CO, H2, and CO2.

[0046] Specifically, in the embodiments of the present invention, since the combustion chamber is located around the first reaction chamber, a uniform heat distribution can be provided to the first reaction chamber, avoiding local overheating or uneven temperature in the first reaction chamber, which would lead to a decrease in reaction efficiency.

[0047] In one embodiment, the combustion chamber may also be located on one circumferential side of the first reaction chamber.

[0048] In existing technologies, the Claus reaction process for sulfur production mainly consists of two stages: a high-temperature thermal reaction and a low-temperature catalytic reaction. The high-temperature thermal reaction is completed in the first reaction chamber, with the temperature typically controlled between 950℃ and 1300℃. The low-temperature catalytic reaction is completed in a first-stage reactor and a second-stage reactor. The temperature of the first-stage reactor is typically controlled between 230℃ and 270℃. This temperature range is favorable for the hydrolysis of organic sulfur, ensuring sulfur recovery. Therefore, it is necessary to cool the mixture entering the first-stage reactor. Figure 1As shown, in an embodiment of the present invention, the reaction section includes a reaction body 10, which has a first inlet, a second inlet and a first outlet; a first conveying pipeline, the first end of which is connected to the first outlet and the second end of which has a product outlet; and a first heat exchanger 22, which is located on the outer periphery of the first conveying pipeline and is used to cool the mixture in the first conveying pipeline.

[0049] In the above technical solution, after hydrogen sulfide gas and air react in the reaction body 10, the products generated by the reaction and the unreacted reactants form a mixture and enter the first conveying pipeline. The first heat exchanger 22 can cool the mixture in the first conveying pipeline. In this way, the mixture before entering the reactor section can be cooled to improve the sulfur yield.

[0050] Specifically, in an embodiment of the present invention, the reaction body 10 has the first reaction chamber described above.

[0051] Specifically, in the embodiments of the present invention, the sulfur recovery device further includes a first liquid inlet pipe 31 and a first gas outlet pipe 46. The first heat exchanger 22 has a first heat exchange chamber. One end of the first liquid inlet pipe 31 is connected to a low-pressure boiler, and the other end of the first liquid inlet pipe 31 is connected to the first heat exchange chamber. One end of the first gas outlet pipe 46 is connected to the first heat exchange chamber, and the other end of the first gas outlet pipe 46 is used to discharge steam.

[0052] In the above technical solution, the high-temperature mixture in the reaction body 10 enters the first conveying pipeline through the first outlet, and the liquid in the low-pressure boiler enters the first heat exchange chamber through the first liquid inlet pipe 31. The high-temperature mixture exchanges heat with the liquid, and the high-temperature mixture transfers heat to the liquid, causing the liquid temperature to rise and turn into steam. The steam is discharged through the first gas outlet pipe 46, and the temperature of the mixture decreases. In this way, the mixture before entering the reactor section can be cooled down, so as to improve the sulfur yield.

[0053] Specifically, in the embodiments of the present invention, the liquid in the low-pressure boiler is water, and the steam discharged from the first steam outlet pipe 46 is low-pressure steam, which is sent into the steam pipeline network for recovery.

[0054] Preferably, in an embodiment of the present invention, the first heat exchanger 22 is a plate heat exchanger.

[0055] In the prior art, the reaction equation for a single-stage reactor is: 2H₂S + SO₂ = 2H₂O + 3S. Since the temperature of the single-stage reactor is typically controlled between 230℃ and 270℃, the product after the reaction is gaseous. Therefore, it is necessary to cool the mixture after the reaction to convert the gaseous sulfur into liquid sulfur, and then recover the liquid sulfur through the receiving structure 13. Therefore, if... Figure 1 As shown, in an embodiment of the present invention, the sulfur recovery device further includes a first pipeline 45, the second end of which is provided with a gas outlet, and one end of the first pipeline 45 is connected to the gas outlet; a first reactor 20, having a second reaction chamber and a fifth inlet and a second outlet connected to the second reaction chamber, the fifth inlet being connected to the other end of the first pipeline 45; a second conveying pipeline, including a first main pipe 47 and a first branch pipe 34 and a second branch pipe 27 both connected to the first main pipe 47, the first main pipe 47 being connected to the second outlet, the first branch pipe 34 being connected to the receiving structure 13, and the second branch pipe 27 being used to discharge gas; and a second heat exchanger 23, located on the outer periphery of the first main pipe 47, the second heat exchanger 23 being used to cool the mixture in the first main pipe 47.

[0056] In the above technical solution, the unreacted gases (H2S and SO2) cooled by the first heat exchanger 22 are transported to the first reactor 20 through the fifth inlet via the first pipeline 45 and reacted in the first reactor 20. The products generated by the reaction and the unreacted reactants form a mixture. The mixture enters the first main pipe 47 through the second outlet. The second heat exchanger 23 is used to cool the mixture after the reaction in the first reactor 20 to turn the gaseous sulfur into liquid sulfur. The cooled gas is discharged through the second branch pipe 27, and the liquid sulfur flows to the receiving structure 13 through the first branch pipe 34.

[0057] Specifically, in an embodiment of the present invention, the second heat exchanger 23 is a waste heat recovery unit.

[0058] Specifically, in an embodiment of the present invention, the sulfur recovery device further includes a central pipe 44, one end of which is connected to a first outlet and the other end of which is connected to a first pipeline 45. The high-temperature mixture in the central pipe 44 is mixed with the mixture cooled by the first heat exchanger 22, thereby adjusting the temperature of the mixture.

[0059] like Figure 1 As shown in the embodiment of the present invention, the sulfur recovery device further includes a second liquid inlet pipe 32 and a second gas outlet pipe 48. The second heat exchanger 23 has a second heat exchange chamber. One end of the second liquid inlet pipe 32 is connected to a low-pressure boiler, and the other end of the second liquid inlet pipe 32 is connected to the second heat exchange chamber. One end of the second gas outlet pipe 48 is connected to the second heat exchange chamber, and the other end of the second gas outlet pipe 48 is used to discharge steam.

[0060] In the above technical solution, the mixture in the first reactor 20 enters the first main pipe 47 through the second outlet, and the liquid in the low-pressure boiler enters the second heat exchange chamber through the second liquid inlet pipe 32. The mixture and the liquid exchange heat, and the mixture transfers heat to the liquid. The liquid temperature rises and turns into steam. The steam is discharged through the second gas outlet pipe 48, and the temperature of the mixture decreases so that the gaseous sulfur turns into liquid sulfur. The cooled gas is discharged through the second branch pipe 27, and the liquid sulfur flows into the receiving structure 13 through the first branch pipe 34.

[0061] Specifically, in the embodiments of the present invention, the steam discharged from the second exhaust pipe 48 is low-pressure steam. The low-pressure steam is sent into the steam pipeline network. Low-pressure steam refers to steam used in industrial production processes with a pressure lower than that of conventional low-pressure steam, usually below 0.5 bar (approximately equal to 0.5 atmospheres).

[0062] After the second heat exchanger 23 cools the gas in the second branch pipe 27, since the temperature of the second-stage reactor is usually controlled between 230℃ and 270℃, it is necessary to heat the gas in the second branch pipe 27. Therefore, if... Figure 1 As shown in the embodiment of the present invention, the sulfur recovery device further includes a third heat exchanger 25, which is located on the outer periphery of the second branch pipe 27 and is used to heat the gas in the second branch pipe 27.

[0063] In the above technical solution, the third heat exchanger 25 can heat the gas in the second branch pipe 27 to increase the temperature of the gas in the second branch pipe 27, thereby improving the reaction efficiency.

[0064] Specifically, in the embodiments of the present invention, the third heat exchanger 25 is a plate heat exchanger, and the third heat exchanger 25 has a fourth heat exchange chamber. The sulfur recovery device also includes a fifth air inlet pipe 36 and a first liquid outlet pipe 51. One end of the fifth air inlet pipe 36 is used to introduce medium-pressure steam, the temperature of which is between 380°C and 420°C. The other end of the fifth air inlet pipe 36 is connected to the fourth heat exchange chamber. One end of the first liquid outlet pipe 51 is connected to the fourth heat exchange chamber, and the other end of the first liquid outlet pipe 51 is used to discharge condensate. The medium-pressure steam is introduced into the fourth heat exchange chamber through the fifth air inlet pipe 36. The gas in the second branch pipe 27 exchanges heat with the medium-pressure steam, and the gas in the second branch pipe 27 is heated. The medium-pressure steam is cooled and condensed, and then discharged through the first liquid outlet pipe 51.

[0065] In the prior art, the reaction equation for the two-stage reactor is: 2H₂S + SO₂ = 2H₂O + 3S. Since the temperature of the two-stage reactor is typically controlled between 230℃ and 270℃, the product after the reaction is gaseous. Therefore, it is necessary to cool the mixture after the reaction to convert the gaseous sulfur into liquid sulfur, and then recover the liquid sulfur through the receiving structure 13. Therefore, if... Figure 1 As shown, in an embodiment of the present invention, the sulfur recovery device further includes a second reactor 30 having a third reaction chamber and a sixth inlet and a third outlet connected to the third reaction chamber, the sixth inlet being connected to a second branch pipe 27; a third conveying pipeline including a second main pipe 49 and a third branch pipe 35 and a fourth branch pipe 43 both connected to the second main pipe 49, the second main pipe 49 being connected to the third outlet, the third branch pipe 35 being connected to the receiving structure 13, and the fourth branch pipe 43 being used to discharge gas; and a fourth heat exchanger 24 located on the outer periphery of the second main pipe 49, the fourth heat exchanger 24 being used to cool the mixture.

[0066] In the above technical solution, the mixture after being cooled by the second heat exchanger 23 and heated by the third heat exchanger 25 is transported to the second reactor 30 through the sixth inlet via the second branch pipe 27 and reacted in the second reactor 30. The products generated by the reaction and the unreacted reactants form a mixture. The mixture enters the second main pipe 49 through the third outlet. The fourth heat exchanger 24 is used to cool the mixture after the reaction in the second reactor 30 to turn gaseous sulfur into liquid sulfur. The cooled gas is discharged through the fourth branch pipe 43, and the liquid sulfur flows to the receiving structure 13 through the third branch pipe 35.

[0067] Specifically, in the embodiments of the present invention, the first reactor 20 is a single-stage reactor and the second reactor 30 is a two-stage reactor.

[0068] like Figure 1 As shown in the embodiment of the present invention, the sulfur recovery device further includes a third liquid inlet pipe 37 and a third gas outlet pipe 52. The fourth heat exchanger 24 has a third heat exchange chamber. One end of the third liquid inlet pipe 37 is connected to the low-pressure boiler, and the other end of the third liquid inlet pipe 37 is connected to the third heat exchange chamber. One end of the third gas outlet pipe 52 is connected to the third heat exchange chamber, and the other end of the third gas outlet pipe 52 is used to discharge steam.

[0069] In the above technical solution, the mixture in the second reactor 30 enters the second main pipe 49 through the third outlet, and the liquid in the low-pressure boiler enters the third heat exchange chamber through the third liquid inlet pipe 37. The mixture and the liquid exchange heat, and the mixture transfers heat to the liquid. The liquid temperature rises and turns into steam. The steam is discharged through the third gas outlet pipe 52. The temperature of the mixture decreases so that the gaseous sulfur turns into liquid sulfur. The cooled gas is discharged through the fourth branch pipe 43, and the liquid sulfur flows into the receiving structure 13 through the third branch pipe 35.

[0070] Specifically, in the embodiments of the present invention, the fourth heat exchanger 24 is a plate heat exchanger, and the steam discharged from the third outlet pipe 52 is sent into the steam pipe network for recovery.

[0071] like Figure 1 As shown in the embodiment of the present invention, the sulfur recovery device further includes an analysis unit 50, which is installed on the fourth branch pipe 43. The analysis unit 50 is used to detect the content of gas, and the controller is connected to the analysis unit 50 for control.

[0072] In the above technical solution, by setting up an analysis unit 50, the gas content of the fourth branch pipe 43 can be detected, and the air intake of external air into the first reaction chamber can be adjusted according to the gas content, thereby improving the sulfur yield.

[0073] Specifically, in the embodiments of the present invention, the analysis unit 50 is an H2S / SO2 analyzer. The specific structure of the H2S / SO2 analyzer can be referred to the prior art, and will not be described in detail here.

[0074] Specifically, in the embodiments of the present invention, the analysis unit 50 detects the content of H2S and SO2. When the H2S content is high and the SO2 content is low, the intake of external air is increased; when the H2S content is low and the SO2 content is high, the amount of external air used is reduced.

[0075] Because the sulfur generated during the reaction in the reaction body 10, the first reactor 20, and the second reactor 30 is difficult to completely separate, therefore, as Figure 1 As shown, in an embodiment of the present invention, the sulfur recovery device further includes a sulfur separation section 80, which is disposed on the fourth branch pipe 43. The sulfur separation section 80 has a second liquid outlet. A fourth collection pipe 26 is connected at one end to the receiving structure 13 and at the other end to the second liquid outlet. The sulfur separation section 80 is used to separate the liquid sulfur in the fourth branch pipe 43 from the fourth branch pipe 43 and allow it to enter the receiving structure 13 through the fourth collection pipe 26.

[0076] In the above technical solution, the sulfur separation unit 80 can separate the liquid sulfur that has not been separated in the reaction body 10, the first reactor 20 and the second reactor 30, thereby ensuring the full recovery of sulfur. The liquid sulfur enters the receiving structure 13 through the fourth collection pipe 26 from the fourth liquid outlet.

[0077] Specifically, in the embodiments of the present invention, the sulfur separation section 80 is a sulfur separator. The specific structure of the sulfur separator can be referred to the prior art, and will not be described in detail here.

[0078] Specifically, in an embodiment of the present invention, the sulfur recovery device further includes a hydrogenation reactor, which is disposed on the fourth branch pipe 43 and downstream of the analysis section 50. The hydrogenation reactor is used to treat the incompletely converted sulfides in the gas in the fourth branch pipe 43. After the hydrogenation reaction, the sulfides in the tail gas are converted into hydrogen sulfide.

[0079] Specifically, in embodiments of the present invention, the sulfur recovery device further includes a quench tower, which is installed on the fourth branch pipe 43 and located downstream of the hydrogenation reactor. The function of the quench tower is to cool the high-temperature gas from the hydrogenation reactor, creating suitable temperature conditions for the subsequent absorption process. Its operation is as follows: the high-temperature gas is transported from the hydrogenation reactor to the quench tower, where it comes into contact with a sprayed cooling liquid (such as water or a coolant), absorbing heat from the gas and thus reducing its temperature. The quench tower is typically equipped with a temperature control device to ensure that the high-temperature gas is cooled to a suitable absorption temperature, preventing hydrogen sulfide from re-vaporizing at excessively high temperatures. After cooling, any droplets that may be carried in the high-temperature gas are separated by a demister or cyclone separator to prevent them from affecting the subsequent absorption process.

[0080] Specifically, in embodiments of the present invention, the sulfur recovery device further includes an absorption tower 90, a regeneration tower 11, a second pipeline 41, and a third pipeline 53. The absorption tower 90 is used to absorb hydrogen sulfide cooled from the quench tower. The interior of the absorption tower 90 is filled with an absorbent liquid, such as an amine solution. The amine solution can react with the hydrogen sulfide in the cooled gas. The cooled gas enters the absorption tower 90 and contacts the absorbent liquid in a countercurrent or bubbling manner. The hydrogen sulfide in the gas is absorbed by the absorbent liquid, forming a hydrogen sulfide-rich solution. The function of the regeneration tower 11 is to regenerate the hydrogen sulfide-rich solution in the absorption tower 90. The process is as follows: the hydrogen sulfide-rich solution in the absorption tower 90 is sent into the regeneration tower 11, and the hydrogen sulfide is desorbed from the solution by heating (such as steam heating). In this way, the hydrogen sulfide and the amine solution are desorbed and separated. The amine solution after desorbing the hydrogen sulfide is sent back to the absorption tower 90 for the absorption tower 90 to absorb hydrogen sulfide again. The absorption tower 90 and the regeneration tower 11 are connected by a third pipeline 53, which can transport the hydrogen sulfide-rich solution in the absorption tower 90 to the regeneration tower 11. The absorption tower 90 and the regeneration tower 11 are connected by a second pipeline 41, which can return the amine solution after desorption of hydrogen sulfide to the absorption tower 90.

[0081] Specifically, in an embodiment of the present invention, the sulfur recovery device further includes a reflux pipeline 29, one end of which is connected to the regeneration tower 11 and the other end of which is connected to the feed pipeline 42. Since hydrogen sulfide and amine solution are desorbed and separated in the regeneration tower 11, the desorbed hydrogen sulfide is returned to the feed pipeline 42 through the reflux pipeline 29 so as to generate sulfur again.

[0082] Specifically, in the embodiments of the present invention, the sulfur recovery device further includes a tail gas incineration section 12 and a fourth pipeline 55. The tail gas incineration section 12 is a tail gas incinerator. One end of the fourth pipeline 55 is connected to the absorption tower 90, and the other end of the fourth pipeline 55 is connected to the tail gas incineration section 12. The absorption tower 90 can absorb hydrogen sulfide in the gas cooled from the quench tower. The SO2 that is not absorbed in the absorption tower 90 is transported to the tail gas incineration section 12 through the fourth pipeline 55 for incineration. After incineration, it is discharged into the atmosphere through the chimney.

[0083] Specifically, in the embodiments of the present invention, the sulfur recovery device further includes a fifth pipeline 28 and a third regulating valve. One end of the fifth pipeline 28 is connected to the fourth branch pipe 43, and the other end of the fifth pipeline 28 is connected to the tail gas incineration section 12. The third regulating valve is installed on the fifth pipeline 28. When the absorption tower 90 or the regeneration tower 11 malfunctions, the third regulating valve is opened, and the gas directly enters the tail gas incineration section 12 for incineration. After incineration, the gas is discharged into the atmosphere through the chimney.

[0084] Specifically, in the embodiments of the present invention, the sulfur recovery device further includes a sixth air inlet pipe 17 and a seventh air inlet pipe 16. The seventh air inlet pipe 16 is used to introduce oxygen into the first reaction chamber. Introducing oxygen can raise the temperature in the first reaction chamber. However, in the actual operation of the sulfur recovery device, the seventh air inlet pipe 16 is not put into use because it does not meet safety requirements. The sixth air inlet pipe 17 is used to introduce SWS (acid water stripping gas) gas into the first reaction chamber.

[0085] Specifically, in the embodiments of the present invention, the amount of methanol carried by the acid gas during temperature changes is simulated using Aspen Plus software. The physical property method selected is NRTL, and the gas-liquid separation structure 40 utilizes the Flash2 module. The parameters of the gas-liquid separation structure 40 are shown in the table below:

[0086] Temperature / °C 40 Pressure / MPa 0.25

[0087] Specifically, in the embodiments of the present invention, when the temperature of the acidic gas is 71.3°C, the content of the acidic gas is as shown in the table below:

[0088]

[0089] Specifically, in the embodiments of the present invention, sensitivity analysis was performed using Aspen Plus, and the relationship between the methanol concentration in the acidic gas and the temperature of the acidic gas was obtained as shown in the table below:

[0090]

[0091] When methanol enters the first reaction chamber, the reaction equation is: 2CH3OH + 3O2 = 2CO2 + 4H2O; therefore, it can be calculated that when the acid gas flow rate is 5000 Nm... 3 When the oxygen volume content in the air is 20.9%, the external air flow rate consumed at different acid gas temperatures can be calculated, as shown in the table below:

[0092]

[0093] Specifically, such as Figure 2 As shown in the embodiment of the present invention, the data in the above table is plotted as a curve using the Oringe software. The horizontal axis represents the temperature of the acidic gas, and the vertical axis represents the consumed external airflow. The formula for the amount of air consumed to carry methanol corresponding to the acidic gas temperature is fitted as: V = exp(6.78603 + 0.05967t + 7.14961 * 10^6) -5 t 2 ), where t is the temperature of the acid gas and V is the amount of air consumed by methanol.

[0094] Specifically, in the embodiments of the present invention, since the temperatures detected in the above table are in the low-temperature methanol washing unit upstream of the sulfur recovery unit, according to the actual on-site temperature measurement, the temperature detected by the temperature detection component on the first inlet pipe 15 is 15°C lower than the temperature detected by the low-temperature methanol washing unit, and the above formula is based on an acid gas flow rate of 5000 Nm³. 3 The value is obtained from / h. Therefore, the formula for the acid gas temperature and the amount of air consumed to carry methanol is: V=(V1 / 5000)exp[6.78603+0.05967(t-15)+7.14961*10-5(t-15)]. 2 ], where t is the temperature of the acid gas and V is the amount of air consumed by methanol.

[0095] Specifically, in the embodiments of the present invention, the amount of external air required to handle changes in the temperature of the acidic gas during the actual operation of the sulfur recovery device is shown in the table below:

[0096]

[0097] Specifically, in the embodiments of the present invention, through actual operation verification of the sulfur recovery device, the deviation between the actual external air consumption and the fitted external air consumption is not large, which can better guide actual operation.

[0098] As can be seen from the above description, the embodiments of the present invention achieve the following technical effects: Hydrogen sulfide gas is introduced into the first reaction chamber through the first inlet via the first inlet pipe, and air enters the first reaction chamber through the second inlet. The hydrogen sulfide gas and air react in the first reaction chamber. By installing a temperature detection component on the first inlet pipe, when the temperature of the hydrogen sulfide gas in the first inlet pipe increases, the temperature detection component transmits a signal to the controller. The controller can immediately respond to the temperature change of the hydrogen sulfide gas and adjust the air flow rate entering the second inlet in a timely manner. This avoids methanol being carried into the first reaction chamber due to the increased temperature of the hydrogen sulfide gas, thereby preventing methanol from consuming air in the first reaction chamber. This not only avoids the problem of decreased sulfur production in the first reaction chamber but also prevents the hydrogen sulfide gas-air ratio from deviating from the optimal setting. The present invention, through the correlation control of temperature and air flow rate, accurately compensates for the change in the air-air ratio caused by methanol consuming oxygen, ensuring that the reaction in the first reaction chamber proceeds under optimal conditions and improving the sulfur conversion rate.

[0099] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A sulfur recovery device, characterized in that, include: The reaction section (100) has a first reaction chamber and a first inlet, a second inlet and a product outlet communicating with the first reaction chamber; The feeding section includes a first inlet pipe (15), which is configured to introduce hydrogen sulfide gas into the first reaction chamber via the first inlet. An air intake (200) is used to supply air to the second inlet; The sulfur collection section includes a receiving structure (13) and a first collection pipe (33), the first collection pipe (33) being used to connect the receiving structure (13) to the product outlet; The air distribution ratio adjustment unit includes a controller and a temperature detection component. The temperature detection component is installed on the first air intake pipe (15). The temperature detection component is controlled and connected to the controller. The controller is controlled and connected to the air intake section (200). Based on the relationship between the acid gas temperature and the amount of air consumed to carry methanol, the air flow rate of the air intake section (200) to the second inlet is controlled, so as to accurately compensate for the change in air distribution ratio caused by methanol consuming oxygen.

2. The sulfur recovery device according to claim 1, characterized in that, The air intake (200) includes: The second air intake pipe (21) has an air intake end for introducing external air and an air outlet end connected to the second inlet. A hydrodynamic component (60) is disposed on the second intake pipe (21); A regulating valve assembly is disposed on the second intake pipe (21), and the controller is controlled to the regulating valve assembly and / or the hydrodynamic component (60).

3. The sulfur recovery device according to claim 2, characterized in that, The regulating valve assembly includes a first regulating valve and a second regulating valve, wherein the flow regulation range of the first regulating valve is greater than the flow regulation range of the second regulating valve; or, the air intake (200) further includes a filter (70), wherein the filter (70) is disposed at the air intake end of the second air intake pipe (21), and the filter (70) is used to filter the external air.

4. The sulfur recovery apparatus according to any one of claims 1 to 3, characterized in that, The feeding section also includes: A feed line (42) is configured to allow the passage of a mixture; The gas-liquid separation structure (40) has a first separation chamber and an inlet, a first liquid outlet and a first gas outlet connected to the first separation chamber. The first gas outlet is connected to the first air inlet pipe (15), and the inlet is connected to the inlet pipe (42).

5. The sulfur recovery device according to claim 2, characterized in that, The reaction section further includes a combustion chamber and a third inlet and a fourth inlet communicating with the combustion chamber. The combustion chamber and the first reaction chamber are spaced apart, and the combustion chamber is located on at least one side of the first reaction chamber. The sulfur recovery device further includes: The third intake pipe (38) is connected at one end to the second intake pipe (21) and at the other end to the third inlet. The fourth intake pipe (18) is used to introduce fuel gas at one end and is connected to the fourth inlet at the other end.

6. The sulfur recovery apparatus according to any one of claims 1 to 3, characterized in that, The reaction section (100) includes: The reaction body (10) is provided with a first inlet, a second inlet and a first outlet; A first conveying pipeline, wherein a first end of the first conveying pipeline is connected to the first outlet, and a second end of the first conveying pipeline is provided with the product outlet; The first heat exchanger (22) is located on the outer periphery of the first conveying pipeline and is used to cool the mixture in the first conveying pipeline.

7. The sulfur recovery device according to claim 6, characterized in that, The sulfur recovery unit also includes: The first pipeline (45) has a gas outlet at its second end, and one end of the first pipeline (45) is connected to the gas outlet. The first reactor (20) has a second reaction chamber and a fifth inlet and a second outlet connected to the second reaction chamber, the fifth inlet being connected to the other end of the first pipeline (45); The second delivery pipeline includes a first main pipe (47) and a first branch pipe (34) and a second branch pipe (27) both connected to the first main pipe (47). The first main pipe (47) is connected to the second outlet, the first branch pipe (34) is connected to the receiving structure (13), and the second branch pipe (27) is used to discharge gas. The second heat exchanger (23) is located on the outer periphery of the first main pipe (47) and is used to cool the mixture inside the first main pipe (47).

8. The sulfur recovery device according to claim 7, characterized in that, The sulfur recovery device further includes a second liquid inlet pipe (32) and a second gas outlet pipe (48). The second heat exchanger (23) has a second heat exchange chamber. One end of the second liquid inlet pipe (32) is connected to a low-pressure boiler, and the other end of the second liquid inlet pipe (32) is connected to the second heat exchange chamber. One end of the second gas outlet pipe (48) is connected to the second heat exchange chamber, and the other end of the second gas outlet pipe (48) is used to discharge steam.

9. The sulfur recovery device according to claim 7, characterized in that, The sulfur recovery unit also includes: The second reactor (30) has a third reaction chamber and a sixth inlet and a third outlet connected to the third reaction chamber, the sixth inlet being connected to the second branch pipe (27); The third delivery pipeline includes a second main pipe (49) and a third branch pipe (35) and a fourth branch pipe (43) both connected to the second main pipe (49). The second main pipe (49) is connected to the third outlet, the third branch pipe (35) is connected to the receiving structure (13), and the fourth branch pipe (43) is used to discharge gas. The third heat exchanger (25) is located on the outer periphery of the second branch pipe (27) and is used to heat the gas in the second branch pipe (27). A fourth heat exchanger (24) is located on the outer periphery of the second main pipe (49) and is used to cool the mixture.

10. The sulfur recovery device according to claim 9, characterized in that, The sulfur recovery device further includes a third liquid inlet pipe (37) and a third gas outlet pipe (52). The fourth heat exchanger (24) has a third heat exchange chamber. One end of the third liquid inlet pipe (37) is connected to a low-pressure boiler, and the other end of the third liquid inlet pipe (37) is connected to the third heat exchange chamber. One end of the third gas outlet pipe (52) is connected to the third heat exchange chamber, and the other end of the third gas outlet pipe (52) is used to discharge steam. or, The sulfur recovery device further includes: an analysis unit (50) disposed on the fourth branch pipe (43), the analysis unit (50) being used to detect the gas content, and the controller being connected to the analysis unit (50); or, The sulfur recovery device further includes: a sulfur separation section (80) disposed on the fourth branch pipe (43), the sulfur separation section (80) having a second liquid outlet; a fourth collection pipe (26), one end of the fourth collection pipe (26) being connected to the receiving structure (13), and the other end of the fourth collection pipe (26) being connected to the second liquid outlet, the sulfur separation section (80) being used to separate the liquid sulfur in the fourth branch pipe (43) from the fourth branch pipe (43) and enter the receiving structure (13) through the fourth collection pipe (26).

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