A sulfur recovery system

Abstract

The present invention relates to the technical field of sulfur recovery equipment, and specifically to a sulfur recovery system. The present invention provides a sulfur recovery system, comprising a gas supply system, a reaction system, a separation and reduction system, a cooling and absorption system, a tail gas treatment system, a first tail gas supply component and a second tail gas supply component; the reaction system, the separation and reduction system, the cooling and absorption system and the tail gas treatment system are connected in sequence through pipelines; the reaction system comprises a combustion furnace, a boiler and a condensation component, and the first tail gas supply component is connected between the condensation component and the combustion furnace, and is used to transport part of the tail gas discharged by the condensation component to the combustion furnace. Increasing the process gas flow rate increases the heat carried by the process gas, ensures that the mixed gas volume reaches the lower limit of the sulfur production design flexibility, and avoids pipe blockage and pipeline sulfur accumulation.

Description

Technical Field

[0001] The invention relates to the technical field of sulfur recovery equipment, and in particular to a sulfur recovery system. Background Art

[0002] At present, the process of co-firing gas or hydrogen is often used in low-load production of sulfur recovery. The principle is to use co-firing gas or hydrogen to increase the combustion value of the combustion gas, thereby increasing the furnace temperature of the combustion furnace. However, in this process, the amount of gas or hydrogen used is large, but the process gas flow is still small and the heat carried is low.

[0003] In this way, under low-load operation, due to the small process gas flow and low heat carried, the heat load of the converter and condenser cooler is insufficient, and the converter outlet temperature does not meet the process design indicators, resulting in sulfur accumulation in the pipeline. At the same time, the outlet temperature of the condenser cooler tube is too low, and the fluidity of liquid sulfur deteriorates, causing tube blockage and system shutdown. Summary of the invention

[0004] (I) The problem to be solved by the present invention is that in the process of sulfur recovery at low load, a process of burning gas or hydrogen is used. Due to the small process gas flow rate and low heat carried, the heat load of the converter and the condenser cooler is insufficient, and the converter outlet temperature does not meet the process design index, resulting in sulfur accumulation in the pipeline. At the same time, the outlet temperature of the condenser cooler tube is too low, the fluidity of the liquid sulfur deteriorates, and the tube is blocked.

[0005] (II) Technical solution

[0006] A sulfur recovery system, comprising a gas supply system, a reaction system, a separation and reduction system, a cooling and absorption system, a tail gas treatment system, a first tail gas replenishment component and a second tail gas replenishment component;

[0007] The reaction system, the separation and reduction system, the cooling and absorption system and the tail gas treatment system are connected in sequence through pipelines;

[0008] The reaction system includes a combustion furnace, a boiler and a condensation component, wherein the first tail gas supply component is connected between the condensation component and the combustion furnace, and is used to transport part of the tail gas discharged from the condensation component to the combustion furnace;

[0009] The second tail gas replenishing component is connected between the cooling absorption system and the separation reduction system, and is used to transport part of the tail gas discharged from the cooling absorption system to the separation reduction system.

[0010] According to one embodiment of the present invention, the first tail gas replenishment assembly includes a first pipeline structure and a first steam ejector, and the first pipeline structure includes a first inlet pipe, a first outlet pipe and a first steam pipe;

[0011] One end of the first inlet pipe is connected to the exhaust gas inlet of the first steam injector, the other end of the first inlet pipe is connected to the separation reduction system, the first outlet pipe is connected between the combustion furnace and the mixed gas outlet of the first steam injector, and the first steam pipe is connected to the steam inlet of the first steam injector.

[0012] According to one embodiment of the present invention, the first exhaust gas replenishment component also includes a first regulating valve and a first gas flow meter, the first regulating valve is installed on the first steam pipe and is used to control the amount of steam entering the first steam injector, and the first gas flow meter is installed on the first inlet pipe.

[0013] According to one embodiment of the present invention, the separation and reduction system comprises a tail gas liquid separation tank, a heater and a hydrogenation reactor which are sequentially connected through pipelines;

[0014] The second tail gas replenishment component includes a second pipeline structure and a second steam injector, and the second steam injector includes a second inlet pipe, a second outlet pipe and a second steam pipe;

[0015] The second inlet pipe is connected between the exhaust gas inlet end of the second steam ejector and the exhaust gas outlet of the cooling absorption system, one end of the second outlet pipe is connected to the mixed gas outlet end of the second steam ejector, and the other end of the second outlet pipe is connected to the pipeline between the exhaust gas separator tank and the heater.

[0016] According to one embodiment of the present invention, the second exhaust gas replenishment component further includes a second regulating valve and a second gas flow meter, the second regulating valve is installed on the second steam pipe, and the second gas flow meter is installed on the second inlet pipe.

[0017] According to one embodiment of the present invention, the condensation assembly includes a primary condensation cooler, a secondary condensation cooler, a tertiary condensation cooler and a liquid sulfur pipe, and the primary condensation cooler, the secondary condensation cooler and the tertiary condensation cooler are connected in sequence through pipelines;

[0018] The first-stage condenser cooler, the second-stage condenser cooler and the third-stage condenser cooler are respectively connected to the liquid sulfur pipe.

[0019] According to one embodiment of the present invention, a primary converter is installed on the pipeline between the primary condensation cooler and the secondary condensation cooler, and a secondary converter is installed on the pipeline between the secondary condensation cooler and the tertiary condensation cooler.

[0020] According to one embodiment of the present invention, the cooling absorption system includes a connected quenching tower and a tail gas absorption tower, the air inlet of the quenching tower and the separation and reduction system are connected through an exhaust pipe, and the exhaust port of the tail gas absorption tower and the tail gas treatment system are connected through a tail gas pipe.

[0021] According to one embodiment of the present invention, the tail gas treatment system comprises an incinerator, a second steam generator and a chimney which are connected in sequence, and an incineration blower is installed on the incinerator.

[0022] According to one embodiment of the present invention, the gas supply system includes an ammonia-containing gas separator tank, an acidic gas buffer tank and a combustion furnace blower, and the ammonia-containing gas separator tank, the acidic gas buffer tank and the combustion furnace blower are respectively connected to the combustion furnace through pipelines.

[0023] Beneficial effects of the present invention:

[0024] The present invention provides a sulfur recovery system, comprising a gas supply system, a reaction system, a separation and reduction system, a cooling absorption system, a tail gas treatment system, a first tail gas supply component and a second tail gas supply component; the reaction system, the separation and reduction system, the cooling absorption system and the tail gas treatment system are connected in sequence through pipelines; the reaction system comprises a combustion furnace, a boiler and a condensation component, the first tail gas supply component is connected between the condensation component and the combustion furnace, and is used to transport part of the tail gas discharged by the condensation component to the combustion furnace; the second tail gas supply component is connected between the cooling absorption system and the separation and reduction system, and is used to transport part of the tail gas discharged by the cooling absorption system to the separation and reduction system.

[0025] Part of the tail gas discharged from the condensation component is transported to the combustion furnace through the first tail gas replenishment component, which increases the process gas flow, improves the heat carried, ensures that the mixed gas volume reaches the lower limit of the sulfur production design flexibility, and avoids pipe blockage and sulfur accumulation in the pipeline.

[0026] Part of the tail gas discharged from the cooling absorption system is transported to the separation reduction system through the second tail gas replenishment component to ensure that the mixer gas volume reaches the lower limit of the design flexibility of the tail gas treatment system. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] In order to more clearly illustrate the specific implementation methods of the present invention or the technical solutions in the prior art, the drawings required for use in the specific implementation methods or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are some implementation methods of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0028] Figure 1 A schematic diagram provided for an embodiment of the present invention;

[0029] Figure 2 A connection diagram of a gas supply system, a reaction system and a separation and reduction system provided in an embodiment of the present invention;

[0030] Figure 3 A connection diagram of the separation and reduction system, cooling and absorption system and tail gas treatment system provided in an embodiment of the present invention.

[0031] Icons: 1-acidic acid-containing gas separator tank; 2-acidic gas buffer tank; 3-combustion furnace; 4-boiler; 5-first-stage condenser cooler; 6-second-stage condenser cooler; 7-third-stage condenser cooler; 8-tail gas separator tank; 9-heater; 10-hydrogenation reactor; 11-first steam generator; 12-quenching tower; 13-tail gas absorption tower; 14-incinerator; 15-second steam generator; 16-chimney; 17-incineration blower; 18-liquid sulfur pipe; 19-first pipeline structure; 20-exhaust pipe; 21-tail gas pipe; 22-second pipeline structure; 23-first steam ejector; 231-regulating valve; 24-gas flowmeter; 24-second steam ejector; 25-first converter; 26-second converter. DETAILED DESCRIPTION

[0032] The technical solution of the present invention will be clearly and completely described below in conjunction with the embodiments. Obviously, the described embodiments are part of the embodiments of the present invention, rather than all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0033] The design load elasticity of a large sulfur recovery unit is 30% to 110%. When the unit's processing capacity is lower than the lower limit of the design load, a process of co-firing gas or hydrogen is generally used. However, since the process gas flow is still small and the heat carried is low, it will make it difficult to maintain the temperature of each device in the system, and sulfur vapor will easily be retained, causing pipeline blockage. The process gas refers to the gas generated by the reaction in the combustion furnace 3 and all the remaining gases, that is, the tail gas.

[0034] Specifically, under low-load operation, due to the small process gas flow and low heat carried, the heat load of the converter and condenser cooler is insufficient, and the converter outlet temperature does not meet the process design indicators, resulting in sulfur accumulation in the pipeline. At the same time, the outlet temperature of the condenser cooler tube is too low, and the fluidity of liquid sulfur deteriorates, causing tube blockage and system shutdown.

[0035] like Figure 1-Figure 3 As shown, one embodiment of the present invention provides a sulfur recovery system, including a gas supply system, a reaction system, a separation and reduction system, a cooling and absorption system, a tail gas treatment system, a first tail gas replenishment component and a second tail gas replenishment component;

[0036] The reaction system, separation and reduction system, cooling and absorption system and tail gas treatment system are connected in sequence through pipelines;

[0037] The reaction system includes a combustion furnace 3, a boiler 4 and a condensation component. The first tail gas supply component is connected between the condensation component and the combustion furnace 3, and is used to transport part of the tail gas discharged from the condensation component to the combustion furnace 3;

[0038] The second tail gas replenishing component is connected between the cooling absorption system and the separation reduction system, and is used to transport part of the tail gas discharged from the cooling absorption system to the separation reduction system.

[0039] In this embodiment, if Figure 1 and Figure 2 As shown, the condensation component includes a primary condenser cooler 5, a secondary condenser cooler 6, a tertiary condenser cooler 7 and a liquid sulfur pipe 18. The primary condenser cooler 5, the secondary condenser cooler 6 and the tertiary condenser cooler 7 are connected in sequence through pipelines. A heater and a primary converter 25 are installed in sequence on the pipeline between the primary condenser cooler 5 and the secondary condenser cooler 6. A heater and a secondary converter are installed in sequence on the pipeline between the secondary condenser cooler 6 and the tertiary condenser cooler 7. The liquid sulfur pipe 18 is arranged below the primary condenser cooler 5, the secondary condenser cooler 6 and the tertiary condenser cooler 7, and the primary condenser cooler 5, the secondary condenser cooler 6 and the tertiary condenser cooler 7 are respectively connected to the liquid sulfur pipe 18 through pipelines.

[0040] The combustion gas blows gas or hydrogen into the combustion furnace 3. The high-temperature process gas generated after the combustion in the heating furnace 3 enters the boiler 4 for cooling. At the same time, the boiler 4 generates steam, and the high-temperature process gas is cooled to 320°C. Then the high-temperature process gas enters the primary condenser cooler 5 for further cooling and separation of liquid sulfur. The liquid sulfur enters the liquid sulfur pipe 18 from the primary condenser cooler 5. Then, the high-temperature process gas is heated to the required temperature by the heater, and then enters the primary converter 25 for CLAUS reaction. Then, it enters the secondary condenser cooler 6 for cooling and separation of liquid sulfur into the liquid sulfur pipe 18. Then, the high-temperature process gas enters the heater for heating again and enters the secondary converter 26 for CLAUS reaction, and finally enters the tertiary condenser cooler 7 for cooling and separation of liquid sulfur.

[0041] CLAUS reaction refers to the process in which hydrogen sulfide (H2S) is oxidized by sulfur dioxide (SO2) into sulfur and water.

[0042] In this embodiment, if Figure 2 and Figure 3As shown, the separation and reduction system includes a tail gas separator 8, a heater 9, a hydrogenation reactor 10 and a first steam generator 11, and the tail gas separator 8, the heater 9, the hydrogenation reactor 10 and the first steam generator 11 are connected in sequence through pipelines, wherein the tail gas separator 8 is connected to the exhaust port of the three-stage condensation cooler 7 through a pipeline. The tail gas discharged from the three-stage condensation cooler 7 enters the tail gas separator 8 through a pipeline, and the tail gas separator 8 further captures sulfur mist.

[0043] Preferably, Figure 2 As shown, the first exhaust gas replenishment component includes a first pipeline structure 19 and a first steam ejector 23. The first steam ejector 23 includes a steam inlet and a mixed gas outlet relative to each other. An exhaust gas inlet is also formed on the first steam ejector 23. The exhaust gas inlet and the steam inlet are vertically arranged. After the steam enters the nozzle from the steam inlet, it is ejected at high speed to generate low pressure, and the exhaust gas at the exhaust gas inlet is sucked in and mixed in the mixing chamber. After passing through the expansion tube, the kinetic energy is converted into pressure energy, and the mixed gas is ejected from the mixed gas outlet. The first steam ejector 23 is an existing steam ejector pump.

[0044] In this embodiment, preferably, the first pipeline structure 19 includes a first inlet pipe, a first outlet pipe and a first steam pipe, one end of the first inlet pipe is connected to the exhaust gas inlet of the first steam injector 23, the other end of the first inlet pipe is connected to the exhaust port of the three-stage condenser cooler 7, the first outlet pipe is connected between the combustion furnace 3 and the mixed gas outlet of the first steam injector 23, and the first steam pipe is connected to the steam inlet of the first steam injector 23.

[0045] In this way, after the steam enters the nozzle from the first steam pipe through the steam inlet, it is ejected at high speed to generate low pressure, and the tail gas discharged from the tertiary condenser cooler 7 is sucked into the first inlet pipe and quickly enters the mixing chamber to mix with the steam, and then is ejected from the first outlet pipe into the combustion furnace 3, and the mixed gas of the tail gas and steam is transported to the combustion furnace 3, thereby increasing the process gas flow rate, thereby increasing the heat carried, ensuring that the heat load of the primary converter 25, the secondary converter 26, the primary condenser cooler 5, the secondary condenser cooler 6 and the tertiary condenser cooler 7 is sufficient, the outlet temperatures of the primary converter 25 and the secondary converter 26 meet the process indicators, the pipe side outlet temperatures of the primary condenser cooler 5, the secondary condenser cooler 6 and the tertiary condenser cooler 7 are not too low, the fluidity of the liquid sulfur is normal, and pipe side blockage and sulfur accumulation in the pipeline are avoided.

[0046] In this way, part of the tail gas discharged from the three-stage condenser cooler 7 enters the tail gas separator 8 through the pipeline, and the tail gas separator 8 captures the sulfur mist and then sends it to the tail gas treatment system, and the other part is pressurized and circulated through the first steam ejector 23 and sent to the combustion furnace 3, thereby increasing the process gas flow, increasing the heat carried, and ensuring that the mixed gas volume (acid gas and circulating tail gas) reaches the lower limit of the sulfur production design flexibility, thereby avoiding pipe blockage and sulfur accumulation in the pipeline.

[0047] In addition, when the load is lower than 30%, the combustion heat value of the combustion furnace 3 is insufficient, so that the furnace temperature cannot guarantee the ammonia burning temperature greater than 1250°C. If the ammonia-containing gas is introduced into the furnace, it will lead to incomplete combustion of ammonia and easily generate amides, which can promote the oxidation of SO2 into SO3, causing the catalyst to be deactivated by sulfation, and may also produce ammonia salt crystals and deposits, which will gather on the wall and block the equipment and pipelines.

[0048] In this embodiment, since the process gas flow rate is increased, the combustion calorific value of the combustion furnace 3 is sufficient, ensuring that the furnace temperature can reach the ammonia burning temperature, avoiding the problem of incomplete combustion of ammonia due to insufficient furnace temperature, generating ammonia compounds, causing the catalyst to be deactivated by sulfation, and ammonia salts crystallizing and depositing, gathering on the wall, and clogging equipment and pipelines.

[0049] It should also be noted that in this embodiment, when the load is lower than 30% and the combustion calorific value of the combustion furnace 3 is insufficient, it is still necessary to burn gas or hydrogen. However, since the first steam injector 23 transports the mixed gas of exhaust gas and steam to the combustion furnace 3, the process gas flow rate is increased, and the heat it carries is increased, the combustion calorific value of the combustion furnace 3 can be maintained, ensuring that the temperature in the furnace is appropriate.

[0050] Preferably, the first tail gas replenishment component further includes a first regulating valve 231 and a first gas flow meter 232. The first regulating valve 231 is installed on the first steam pipe to control the amount of steam entering the first steam injector 23. The first gas flow meter 232 is installed on the first inlet pipe to detect the tail gas flow. In this way, by observing the flow value of the first gas flow meter 232, the steam flow can be adjusted through the first regulating valve 231, thereby reducing or increasing the tail gas flow.

[0051] In this embodiment, if Figure 3 As shown, the cooling absorption system includes a connected quenching tower 12 and a tail gas absorption tower 13 , an exhaust pipe 20 is connected between the first steam generator 11 and the air inlet of the quenching tower 12 , and the tail gas discharged from the first steam generator 11 enters the quenching tower 12 through the exhaust pipe 20 .

[0052] The tail gas discharged from the exhaust pipe 20 enters the quenching tower 12 for cooling, and the cooled tail gas enters the tail gas absorption tower 13, and is countercurrently contacted with the methyldiethanolamine (MDEA) solvent, and the H2S and a small amount of CO2 in the tail gas are absorbed by the solvent.

[0053] In this embodiment, if Figure 3 As shown, the exhaust gas treatment system includes an incinerator 14, a second steam generator 15 and a chimney 16 which are connected in sequence. An incineration blower 17 is installed on the incinerator 14. The exhaust port of the exhaust gas absorption tower 13 is connected to the incinerator 14 through a tail gas pipe 21. A part of the exhaust gas discharged from the tail gas absorption tower 13 enters the incinerator 14 through the tail gas pipe 21 for full combustion.

[0054] Preferably, Figure 3 As shown, the second exhaust gas replenishment assembly includes a second pipeline structure 22 and a second steam injector 24, and the second steam injector 24 includes a second inlet pipe, a second outlet pipe and a second steam pipe;

[0055] The second inlet pipe is connected between the exhaust gas inlet end of the second steam ejector 24 and the exhaust port of the exhaust gas absorption tower 13, one end of the second outlet pipe is connected to the mixed gas outlet end of the second steam ejector 24, and the other end of the second outlet pipe is connected to the pipeline between the exhaust gas separator tank 8 and the heater 9.

[0056] In this way, after the steam enters the nozzle through the steam inlet from the second steam pipe, it is ejected at high speed to generate low pressure, sucking the exhaust gas discharged from the exhaust absorption tower 13 into the second inlet pipe and quickly entering the mixing chamber to mix with the steam, and then being ejected from the second outlet pipe into the pipeline between the exhaust gas separator tank 8 and the heater 9, thereby entering the heater 9.

[0057] A part of the tail gas discharged from the tail gas absorption tower 13 is pressurized by the second steam ejector 24 and then circulated to the tail gas heater 9, ensuring that the mixed gas volume (acid gas and circulating tail gas) reaches the lower limit of the design flexibility of the tail gas treatment system, that is, ensuring that the mixed gas volume reaches the lower limit of the processing volume of the hydrogenation reactor 10, the first steam generator 11, the quenching tower 12 and the tail gas absorption tower 13.

[0058] At the same time, another part of the tail gas discharged from the tail gas absorption tower 13 enters the incinerator 14, and is thermally incinerated with fuel gas to burn sulfides into SO2. The flue gas of the incinerator is cooled by the second steam generator 15 and then discharged to the chimney 16.

[0059] Optionally, the second inlet pipe is connected between the tail gas inlet end of the second steam ejector 24 and the tail gas pipe 21, so that the tail gas discharged from the tail gas absorption tower 13 first enters the tail gas pipe 21, and then is divided into parts of the tail gas from the tail gas pipe 21 and enters the second inlet pipe.

[0060] Preferably, the second exhaust gas replenishment component also includes a second regulating valve and a second gas flow meter. Specifically, the second regulating valve is installed on the second steam pipe, and the second gas flow meter is installed on the second inlet pipe. The second regulating valve is used to adjust the amount of steam entering the second steam pipe, and the second gas flow meter is used to detect the gas flow at the second air inlet, so as to facilitate the control of the flow of the mixed gas.

[0061] In this way, the tail gas discharged from the tail gas separator 8 enters the heater 9 for heating and then enters the hydrogenation reactor, where various sulfides are hydrolyzed and hydrogenated to be reduced to H2S. After hydrogenation, the process gas is cooled by the first steam generator 11 and then enters the exhaust pipe 20 and is sent to the quenching tower 12 for further cooling. The quenched tail gas enters the tail gas absorption tower 13, and is countercurrently contacted with the methyldiethanolamine (MDEA) solvent. The H2S and a small amount of CO2 in the process gas are absorbed by the solvent. A part of the tail gas discharged from the top of the tail gas absorption tower 13 is pressurized by the second steam ejector 24 and then circulated to the front of the heater 9. The flow rate of the circulating tail gas is controlled by the second regulating valve and the second gas flow meter to ensure that the gas volume (acid gas and circulating tail gas) of the mixer reaches the lower limit of the design flexibility of the tail gas treatment system. Another part of the exhaust gas discharged from the top of the exhaust gas absorption tower 13 directly enters the exhaust pipe 21 and then enters the incinerator 14, and is thermally incinerated with fuel gas to burn sulfides into SO2. The flue gas of the incinerator 14 is cooled by the second steam generator 15 and then discharged to the chimney 16.

[0062] Preferably, Figure 2 As shown, the gas supply system includes an ammonia-containing gas liquid separator tank 1, an acid gas buffer tank 2 and a combustion furnace blower, wherein the ammonia-containing gas liquid separator tank 1 contains H2S and NH3, while the acid gas buffer tank 2 contains only H2S.

[0063] The ammonia-containing gas liquid separator tank 1, the acid gas buffer tank 2 and the combustion furnace blower are respectively connected to the combustion furnace 3 through pipelines.

[0064] Compared with the traditional low-load operation process, this sulfur recovery system has added the first tail gas replenishment component and the second tail gas replenishment component, which increases the process gas flow and the heat carried. Through experiments, it is found that this sulfur recovery system can achieve stable operation of the entire system when the design lower limit is 10%.

[0065] In the description of the present invention, it should be noted that the terms "upper", "lower", etc., indicating the orientation or positional relationship are based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, the terms "first" and "second" are only used for descriptive purposes and cannot be understood as indicating or implying relative importance.

[0066] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "installation", "connection" and "connection" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be an indirect connection through an intermediate medium, or it can be a connection between the inside of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances. In addition, in the description of the present invention, unless otherwise specified, "plurality" means two or more.

[0067] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, improvements, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A sulfur recovery system, characterized in that: It includes a gas supply system, a reaction system, a separation and reduction system, a cooling and absorption system, a tail gas treatment system, a first tail gas replenishment component and a second tail gas replenishment component; The reaction system, the separation and reduction system, the cooling and absorption system and the tail gas treatment system are connected in sequence through pipelines; The reaction system comprises a combustion furnace (3), a boiler (4) and a condensation component, wherein the first tail gas supply component is connected between the condensation component and the combustion furnace (3) and is used to transport part of the tail gas discharged from the condensation component into the combustion furnace (3); The second tail gas replenishing component is connected between the cooling absorption system and the separation reduction system, and is used to transport part of the tail gas discharged from the cooling absorption system to the separation reduction system; The separation and reduction system comprises a tail gas liquid separation tank (8), a heater (9) and a hydrogenation reactor (10) which are sequentially connected via pipelines; The second tail gas replenishment component comprises a second pipeline structure (22) and a second steam injector (24), and the second steam injector (24) comprises a second inlet pipe, a second outlet pipe and a second steam pipe; The second inlet pipe is connected between the tail gas inlet end of the second steam ejector (24) and the tail gas outlet of the cooling absorption system, one end of the second outlet pipe is connected to the mixed gas outlet end of the second steam ejector (24), and the other end of the second outlet pipe is connected to the pipeline between the tail gas separator tank (8) and the heater (9); The second tail gas replenishment component further includes a second regulating valve and a second gas flow meter, the second regulating valve is installed on the second steam pipe, and the second gas flow meter is installed on the second inlet pipe; The cooling absorption system comprises a quenching tower (12) and a tail gas absorption tower (13) which are connected to each other; the air inlet of the quenching tower (12) and the separation reduction system are connected via an exhaust pipe (20); and the exhaust port of the tail gas absorption tower (13) and the tail gas treatment system are connected via a tail gas pipe (21).

2. A sulfur recovery system according to claim 1, characterized in that: The first tail gas replenishment component comprises a first pipeline structure (19) and a first steam ejector (23), wherein the first pipeline structure (19) comprises a first inlet pipe, a first outlet pipe and a first steam pipe; One end of the first inlet pipe is connected to the exhaust gas inlet of the first steam injector (23), the other end of the first inlet pipe is connected to the separation reduction system, the first outlet pipe is connected between the combustion furnace (3) and the mixed gas outlet of the first steam injector (23), and the first steam pipe is connected to the steam inlet of the first steam injector (23).

3. A sulfur recovery system according to claim 2, characterized in that: The first exhaust gas replenishment component also includes a first regulating valve (231) and a first gas flow meter (232). The first regulating valve (231) is installed on the first steam pipe and is used to control the amount of steam entering the first steam injector (23). The first gas flow meter (232) is installed on the first inlet pipe.

4. A sulfur recovery system according to claim 1, characterized in that: The condensation assembly comprises a primary condensation cooler (5), a secondary condensation cooler (6), a tertiary condensation cooler (7) and a liquid sulfur pipe (18); the primary condensation cooler (5), the secondary condensation cooler (6) and the tertiary condensation cooler (7) are connected in sequence through pipelines; The first-stage condenser cooler (5), the second-stage condenser cooler (6), and the third-stage condenser cooler (7) are respectively connected to the liquid sulfur pipe (18).

5. A sulfur recovery system according to claim 4, characterized in that: A primary converter (25) is installed on the pipeline between the primary condenser cooler (5) and the secondary condenser cooler (6), and a secondary converter (26) is installed on the pipeline between the secondary condenser cooler (6) and the tertiary condenser cooler (7).

6. A sulfur recovery system according to claim 1, characterized in that: The tail gas treatment system comprises an incinerator (14), a second steam generator (15) and a chimney (16) which are connected in sequence, and an incineration blower (17) is installed on the incinerator (14).

7. A sulfur recovery system according to any one of claims 1 to 6, characterized in that: The gas supply system comprises an ammonia-containing gas liquid separator tank (1), an acidic gas buffer tank (2) and a combustion furnace blower. The ammonia-containing gas liquid separator tank (1), the acidic gas buffer tank (2) and the combustion furnace blower are respectively connected to the combustion furnace (3) through pipelines.

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