Hydrogen sulfide selective catalytic oxidation reaction process and multistage integrated system

Abstract

The invention discloses a hydrogen sulfide selective catalytic oxidation reaction process and a multi-stage integrated system. Reaction gas containing certain H2S concentration is introduced into a multi-stage series reactor filled with a catalyst; according to the hydrogen sulfide selective catalytic oxidation reaction sequence, air is distributed to the first-stage reactor to the last-stage reactor in sequence, reaction gas containing 0.8%-1.3% of H2S in each stage of reactor is promoted to be subjected to selective catalytic oxidation reaction through a catalyst, elemental sulfur products are directionally generated, generated sulfur steam is condensed and separated, and the hydrogen sulfide is obtained. And obtaining liquid sulfur from a condensation reaction effluent of the sulfur steam until the introduced reaction gas is completely reacted. The invention has the beneficial effects that the process and the multistage integrated system are suitable for sulfur recovery of medium and low latent sulfur content, the system equipment is designed in a highly integrated manner, the pipeline arrangement and occupied area and space are reduced, the process is shortened, the process is simple, the occupied area is greatly reduced, the control parameters are reduced, and the operation efficiency of the equipment is improved; the sulfur yield is high, and the national emission standard of tail gas SO2 can be directly met.

Description

Technical Field

[0001] The present invention relates to the technical field of acid gas purification technology, and in particular to a hydrogen sulfide selective catalytic oxidation reaction process and a multi-stage integrated system. Background Art

[0002] Hydrogen sulfide (H2S) is a colorless, highly toxic acidic gas. It is the simplest of the sulfur hydrides. It has no noticeable odor at high concentrations, but has a strong rotten egg smell at low concentrations and a sulfur smell at extremely low concentrations. It is a by-product of many industrial processes, such as natural gas extraction, petroleum refining, wastewater treatment, and the paper industry.

[0003] For acid gas containing low concentrations of H2S, the traditional Claus sulfur recovery process can cause the incinerator to not burn properly due to the low acid gas concentration, hindering the conversion of H2S to elemental sulfur. Therefore, the selective catalytic oxidation of hydrogen sulfide (SCO) process can successfully convert low-concentration H2S into high-purity elemental sulfur. The SCO oxidation sulfur production process is a non-equilibrium reaction. With the right catalyst, nearly 100% conversion of H2S to elemental sulfur can be achieved, significantly improving sulfur yields.

[0004] In the 1970s, UOP in the United States pioneered the Selectox process, solving the challenge of sulfur recovery from lean acid gas. Subsequently, Jacobs of the Netherlands proposed the Super Claus process in the 1980s. This process uses a selective oxidation catalyst in the final converter stage to directly convert low-concentration H₂S in the process gas into elemental sulfur, increasing the sulfur recovery rate of the two-stage Claus process from 94% to 99%. Later, a hydrogenation reactor was added to the Super Claus process to convert SO₂ and organic sulfur in the process gas into elemental sulfur and H₂S. The process gas was then fed into a final selective catalytic converter, where almost all H₂S gas was directly converted into elemental sulfur, achieving a total sulfur recovery rate of 99.6%. Compared to the traditional Claus process, this significantly improved sulfur recovery and reduced SO₂ emissions in the tail gas. Furthermore, while achieving high sulfur recovery, this process is significantly shorter and requires significantly less investment than the combined Claus + SCOT tail gas treatment process. Consequently, this selective oxidation sulfur recovery process has been widely used in coal chemical, refinery gas, and natural gas processing.

[0005] Foreign companies that produce sulfur by direct selective oxidation of H2S include BASF, CLARIANT, Shell, Johnson Matthey, Grace, etc. Domestic production and R&D units include Sinopec Qilu Petrochemical Research Institute, CNPC Natural Gas Research Institute, Wuhan Guolitong, etc.

[0006] Most of these selective oxidation catalysts are used in large-scale sulfur recovery units such as Super Claus and Superior Claus. However, for small- to medium-scale acid gas sulfur recovery, the Super Claus process is typically not chosen due to its relatively long process, high investment, and complex operation. Instead, chelated iron wet oxidation technology is used for sulfur recovery. While the chelated iron process is highly mature and simple, making it particularly suitable for desulfurization or sulfur recovery of gases with low to medium sulfur potentials, it has a low solution sulfur capacity, is prone to sulfur blockage during operation, and has poor sulfur quality. Higher sulfur potentials increase operating costs, and these problems have long plagued the oil industry. Therefore, a greener and more efficient sulfur recovery method is needed to address the technical challenges of sulfur recovery from low to medium sulfur potentials. Summary of the Invention

[0007] To solve the above technical problems, the present invention provides a hydrogen sulfide selective catalytic oxidation reaction process and a multi-stage integrated system suitable for small and medium-scale potential sulfur treatment, which can achieve efficient conversion and recovery of hydrogen sulfide.

[0008] The technical solution is as follows: In a first aspect, the present invention provides a process for selective catalytic oxidation of hydrogen sulfide, comprising the following steps:

[0009] Step 1: passing the reaction gas containing a certain H2S concentration into a multi-stage series reactor filled with catalyst;

[0010] Step 2: According to the order of the selective catalytic oxidation reaction of hydrogen sulfide, the air is distributed to the first to the last reactor, and the air volume is Where F is the concentration of H2S in the reaction gas.

[0011] degree, n is the number of stages of multi-stage series reactors, n≥2;

[0012] Step 3: Promoting a selective catalytic oxidation reaction of the reaction gas containing 0.8% to 1.3% H2S concentration in each reactor stage by a catalyst to generate elemental sulfur products, and condensing and separating the generated sulfur vapor until all the reaction of the reaction gas introduced in step 1 is completed;

[0013] Step 4: obtaining liquid sulfur from the condensation reaction effluent, wherein the last stage of the multi-stage series reactor obtains purified gas and the other stages obtain process gas.

[0014] Preferably, the maximum temperature of each reactor in step 3 does not exceed 250°C.

[0015] Preferably, the reaction temperature of the catalyst loaded in the reactor is 150-250°C, and the space velocity is controlled at 800-2400h -1 , the oxygen-sulfur ratio of the catalyst is 0.5-0.6.

[0016] Preferably, the reaction gas in step 1 is one or more of acid gas, low-pressure natural gas, associated gas and other sulfur-containing gases.

[0017] Preferably, the latent sulfur content of the reaction gas is 0.5-20 t / d.

[0018] Preferably, the multi-stage series reactor in step 1 is fed with a total reaction gas having a concentration of 5% H2S, and the reactor in step 2 is a four-stage reactor, each stage of the reactor is equipped with reaction gas and air, wherein the reaction gas is 25% of the total reaction gas and the air volume is In step 3, the reaction gas in each reactor contains 1.25% H2S concentration for selective catalytic oxidation reaction.

[0019] Preferably, nitrogen or tail gas recycling gas or purified gas is added to the reaction gas with H2S concentration higher than 5% for dilution treatment.

[0020] A second aspect of the present invention provides a multi-stage integrated system for a hydrogen sulfide selective catalytic oxidation reaction process, wherein the multi-stage series reactors are integrated together, the inlet of the multi-stage reactor is connected to a reaction gas input pipeline and an air inlet pipe, the outlet of each reactor of the multi-stage reactor is connected to the inlet of a sulfur condenser via a delivery pipeline A, the outlet of the sulfur condenser is connected to a delivery pipeline C and a delivery pipeline B, wherein the delivery pipeline C leads to a tail gas collector, and the delivery pipeline B is connected to the inlet of a reheater, and the outlet of the reheater is connected to a circulation pipeline communicating with the multi-stage reactor;

[0021] The delivery pipeline C and the delivery pipeline B are both provided with a sulfur collecting pipeline, one end of the sulfur collecting pipeline is communicated with the delivery pipeline C and the delivery pipeline B, and the other end is communicated with the liquid sulfur storage tank.

[0022] Preferably, the interior of the multi-stage reactor is divided into a primary reactor, a secondary reactor, a tertiary reactor and a quaternary reactor by partitions, the sulfur condenser is correspondingly divided into four condensation areas, and the reheater is correspondingly divided into three reheating areas;

[0023] The outlet of each stage reactor in the multi-stage reactor is connected to a conveying pipe A which is fed into the corresponding condensing area of ​​the sulfur condenser for condensation and separation. After separation, the sulfur is fed into the corresponding reheating area of ​​the reheater through a conveying pipe B for heating. After heating, the sulfur is fed into the corresponding reactor through a circulation pipe.

[0024] Preferably, temperature detectors are provided in the first-stage reactor, the second-stage reactor, the third-stage reactor and the fourth-stage reactor of the multi-stage reactor, and a residual oxygen online detector is installed at the outlet of the fourth-stage reactor.

[0025] Compared with the prior art, the present invention has the following beneficial effects: the process and system are suitable for sulfur recovery with medium and low sulfur potential, and can solve the long-standing problems of low sulfur recovery rate, difficulty in meeting the standards for tail gas SO2 emissions, complicated process flow and equipment, and solid waste or wastewater generation in the field of small and medium-sized sulfur recovery. In addition, the highly integrated design of the equipment in the system greatly improves the operating efficiency of the equipment, reduces pipeline layout and floor space, shortens the sulfur recovery process, reduces control parameters, has a high degree of automation, has a high sulfur recovery rate, can directly meet the national standards for tail gas SO2 emissions, and reduces investment and operating costs. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 It is a structural schematic diagram of the present invention. DETAILED DESCRIPTION

[0027] The present invention will be further described below with reference to the embodiments and accompanying drawings.

[0028] like Figure 1 As shown, a process for selective catalytic oxidation of hydrogen sulfide comprises the following steps:

[0029] Step 1: passing the reaction gas containing a certain H2S concentration into a multi-stage series reactor filled with catalyst;

[0030] Step 2: According to the order of the selective catalytic oxidation reaction of hydrogen sulfide, the air is distributed to the first to the last reactor, and the air volume is Where F is the concentration of H2S in the reaction gas.

[0031] degree, n is the number of stages of multi-stage series reactors, n≥2;

[0032] Step 3: Promoting a selective catalytic oxidation reaction of the reaction gas containing 0.8% to 1.3% H2S concentration in each reactor stage by a catalyst to generate elemental sulfur products, and condensing and separating the generated sulfur vapor until all the reaction of the reaction gas introduced in step 1 is completed;

[0033] Step 4: obtaining liquid sulfur from the condensation reaction effluent, wherein the last stage of the multi-stage series reactor obtains purified gas and the other stages obtain process gas.

[0034] The maximum temperature of each reactor in step 3 does not exceed 250°C.

[0035] The reaction temperature of the catalyst loaded in the reactor is 150-250°C. The reactor space velocity mainly depends on the catalyst activity and the H2S concentration in the reaction gas. The allowable space velocity is controlled at 800-2400h -1If the allowed H2S reaction ratio in each reactor stage is higher, in order to ensure the sulfur yield, the space velocity is appropriately lowered, otherwise the space velocity is increased; the oxygen-sulfur ratio of the catalyst is 0.5-0.6. If the catalyst conversion efficiency decreases, the oxygen-sulfur ratio can be appropriately increased. When the catalytic performance is better, the oxygen-sulfur ratio can be appropriately reduced, but the minimum oxygen-sulfur ratio should not be lower than the theoretical stoichiometric value, i.e., 0.5; the composition and concentration of the catalyst are 52.2%-63.8% of aluminum oxide, 14.4%-17.6% of magnesium oxide, 20.7%-25.3% of titanium dioxide, 1.8%-2.2% of sodium oxide, and 0.9%-1.1% of manganese dioxide.

[0036] The reaction gas in step 1 includes one or more of acid gas, low-pressure natural gas, associated gas and other sulfur-containing gases, and the potential sulfur content is 0.5-20t / d.

[0037] In step 1, a total reaction gas with a concentration of 5% H2S is introduced into the multi-stage series reactor, and the reactor in step 2 is a four-stage reactor, each stage of the reactor is equipped with reaction gas and air, wherein the reaction gas is 25% of the total reaction gas and the air volume is In step three, the selective catalytic oxidation reaction is carried out in each reactor stage using a reaction gas containing 1.25% H2S. This quantitative oxidation reaction ensures that the heat release in each reactor stage is limited, and the temperature rise is low. For this type of non-equilibrium exothermic reaction, the selectivity for sulfur production is extremely high, reaching nearly 100% conversion. Conventional multi-stage Claus reactions, however, are limited by chemical equilibrium and cannot achieve 100% conversion of H2S to sulfur.

[0038] If reaction gas containing 5% H2S enters the multi-stage reactor 1 and is supplied with sufficient air, a high heat release will result, requiring a large amount of heat removal. Even so, the heat released by the reaction will cause the bed temperature to rise significantly, reaching the hotspot temperature. There is always a lag in the increase or decrease in bed temperature caused by the reaction heat, making it difficult to immediately detect the increase or decrease in reaction heat caused by changes in H2S concentration. This will directly affect the product conversion efficiency and may lead to excess H2S or excess SO2 in the exhaust gas. Regardless of which substance is excessive, the sulfur yield will be reduced.

[0039] For reaction gases with H2S concentration higher than 5%, nitrogen or tail gas recycle gas or purified gas is added for dilution. The dilution treatment can make the H2S gas concentration reach the H2S concentration range required by this process, which is beneficial to improving the application range of this process, and can flexibly adjust the H2S concentration of acid gas, thereby improving the adaptability of sulfur recovery in low and medium potential sulfur content occasions.

[0040] The reaction principle of the hydrogen sulfide selective catalytic oxidation process is based on the one-step selective oxidation of H2S to directly generate S, and the reaction follows the following reaction formula:

[0041] H2S+1 / 2O2=S+H2SΔH=-217kJ / mol K(200℃)=1×10 14

[0042] This reaction is a non-equilibrium reaction and can convert H2S into S by 100%. The final reaction product of the system is S. The sulfur-containing substances in the process are mainly H2S and S, and the tail gas produces almost no SO2 or a very small amount of SO2.

[0043] A multi-stage integrated system for a hydrogen sulfide selective catalytic oxidation reaction process is capable of implementing the aforementioned hydrogen sulfide selective catalytic oxidation reaction process. The multi-stage series reactors are integrated into a multi-stage reactor 1. The inlet of the multi-stage reactor 1 is connected to a reaction gas input pipeline 5 and an air intake pipe 11. The outlet of each reactor stage of the multi-stage reactor 1 is connected to the inlet of a sulfur condenser 2 via a delivery pipeline A6. The outlet of the sulfur condenser 2 is connected to a delivery pipeline C7 and a delivery pipeline B8, respectively. The delivery pipeline C7 leads to a tail gas collector 9, and the delivery pipeline B8 is connected to the inlet of a reheater 3. The outlet of the reheater 3 is connected to a circulation pipeline connected to the multi-stage reactor 1.

[0044] The delivery pipeline C7 and the delivery pipeline B8 are both provided with a sulfur collecting pipeline 10 , one end of the sulfur collecting pipeline 10 is communicated with the delivery pipeline C7 and the delivery pipeline B8 , and the other end is communicated with the liquid sulfur storage tank 4 .

[0045] The multi-stage reactor 1 is divided into a primary reactor 101, a secondary reactor 102, a tertiary reactor 103 and a quaternary reactor 104 by partitions. The inlet and outlet ends of the sulfur condenser 2 are divided into four areas in a cross shape, including condensation area a 201, condensation area b 202, condensation area c 203 and condensation area d 204. The reheater 3 is also divided into three reheating areas accordingly.

[0046] The reaction gas input pipeline 5 and the first air inlet pipe 11a are connected to the primary reactor 101. The first delivery pipeline A601 at the outlet end of the primary reactor 101 is correspondingly connected to the inlet of the a-zone condenser 201. The outlet of the a-zone condenser 201 is connected to the first delivery pipeline B801. The other end of the first delivery pipeline B801 is connected to the inlet of the first reheating zone in the reheater 3. The outlet of the first reheating zone is connected to the secondary reactor 102 through the first circulation pipeline 102a.

[0047] The inlet of the secondary reactor 102 is connected to the second air inlet pipe 11b, and the outlet thereof is provided with a second delivery pipe A602, which is connected to the condenser 202 in zone b. A second delivery pipe B802 is provided at the outlet of the condenser 202 in zone b. The other end of the second delivery pipe B802 is connected to the inlet of the second reheating region in the reheater 3, and the outlet of the second reheating region is connected to the tertiary reactor 103 through the second circulation pipe 103a.

[0048] The inlet of the tertiary reactor 103 is connected to the third air inlet pipe 11c, and the outlet thereof is provided with a third delivery pipe A603, which is connected to the condensation 203 of zone C. A third delivery pipe B803 is provided at the outlet of the condensation 203 of zone C. The other end of the third delivery pipe B803 is connected to the inlet of the third reheating region in the reheater 3, and the outlet of the third reheating region is connected to the quaternary reactor 104 through the third circulation pipe 104a.

[0049] The inlet of the four-stage reactor 104 is connected to the fourth air inlet pipe 11d, and its outlet is connected to the d-zone condenser 204 through the fourth delivery pipe A604. The outlet of the d-zone condenser 204 is connected to the delivery pipe C7 leading to the tail gas collector 9. The first delivery pipe B801, the second delivery pipe B802, the third delivery pipe B803 and the delivery pipe C7 are all connected to the sulfur collection pipe 10 connected to the liquid sulfur storage tank 4.

[0050] Reheater 3 offers a wide range of heat sources, including thermal oil, steam, and high-temperature flue gas. The optimal heating method should be selected based on available utilities. Generally speaking, oil and gas processing companies have high steam production and often have a surplus of steam available. Under these conditions, steam heating is preferred because it is clean, convenient, and provides stable operation and control. For desulfurization and sulfur recovery operations at the wellhead or in remote locations, where available utility resources are limited, thermal oil or flue gas heating is generally recommended.

[0051] Temperature detectors are installed in the primary reactor 101, secondary reactor 102, tertiary reactor 103, and quaternary reactor 104 of the multi-stage reactor 1. An online residual oxygen detector is installed at the outlet of the quaternary reactor 104. The temperature of the multi-stage reactor 1 is controlled at 150-250°C. The inlet temperatures of the secondary reactor 102, tertiary reactor 103, and quaternary reactor 104 are uniformly controlled by the reheater 3, and generally enter each reactor at the same temperature. The inlet temperature of the primary reactor 101 is affected by the preceding preheater and can be flexibly adjusted as needed.

[0052] The temperature detector within the multi-stage reactor 1 and the online residual oxygen detector at the outlet of the fourth-stage reactor 104 work together to determine the catalyst's operating performance based on the temperature rise of each reactor stage and the residual oxygen value at the reactor outlet. Real-time detection of the residual oxygen concentration allows for timely adjustment and correction of the air distribution ratio of the fourth-stage reactor 104. Even if the conversion rate of a reactor stage fluctuates due to catalyst performance, the air distribution of the fourth-stage reactor 104 can be flexibly adjusted to compensate for the sulfur yield loss caused by the decline in the efficiency of the previous stage's catalytic reaction, thereby promoting the complete conversion of H2S to S. This staged reaction and air distribution control strategy ensures the same H2S conversion rate for each stage without worrying about excessive air supply or excessive exothermic temperature rise, which could lead to excessive catalytic oxidation of H2S by the catalyst to produce SO2 byproducts.

[0053] Example 1

[0054] 5% H2S is introduced into the primary reactor 101 through the reaction gas input line 5, and an amount of air capable of reacting 1.25% H2S is introduced through the first air inlet pipe 11a. The reaction gas and air undergo a selective catalytic oxidation reaction over the catalyst in the primary reactor 101. After the reaction is completed, the process gas is fed into the sulfur condenser 2 through the conveying line A6. After condensation in the condensation zone a 201 of the sulfur condenser 2, the converted sulfur is conveyed to the liquid sulfur storage tank 4 through the sulfur collection line 10 on the conveying line C7. The remaining unreacted process gas is fed into the reheater 3 through the conveying line B8 for heating. After heating, it enters the secondary reactor 102 through the circulation line, condenses in the condensation zone b 202, and is subsequently circulated to the condensation zone d 204. When the process gas emerges from the condensation zone d 204, the concentration of residual H2S or SO2 in the tail gas after four reactions and condensations is extremely low, fully meeting the tail gas emission requirements, and is then fed into the tail gas collector 9.

[0055] Example 2

[0056] By using a multi-stage integrated system as in Example 1, the H2S concentration was adjusted and the amount of air introduced into each reactor stage was changed accordingly to ensure that 0.8% H2S was converted in each reactor stage. After multiple cycles, it was ensured that all H2S was converted into S, and the reaction selectivity for producing S was close to 100%.

[0057] Example 3

[0058] By using a multi-stage integrated system as in Example 1, the H2S concentration was adjusted and the amount of air introduced into each reactor stage was changed accordingly to ensure that 1.3% H2S concentration was converted in each reactor stage. After multiple cycles, it was ensured that all H2S was converted into S, and the reaction selectivity for generating S was close to 100%.

[0059] This process and multi-stage integrated system uses highly integrated equipment with a simple process, which shortens the sulfur recovery process, significantly reduces space occupation, reduces control parameters, has a high degree of automation, and has a high sulfur recovery rate. It can directly meet national standards for tail gas SO2 emissions and can reduce investment and operating costs.

[0060] Finally, it should be noted that the above description is only a preferred embodiment of the present invention. Under the guidance of the present invention, ordinary technicians in this field can make various similar expressions without violating the purpose and claims of the present invention. Such changes fall within the scope of protection of the present invention.

Claims

1. A process for selective catalytic oxidation of hydrogen sulfide, characterized in that: The steps include: Step 1: passing the reaction gas containing a certain H2S concentration into a multi-stage series reactor filled with catalyst; Step 2: Air is supplied to the first to last reactors in the order of the selective catalytic oxidation reaction of hydrogen sulfide. Where F is the concentration of H2S in the reaction gas, n is the number of stages of the multi-stage series reactor, n ≥ 2; Step 3: Promoting a selective catalytic oxidation reaction of the reaction gas containing 0.8% to 1.3% H2S concentration in each reactor stage by a catalyst to generate elemental sulfur products, and condensing and separating the generated sulfur vapor until all the reaction of the reaction gas introduced in step 1 is completed; Step 4: obtaining liquid sulfur from the condensation reaction effluent of the sulfur vapor, wherein the last stage reactor of the multi-stage series reactor obtains purified gas, and the other stages reactors obtain process gas.

2. The selective catalytic oxidation process for hydrogen sulfide according to claim 1, characterized in that: The maximum temperature of each reactor in step 3 does not exceed 250°C.

3. The selective catalytic oxidation process for hydrogen sulfide according to claim 1, characterized in that: The reaction temperature of the catalyst loaded in the reactor is 150-250°C, and the space velocity is controlled at 800-2400h -1 , the oxygen-sulfur ratio of the catalyst is 0.5-0.

6.

4. The selective catalytic oxidation process for hydrogen sulfide according to claim 1, 2 or 3, characterized in that: The reaction gas in step 1 is one or more of acid gas, low-pressure natural gas, associated gas and other sulfur-containing gases.

5. The process for selective catalytic oxidation of hydrogen sulfide according to claim 4, characterized in that: The latent sulfur content of the reaction gas is 0.5-20t / d.

6. The process for selective catalytic oxidation of hydrogen sulfide according to claim 4, characterized in that: In step 1, a total reaction gas with a 5% H2S concentration is introduced into the multi-stage series reactor, and the reactor in step 2 is a four-stage reactor, each stage of the reactor is equipped with reaction gas and air, wherein the reaction gas accounts for 25% of the total reaction gas. In step 3, the reaction gas in each reactor contains 1.25% H2S concentration for selective catalytic oxidation reaction.

7. The process for selective catalytic oxidation of hydrogen sulfide according to claim 6, characterized in that: For reaction gases with H2S concentration higher than 5%, nitrogen or tail gas recycling gas or purified gas is added for dilution.

8. A multi-stage integrated system for implementing the process according to any one of claims 1 to 7, characterized in that: The multi-stage series reactor is an integrated multi-stage reactor (1), wherein the inlet of the multi-stage reactor (1) is connected to a reaction gas input pipeline (5) and an air inlet pipe (11), and the outlet of each stage reactor of the multi-stage reactor (1) is connected to the inlet of a sulfur condenser (2) through a conveying pipeline A (6), and the outlet of the sulfur condenser (2) is connected to a conveying pipeline C (7) and a conveying pipeline B (8), wherein the conveying pipeline C (7) leads to a tail gas collector (9), and the conveying pipeline B (8) is connected to the inlet of a reheater (3), and the outlet of the reheater (3) is connected to a circulation pipeline communicating with the multi-stage reactor (1); The delivery pipeline C (7) and the delivery pipeline B (8) are both provided with a sulfur collecting pipeline (10), one end of the sulfur collecting pipeline (10) is communicated with the delivery pipeline C (7) and the delivery pipeline B (8), and the other end is communicated with the liquid sulfur storage tank (4).

9. The multi-level integrated system according to claim 8, characterized in that: The interior of the multi-stage reactor (1) is divided into a primary reactor (101), a secondary reactor (102), a tertiary reactor (103) and a quaternary reactor (104) by partitions, the sulfur condenser (2) is correspondingly divided into four condensation areas, and the reheater (3) is correspondingly divided into three reheating areas; The conveying pipe A (6) connected to the outlet of each stage reactor in the multi-stage reactor (1) is led into the corresponding condensation area of ​​the sulfur condenser (2) for condensation separation, and after separation, it is sent to the corresponding reheating area of ​​the reheater (3) through the conveying pipe B (8) for heating, and then passed into the corresponding reactor through the circulation pipe after heating.

10. The multi-level integrated system according to claim 9, characterized in that: Temperature detectors are provided in the first-stage reactor (101), the second-stage reactor (102), the third-stage reactor (103) and the fourth-stage reactor (104) of the multi-stage reactor (1), and a residual oxygen online detector is installed at the outlet of the fourth-stage reactor (104).

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