An apparatus for continuously producing COS and a method of using the same

Abstract

This invention discloses a continuous COS production apparatus and its usage method. The system includes a CO gas source pipeline, a CO purifier, a CO heating device, a sulfur feeding device, a segmented heating sulfur melting kettle, a COS synthesis catalytic reactor, and a sulfur recovery device. In use, the CO gas is dehydrated and purified, then heated to 400-500°C by the CO heating device, and then introduced into molten sulfur liquid. This brings out a CO mixture containing sulfur vapor, which reacts under the action of a catalyst to synthesize high-concentration COS gas. Unreacted sulfur vapor is cooled and recovered to the sulfur feeding device for reuse. This invention utilizes segmented heating to ensure the continuous generation of sulfur vapor required for the COS reaction, allowing the COS production reaction to proceed continuously. Online recovery of unreacted sulfur avoids pipe blockage by solid sulfur. Furthermore, continuous production significantly reduces the scale of the reaction apparatus.

Description

Technical Field

[0001] This invention relates to the field of chemical raw material preparation technology, specifically to an apparatus for the continuous preparation of COS and its usage method. Background Technology

[0002] Carbonyl sulfide (COS, also known as carbon oxysulfide) is widely used not only as an intermediate raw material in the synthesis of pesticides, pharmaceuticals, and other chemical products, such as in the synthesis of thiocarbamate pesticides like chlorpyrifos, chlorpyrifos, and oat fumigants, but also as a fumigant for protecting stored grains. Furthermore, high-purity COS can be used in the precision etching of electronic wafer components in the aerospace, machinery, and chemical industries, with a particularly rapid development trend in the etching of electronic components.

[0003] Currently, carbonyl sulfide synthesis processes are divided into wet and dry methods. The most common wet process involves the reaction of sulfuric acid with ammonium thiocyanate. For example, CN110127702A discloses a method and apparatus for preparing carbonyl sulfide gas. This method involves adding ammonium thiocyanate solution and concentrated sulfuric acid dropwise into a sulfuric acid solution of a certain concentration for reaction. The generated carbon oxysulfide gas is condensed, dried, compressed, and then packaged. Dry synthesis methods, such as those disclosed in patents CN205653172U, CN205683986U, and CN114669298A, mainly involve the reaction of CO and sulfur vapor under catalytic conditions to generate carbonyl sulfide. This method is characterized by its simple process, high yield, and environmental friendliness, making it the preferred method for large-scale industrial production of carbonyl sulfide gas. Therefore, many corresponding synthesis apparatus process patents have been published. For example, patent CN108786665A involves a carbonyl sulfide preparation apparatus and its usage method, including a sulfur melter, reactor, condenser, separation hydrazine, and product collection bottle connected in sequence. CN214810706U discloses a tubular fixed-bed reactor for producing carbonyl sulfur. By incorporating upper and lower inlet pipes, it not only ensures thorough mixing of sulfur vapor with CO but also allows for precise control of liquid sulfur vaporization, improving raw material utilization and production yield. CN 205683986U discloses a reaction vessel for synthesizing carbonyl sulfur, featuring a sulfur-fixing device between the discharge port and the discharge pipe, achieving better sulfur fixation and easier maintenance.

[0004] However, all the carbonyl sulfur production processes currently available in the literature are intermittent methods. This means that the production is interrupted due to the unsustainable supply of sulfur vapor or the unsustainable removal of sulfur, resulting in a large amount of energy wasted when starting and stopping production. Summary of the Invention

[0005] To address the shortcomings of existing technologies, this invention provides an apparatus and method for continuous COS production. By using segmented heating, the sulfur vapor required for the COS reaction can be continuously generated, allowing the COS production reaction to proceed continuously. Furthermore, by recovering unreacted sulfur online, blockage of pipelines by solid sulfur is avoided.

[0006] The present invention adopts the following technical solution:

[0007] A continuous COS production apparatus system includes a CO gas source pipeline, a sulfur feeding device, a segmented heating and melting sulfur reactor, a COS synthesis catalytic reactor, and a sulfur recovery device. The segmented heating and melting sulfur reactor is equipped with a liquid sulfur inlet, a CO inlet, and a mixed gas outlet. The liquid sulfur inlet is located on the lower part of the side wall of the segmented heating and melting sulfur reactor. The CO inlet and the mixed gas outlet are located at the top of the segmented heating and melting sulfur reactor, and the CO inlet extends into the bottom inner side of the segmented heating and melting sulfur reactor via a conduit. The top of the sulfur recovery device is equipped with... The device includes a product gas inlet and a COS gas collection port, with a liquid sulfur separation outlet at the bottom. The product gas inlet extends into the sulfur recovery unit via a conduit. The CO gas source pipeline is connected to the CO inlet. The liquid sulfur outlet on the sulfur feeding device is connected to the liquid sulfur inlet. The mixed gas outlet is connected to the feed gas inlet on the COS synthesis catalytic reactor. The product gas outlet on the COS synthesis catalytic reactor is connected to the product gas inlet. The liquid sulfur separation outlet is connected to the liquid sulfur recovery inlet on the sulfur feeding device.

[0008] Preferably, the segmented heating sulfur melting kettle is divided into an upper section, a middle section and a lower section for segmented heating. The temperature control zone of the upper section is 500-520℃, the temperature control zone of the middle section is 450-460℃, and the temperature control zone of the lower section is 300-180℃. The liquid sulfur inlet is located in the lower section.

[0009] More preferably, the length ratio of the upper, middle and lower parts of the segmented heating sulfur melting kettle is 2:(3-5):1.

[0010] The system also includes a CO purifier and a CO heating device, and the CO gas source pipeline, CO purifier, CO heating device and CO inlet are connected in series.

[0011] The system also includes a first liquid sulfur transfer pump and a second liquid sulfur transfer pump. The first liquid sulfur transfer pump is installed on the connecting pipeline between the liquid sulfur outlet and the liquid sulfur inlet, and is used to pump the liquid sulfur in the sulfur feeding device to the segmented heating and melting sulfur kettle. The second liquid sulfur transfer pump is installed on the connecting pipeline between the liquid sulfur separation outlet and the liquid sulfur recovery inlet, and is used to transport the liquid sulfur recovered by liquefaction separation in the sulfur recovery device to the sulfur feeding device for recycling.

[0012] The upper end of the sulfur feeding device is also equipped with a nitrogen inlet, a sulfur powder inlet with a switch valve, and a nitrogen outlet, and its outer side is equipped with a first heat insulation jacket.

[0013] The outer side of the sulfur recovery device's vessel body is equipped with a second heat-insulating jacket, which has a cooling water inlet and a cooling water outlet for cooling the vessel body of the sulfur recovery device.

[0014] Preferably, the insulation type of the first insulation jacket is one of electric heating, steam heating or bath heating.

[0015] A method of using an apparatus system capable of continuously preparing COS includes the following steps:

[0016] S1. Load sulfur powder into the sulfur feeding device, close the feed valve, and purge with nitrogen gas for purging.

[0017] S2. Set the constant temperature of the sulfur feeding device, the heating temperature of the segmented heating sulfur melting kettle, and the reaction temperature of the COS synthesis catalytic reactor as required.

[0018] S3. The liquid sulfur, which has been pre-melted at a constant temperature in the sulfur feeding device, is sent into the segmented heating sulfur melting kettle, and CO gas is introduced into the segmented heating sulfur melting kettle. The CO mixed gas containing sulfur vapor is then introduced into the COS synthesis catalytic reactor, where it reacts under the action of the catalyst to produce COS mixed gas.

[0019] The S4 and COS mixture enters the sulfur recovery unit for cooling. The sulfur vapor containing unreacted sulfur is liquefied by cooling and sinks to the bottom of the vessel, and is then sent to the sulfur feeding unit for reuse. The high-concentration COS gas separated is sent to the product processing unit for treatment.

[0020] In step S3, when the volume of liquid sulfur in the sulfur feeding device is less than 40% of the capacity, the feed valve is opened online and sulfur powder is added to continuously pre-melt sulfur. When the liquid sulfur in the segmented heating sulfur melting kettle reaches 50% of the capacity, 10 cubic meters of CO gas per hour is dehydrated and purified by a CO purifier, and then heated by a CO heating device before being introduced into the molten sulfur liquid in the sulfur feeding device.

[0021] In step S2, the temperature range of the first insulation jacket of the sulfur feeding device is 125-130℃, and the temperature range of the catalytic reaction device is 450-460℃.

[0022] In step S4, the temperature of the vessel body of the sulfur recovery device is 125-130℃.

[0023] The heating temperature of the CO heating device is 400-500℃.

[0024] The pipes connecting the first liquid sulfur transfer pump and the second liquid sulfur transfer pump are insulated at 128-130℃.

[0025] The CO gas source pipeline is also equipped with a flow controller.

[0026] The technical solution of this invention has the following advantages:

[0027] A. This invention provides a novel process apparatus and process route for the continuous production of carbonyl sulfur. Through segmented heating, the sulfur vapor required for the COS reaction can be continuously generated, and the reaction to prepare COS can be carried out continuously.

[0028] B. In this invention, unreacted sulfur can be recycled online in liquid form, avoiding the blockage of pipelines caused by sulfur solidification.

[0029] C. This invention achieves the goal of continuous production and can significantly reduce the size of the reaction device. Attached Figure Description

[0030] To more clearly illustrate the specific embodiments of the present invention, the accompanying drawings used in the specific embodiments will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0031] Figure 1 This is a schematic diagram of the overall structure of the apparatus system for continuously preparing COS according to the present invention.

[0032] The diagram is labeled as follows:

[0033] 1-CO gas source pipeline; 2-CO purifier; 3-CO heating device; 4-sulfur feeding device, 41-nitrogen inlet, 42-sulfur powder inlet, 43-nitrogen outlet, 44-liquid sulfur outlet, 45-liquid sulfur recovery inlet; 5-segmented heated sulfur melting kettle, 51-liquid sulfur inlet, 52-CO inlet, 53-mixed gas outlet; 6-COS synthesis catalytic reactor, 61-raw material gas inlet, 62-product gas outlet; 7-sulfur recovery device, 71-product gas inlet, 72-COS gas collection port, 73-liquid sulfur separation outlet, 74-cooling water outlet, 75-cooling water inlet; 8-first liquid sulfur transfer pump; 9-second liquid sulfur transfer pump; 10-flow controller.

[0034] a-Upper section; b-Middle section; c-Lower section; d-First insulation jacket; e-Second insulation jacket. Detailed Implementation

[0035] The technical solution of the present invention will now be clearly and completely described with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0036] like Figure 1 As shown, this invention provides a continuous COS production apparatus system, including a CO gas source pipeline 1, a sulfur feeding device 4, a segmented heating and melting sulfur reactor 5, a COS synthesis catalytic reactor 6, and a sulfur recovery device 7. The segmented heating and melting sulfur reactor 5 is equipped with a liquid sulfur inlet 51, a CO inlet 52, and a mixed gas outlet 53. The liquid sulfur inlet 51 is located on the lower part of the side wall of the segmented heating and melting sulfur reactor 5, while the CO inlet 52 and the mixed gas outlet 53 are located at the top of the segmented heating and melting sulfur reactor 5. The CO inlet 52 extends into the bottom inner side of the segmented heating and melting sulfur reactor 5 through a conduit. The sulfur recovery device 7... The top of the device is equipped with a product gas inlet 71 and a COS gas collection port 72, and the bottom is equipped with a liquid sulfur separation outlet 73. The product gas inlet 71 extends into the sulfur recovery device 7 through a conduit. The CO gas source pipeline 1 is connected to the CO inlet 52. The liquid sulfur outlet 44 on the sulfur feeding device 4 is connected to the liquid sulfur inlet 51. The mixed gas outlet 53 is connected to the raw material gas inlet 61 on the COS synthesis catalytic reactor 6. The product gas outlet 62 on the COS synthesis catalytic reactor 6 is connected to the product gas inlet 71. The liquid sulfur separation outlet 73 is connected to the liquid sulfur recovery inlet 45 on the sulfur feeding device 4.

[0037] Furthermore, the segmented heating sulfur melting kettle 5 is divided into an upper section a, a middle section b, and a lower section c for segmented heating. The temperature control zone of the upper section a is 500-520℃, the temperature control zone of the middle section b is 450-460℃, and the temperature control zone of the lower section c is 300-180℃. The liquid sulfur inlet 51 is located in the lower section c. The length ratio of the upper, middle, and lower sections of the segmented heating sulfur melting kettle 5 is 2:(3-5):1.

[0038] The system also includes a CO purifier 2, a CO heating device 3, a first liquid sulfur transfer pump 8, and a second liquid sulfur transfer pump 9. The CO gas source pipeline 1, CO purifier 2, CO heating device 3, and CO inlet 52 are connected in series. The first liquid sulfur transfer pump 8 is located on the connecting pipeline between the liquid sulfur outlet 44 and the liquid sulfur inlet 51, and is used to pump the liquid sulfur in the sulfur feeding device 4 to the segmented heating sulfur melting kettle 5. The second liquid sulfur transfer pump 9 is located on the connecting pipeline between the liquid sulfur separation outlet 73 and the liquid sulfur recovery inlet 45, and is used to transport the liquid sulfur liquefied and recovered in the sulfur recovery device 7 to the sulfur feeding device 4 for recycling.

[0039] The upper end of the sulfur feeding device 4 is also equipped with a nitrogen inlet 41, a sulfur powder inlet 42 with a switch valve, and a nitrogen outlet 43. The outer side of its vessel body is equipped with a first heat insulation jacket d, and the heat insulation type of the first heat insulation jacket d is one of electric heating, steam heating, or bath heating. The outer side of the vessel body of the sulfur recovery device 7 is equipped with a second heat insulation jacket e, and the second heat insulation jacket e is equipped with a cooling water inlet 75 and a cooling water outlet 74, which are used to cool the vessel body of the sulfur recovery device 7 and liquefy the unreacted sulfur vapor in the product mixture gas into liquid sulfur.

[0040] In addition, the CO gas source pipeline 1 is also equipped with a flow controller 10 for controlling the flow rate of CO entering the sulfur feeding device 4.

[0041] The usage of the system will be described in detail below with reference to specific embodiments.

[0042] Example 1

[0043] This embodiment provides a method for using a device system capable of continuously preparing COS, specifically including the following steps:

[0044] S1. Load 400L of sulfur powder into the 500L sulfur feeding device 4, close the feed valve, and purge with nitrogen for 15 minutes to replace the gas.

[0045] S2. The sulfur feeding device 4 is kept at a constant temperature of 130℃. The temperature of the 500L segmented heating sulfur melting kettle 5 is set at 500℃ in the upper section, 460℃ in the middle section, and 300℃ in the lower section. At the same time, the temperature of the COS synthesis catalytic reactor is set at 460℃, and the temperature of the sulfur conveying pipeline is controlled at 130℃.

[0046] S3. After the temperatures stabilize, the liquid sulfur in the sulfur feeding device 4 is slowly fed into the segmented heating sulfur melting kettle 5 by the first liquid sulfur transfer pump 8. When the liquid sulfur in the sulfur feeding device 4 is less than 200L, the feed valve can be opened online to add sulfur powder and continue to pre-melt the sulfur. When the liquid sulfur in the segmented heating sulfur melting kettle 5 reaches 250L, 10 cubic meters of CO gas per hour is dehydrated and purified by the CO purifier 2, and then heated by the CO heating device 3 and passed into the molten sulfur liquid in the sulfur feeding device 4. The CO mixed gas containing sulfur vapor is then introduced into the COS synthesis catalytic reactor 6, where it reacts under the action of the catalyst to produce COS mixed gas.

[0047] S4. The COS mixed gas from the COS synthesis catalytic reactor 6 is cooled to 130°C by a 300L sulfur recovery unit 7. The sulfur vapor containing unreacted sulfur is liquefied by cooling and sinks to the bottom of the reactor. When the recovered liquid sulfur reaches 100L, the recovered liquid sulfur is sent to the sulfur feeding unit 4 for reuse through the second liquid sulfur transfer pump 9. The high-concentration COS gas is sent to the product area for treatment.

[0048] The entire reaction process involves adding approximately 200 kg of sulfur powder per batch, with a continuous reaction time of 12 hours. By adjusting the amount of sulfur powder added, continuous production shift schedules can be easily implemented. The unit operated continuously for 30 days without any pipe blockage. The concentration of the produced COS gas reached 92.8% after preliminary purification. It can produce 1.2 tons of high-concentration COS gas per day.

[0049] Example 2

[0050] This embodiment provides a method for using a device system capable of continuously preparing COS, specifically including the following steps:

[0051] S1. Load 80L of sulfur powder into the 100L sulfur feeding device 4, close the feed valve, and purge with nitrogen for 15 minutes to replace the gas.

[0052] S2. The sulfur feeding device 4 is kept at a constant temperature of 128°C. The temperature of the 150L segmented heating sulfur melting kettle 5 is set at 520°C in the upper section, 450°C in the middle section, and 180°C in the lower section. At the same time, the temperature of the COS synthesis catalytic reactor is set at 450°C, and the temperature of the sulfur conveying pipeline is controlled at 128°C.

[0053] S3. After the temperatures stabilize, the liquid sulfur in the sulfur feeding device 4 is slowly fed into the segmented heating sulfur melting kettle 5 by the first liquid sulfur transfer pump 8. When the liquid sulfur in the sulfur feeding device 4 is less than 20L, the feed valve can be opened online to add sulfur powder and continue to pre-melt the sulfur. When the liquid sulfur in the segmented heating sulfur melting kettle 5 reaches 100L, 2 cubic meters of CO gas per hour is dehydrated and purified by the CO purifier 2, heated by the CO heating device 3, and then passed into the molten sulfur liquid in the sulfur feeding device 4. The CO mixed gas containing sulfur vapor is then introduced into the COS synthesis catalytic reactor 6, where it reacts under the action of the catalyst to produce COS mixed gas.

[0054] S4. The COS mixed gas from the COS synthesis catalytic reactor 6 is cooled to 130°C by a 50L sulfur recovery unit 7. The sulfur vapor containing unreacted sulfur is liquefied by cooling and sinks to the bottom of the reactor. When the recovered liquid sulfur reaches 20L, the recovered liquid sulfur is sent to the sulfur feeding unit 4 for reuse through the second liquid sulfur transfer pump 9. The high-concentration COS gas is sent to the product area for treatment.

[0055] The entire reaction process involves adding approximately 35 kg of sulfur powder per batch, with a continuous reaction time of 12 hours. By adjusting the amount of sulfur powder added, continuous production shift schedules can be easily implemented. The unit operated continuously for 45 days without any pipe blockages. The concentration of the produced COS gas reached 93.1% after preliminary purification. It can produce 240 kg of high-concentration COS gas per day.

[0056] In summary, this invention provides a novel process apparatus and process route for the continuous production of carbonyl sulfide. Through segmented heating, the sulfur vapor required for the COS reaction can be continuously generated, allowing the COS preparation reaction to proceed continuously. Unreacted sulfur can be recovered and reused online in liquid form, avoiding pipeline blockage caused by sulfur solidification. This invention achieves continuous production and can significantly reduce the scale of the reaction apparatus.

[0057] Obviously, the above embodiments and application examples are merely illustrative and not intended to limit the implementation. Those skilled in the art will recognize that other variations or modifications can be made based on the above description. It is neither necessary nor possible to exhaustively list all possible implementations. However, obvious variations or modifications derived therefrom are still within the scope of this invention.

Claims

1. A device system for continuously preparing COS, characterized in that, The system includes a CO gas source pipeline (1), a sulfur feeding device (4), a segmented heating and melting sulfur reactor (5), a COS synthesis catalytic reactor (6), and a sulfur recovery device (7). The segmented heating and melting sulfur reactor (5) is provided with a liquid sulfur inlet (51), a CO inlet (52), and a mixed gas outlet (53). The liquid sulfur inlet (51) is located on the lower side wall of the segmented heating and melting sulfur reactor (5). The CO inlet (52) and the mixed gas outlet (53) are located at the top of the segmented heating and melting sulfur reactor (5), and the CO inlet (52) extends into the bottom of the inner side of the segmented heating and melting sulfur reactor (5) through a conduit. The sulfur recovery device (7) is provided with a product gas inlet (71) and a CO gas outlet (73) at the top. The OS gas collection port (72) has a liquid sulfur separation outlet (73) at its bottom. The product gas inlet (71) extends into the sulfur recovery device (7) through a conduit. The CO gas source pipeline (1) is connected to the CO inlet (52). The liquid sulfur outlet (44) on the sulfur feeding device (4) is connected to the liquid sulfur inlet (51). The mixed gas outlet (53) is connected to the raw material gas inlet (61) on the COS synthesis catalytic reactor (6). The product gas outlet (62) on the COS synthesis catalytic reactor (6) is connected to the product gas inlet (71). The liquid sulfur separation outlet (73) is connected to the liquid sulfur recovery inlet (45) on the sulfur feeding device (4). The segmented heating sulfur melting kettle (5) is divided into an upper section (a), a middle section (b) and a lower section (c) for segmented heating. The temperature control zone of the upper section (a) is 500-520℃, the temperature control zone of the middle section (b) is 450-460℃, and the temperature control zone of the lower section (c) is 300-180℃. The length ratio of the upper, middle and lower sections of the segmented heating sulfur melting kettle (5) is 2:(3-5):

1.

2. The apparatus system for continuously preparing COS according to claim 1, characterized in that, The liquid sulfur inlet (51) is located in the lower section (c).

3. The apparatus system for continuously preparing COS according to claim 1, characterized in that, The system also includes a CO purifier (2) and a CO heating device (3), and the CO gas source pipeline (1), CO purifier (2), CO heating device (3) and CO inlet (52) are connected in series.

4. The apparatus system for continuously preparing COS according to claim 1, characterized in that, The system also includes a first liquid sulfur transfer pump (8) and a second liquid sulfur transfer pump (9). The first liquid sulfur transfer pump (8) is installed on the connecting pipeline between the liquid sulfur outlet (44) and the liquid sulfur inlet (51) to pump the liquid sulfur in the sulfur feeding device (4) to the segmented heating sulfur melting kettle (5). The second liquid sulfur transfer pump (9) is installed on the connecting pipeline between the liquid sulfur separation outlet (73) and the liquid sulfur recovery inlet (45) to transport the liquid sulfur liquefied and recovered in the sulfur recovery device (7) to the sulfur feeding device (4) for recycling.

5. The apparatus system for continuously preparing COS according to claim 1, characterized in that, The upper end of the sulfur feeding device (4) is also provided with a nitrogen inlet (41), a sulfur powder inlet (42) with a switch valve, and a nitrogen outlet (43), and its outer side is provided with a first heat-insulating jacket (d). The sulfur recovery device (7) has a second heat insulation jacket (e) on the outside of the vessel body. The second heat insulation jacket (e) is provided with a cooling water inlet (75) and a cooling water outlet (74) for cooling the vessel body of the sulfur recovery device (7).

6. The apparatus system for continuously preparing COS according to claim 5, characterized in that, The insulation type of the first insulation jacket (d) is one of electric heating, steam heating or bath heating.

7. The method of using the apparatus system for continuous COS preparation according to any one of claims 1-6, characterized in that, Includes the following steps: S1. Sulfur powder is loaded into the sulfur feeding device (4), the feed valve is closed, and nitrogen is introduced for purging. S2. Set the constant temperature of the sulfur feeding device (4), the heating temperature of the segmented heating sulfur melting kettle (5), and the reaction temperature of the COS synthesis catalytic reactor (6) as required. S3. The liquid sulfur that has been pre-melted at a constant temperature in the sulfur feeding device (4) is sent into the segmented heating sulfur melting kettle (5), and CO gas is introduced into the segmented heating sulfur melting kettle (5). The CO mixed gas containing sulfur vapor is introduced into the COS synthesis catalytic reactor (6), and the reaction is carried out under the action of the catalyst to produce COS mixed gas. S4 and COS mixed gas enter the sulfur recovery unit (7) for cooling. The sulfur vapor containing unreacted sulfur is cooled and liquefied, then sinks to the bottom of the vessel and is sent to the sulfur feeding unit (4) for reuse. The separated high-concentration COS gas is sent to the product processing unit for treatment.

8. The method of use according to claim 7, characterized in that, In step S3, when the volume of liquid sulfur in the sulfur feeding device (4) is less than 40% of the volume, the feed valve is opened online and sulfur powder is added to continuously pre-melt sulfur. When the liquid sulfur in the segmented heating sulfur melting kettle (5) reaches 50% of the volume, 10 cubic meters of CO gas per hour is dehydrated and purified by the CO purifier (2), and then heated by the CO heating device (3) and introduced into the molten sulfur liquid in the sulfur feeding device (4).

9. The method of use according to claim 7, characterized in that, In step S2, the temperature range of the first insulation jacket (d) of the sulfur feeding device (4) is 125-130℃, and the temperature range of the catalytic reaction device is 450-460℃.

10. The method of use according to claim 7, characterized in that, In step S4, the temperature of the vessel body of the sulfur recovery device is 125-130℃.

11. The method of use according to claim 8, characterized in that, The heating temperature of the CO heating device (3) is 400-500℃.

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