A sulfur recovery system coupled with a thermal storage device and its control method

Abstract

This invention provides a sulfur recovery system coupled with a thermal storage device and its control method. The system includes a thermal storage device, a reactor, a sulfur recovery device, and an incinerator. The sulfur recovery device includes a reheater, a converter, and a sulfur cooler. The thermal storage device includes a high-temperature storage tank, a steam generator, a low-temperature storage tank, and a heating device connected sequentially. Modified liquid sulfur material that can be circulated and transported is stored in the thermal storage device. The high-temperature storage tank is connected to the reheater, the reheater is connected to the steam generator and / or the low-temperature storage tank, the steam generator is connected to the low-temperature storage tank, the low-temperature storage tank is connected to the sulfur cooler, the sulfur cooler is connected to the waste heat boiler of the reactor, the waste heat boiler is connected to the heating device, the heating device is connected to the high-temperature storage tank, and the high-temperature storage tank is connected to the steam generator. This invention can aggregate and complementarily couple multiple different grades of energy in the sulfur recovery system, and can not only heat the process gas in the reheater, but also produce high-pressure steam in centralized production.

Description

Technical Field

[0001] This invention relates to the field of sulfur recovery technology, and in particular to a sulfur recovery system coupled with a thermal storage device and its control method. Background Technology

[0002] Sulfur recovery systems are the primary systems for treating H2S-containing acidic gases produced in coal chemical, petrochemical, and fine chemical plants, and for generating sulfur as a byproduct. Existing technologies include numerous sulfur recovery systems and processes, such as two-stage Claus systems, three-stage Claus systems, modified three-stage Claus systems, two-stage Claus systems with selective hydrogenation and selective oxidation, two-stage Claus systems with conventional SCOT, two-stage Claus systems with LS SCOT, two-stage Claus systems with Super SCOT, etc. For example, [the following is an example / example]. Figure 1 The process shown is a conventional two-stage Claus + selective oxidation process (or two-stage Claus + super Claus process).

[0003] Existing sulfur recovery systems typically include waste heat boilers, multi-stage sulfur coolers, multi-stage heaters, multi-stage converters, and incinerators. The sulfur coolers need to release heat to the outside environment, and the heaters require external heating. Therefore, to improve energy efficiency, in existing technologies, the heat generated from the combustion of acidic gas is usually used in the waste heat boiler to produce high / medium-pressure saturated steam (approximately 5.5 MPa, 271°C). Part of this steam is used as a heat source for the process gas heaters, while the remainder enters the steam network for other uses. The heat released by the process gas in the sulfur condenser is typically used to generate low-pressure saturated steam (approximately 0.4 MPa, 145°C).

[0004] However, for the entire sulfur recovery system (as shown in the appendix) Figure 1 As shown in the figure, steam of different calorific values ​​is often generated during the operation of the entire system, and the distribution is relatively dispersed. Corresponding steam pipelines of different calorific values ​​need to be built in the plant area, which leads to a complex layout of steam pipelines in the system. At the same time, the generation of low-calorific-value steam will increase the difficulty of heat reuse and may even be regarded as waste heat, which is not conducive to improving the energy utilization efficiency of the entire system. Summary of the Invention

[0005] In view of this, the present invention aims to propose a sulfur recovery system and its control method coupled with a thermal storage device, so as to solve the problem that the sulfur recovery system in the prior art generates steam with different heat grades, resulting in a complex steam pipeline layout and low energy utilization efficiency of the entire system.

[0006] To achieve the above objectives, the technical solution of the present invention is implemented as follows: A sulfur recovery system coupled with a thermal storage device includes a thermal storage device, a reactor, a sulfur recovery device, and an incinerator, wherein the reactor, sulfur recovery device, and incinerator are connected in sequence; the reactor is equipped with a waste heat boiler, and the sulfur recovery device includes at least two sulfur recovery groups connected in sequence, each sulfur recovery group including a reheater, a converter, and a sulfur cooler connected in sequence; the thermal storage device includes a high-temperature storage tank, a steam generator, a low-temperature storage tank, and a heating device connected end-to-end, and the thermal storage device contains modified liquid sulfur material that can be circulated and transported, and the outlet of the high-temperature storage tank can be connected to each The material inlet of each reheater is connected, and the material outlet of each reheater is connected to the feed inlet of the steam generator and / or the feed inlet of the cryogenic storage tank. The discharge outlet of the steam generator is connected to the feed inlet of the cryogenic storage tank, and the discharge outlet of the cryogenic storage tank is connected to the material inlet of each sulfur cooler. The material outlet of each sulfur cooler is connected to the material inlet of the waste heat boiler, and the material outlet of the waste heat boiler is connected to the feed inlet of the heating device. The discharge outlet of the heating device is connected to the feed inlet of the high-temperature storage tank, and the discharge outlet of the high-temperature storage tank is connected to the feed inlet of the steam generator.

[0007] Furthermore, the thermal storage device includes a first main pipe, the inlet of which is connected to the outlet of the high-temperature storage tank, and the outlet of the first main pipe is connected to the inlet of the steam generator and the material inlet of each reheater.

[0008] Furthermore, the thermal storage device includes a second main pipe, the inlet of which is connected to the material outlet of each reheater, and the outlet of which is connected to the inlet of the steam generator and / or the inlet of the cryogenic storage tank.

[0009] Furthermore, the heat storage device includes a third main pipe and a fourth main pipe. The inlet of the third main pipe is connected to the outlet of the low-temperature storage tank, and the outlet of the third main pipe is connected to the material inlet of each sulfur cooler. The inlet of the fourth main pipe is connected to the material outlet of each sulfur cooler, and the outlet of the fourth main pipe is connected to the material inlet of the waste heat boiler.

[0010] Furthermore, the heat storage device includes a first pipe, one end of which is connected to a third main pipe and the other end of which is connected to a fourth main pipe.

[0011] Furthermore, the heat storage device includes a second pipe and a third pipe. One end of the second pipe is connected to the third main pipe, and the other end is connected to the material inlet of the incinerator. One end of the third pipe is connected to the material outlet of the incinerator, and the other end is connected to the material outlet of the waste heat boiler.

[0012] Furthermore, in the flow direction of the process gas, a primary sulfur cooler is provided between the reactor and the sulfur recovery device. The sulfur recovery device includes a first-stage reheater, a first-stage converter, a first-stage sulfur cooler, a second-stage reheater, a second-stage converter, a second-stage sulfur cooler, a third-stage reheater, a third-stage converter, and a third-stage sulfur cooler connected in sequence. The process gas outlet of the primary sulfur cooler is connected to the process gas inlet of the first-stage reheater, and the process gas outlet of the third-stage sulfur cooler is connected to the process gas inlet of the incinerator.

[0013] Furthermore, the thermal storage device includes a first main pipe and a second main pipe. The inlet of the first main pipe is connected to the outlet of the high-temperature storage tank, and the outlet of the first main pipe is connected to the inlet of the steam generator, the material inlet of the first-stage reheater, the material inlet of the second-stage reheater, and the material inlet of the third-stage reheater, respectively. The inlet of the second main pipe is connected to the material outlet of the first-stage reheater, the material outlet of the second-stage reheater, and the material outlet of the third-stage reheater, respectively. The outlet of the second main pipe is connected to the inlet of the low-temperature storage tank.

[0014] Furthermore, the heat storage device includes a third main pipe and a fourth main pipe. The inlet of the third main pipe is connected to the outlet of the low-temperature storage tank. The outlet of the third main pipe is connected to the material inlet of the primary sulfur cooler, the material inlet of the first-stage sulfur cooler, the material inlet of the second-stage sulfur cooler, and the material inlet of the third-stage sulfur cooler. The inlet of the fourth main pipe is connected to the material outlet of the primary sulfur cooler, the material outlet of the first-stage sulfur cooler, the material outlet of the second-stage sulfur cooler, and the material outlet of the third-stage sulfur cooler. The outlet of the fourth main pipe is connected to the material inlet of the waste heat boiler.

[0015] A control method for a sulfur recovery system of a coupled thermal energy storage device is provided, applied to the sulfur recovery system of the coupled thermal energy storage device. The control method includes: S1, acquiring the process gas outlet temperature Ta of the waste heat boiler in real time; S2, if Ta > 260℃, increasing the discharge flow rate at the outlet of the low-temperature storage tank and increasing the opening of the regulating valve B in the first pipe; if Ta < 230℃, decreasing the discharge flow rate at the outlet of the low-temperature storage tank and decreasing the opening of the regulating valve B in the first pipe; S3, acquiring the process gas outlet temperature Tbi of each sulfur cooler and the process gas outlet temperature Tbi of each reheater in real time. S4. If Tbi > 160℃, increase the opening of the regulating valve at the corresponding sulfur cooler material inlet; if Tbi < 150℃, decrease the opening of the regulating valve at the corresponding sulfur cooler material inlet; if Tci < 240℃, increase the opening of the regulating valve at the corresponding reheater material inlet; if Tci > 260℃, decrease the opening of the regulating valve at the corresponding reheater material inlet; S5. Obtain the exhaust gas outlet temperature Td of the incinerator in real time; S6. If Td > 160℃, increase the opening of the regulating valve R in the second pipe; if Td < 150℃, decrease the opening of the regulating valve R in the second pipe.

[0016] Compared with existing technologies, the sulfur recovery system and control method of the coupled thermal storage device described in this invention have the following advantages: The present invention discloses a sulfur recovery system and its control method with a coupled thermal storage device. By coupling a thermal storage device into an existing sulfur recovery system, it can store and concentrate the high-grade heat (approximately 1200°C) generated by the waste heat boiler and the low-grade heat (approximately 160°C) generated by the sulfur cooler in the material. The material can be further heated by heating devices (such as electrical energy or chemical energy), achieving the aggregation and complementary coupling of multiple energy grades in the sulfur recovery system. Simultaneously, the energy aggregated in the material can not only heat the process gas in the reheater but also utilize the surplus energy of the entire sulfur recovery system. This is unique within the entire system. The present invention provides a centralized steam generator that produces medium- and high-pressure steam, which can be uniformly fed into an external steam network. Compared with the existing sulfur recovery system, the steam generated in this system not only has a higher overall calorific value and a more uniform calorific value type, but also avoids the generation of unnecessary low-calorific-value steam, reducing waste heat generation and improving the energy utilization efficiency of the entire system. In addition, the steam generation location of this application is more centralized, and the steam pipeline and steam generator do not need to be set in the sulfur recovery device, which also avoids the situation of the steam pipeline being too dispersed in the prior art, and can significantly reduce the complexity of the steam pipeline layout in the prior art. Attached Figure Description

[0017] The accompanying drawings, which form part of this invention, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an undue limitation of the invention. In the drawings: Figure 1 This is a schematic diagram of the existing two-stage Claus + super Claus process; Figure 2 This is a first schematic diagram of a sulfur recovery system of a coupled thermal storage device according to an embodiment of the present invention; Figure 3 This is a second schematic diagram of a sulfur recovery system of a coupled thermal storage device according to an embodiment of the present invention; Figure 4 This is a third schematic diagram of a sulfur recovery system of a coupled thermal storage device according to an embodiment of the present invention; Figure 5 This is a fourth schematic diagram of a sulfur recovery system of a coupled thermal storage device according to an embodiment of the present invention.

[0018] Explanation of reference numerals in the attached figures: 1. High-temperature storage tank; 101. High-temperature pump; 2. Steam generator; 3. Low-temperature storage tank; 301. Low-temperature pump; 4. Electric heater; 5. Combustion heater; 6. First main pipe; 7. Second main pipe; 8. Third main pipe; 9. Fourth main pipe; 10. First pipe; 11. Second pipe; 12. Third pipe. Detailed Implementation

[0019] The inventive concepts of this disclosure will be described below using terminology commonly used by those skilled in the art to communicate the essence of their work to others skilled in the art. However, these inventive concepts may be embodied in many different forms and should not be construed as limited to the embodiments described herein.

[0020] It should be noted that, unless otherwise specified, the embodiments and features described in the embodiments of this invention can be combined with each other. To highlight the accompanying drawings of the sulfur recovery system of this application (attached...), Figure 2-5 (and drawings of the existing two-stage Claus + super Claus process (attached)) Figure 1 The distinction between the two is made to facilitate the differentiation of the related pipelines of the thermal storage device for which this application is made improvements. This application addresses the following: Figure 2-5 The pipelines related to the thermal storage device are illustrated in red and blue. Regarding the flow of two groups of substances in the system of this application, the sulfur-containing process gas is referred to as "process gas" and the circulating modified liquid sulfur material is referred to as "material".

[0021] The present invention will now be described in detail with reference to the accompanying drawings and embodiments.

[0022] In existing sulfur recovery systems, steam of different calorific values ​​is often generated during the operation of the system and is relatively dispersed. Corresponding steam pipelines of different calorific values ​​need to be built within the plant area, resulting in a complex steam pipeline layout in the system. At the same time, the generation of low-calorific-value steam increases the difficulty of heat reuse and may even be regarded as waste heat, which is not conducive to improving the energy utilization efficiency of the entire system.

[0023] To address the problem that existing sulfur recovery systems generate steam of varying calorific values, resulting in complex steam pipeline layouts and low overall system energy efficiency, this embodiment proposes a sulfur recovery system coupled with a thermal storage device, as shown in the attached figure. Figure 2-5 As shown, the sulfur recovery system includes a heat storage device, a reactor, a sulfur recovery device, an incinerator, and a chimney, which are connected in sequence.

[0024] The sulfur recovery device can be any existing sulfur recovery system, such as a two-stage Claus, a three-stage Claus, a modified three-stage Claus, a two-stage Claus + selective hydrogenation + selective oxidation, a two-stage Claus + conventional SCOT, a two-stage Claus + LS SCOT, a two-stage Claus + Super SCOT, etc. For ease of description of the equipment below, this application provides a brief description of the sulfur recovery device, which includes at least two sequentially connected sulfur recovery groups. Each sulfur recovery group includes a reheater, a converter, and a sulfur cooler sequentially connected. The sulfur outlet of each sulfur cooler is equipped with a sulfur sealing tank for collecting and recovering sulfur. For two adjacent upstream and downstream sulfur recovery groups, the process gas outlet of the sulfur cooler in the upstream sulfur recovery group is connected to the process gas inlet of the reheater in the downstream sulfur recovery group; the process gas outlet of the last stage sulfur cooler is connected to the process gas inlet of the incinerator.

[0025] In existing sulfur recovery technologies, a sulfur cooler and a corresponding sulfur sealing tank are often installed between the reactor and the sulfur recovery unit, as shown in the attached figures of this application. Of course, some existing sulfur recovery technologies also have schemes that do not require an additional primary sulfur cooler, i.e., the reactor is directly connected to the reheater of the first-stage sulfur recovery unit, which will not be elaborated upon in this application.

[0026] In existing sulfur recovery systems, low-pressure steam is typically generated by heat exchange between high-temperature process gas and water in various stages of sulfur coolers. Furthermore, existing reactors, including waste heat boilers, also use high-temperature process gas to heat water, producing medium- and high-pressure steam. Consequently, existing sulfur recovery systems generate steam of varying calorific values ​​at multiple steam generation points during operation, and these steam sources are relatively dispersed.

[0027] Based on this, the main technical improvement of this application is: setting up a heat storage device in the sulfur recovery system to provide heat or cold to some equipment in the sulfur recovery system, and using the heat storage device to centrally generate steam, so that there is only one steam generation location in the entire sulfur recovery system, and correspondingly generates steam of the same heat quality.

[0028] Specifically: The thermal storage device includes a high-temperature storage tank 1, a steam generator 2, a low-temperature storage tank 3, and a heating device connected in sequence. The thermal storage device contains modified liquid sulfur material that can be circulated and transported. The outlet of the high-temperature storage tank 1 can be connected to the material inlet of each reheater. The material outlet of each reheater can be connected to the inlet of the steam generator 2 and / or the inlet of the low-temperature storage tank 3. The outlet of the steam generator 2 is connected to the inlet of the low-temperature storage tank 3. The outlet of the low-temperature storage tank 3 can be connected to the material inlet of each sulfur cooler. The material outlet of each sulfur cooler can be connected to the material inlet of the waste heat boiler. The material outlet of the waste heat boiler is connected to the inlet of the heating device. The outlet of the heating device is connected to the inlet of the high-temperature storage tank 1.

[0029] This application incorporates a heat storage device in the sulfur recovery system. Through material circulation, the high-temperature material (approximately 430°C) in the high-temperature storage tank 1 is sent to the reheater between the high-temperature storage tank 1 and the low-temperature storage tank 3 to heat the process gas. The medium-high temperature material after heat exchange enters the only steam generator 2 in the entire system to centrally generate medium- and high-pressure steam. Then, the low-temperature material (approximately 120°C) flows out of the steam generator 2 and into the low-temperature storage tank 3. Of course, under certain circumstances, the material after heat exchange in the reheater can be cooled to approximately 120°C-150°C and can be directly transported to the low-temperature storage tank 3.

[0030] Between the low-temperature storage tank 3 and the high-temperature storage tank 1, the low-temperature material (approximately 120°C) in the low-temperature storage tank 3 is sent to the sulfur cooler to cool the process gas. The medium-low temperature material (approximately 160°C) after heat exchange is sent from the sulfur cooler to the waste heat boiler to exchange heat with the high-temperature process gas generated by the reactor to form medium-high temperature material (above 300°C). The medium-high temperature material flowing out of the waste heat boiler enters the heating device to supplement heat and form high-temperature material (approximately 430°C), and is then sent to the high-temperature storage tank 1.

[0031] Therefore, by coupling a thermal storage device into the existing sulfur recovery system, this application can store and concentrate the high-grade heat (approximately 1200°C) generated by the waste heat boiler and the low-grade heat (approximately 160°C) generated by the sulfur cooler in the material. The material can then be supplemented with heat through heating devices (such as electrical or chemical energy), achieving the aggregation and complementary coupling of multiple energy grades within the sulfur recovery system. Simultaneously, the energy aggregated in the material can not only heat the process gas in the reheater but also utilize the surplus energy of the entire sulfur recovery system in the single steam generator 2 within the system. This method generates medium- and high-pressure steam, which can be uniformly sent to an external steam network for use. Compared with existing sulfur recovery systems, this method not only produces steam with a higher overall calorific value and a more uniform calorific value type, but also avoids the generation of unnecessary low-calorific-value steam, reducing waste heat generation and improving the energy utilization efficiency of the entire system. In addition, the steam generation location in this application is more concentrated, and neither the steam pipeline nor the steam generator 2 needs to be set in the sulfur recovery device. This also avoids the situation where the steam pipeline distribution is too dispersed in the prior art, and can significantly reduce the complexity of the steam pipeline layout in the prior art.

[0032] The heating device can be an electric heater 4 and / or a combustion heater 5. In actual implementation, since the heat storage device can couple and concentrate the heat from the waste heat boiler and the sulfur cooler, if the heat generated by the system itself in the sulfur recovery system can reach dynamic balance or have a slight surplus, the heating device may not be required in this application, or only one of the electric heater 4 and the combustion heater 5 may be required.

[0033] Preferably, this application provides an electric heater 4 and a combustion heater 5 between the material outlet of the waste heat boiler and the feed inlet of the high-temperature storage tank 1. The material can be supplemented with electric heating or with chemical heat such as gas combustion. Compared with the traditional electric heating method of reheaters in the prior art (directly heating the process gas), this application can turn on the electric heater 4 only during off-peak hours and use the high-temperature storage tank 1 for energy storage, realizing the "peak shaving and valley filling" of power resources and effectively reducing operating costs.

[0034] Meanwhile, when there is surplus gas or other heat sources in the plant area that are temporarily inconvenient to store, this surplus energy can be stored in the material of the heat storage device through a heating device. When there is an external heat demand, this surplus energy can be converted into sufficient medium- and high-pressure steam for transportation or supply to the reheater. It is equivalent to the heat storage device equipping the sulfur recovery system and the entire plant with a heat "heat bank", which can undertake the peak-shaving and buffering role of the entire plant's energy. Correspondingly, the discharge port of the high-temperature storage tank 1 can also be connected to the inlet of the steam generator 2, so that when there is a surplus of stored energy in the system, the high-temperature storage tank 1 can directly supply high-temperature materials to the steam generator 2. This not only outputs the surplus energy in the system to the outside world, but also helps to ensure the external demand for steam or heating.

[0035] Regarding the piping arrangement of the aforementioned thermal storage device (red and blue lines in the accompanying drawings), specifically: The thermal storage device includes a first main pipe 6, the inlet of which is connected to the outlet of the high-temperature storage tank 1, and the outlet of the first main pipe 6 is connected to the material inlet of each reheater. Alternatively, the outlet of the first main pipe 6 can be connected to both the inlet of the steam generator 2 and the material inlet of each reheater. Preferably, the reheaters in this application are arranged in parallel, taking material flow as a reference. However, the reheaters can also be arranged in series, meaning the material flows through each reheater sequentially.

[0036] The heat storage device includes a second main pipe 7, the inlet of which is connected to the material outlet of each reheater, and the outlet of which is connected to the inlet of the steam generator 2 and / or the inlet of the cryogenic storage tank 3, so that the material after heat exchange in the reheater can be sent to the steam generator 2 or the cryogenic storage tank 3.

[0037] For the different pipeline design layouts related to the first main pipe 6 and the second main pipe 7: As attached Figure 2 As shown, when the first main pipe 6 is connected only to the material inlet of each reheater, the outlet of the second main pipe 7 is connected to the inlet of the steam generator 2. Alternatively, the outlet of the second main pipe 7 can be connected to both the inlet of the steam generator 2 and the inlet of the cryogenic storage tank 3. This allows for adjustment of the material flow direction based on actual conditions after material temperature fluctuations occur following heat exchange in the reheater. In this case, the reheater and the steam generator 2 can be considered to be connected in series.

[0038] As attached Figure 3As shown, with the outlet of the first main pipe 6 connected to the inlet of the steam generator 2 and the material inlet of each reheater, preferably, the outlet of the second main pipe 7 is connected to the inlet of the cryogenic storage tank 3. This creates a parallel connection between the first main pipe 6 and the second main pipe 7, the steam generator 2, and each reheater. This allows for more precise control of the amount of material flowing to each reheater and the steam generator 2. It also helps the high-temperature material in the high-temperature storage tank 1 to carry excess energy to participate in steam generation, ensuring the quality of the steam generated by the steam generator 2. This results in a higher overall calorific value and a more uniform calorific value type for the steam generated by the system.

[0039] The thermal storage device includes a third main pipe 8 and a fourth main pipe 9. The inlet of the third main pipe 8 is connected to the outlet of the cryogenic storage tank 3, and the outlet of the third main pipe 8 is connected to the material inlet of each sulfur cooler. The inlet of the fourth main pipe 9 is connected to the material outlet of each sulfur cooler, and the outlet of the fourth main pipe 9 is connected to the material inlet of the waste heat boiler. Preferably, the sulfur coolers are connected in parallel between the third main pipe 8 and the fourth main pipe 9, thereby enabling more precise control of the material flow to each sulfur cooler. Of course, the sulfur coolers can also be arranged in series, that is, the material flows through each sulfur cooler sequentially.

[0040] The heat storage device includes a first pipe 10, one end of which is connected to a third main pipe 8 and the other end of which is connected to a fourth main pipe 9. This allows the low-temperature material in the low-temperature storage tank 3 to be directly transported to the waste heat boiler for heat exchange with the process gas. Especially when some of the material is used for steam generation, the low-temperature material accumulated in the low-temperature storage tank 3 can be directly sent to the waste heat boiler and heating device and circulated back to the high-temperature storage tank 1. Even after the reactor, sulfur recovery device, incinerator and other equipment are shut down, the material in the heat storage device can still be circulated through the first pipe 10 to maintain the normal steam output of the steam generator 2.

[0041] The thermal storage device includes a second pipe 11 and a third pipe 12. One end of the second pipe 11 is connected to the third main pipe 8, and the other end is connected to the material inlet of the incinerator. One end of the third pipe 12 is connected to the material outlet of the incinerator, and the other end is connected to the material outlet of the waste heat boiler. After a certain amount of cryogenic material accumulates in the cryogenic storage tank 3, to ensure the heat balance in the sulfur recovery system and to prevent excessive cryogenic material from causing cryogenic shocks to the process gas in the sulfur cooler and waste heat boiler, thus affecting the balance of the upstream and downstream sulfur recovery process reactions, some of the cryogenic material in the cryogenic storage tank 3 can be directly guided to the second pipe 11. After heat exchange with the high-temperature tail gas in the incinerator, it flows through the third pipe 12 to the heating device, and after heating, flows into the high-temperature storage tank 1 for storage. Even after the reactor, sulfur recovery device, incinerator, and other equipment are shut down, the material in the thermal storage device can still circulate through the second pipe 11 and the third pipe 12, maintaining the normal steam output of the steam generator 2. Meanwhile, the second pipe 11 and the third pipe 12 enable the low-temperature material to exchange heat with the high-temperature exhaust gas of the incinerator, which helps to recover some of the heat carried in the exhaust gas and couple it into the heat storage device, thereby improving energy utilization efficiency and avoiding heat waste.

[0042] The modified liquid sulfur material comprises elemental sulfur and depolymers, with elemental sulfur accounting for 90%-95% by mass and depolymers accounting for 5%-10% by mass. The depolymers are substances that enhance the depolymerization of long-chain sulfur molecules to reduce the viscosity of the liquid sulfur, ensuring good fluidity of the modified liquid sulfur material within a temperature range of 120-440°C, with the viscosity consistently below 0.05 Pa∙s. Specifically, the depolymers are H₂S or halogen molecules. In the thermal storage device of this application, the modified liquid sulfur material primarily serves as a heat carrier, flowing and exchanging heat between relevant equipment.

[0043] A high-temperature pump 101 is installed at the outlet of the high-temperature storage tank 1, and a low-temperature pump 301 is installed at the outlet of the low-temperature storage tank 3 to ensure the flow of modified liquid sulfur material in the thermal storage device. The high-temperature storage tank 1 and the low-temperature storage tank 3 described in this application can store materials and the energy they carry. This buffers fluctuations in the system operation related to process gas, materials, and energy, and helps maintain a stable temperature environment in the sulfur recovery system, ensuring the balance of related reactions. During stable system operation, the material temperature in the low-temperature storage tank 3 is maintained at approximately 130°C, and the material temperature in the high-temperature storage tank 1 is maintained at approximately 430°C.

[0044] Under relatively ideal conditions, or without considering the effects of material fluctuations and energy fluctuations, the high-temperature storage tank 1 and the low-temperature storage tank 3 may not be installed in the thermal storage device. Only a material pump needs to be installed in the thermal storage device to meet the flow and circulation of the material. In this case, the thermal storage device does not need to store heat, and the material only serves as a heat transfer medium to transfer and transport heat.

[0045] For steam generator 2, it includes a preheater, an evaporator, and a superheater connected in sequence. The material flows sequentially through the material channels of the superheater, the evaporator, and the preheater. The water component flows sequentially through the water component channels of the preheater, the evaporator, and the superheater, so that the water and the material exchange heat sufficiently to form medium- and high-pressure steam, which can be transported to the steam pipeline network outside the system. Here, the water component can be regarded as water and / or steam, which needs to be determined according to the actual working conditions of the material. Since the principle of water heating to form steam can be consulted in relevant literature, it will not be elaborated here.

[0046] This application takes the "two-stage Claus + selective oxidation process" as an example to further introduce the relevant technical improvements in this application. Example 1

[0047] As attached Figure 2 As shown, the "two-stage Claus + selective oxidation process" can be regarded as a sulfur recovery unit consisting of three sulfur recovery groups connected in sequence. Acid gas and a portion of air are sent to the reactor, while the remaining air is sent to the converter of the third-stage sulfur recovery group, thus forming a two-stage Claus system in the first two stages and a selective oxidation system (or super Claus system) in the third stage.

[0048] Specifically, in the flow direction of the process gas, a primary sulfur cooler is installed between the reactor and the sulfur recovery device. The sulfur recovery device includes a first-stage reheater, a first-stage converter, a first-stage sulfur cooler, a second-stage reheater, a second-stage converter, a second-stage sulfur cooler, a third-stage reheater, a third-stage converter, and a third-stage sulfur cooler connected in sequence. The process gas outlet of the primary sulfur cooler is connected to the process gas inlet of the first-stage reheater, and the process gas outlet of the third-stage sulfur cooler is connected to the process gas inlet of the incinerator.

[0049] The thermal storage device includes a high-temperature storage tank 1, a steam generator 2, a low-temperature storage tank 3, and a heating device connected in sequence from end to end. As this has already been introduced, it will not be described again.

[0050] Regarding the main pipeline layout of the thermal storage device in this embodiment (see Appendix) Figure 2(Represented by red lines in the middle) The inlet of the first main pipe 6 is connected to the outlet of the high-temperature storage tank 1, and the outlet of the first main pipe 6 is connected to the material inlet of the first-stage reheater, the material inlet of the second-stage reheater, and the material inlet of the third-stage reheater, respectively. The feed inlet of the second main pipe 7 is connected to the material outlet of the first-stage reheater, the material outlet of the second-stage reheater, and the material outlet of the third-stage reheater, respectively, and the discharge outlet of the second main pipe 7 is connected to the feed inlet of the steam generator 2.

[0051] The inlet of the third main pipe 8 is connected to the outlet of the cryogenic storage tank 3. The outlet of the third main pipe 8 is connected to the material inlet of the primary sulfur cooler, the material inlet of the first-stage sulfur cooler, the material inlet of the second-stage sulfur cooler, and the material inlet of the third-stage sulfur cooler. The inlet of the fourth main pipe 9 is connected to the material outlet of the primary sulfur cooler, the material outlet of the first-stage sulfur cooler, the material outlet of the second-stage sulfur cooler, and the material outlet of the third-stage sulfur cooler. The outlet of the fourth main pipe 9 is connected to the material inlet of the waste heat boiler. Example 2

[0052] As attached Figure 3 As shown, most of the technical content in this embodiment is exactly the same as that in embodiment 1. The difference is that the connection between the first main pipe 6 and the second main pipe 7 in this embodiment is different from that in embodiment 1.

[0053] Specifically, the outlet of the first main pipe 6 is connected to the inlet of the steam generator 2, the material inlet of the first-stage reheater, the material inlet of the second-stage reheater, and the material inlet of the third-stage reheater, respectively. The outlet of the second main pipe 7 is connected to the inlet of the cryogenic storage tank 3. Accordingly, the steam generator 2, the first-stage reheater, the second-stage reheater, and the third-stage reheater are connected in parallel between the first main pipe 6 and the second main pipe 7. Example 3

[0054] As attached Figure 4 As shown, most of the technical content in this embodiment is exactly the same as that in embodiment 2. The difference is that this embodiment additionally sets two auxiliary pipelines (in the appendix). Figure 4 (Represented by blue lines), denoted as Form 1 and Form 2 respectively; the heat storage device can be configured with Form 1 or Form 2, or both Form 1 and Form 2 simultaneously. Specifically: Form 1: The heat storage device includes a first pipe 10, one end of which is connected to a third main pipe 8, and the other end of which is connected to a fourth main pipe 9.

[0055] Form 2: The heat storage device includes a second pipe 11 and a third pipe 12. One end of the second pipe 11 is connected to the third main pipe 8, and the other end is connected to the material inlet of the incinerator. One end of the third pipe 12 is connected to the material outlet of the incinerator, and the other end is connected to the material outlet of the waste heat boiler.

[0056] Based on Example 3, for the sulfur recovery system, especially the sulfur recovery process combined with a thermal storage device, in order to improve the stability and intelligence of the entire system operation, as shown in the appendix... Figure 5 As shown, the waste heat boiler is equipped with a temperature detector A at the process gas outlet, a regulating valve B in the first pipe 10, a temperature detector C at the process gas outlet of the primary sulfur cooler, a regulating valve D at the material inlet of the primary sulfur cooler, a temperature detector E at the process gas outlet of the first-stage reheater, a regulating valve F at the material inlet of the first-stage reheater, a temperature detector G at the process gas outlet of the first-stage sulfur cooler, a regulating valve H at the material inlet of the first-stage sulfur cooler, a temperature detector I at the process gas outlet of the second-stage reheater, and a regulating valve J at the material inlet of the second-stage sulfur cooler. Temperature detector K is installed at the process gas outlet of the reactor; regulating valve L is installed at the material inlet of the secondary sulfur cooler; temperature detector M is installed at the process gas outlet of the tertiary reheater; regulating valve N is installed at the material inlet of the tertiary reheater; temperature detector O is installed at the process gas outlet of the tertiary sulfur cooler; regulating valve P is installed at the material inlet of the tertiary sulfur cooler; temperature detector Q is installed at the tail gas outlet of the incinerator; regulating valve R is installed in the second pipe 11; temperature detector S is installed at the feed inlet of high temperature storage tank 1; temperature detector T is installed at the feed inlet of low temperature storage tank 3; and regulating valve U is installed at the water inlet of steam generator 2.

[0057] Based on this, this application proposes a control method for a sulfur recovery system coupled with a thermal storage device, comprising: S1. Real-time acquisition of the process gas outlet temperature Ta of the waste heat boiler; S2. If Ta > 260℃, increase the output flow rate of the cryogenic pump 301 (i.e., increase the discharge flow rate of the cryogenic storage tank 3 outlet) and increase the opening of the regulating valve B in the first pipe 10; if Ta < 230℃, decrease the output flow rate of the cryogenic pump 301 (i.e., decrease the discharge flow rate of the cryogenic storage tank 3 outlet) and decrease the opening of the regulating valve B in the first pipe 10. S3. Real-time acquisition of process gas outlet temperature Tbi of each sulfur cooler and process gas outlet temperature Tci of each reheater. Since this application includes at least two reheaters and at least two sulfur coolers, in order to facilitate differentiation in the following text and maintain naming consistency, the natural number i is used as a designation, and is consistent with each stage of reheater and sulfur cooler. For example, the process gas outlet temperature of the first-stage sulfur cooler is denoted as Tb1, the process gas outlet temperature of the second-stage reheater is denoted as Tc2, and correspondingly, the process gas outlet temperature of the primary sulfur cooler is denoted as Tb0.

[0058] S4. If Tbi > 160℃, increase the regulating valve at the corresponding sulfur cooler material inlet; if Tbi < 150℃, decrease the regulating valve at the corresponding sulfur cooler material inlet; if Tci < 240℃, increase the regulating valve at the corresponding reheater material inlet; if Tci > 260℃, decrease the regulating valve at the corresponding reheater material inlet. S5. Real-time acquisition of the exhaust gas outlet temperature Td of the incinerator; S6. If Td > 160℃, increase the opening of the regulating valve R in the second pipe 11; if Td < 150℃, decrease the opening of the regulating valve R in the second pipe 11.

[0059] Therefore, this application detects, analyzes, and controls the various equipment nodes (such as waste heat boilers, reheaters, sulfur coolers, incinerators, etc.) that exchange heat between materials and process gas. By adjusting the material flow rate of the corresponding equipment nodes, the temperature of the process gas in each equipment node can be controlled in a timely and accurate manner, so that the process gas in the sulfur recovery system can always be maintained within the temperature range required for the reaction, thereby ensuring the normal, stable, and continuous operation of the sulfur recovery process.

[0060] While the aforementioned control methods can intelligently and accurately regulate the operating conditions of each equipment node, the upstream and downstream (series) relationships of process airflow and the parallel or series relationships of material flow between these nodes mean that adjusting the material flow in one node may affect the operating conditions of other nodes, creating a ripple effect. This can lead to continuous fluctuations in the operating conditions of the entire sulfur recovery system due to individual control operations, which is detrimental to the continuous and stable operation of the entire system. Furthermore, during the start-up phase of a system requiring frequent adjustments, the process from start-up to stable operation will require a relatively long adjustment period, which undoubtedly hinders the reduction of system start-up time and affects actual production efficiency.

[0061] Therefore, in order to improve the stability of the entire control process and minimize the overall impact of a single control measure, this application optimizes and improves the control method, specifically: The control method (if implemented during the system start-up phase, it can also be referred to as a start-up method for a sulfur recovery system coupled with a thermal storage device) includes: A1. Real-time acquisition of the process gas outlet temperature Ta of the waste heat boiler; A2. If Ta > 260℃, increase the output flow rate of the cryogenic pump 301, increase the opening of the regulating valve B in the first pipe 10, and return to step A1; if Ta < 230℃, decrease the output flow rate of the cryogenic pump 301, decrease the opening of the regulating valve B in the first pipe 10, and return to step A1; if 230℃ ≤ Ta ≤ 260℃, proceed to step A3. A3. Real-time acquisition of the process gas outlet temperature Tb0 of the primary sulfur cooler; A4. If Tb0 > 160℃, adjust the regulating valve D at the material inlet of the primary sulfur cooler and return to step A1; if Tb0 < 150℃, adjust the regulating valve D at the material inlet of the primary sulfur cooler and return to step A1; if 150℃ ≤ Tb0 ≤ 160℃, proceed to step A5. A5. Real-time acquisition of the process gas outlet temperature Tc1 of the first-stage reheater; A6. If Tc1 < 240℃, increase the output flow rate of high-temperature pump 101 (i.e., increase the discharge flow rate of high-temperature storage tank 1), adjust the regulating valve F at the material inlet of the first-stage reheater, and return to step A5; if Tc1 > 260℃, decrease the output flow rate of high-temperature pump 101 (i.e., decrease the discharge flow rate of high-temperature storage tank 1), adjust the regulating valve F at the material inlet of the first-stage reheater, and return to step A5; if 240℃ ≤ Tc1 ≤ 260℃, proceed to step A7. A7. Real-time acquisition of the process gas outlet temperature Tb1 of the first-stage sulfur cooler; A8. If Tb1 > 160℃, increase the regulating valve H at the material inlet of the first-stage sulfur cooler and return to step A3; if Tb1 < 150℃, decrease the regulating valve H at the material inlet of the first-stage sulfur cooler and return to step A3; if 150℃ ≤ Tb1 ≤ 160℃, proceed to step A9. A9. Real-time acquisition of the process gas outlet temperature Tc2 of the secondary reheater; A10. If Tc2 < 240℃, increase the regulating valve J at the material inlet of the secondary reheater and return to step A5; if Tc2 > 260℃, decrease the regulating valve J at the material inlet of the secondary reheater and return to step A5; if 240℃ ≤ Tc2 ≤ 260℃, proceed to step A11. A11. Real-time acquisition of the process gas outlet temperature Tb2 of the secondary sulfur cooler; A12. If Tb2 > 160℃, increase the regulating valve L at the material inlet of the secondary sulfur cooler and return to step A7; if Tb2 < 150℃, decrease the regulating valve L at the material inlet of the secondary sulfur cooler and return to step A7; if 150℃ ≤ Tb2 ≤ 160℃, proceed to step A13. A13. Real-time acquisition of the process gas outlet temperature Tc3 of the third-stage reheater; A14. If Tc3 < 240℃, increase the regulating valve N at the material inlet of the third-stage reheater and return to step A9; if Tc3 > 260℃, decrease the regulating valve N at the material inlet of the third-stage reheater and return to step A9; if 240℃ ≤ Tc3 ≤ 260℃, proceed to step A15. A15. Real-time acquisition of the process gas outlet temperature Tb3 of the three-stage sulfur cooler; A16. If Tb3 > 160℃, adjust the regulating valve P at the material inlet of the third-stage sulfur cooler and return to step A11; if Tb3 < 150℃, adjust the regulating valve P at the material inlet of the third-stage sulfur cooler and return to step A11; if 150℃ ≤ Tb3 ≤ 160℃, proceed to step A17. A17. Real-time acquisition of the exhaust gas outlet temperature Td of the incinerator; A18. If Td > 160℃, increase the opening of the regulating valve R in the second pipe 11 and return to step A15; if Td < 150℃, decrease the opening of the regulating valve R in the second pipe 11 and return to step A15; if 150℃ ≤ Td ≤ 160℃, the process can end, or it can return to step S1 (forming a logic closed loop).

[0062] Therefore, for each equipment node related to heat exchange between materials and process gas, this application uses the aforementioned control method to more precisely regulate the process gas temperature and material flow rate of each relevant equipment. Especially during the analysis and control processes in steps A4, A8, A10, A12, A14, and A16, based on the upstream and downstream relationship of each equipment node in the process gas flow direction, when the relevant process gas temperature does not meet the preset temperature, on the one hand, the corresponding material valve is adjusted in a timely manner; on the other hand, after adjusting a single equipment node, feedback can be promptly sent to the upstream equipment of that equipment node, and the upstream equipment node is then adjusted again. By implementing sequential control, a "step-by-step upward iteration" is formed within a certain control range. This allows for timely and effective step-by-step control of upstream equipment nodes in the face of the unavoidable situation where "the control of downstream equipment nodes induces fluctuations in upstream operating conditions." On the one hand, it can promptly and effectively eliminate fluctuations in the operating conditions of other equipment induced by the control of a single equipment, which helps to reduce the impact of related fluctuations on each equipment node and effectively improves the accuracy of the control of each equipment node. On the other hand, it also prevents the accumulation of fluctuations induced by the control of each individual equipment node in the system, which is conducive to the continuous and stable operation of the entire system.

[0063] Furthermore, this control method can also be used in the start-up phase of the entire sulfur recovery system. With each "upward iteration" after regulation, the fluctuations induced by the relevant regulation can be eliminated quickly and effectively. This can effectively shorten the time from system start-up to stable operation, improve the system's start-up efficiency, and enable the system to enter a normal and stable operating state more quickly, which is conducive to improving production efficiency.

[0064] In addition to the control measures related to various equipment nodes involved in the heat exchange between materials and process gas, the control methods in this application also include: material temperature control methods for high-temperature storage tank 1 and low-temperature storage tank 3, to ensure as much as possible that the material operating conditions in high-temperature storage tank 1 and low-temperature storage tank 3 can meet the usage requirements of the relevant downstream equipment nodes. Specifically: The material temperature control method of the high-temperature storage tank 1 includes: B1. Real-time acquisition of the inlet temperature Te of high-temperature storage tank 1; B2. Determine if Te < 430℃; if yes, start the heating device to heat the material to be entered into the high-temperature storage tank 1; if no, maintain the current operating status.

[0065] The material entering the high-temperature storage tank 1 is the material that flows out after heat exchange in the waste heat boiler. The temperature of the process gas entering the waste heat boiler is about 600~700℃, and the temperature of the flue gas generated by the incinerator is about 1200~1300℃. In terms of the structure and performance of the waste heat boiler currently used by the applicant, if the temperature of the material entering the waste heat boiler is around 130℃, the temperature of the material flowing out of the waste heat boiler will often not exceed 430℃. Therefore, it is necessary to regulate the temperature of the material in the high-temperature storage tank 1 by supplementing the heat of the material through the electric heater 4 and / or the combustion heater 5.

[0066] The material temperature control method of the cryogenic storage tank 3 includes: C1. Real-time acquisition of the inlet temperature Tf of the cryogenic storage tank 3; C2. Determine if Tf > 140℃; if yes, increase the opening of the regulating valve U at the inlet of steam generator 2; if no, maintain the current operating state.

[0067] Therefore, when the temperature of the material to be introduced into the cryogenic storage tank 3 is greater than 140°C, the water flow rate in the steam generator 2 can be increased, so that the excess heat carried by the material can be used to produce more medium-pressure steam.

[0068] 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 principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A sulfur recovery system coupled with a thermal storage device, characterized in that, The sulfur recovery system includes a heat storage device, a reactor, a sulfur recovery device, and an incinerator, which are connected in sequence. The reactor is equipped with a waste heat boiler, and the sulfur recovery device includes at least two sulfur recovery groups connected in sequence. Each sulfur recovery group includes a reheater, a converter, and a sulfur cooler connected in sequence. The heat storage device includes a high-temperature storage tank (1), a steam generator (2), a low-temperature storage tank (3), and a heating device connected in sequence. Modified liquid sulfur material is circulated and transported within the heat storage device. The outlet of the high-temperature storage tank (1) is connected to the material inlet of each reheater. The material outlet of each reheater is connected to the inlet of the steam generator (2) and / or the inlet of the low-temperature storage tank (3). The outlet of the steam generator (2) is connected to the inlet of the low-temperature storage tank (3). The outlet of the low-temperature storage tank (3) is connected to the material inlet of each sulfur cooler. The material outlet of each sulfur cooler is connected to the material inlet of the waste heat boiler. The material outlet of the waste heat boiler is connected to the inlet of the heating device. The outlet of the heating device is connected to the inlet of the high-temperature storage tank (1). The outlet of the high-temperature storage tank (1) is connected to the inlet of the steam generator (2).

2. The sulfur recovery system of the coupled thermal storage device according to claim 1, characterized in that, The thermal storage device includes a first main pipe (6), the inlet of which is connected to the outlet of the high-temperature storage tank (1), and the outlet of the first main pipe (6) is connected to the inlet of the steam generator (2) and the material inlet of each reheater.

3. The sulfur recovery system of the coupled thermal storage device according to claim 1, characterized in that, The thermal storage device includes a second main pipe (7), the inlet of which is connected to the material outlet of each reheater, and the outlet of which is connected to the inlet of the steam generator (2) and / or the inlet of the cryogenic storage tank (3).

4. The sulfur recovery system of the coupled thermal storage device according to claim 1, characterized in that, The heat storage device includes a third main pipe (8) and a fourth main pipe (9). The inlet of the third main pipe (8) is connected to the outlet of the low-temperature storage tank (3). The outlet of the third main pipe (8) is connected to the material inlet of each sulfur cooler. The inlet of the fourth main pipe (9) is connected to the material outlet of each sulfur cooler. The outlet of the fourth main pipe (9) is connected to the material inlet of the waste heat boiler.

5. The sulfur recovery system of a coupled thermal storage device according to claim 4, characterized in that, The heat storage device includes a first pipe (10), one end of which is connected to a third main pipe (8), and the other end is connected to a fourth main pipe (9).

6. The sulfur recovery system of a coupled thermal storage device according to claim 4, characterized in that, The heat storage device includes a second pipe (11) and a third pipe (12). One end of the second pipe (11) is connected to the third main pipe (8), and the other end is connected to the material inlet of the incinerator. One end of the third pipe (12) is connected to the material outlet of the incinerator, and the other end is connected to the material outlet of the waste heat boiler.

7. The sulfur recovery system of a coupled thermal storage device according to claim 1, characterized in that, In the flow direction of the process gas, a primary sulfur cooler is provided between the reactor and the sulfur recovery device. The sulfur recovery device includes a first-stage reheater, a first-stage converter, a first-stage sulfur cooler, a second-stage reheater, a second-stage converter, a second-stage sulfur cooler, a third-stage reheater, a third-stage converter, and a third-stage sulfur cooler connected in sequence. The process gas outlet of the primary sulfur cooler is connected to the process gas inlet of the first-stage reheater, and the process gas outlet of the third-stage sulfur cooler is connected to the process gas inlet of the incinerator.

8. A sulfur recovery system for a coupled thermal storage device according to claim 7, characterized in that, The thermal storage device includes a first main pipe (6) and a second main pipe (7). The inlet of the first main pipe (6) is connected to the outlet of the high-temperature storage tank (1). The outlet of the first main pipe (6) is connected to the inlet of the steam generator (2), the material inlet of the first-stage reheater, the material inlet of the second-stage reheater, and the material inlet of the third-stage reheater, respectively. The inlet of the second main pipe (7) is connected to the material outlet of the first-stage reheater, the material outlet of the second-stage reheater, and the material outlet of the third-stage reheater, respectively. The outlet of the second main pipe (7) is connected to the inlet of the low-temperature storage tank (3).

9. A sulfur recovery system for a coupled thermal storage device according to claim 7, characterized in that, The heat storage device includes a third main pipe (8) and a fourth main pipe (9). The inlet of the third main pipe (8) is connected to the outlet of the low-temperature storage tank (3). The outlet of the third main pipe (8) is connected to the material inlet of the primary sulfur cooler, the material inlet of the first-stage sulfur cooler, the material inlet of the second-stage sulfur cooler, and the material inlet of the third-stage sulfur cooler. The inlet of the fourth main pipe (9) is connected to the material outlet of the primary sulfur cooler, the material outlet of the first-stage sulfur cooler, the material outlet of the second-stage sulfur cooler, and the material outlet of the third-stage sulfur cooler. The outlet of the fourth main pipe (9) is connected to the material inlet of the waste heat boiler.

10. A control method for a sulfur recovery system coupled with a thermal storage device, characterized in that, The control method is applied to the sulfur recovery system of the coupled thermal storage device according to any one of claims 1-9; the control method includes: S1. Real-time acquisition of the process gas outlet temperature Ta of the waste heat boiler; S2. If Ta > 260℃, increase the discharge flow rate at the outlet of the low-temperature storage tank (3) and increase the opening of the regulating valve B in the first pipe (10); if Ta < 230℃, decrease the discharge flow rate at the outlet of the low-temperature storage tank (3) and decrease the opening of the regulating valve B in the first pipe (10). S3. Real-time acquisition of process gas outlet temperature Tbi of each sulfur cooler and process gas outlet temperature Tci of each reheater. S4. If Tbi > 160℃, increase the regulating valve at the corresponding sulfur cooler material inlet; if Tbi < 150℃, decrease the regulating valve at the corresponding sulfur cooler material inlet; if Tci < 240℃, increase the regulating valve at the corresponding reheater material inlet; if Tci > 260℃, decrease the regulating valve at the corresponding reheater material inlet. S5. Real-time acquisition of the exhaust gas outlet temperature Td of the incinerator; S6. If Td > 160℃, increase the opening of the regulating valve R in the second pipe (11); if Td < 150℃, decrease the opening of the regulating valve R in the second pipe (11).

Images