A control system and control method for the formation of thiosulfate from sulfides

Abstract

This invention provides a control system and method for the generation of thiosulfate from sulfides. The system includes: a microchannel reactor, used to perform operations corresponding to the preset requirements on the internal airflow and sulfide waste alkali solution when the reaction conditions reach the preset requirements, and to transport the generated reaction products to a gas-liquid separation unit; the gas-liquid separation unit, connected to the microchannel reactor via pipeline, is used to separate the reaction products into gas and liquid phases, and, based on triggering different reaction conditions, controls a circulating pump to deliver sulfide waste alkali solution and / or separated liquid to the microchannel reactor. This embodiment of the system, by setting up a microchannel reactor, not only accelerates the mass transfer rate from air to the liquid phase, thereby accelerating the oxidation reaction of sulfides and effectively shortening the reaction time; but also, by combining the microchannel reactor and the gas-liquid separation unit, it can achieve automated preparation of thiosulfate, improving the conversion efficiency of sulfides.

Description

Technical Field

[0001] This invention belongs to the field of wastewater treatment technology, and in particular relates to a control system and control method for the generation of thiosulfate from sulfides. Background Technology

[0002] Currently, approximately 98% of ethylene production globally utilizes tubular furnace steam cracking technology. This process generates large amounts of acidic gases such as carbon dioxide and hydrogen sulfide, which pose risks to subsequent distillation and separation processes, causing corrosion of equipment and pipelines. The process uses sodium hydroxide for absorption, known as alkaline washing. During absorption, the replenishment of fresh alkali and the discharge of waste alkali solution result in a large volume of ethylene waste alkali solution. This waste alkali solution contains significant amounts of organic matter and inorganic salts such as Na₂S and Na₂CO₃. Due to the condensation of heavy components in the cracked gas and the polymerization of diene compounds during alkaline washing, a large amount of organic matter enters the waste alkali solution, forming an oily substance commonly known as "butter." Therefore, treating this type of wastewater is quite challenging. Conventional treatment methods combine pretreatment and biological treatment. Pretreatment methods include neutralization, oxidation, or biological processes before the wastewater is sent to a comprehensive wastewater treatment plant for biological treatment.

[0003] Oxidation is the most common method, which mainly converts sulfides in waste alkaline solutions into sulfates through oxidation. Oxidation of sulfides can use ozone, air, hydrogen peroxide, etc., as oxidants. Using air as the oxidant is the most economical method. The oxidation reaction process of sulfides under air conditions is as follows:

[0004] 2S2 - +H₂O + O₂ → S₂O₃ 2- +2OH - (1);

[0005] 2HS- + 2O2 → S2O3 2- +H2O (2);

[0006] S2O3 2- +2O₂ + H₂O → 2SO₄ 2- +2H + (3);

[0007] Sulfides are converted into thiosulfates, as shown in (1). The generated thiosulfates are further oxidized to sulfates. Compared with sulfates, thiosulfates have higher economic value. If sulfides in sulfur-containing wastewater are efficiently and selectively converted into thiosulfates for utilization, it will not only reduce the amount of sludge discharged during wastewater treatment, but also create certain economic value for enterprises.

[0008] Currently, many systems for preparing thiosulfate based on sulfides usually require manual control of each process step. This preparation process is not only time-consuming and labor-intensive, but also prone to uncontrollable processes due to human subjective factors, which can affect the conversion rate of sulfides. Summary of the Invention

[0009] This invention provides a control system and method for generating thiosulfate based on sulfides. This control system can not only realize the automated preparation of thiosulfate, but also improve the conversion rate of sulfides.

[0010] To achieve the above objectives, according to a first aspect of the present application, a control system for generating thiosulfate based on sulfides is provided. The system includes: a microchannel reactor, used to perform operations corresponding to the preset requirements on the internal airflow and sulfide waste alkali solution when the reaction conditions reach the preset requirements, and to transport the generated reaction products to a gas-liquid separation unit; the gas-liquid separation unit is connected to the microchannel reactor through a pipeline, used to perform gas-liquid separation on the reaction products, and to control a circulating pump to deliver sulfide waste alkali solution and / or separated liquid to the microchannel reactor based on the triggering of different reaction conditions.

[0011] Optionally, the system further includes: an analysis unit; the analysis unit is connected to the gas-liquid separation unit via a pipeline, and is used to collect the separated liquid from the output end of the gas-liquid separation unit based on a preset detection time trigger, and analyze the sulfide concentration and thiosulfate concentration in the separated liquid to generate analysis results.

[0012] Optionally, the system further includes: a first conveying unit connected to the microchannel reactor via a pipeline; used to convey nitrogen to the microchannel reactor to replace the air inside the system according to a preset number of times based on the triggering of the sulfide waste alkali liquid volume in the gas-liquid separation unit; and to convey the compressed air stream to the microchannel reactor according to a first preset flow rate based on the triggering of a preset reaction temperature.

[0013] Optionally, the gas-liquid separation unit includes a gas-liquid separator; the output end of the gas-liquid separator is connected to the input end of the circulating pump, and the output end of the circulating pump is connected to the input end of the microchannel reactor; the gas-liquid separator is used to deliver sulfide waste alkali solution to the microchannel reactor through the circulating pump at a second preset flow rate after the air in the system has been replaced by nitrogen, and to end the delivery operation when the system temperature reaches a preset reaction temperature. The gas-liquid separator is also used to deliver sulfide waste alkali solution and separated liquid to the microchannel reactor through the circulating pump at a second preset flow rate when the system pressure reaches a preset reaction pressure and the air flow delivery rate reaches a first preset flow rate.

[0014] Optionally, the gas-liquid separation unit further includes a constant temperature water tank; the gas-liquid separator is provided with a jacket, and the jacket contains circulating hot water; the constant temperature water tank is connected to the jacket through a pipeline for heating the circulating hot water, and the heated circulating hot water is transported to the jacket through a hot water circulation pump to control the system temperature to be maintained at a preset reaction temperature.

[0015] Optionally, the gas-liquid separator is further provided with a back pressure valve; the back pressure valve is used to output the separated gas after separation by the gas-liquid separator and adjust the pressure of the system to a preset reaction pressure.

[0016] Optionally, the gas-liquid separator is further provided with a level gauge and a drain valve; the level gauge is used to adjust the volume of the separated liquid retained in the gas-liquid separator; the drain valve is used to discharge the excess separated liquid in the gas-liquid separator according to a third preset flow rate, so that the liquid level in the level gauge remains constant.

[0017] Optionally, the microchannel reactor is used to perform an oxidation reaction on the internal airflow and sulfide waste alkaline solution when the reaction conditions reach the first preset condition; and to perform a reaction stop operation on the internal airflow and sulfide waste alkaline solution when the reaction time reaches the preset reaction time.

[0018] Optionally, the first delivery unit includes: a pneumatic pump and a flow meter; the pneumatic pump is connected to the microchannel reactor via a pipeline, and the pneumatic pump is used to compress the collected air into an airflow and deliver it to the microchannel reactor; the flow meter is installed on the input pipeline of the microchannel reactor and is used to control the airflow output by the pneumatic pump to be delivered to the microchannel reactor according to a first preset flow rate;

[0019] To achieve the above objectives, according to a second aspect of the present application, a control method for the generation of thiosulfate based on sulfides is also provided. The method includes: when the system temperature is detected to reach a preset reaction temperature, controlling a conveying unit to deliver compressed air to a microchannel reactor at a first preset flow rate; and controlling a back pressure valve to adjust the system pressure to a preset reaction pressure; generating a first trigger command; based on the first trigger command, controlling a gas-liquid conveying unit to deliver the contained sulfide waste alkali solution to a microchannel reaction unit at a second preset flow rate; and monitoring the reaction time in the microchannel reactor. When the monitoring result indicates that the reaction time has reached a preset reaction time, controlling the microchannel reactor to terminate the reaction operation.

[0020] According to a third aspect of the present invention, a computer-readable medium is also provided, on which a computer program is stored, wherein the program, when executed by a processor, implements the control method as described in the first aspect.

[0021] Compared with existing technologies, this invention provides a control system for the generation of thiosulfate from sulfides. The system includes: a microchannel reactor, used to perform operations corresponding to the preset requirements on the internal airflow and sulfide waste alkali solution when the reaction conditions reach the preset requirements, and to transport the generated reaction products to a gas-liquid separation unit; the gas-liquid separation unit, connected to the microchannel reactor via pipeline, used to separate the reaction products into gas and liquid phases, and, based on triggering different reaction conditions, controls a circulating pump to deliver sulfide waste alkali solution and / or separated liquid to the microchannel reactor. This system, by setting up a microchannel reactor, not only accelerates the mass transfer rate from air to the liquid phase, thereby accelerating the oxidation reaction of sulfides and effectively shortening the reaction time; but also, by combining the microchannel reactor and the gas-liquid separation unit, it can achieve automated preparation of thiosulfate, improving the conversion efficiency of sulfides. Attached Figure Description

[0022] The following sections will describe some specific embodiments of the invention in a detailed manner by way of example and not limitation, with reference to the accompanying drawings. The same reference numerals in the drawings denote the same or similar parts or portions. Those skilled in the art should understand that these drawings are not necessarily drawn to scale. In the drawings:

[0023] Figure 1 This is a schematic diagram of a control system for generating thiosulfate based on sulfides, provided in an embodiment of the present invention.

[0024] Figure 2 This is a schematic flowchart of a method for controlling the formation of thiosulfate based on sulfides, provided in an embodiment of the present invention.

[0025] Figure 3 This is a schematic diagram showing the changes in the concentrations of Na2S and Na2S2O3 in the oxidized waste alkaline solution over time, as measured in Example 1.

[0026] Figure 4 This is a schematic diagram showing the changes in the concentrations of Na2S and Na2S2O3 in the oxidized waste alkaline solution as of time, as measured in Comparative Example 1.

[0027] Figure 5 The table shows the experimental conditions and results for Examples 2-8. Detailed Implementation

[0028] To make the objectives, features, and advantages of this invention more apparent and understandable, the technical solutions of the embodiments of this invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only a part of the embodiments of this invention, and not all of them. All other embodiments obtained by those skilled in the art based on the embodiments of this invention without creative effort are within the scope of protection of this invention.

[0029] like Figure 1 The diagram shown is a schematic diagram of a control system for generating thiosulfate based on sulfides, according to an embodiment of the present invention.

[0030] A control system for the generation of thiosulfate from sulfides, the system comprising:

[0031] A microchannel reactor is used to perform operations on the internal airflow and sulfide waste alkaline solution in accordance with the preset requirements when the reaction conditions meet the preset requirements, and to transport the generated reaction products to a gas-liquid separation unit.

[0032] A gas-liquid separation unit is connected to the microchannel reactor via a pipeline and is used to separate the reaction products into gas and liquid. Based on the triggering of different reaction conditions, it controls a circulating pump to deliver sulfide waste alkaline solution and / or separated liquid to the microchannel reactor.

[0033] The first delivery unit is connected to the microchannel reactor via a pipeline; it is used to deliver nitrogen to the microchannel reactor to replace the air inside the system according to a preset number of times based on the triggering of the sulfide waste alkali liquid volume in the gas-liquid separation unit; and to deliver the compressed air stream to the microchannel reactor according to a first preset flow rate based on the triggering of the preset reaction temperature.

[0034] For example, the microchannel reactor is used to perform an oxidation reaction on the internal airflow and sulfide waste alkaline solution when the reaction conditions reach a first preset condition; and to stop the reaction on the internal airflow and sulfide waste alkaline solution when the reaction time reaches a preset reaction time. The first delivery unit includes: a pneumatic pump and a flow meter; the pneumatic pump is connected to the microchannel reactor through a pipeline, and the pneumatic pump is used to compress the collected air into an airflow and deliver it to the microchannel reactor; the flow meter is installed on the input pipeline of the microchannel reactor and is used to control the airflow output by the pneumatic pump to be delivered to the microchannel reactor according to the first preset flow rate.

[0035] Specifically, a microchannel reactor is a miniature reactor manufactured using precision machining technology, with channel equivalent diameters ranging from 10 to 300 micrometers (or 1000 micrometers). The "micro" in microchannel reactor refers to the micrometer-level channel size of the process fluid, not the small external size of the microreactor or the low yield of the product. Microchannel reactors can contain millions or even tens of millions of microchannels, thus achieving very high throughput. The internal microstructure of a microchannel reactor gives it an extremely large specific surface area, hundreds or even thousands of times larger than that of a stirred tank reactor. Microchannel reactors possess excellent heat and mass transfer capabilities, enabling instantaneous and uniform mixing of materials and highly efficient heat transfer.

[0036] The microchannel reactor in this embodiment can fully disperse the airflow in the sodium sulfide waste alkaline solution, so that the two can come into full contact and undergo a full chemical reaction under the first preset conditions to generate reaction products; then the microchannel reactor can also transport the reaction products to the gas-liquid separation unit.

[0037] After separation, the gas-liquid separation unit generates separated gas and separated liquid; the separated gas is discharged through the gas-liquid separation unit, and the separated liquid is divided into two parts; the first part of the separated liquid is transported to the input end of the microchannel reactor as a circulating liquid, and the second part of the separated liquid is ready for output.

[0038] This embodiment of the system utilizes a microchannel reactor, which has high mass transfer efficiency between the gas and liquid phases, to accelerate the mass transfer rate from air to the liquid phase. This, in turn, speeds up the oxidation reaction of sodium sulfide, effectively shortens the reaction time, and improves the conversion efficiency of sodium sulfide.

[0039] In a preferred embodiment, the gas-liquid separation unit includes a gas-liquid separator and a constant-temperature water bath; the output end of the gas-liquid separator is connected to the input end of the circulating pump, and the output end of the circulating pump is connected to the input end of the microchannel reactor; the gas-liquid separator is used to deliver sulfide waste alkali solution to the microchannel reactor through the circulating pump at a second preset flow rate after the air in the system has been replaced by nitrogen, and to end the delivery operation when the system temperature reaches a preset reaction temperature. The gas-liquid separator is also used to deliver sulfide waste alkali solution and separated liquid to the microchannel reactor through the circulating pump at a second preset flow rate when the system pressure reaches a preset reaction pressure and the air flow rate reaches a first preset flow rate.

[0040] The gas-liquid separator is equipped with a jacket containing circulating hot water. The constant temperature water tank is connected to the jacket via a pipeline to heat the circulating hot water and to pump the heated circulating hot water to the jacket via a hot water circulation pump to control the system temperature to be maintained at a preset reaction temperature.

[0041] The gas-liquid separator is equipped with a back pressure valve; the back pressure valve is used to output the separated gas after separation by the gas-liquid separator and adjust the pressure of the system to a preset reaction pressure.

[0042] The gas-liquid separator is equipped with a level gauge; the level gauge is used to adjust the volume of the retained liquid in the gas-liquid separator.

[0043] The gas-liquid separator is equipped with a drain valve; the drain valve is used to discharge excess separated liquid in the gas-liquid separator according to a third preset flow rate so that the liquid level in the level gauge remains constant.

[0044] For example: a control system for the generation of thiosulfate based on sulfides includes: a controller, and a microchannel reactor, a gas-liquid separator, a constant temperature water bath, a gas pressure pump, a circulation pump, a hot water circulation pump, a back pressure valve, a pressure gauge, and an analysis unit, all electrically connected to the controller.

[0045] The output of the pneumatic pump is connected to the input of the bottom of the microchannel reactor via a pipeline; the output of the top of the microchannel reactor is connected to the input of the top of the gas-liquid separator via a pipeline; the output of the bottom of the gas-liquid separator is connected to the input of the circulating pump via a pipeline; the output of the circulating pump is connected to the input of the bottom of the microchannel reactor via a pipeline. A back pressure valve and a pressure gauge for detecting system pressure are installed on the top of the gas-liquid separator; a level gauge is also installed on the side of the gas-liquid separator, one end of which is connected to the side of the gas-liquid separator; a jacket is also installed on the gas-liquid separator; circulating hot water for heating the gas-liquid separator is installed inside the jacket; the output of the jacket is connected to the input of the constant temperature water bath via a pipeline; the output of the constant temperature water bath is connected to the input of the hot water circulating pump via a pipeline, and the output of the hot water circulating pump is connected to the input of the jacket via a pipeline; a drain valve is also installed at the bottom of the gas-liquid separator, and an emergency vent valve is installed at the top.

[0046] The control system in this embodiment is based on an automated process to achieve automated preparation of thiosulfate, which not only reduces the phenomenon of uncontrollable process due to human subjective factors during production, but also improves the conversion rate of sulfides.

[0047] In a preferred embodiment, the control system further includes an analysis unit connected to the controller; the analysis unit is connected to the drain valve via a pipeline.

[0048] like Figure 2 The diagram shown is a flowchart illustrating a method for controlling the generation of thiosulfate from sulfides according to an embodiment of the present invention.

[0049] A method for controlling the formation of thiosulfate from sulfides includes at least the following steps:

[0050] S201, when the system temperature is detected to have reached the preset reaction temperature, the control delivery unit delivers the compressed air flow to the microchannel reactor according to the first preset flow rate; and controls the back pressure valve to adjust the system pressure to the preset reaction pressure; and generates the first trigger command;

[0051] S202, based on the first trigger command, control the gas-liquid conveying unit to deliver the contained sulfide waste alkaline solution to the microchannel reaction unit according to the second preset flow rate; and detect the reaction time in the microchannel reactor. When the monitoring result indicates that the reaction time has reached the preset reaction time, control the microchannel reactor to end the reaction operation.

[0052] Specifically, the gas pump is controlled to input nitrogen into the system according to a preset number of cycles, and the system pressure is monitored by a pressure gauge. When the monitoring result indicates that the system pressure has reached the preset reaction pressure, the circulation pump is controlled to start. When the monitoring result indicates that the system pressure has not reached the preset reaction pressure, the back pressure valve is controlled to adjust the system pressure until the system pressure reaches the preset reaction pressure. The sulfide waste alkaline solution in the gas-liquid separator is controlled by the flow meter at the output end of the circulation pump to be delivered to the microchannel reactor according to a second preset flow rate, generating a second trigger command.

[0053] The constant temperature water tank and hot water circulation pump are activated based on the second trigger command; the system temperature is monitored; when the monitoring result indicates that the system temperature has reached the preset reaction temperature, the circulation pump is shut down, and a third trigger command is generated; based on the third trigger command, the air pressure pump is controlled to deliver compressed air to the microchannel reactor according to the first preset flow rate, and the system pressure is monitored by the pressure gauge; when the monitoring result indicates that the system pressure has reached the preset reaction pressure, the air flow rate is adjusted by the flow meter; when the monitoring result indicates that the system pressure has not reached the preset reaction pressure, the back pressure valve is controlled to adjust the system pressure until the system pressure reaches the preset reaction pressure, and the first trigger command is generated.

[0054] Based on the first trigger command, the circulation pump is controlled to start, and the flow rate of the sulfide waste alkali solution input into the microchannel reactor is controlled by the flow meter, generating a fourth trigger command; based on the fourth trigger command, the reaction time in the microchannel reactor is monitored; when the monitoring result indicates that the reaction time has reached the preset reaction time, the microchannel reactor is controlled to end the reaction operation.

[0055] Based on the preset detection time, the separated liquid output from the drain valve is analyzed to obtain the sulfide concentration analysis results and the thiosulfate concentration analysis results.

[0056] This embodiment is based on an automated process for preparing thiosulfate, which can terminate the reaction in a timely manner, so that the concentration of sulfides in the waste alkaline solution reaches the acceptable discharge standard of the wastewater treatment pond, while obtaining a high thiosulfate yield.

[0057] The reaction conditions in this embodiment are as follows:

[0058] Preset reaction temperature: T = 40-150℃, optimal T = 70-90℃;

[0059] Preset reaction pressure: P = 0.1-2.0 MPa, optimal P = 0.6-1.0 MPa;

[0060] Initial sulfide concentration: C0 = 1×10²~1×10⁶ mg / L;

[0061] Liquid flow velocity in the microchannel reactor: V = 10–100 m / s;

[0062] Airflow (Q) o ) and waste alkali solution circulation flow rate (Q) R The proportion of R is: R = 0.005~0.75;

[0063] Preset reaction time: 60–300 min.

[0064] Example 1

[0065] 2L of wastewater containing 23449mg / L Na2S was placed into a gas-liquid separator, with the wastewater volume accounting for 1 / 3 of the total volume of the separator. Nitrogen gas was introduced into the system to reach a pressure of 1MPa, and then vented. This step was repeated twice to ensure that the air in the system was replaced as much as possible with nitrogen. The circulation pump was turned on to circulate the waste alkali solution at a flow rate of 80L / h. The constant temperature water bath and hot water circulation pump were turned on to maintain the system temperature at 90℃. Once the system temperature stabilized, the waste alkali solution circulation pump was turned off. Then, air was introduced into the system at a flow rate of 36L / h to reach a pressure of 1MPa. The flow rate of the gas mass flow meter was adjusted to ensure that the air flow rate introduced into the system was 36L / h. The waste alkali solution circulation pump was turned on to maintain a flow rate of 80L / h, and timing was started. During the reaction, samples were periodically taken from the bottom of the gas-liquid separator to monitor the concentrations of Na2S and Na2S2O3 in the oxidized waste alkali solution. The changes in the concentrations of Na2S and Na2S2O3 in the oxidized waste alkaline solution measured in Implementation 1 over time are as follows: Figure 3 As shown in the figure, the yield of Na2S2O3 is calculated using the following formula (1):

[0066]

[0067] like Figure 3 The diagram shown illustrates the changes in Na2S and Na2S2O3 concentrations in the oxidized waste alkaline solution over time, as measured in Example 1. Figure 3It can be seen that as the oxidation reaction time increases, the concentration of Na2S in the waste alkaline solution decreases rapidly, while the concentration of Na2S2O3 initially increases rapidly, reaches its maximum value, and then decreases rapidly. In this embodiment, the yield of Na2S2O3 reaches its highest level, approximately 92%, when the oxidation reaction time reaches 200 min. The results of this embodiment indicate that in the process of treating waste alkaline solution using the air oxidation method, the method of this invention can control the oxidation reaction time and terminate the reaction at an appropriate time, so that the concentration of sulfides in the waste alkaline solution reaches the acceptable discharge standard of the wastewater treatment pond, while obtaining a high thiosulfate yield.

[0068] Comparative Example 1

[0069] Comparative Example 1 followed essentially the same reaction conditions as Example 1, but without using a microchannel reactor. Under these conditions, the oxidation of Na₂S still occurred. However, because the degree of mixing and contact between the gas and liquid phases was much lower than when using a microchannel reactor, the oxidation rate of Na₂S was significantly lower, as demonstrated by the experimental results below.

[0070] 2L of wastewater containing 22350mg / L Na2S was placed into a gas-liquid separator, with the wastewater volume accounting for 1 / 3 of the total volume of the separator. Nitrogen gas was introduced into the system to reach a pressure of 1MPa, and then vented. This step was repeated twice to ensure that the air in the system was replaced as completely as possible with nitrogen. The circulation pump was turned on to circulate the waste alkali solution at a flow rate of 80L / h. The constant temperature water bath and hot water circulation pump were turned on to maintain the system temperature at 90℃. Once the system temperature stabilized, the waste alkali solution circulation pump was stopped. Then, air was introduced into the system at a flow rate of 36L / h to reach a pressure of 1MPa. The flow rate of the gas mass flow meter was adjusted to ensure that the air flow rate introduced into the system was 36L / h. The waste alkali solution circulation pump was turned on to maintain a flow rate of 80L / h, and timing was started. During the reaction, samples were periodically taken from the bottom of the gas-liquid separator to monitor the concentrations of Na2S and Na2S2O3 in the oxidized waste alkali solution. Figure 4 The figure shows a schematic diagram of the changes in the concentrations of Na2S and Na2S2O3 in the oxidized waste alkaline solution as of time, as measured in Comparative Example 1.

[0071] Examples 2-9

[0072] Examples 2-9 illustrate experimental verification using the method of the present invention under different reaction conditions, and the experimental results are as follows: Figure 5 Table 2 shows the results. As can be seen from the data in Table 2, the method of this invention can efficiently and in high yield convert sulfides into thiosulfates; Table 2 also shows the experimental conditions and results of Examples 2-9.

[0073] The basic principles of this application have been described above with reference to specific embodiments. However, it should be noted that the advantages, benefits, and effects mentioned in this application are merely examples and not limitations, and should not be considered as essential features of each embodiment of this application. Furthermore, the specific details disclosed above are for illustrative and facilitative purposes only, and are not limitations. These details do not limit the application to the necessity of employing the aforementioned specific details for implementation.

[0074] The present invention also provides an electronic device, comprising: a processor; a memory for storing executable instructions of the processor; the processor being configured to read the executable instructions from the memory and execute the instructions to implement the control method for generating thiosulfate based on sulfides according to the present invention.

[0075] In addition to the methods and apparatus described above, embodiments of this application may also be computer program products, which include computer program instructions that, when executed by a processor, cause the processor to perform the steps in the methods according to various embodiments of this application described in the "Exemplary Methods" section above.

[0076] The computer program product can be written in any combination of one or more programming languages ​​to perform the operations of the embodiments of this application. The programming languages ​​include object-oriented programming languages ​​such as Java and C++, as well as conventional procedural programming languages ​​such as C or similar languages. The program code can be executed entirely on the user's computing device, partially on the user's computing device, as a standalone software package, partially on the user's computing device and partially on a remote computing device, or entirely on a remote computing device or server.

[0077] Furthermore, embodiments of this application may also be computer-readable storage media storing computer program instructions thereon, which, when executed by a processor, cause the processor to perform the steps in the methods according to the following embodiments of this application described in the "Exemplary Methods" section above.

[0078] The computer-readable storage medium may be any combination of one or more readable media. A readable medium may be a readable signal medium or a readable storage medium. A readable storage medium may, for example, include, but is not limited to, electrical, magnetic, optical, electromagnetic, infrared, or semiconductor systems, apparatuses, or devices, or any combination thereof. More specific examples of readable storage media (a non-exhaustive list) include: electrical connections having one or more wires, portable disks, hard disks, random access memory (RAM), read-only memory (ROM), erasable programmable read-only memory (EPROM or flash memory), optical fibers, portable compact disk read-only memory (CD-ROM), optical storage devices, magnetic storage devices, or any suitable combination thereof.

[0079] The basic principles of this application have been described above with reference to specific embodiments. However, it should be noted that the advantages, benefits, and effects mentioned in this application are merely examples and not limitations, and should not be considered as essential features of each embodiment of this application. Furthermore, the specific details disclosed above are for illustrative and facilitative purposes only, and are not limitations. These details do not limit the application to the necessity of employing the aforementioned specific details for implementation.

[0080] The block diagrams of devices, apparatuses, devices, and systems involved in this application are merely illustrative examples and are not intended to require or imply that they must be connected, arranged, or configured in the manner shown in the block diagrams. As those skilled in the art will recognize, these devices, apparatuses, devices, and systems can be connected, arranged, and configured in any manner. Words such as “comprising,” “including,” “having,” etc., are open-ended terms meaning “including but not limited to,” and are used interchangeably with them. The terms “or” and “and” as used herein refer to the terms “and / or,” and are used interchangeably with them unless the context clearly indicates otherwise. The term “such as” as used herein refers to the phrase “such as but not limited to,” and is used interchangeably with it.

[0081] It should also be noted that in the apparatus, equipment, and methods of this application, the components or steps can be disassembled and / or recombined. These disassemblies and / or recombinations should be considered as equivalent solutions of this application.

[0082] The above description of the disclosed aspects is provided to enable any person skilled in the art to make or use this application. Various modifications to these aspects will be readily apparent to those skilled in the art, and the general principles defined herein can be applied to other aspects without departing from the scope of this application. Therefore, this application is not intended to be limited to the aspects shown herein, but rather to be accorded the widest scope consistent with the principles and novel features disclosed herein.

[0083] The above description has been given for purposes of illustration and description. Furthermore, this description is not intended to limit the embodiments of this application to the forms disclosed herein. Although numerous exemplary aspects and embodiments have been discussed above, those skilled in the art will recognize certain variations, modifications, alterations, additions, and sub-combinations thereof.

[0084] In the description of this specification, references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the present invention. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of those different embodiments or examples.

[0085] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this invention, "a plurality of" means two or more, unless otherwise explicitly specified.

[0086] The above description is merely a specific embodiment of the present invention, but the scope of protection of the present invention is not limited thereto. Any variations or substitutions that can be easily conceived by those skilled in the art within the technical scope disclosed in the present invention should be included within the scope of protection of the present invention. Therefore, the scope of protection of the present invention should be determined by the scope of the claims.

Claims

1. A control system for the generation of thiosulfate from sulfides, characterized in that, The system includes: A microchannel reactor is used to perform operations on the internal airflow and sulfide waste alkaline solution in accordance with the preset requirements when the reaction conditions meet the preset requirements, and to transport the generated reaction products to a gas-liquid separation unit. The gas-liquid separation unit is connected to the microchannel reactor via a pipeline and is used to separate the reaction products into gas and liquid. Based on the triggering of different reaction conditions, it controls the circulating pump to deliver sulfide waste alkaline solution and / or separation liquid to the microchannel reactor. The gas-liquid separation unit includes a gas-liquid separator; The output end of the gas-liquid separator is connected to the input end of the circulating pump, and the output end of the circulating pump is connected to the input end of the microchannel reactor. The gas-liquid separator is used to transport sulfide waste alkaline solution to the microchannel reactor by a circulating pump at a second preset flow rate after the air in the system has been replaced by nitrogen, and to end the transport operation when the system temperature is determined to reach the preset reaction temperature. The gas-liquid separator is also used to deliver sulfide waste alkali liquid and separation liquid to the microchannel reactor through the circulating pump at a second preset flow rate when the system pressure reaches the preset reaction pressure and the air flow rate reaches the first preset flow rate.

2. The system according to claim 1, characterized in that, Also includes: Analysis unit; The analysis unit is connected to the gas-liquid separation unit via a pipeline. It is used to collect the separated liquid from the output end of the gas-liquid separation unit based on a preset detection time, and to analyze the concentration of sulfide and thiosulfate in the separated liquid to generate analysis results.

3. The system according to claim 1, characterized in that, Also includes: The first delivery unit is connected to the microchannel reactor via a pipeline; Nitrogen is delivered to the microchannel reactor to replace the air inside the system according to a preset number of times, triggered by the volume of sulfide waste alkali liquid in the gas-liquid separation unit; and compressed air is delivered to the microchannel reactor according to a first preset flow rate, triggered by a preset reaction temperature.

4. The system according to claim 1, characterized in that, The gas-liquid separation unit also includes a constant temperature water bath; The gas-liquid separator is equipped with a jacket, and the jacket contains circulating hot water. The constant temperature water tank is connected to the jacket via a pipeline to heat the circulating hot water, and the heated circulating hot water is delivered to the jacket via a hot water circulation pump to control the system temperature to be maintained at a preset reaction temperature.

5. The system according to claim 1, characterized in that, The gas-liquid separator is equipped with a level gauge and a drain valve; the level gauge is used to adjust the volume of the separated liquid retained in the gas-liquid separator; the drain valve is used to discharge the excess separated liquid in the gas-liquid separator according to a third preset flow rate, so that the liquid level in the level gauge remains constant. The gas-liquid separator is also equipped with a back pressure valve; the back pressure valve is used to output the separated gas after separation by the gas-liquid separator and adjust the pressure of the system to the preset reaction pressure.

6. The system according to claim 1, characterized in that, The microchannel reactor is used to perform an oxidation reaction on the internal airflow and sulfide waste alkaline solution when the reaction conditions reach the first preset condition; and to stop the reaction on the internal airflow and sulfide waste alkaline solution when the reaction time reaches the preset reaction time.

7. The system according to claim 1, characterized in that, The first delivery unit includes a pneumatic pump and a flow meter. The pneumatic pump is connected to the microchannel reactor via a pipeline. The pneumatic pump is used to compress the collected air into an airflow and deliver it to the microchannel reactor. The flow meter is installed on the input pipeline of the microchannel reactor and is used to control the airflow output by the pneumatic pump to be delivered to the microchannel reactor according to a first preset flow rate.

8. A control method applied to the control system as described in any one of claims 1-7, characterized in that, The control method includes: When the system temperature is detected to have reached the preset reaction temperature, the control delivery unit delivers compressed air to the microchannel reactor according to the first preset flow rate; and controls the back pressure valve to adjust the system pressure to the preset reaction pressure; and generates the first trigger command. Based on the first trigger command, the gas-liquid conveying unit is controlled to deliver the sulfide waste alkaline solution to the microchannel reaction unit according to the second preset flow rate; and the reaction time in the microchannel reactor is detected. When the monitoring result indicates that the reaction time has reached the preset reaction time, the microchannel reactor is controlled to end the reaction operation.

9. A computer-readable medium having a computer program stored thereon, the program being executed by a processor to implement the control method as described in claim 8.

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