Short-process energy-saving system for producing calcium oxide from carbide slag and control method of short-process energy-saving system

Abstract

The invention discloses a short-process energy-saving system for producing calcium oxide from carbide slag and a control method thereof, and the system comprises a feeding unit used for quantitatively injecting a preset mass of carbide slag raw material and carrying out iron and silicon removal operation on the carbide slag raw material to obtain primarily screened carbide slag; the drying unit is connected with the outlet end of the feeding unit and used for drying the primarily screened carbide slag to obtain dried carbide slag; the flow mixer is connected with the outlet end of the drying unit and used for mixing the dried carbide slag with the first waste heat output airflow to form first mixed flow carbide slag; a material inlet of the calcining unit is connected with the flow mixer, and the calcining unit is used for receiving the second waste heat output airflow, mixing the first mixed flow carbide slag with the second waste heat airflow, and carrying out calcining and heat preservation operation to generate a first calcium oxide finished product; the input end of the waste heat recovery unit is connected with the hot airflow output end of the calcining unit, the first output end is connected with the flow mixer to provide first waste heat output airflow, and the second output end is connected with the air inlet of the calcining unit to provide second waste heat output airflow.

Description

Technical Field

[0001] The present invention relates to the field of solid waste resource recycling and circular economy production. More specifically, the present application relates to a short-process energy-saving system for producing calcium oxide from carbide slag and a control method thereof. Background Art

[0002] Carbide slag is the waste residue produced by the hydrolysis of calcium carbide during the production process of calcium carbide PVC industry. The national calcium carbide PVC industry produces about 35 million tons of carbide slag every year. The main component of carbide slag is calcium hydroxide, accounting for about 90% of its mass fraction, and the rest is oxides or compounds such as silicon, aluminum, iron, and magnesium. These impurities reduce the activity of carbide slag and make it difficult to use.

[0003] At present, the main use of carbide slag is cement production, with about 12 million tons of carbide slag used for this purpose each year, accounting for about 40% of the total production. Carbide slag is also used for desulfurization and other acidic water and gas neutralization, but due to its poor activity, it is difficult to promote its use in these fields. More than 10 million tons of carbide slag are stored each year, causing environmental pollution and waste of resources.

[0004] On the other hand, the calcium carbide PVC industry requires a large amount of calcium oxide, which is usually produced by limestone mining. Therefore, the recycling of calcium resources from calcium carbide slag in this industry not only meets the requirements of green and low-carbon development, but also reduces carbon dioxide emissions. The production of each ton of calcium oxide can reduce 0.78 tons of carbon dioxide emissions.

[0005] The particle size distribution of carbide slag powder is wide, and the calcination temperature and time are difficult to control, resulting in poor product quality stability; the high-temperature viscosity of calcium-based materials increases, which makes the suspension preheater link easy to hang, block and sinter; the fluidized calcination time is short and requires higher temperature, resulting in high energy consumption and difficulty in utilizing flue gas waste heat; the material is unevenly dispersed in the calcining furnace, resulting in sedimentation and accumulation problems.

[0006] Currently, the production of calcium oxide from carbide slag faces a situation where the process is simple but the technical challenges are relatively large. The problems that need to be solved mainly focus on powder material handling, calcination temperature control, system energy consumption optimization and anti-clogging. Summary of the invention

[0007] A series of simplified concepts are introduced in the Summary of the Invention section, which will be further described in detail in the Detailed Description of the Invention section. The Summary of the Invention section of this application does not mean to attempt to define the key features and essential technical features of the claimed technical solution, nor does it mean to attempt to determine the scope of protection of the claimed technical solution.

[0008] In the first aspect, the present application proposes a short-process energy-saving system for producing calcium oxide from carbide slag, the system comprising: A feeding unit is used to quantitatively inject a preset mass of carbide slag raw material, and remove iron and silicon from the preset mass of carbide slag to obtain primary screening carbide slag; A drying unit, wherein the material inlet of the drying unit is connected to the outlet of the feeding unit, and the drying unit is used to dry the pre-screened carbide slag to obtain dried carbide slag; A mixer, wherein the material inlet of the mixer is connected to the outlet of the drying unit, and the mixer is used to mix the dried carbide slag and the first waste heat output airflow to obtain a first mixed-flow carbide slag; A calcining unit, wherein the feed inlet of the calcining unit is connected to the discharge outlet of the mixer, the air inlet of the calcining unit is used to receive a second waste heat output airflow, the second waste heat output airflow is used to form a second mixed flow carbide slag with the first mixed flow carbide slag, and the calcining unit is used to perform calcination and heat preservation operations on the second mixed flow carbide slag to obtain a first finished calcium oxide product; A waste heat recovery unit, wherein the input end of the waste heat recovery unit is connected to the hot air flow output end of the calcining unit, the first output end of the waste heat recovery unit is connected to the mixer, the first output end of the waste heat recovery unit is used to provide the first waste heat output air flow to the mixer, the second output end of the waste heat recovery unit is connected to the air inlet of the calcining unit, and the second output end of the waste heat recovery unit is used to pass the second waste heat output air flow to the calcining unit.

[0009] In a feasible embodiment, the above-mentioned loading unit includes a raw material intermediate bin, a quantitative belt and an iron and silicon removal device. The above-mentioned raw material intermediate bin, the above-mentioned quantitative belt and the above-mentioned iron and silicon removal device are arranged in sequence on the moving path of the calcium carbide slag raw material, and the discharge port of the above-mentioned iron and silicon removal device is arranged corresponding to the feed port of the above-mentioned drying unit.

[0010] In a feasible embodiment, the drying unit comprises a dryer, a drying cyclone separator, a first intermediate bin, a first rotary discharger, a first drying bag dust collector, a second intermediate bin and a second rotary discharger; The material inlet end of the dryer is arranged correspondingly to the material outlet end of the iron and silicon removal device; The outlet end of the dryer is connected to the inlet end of the drying cyclone separator; The outlet pipe of the above-mentioned drying cyclone separator is connected to the above-mentioned first drying bag dust collector; The flow pipe of the drying cyclone separator, the first intermediate bin and the first rotary discharger are connected in sequence; The flow pipe of the first dry bag dust collector, the second intermediate bin and the second rotary discharger are connected in sequence; The gas output end of the first dry bag filter is connected to the system induced draft fan.

[0011] In a feasible implementation manner, the calcining unit comprises a low-nitrogen burner, a hot blast furnace, a dynamic calcining device, a circulating constant temperature furnace and a third rotary discharger; The low nitrogen burner is connected to the first input port of the hot blast furnace, the second input port of the hot blast furnace receives the second waste heat output airflow, and the output port of the hot blast furnace is connected to the gas input port of the dynamic calcining device; The material input port of the dynamic calcining device is connected to the outlet end of the mixer, the outlet end of the dynamic calcining device is connected to the inlet end of the circulating constant temperature furnace, the material outlet end of the circulating constant temperature furnace is connected to the third rotary discharger, and the airflow outlet end of the circulating constant temperature furnace is connected to the waste heat recovery unit.

[0012] In a feasible implementation manner, the waste heat recovery unit comprises a waste heat distributor, a blower, a second bag filter and an internal circulation fan; The airflow outlet end of the above-mentioned circulating constant temperature furnace is connected to the tube side inlet of the above-mentioned waste heat distributor, the output end of the above-mentioned blower is connected to the shell side inlet of the above-mentioned waste heat distributor, the shell side first outlet of the above-mentioned waste heat distributor is connected to the above-mentioned mixer, the shell side second outlet of the above-mentioned waste heat distributor is connected to the input end of the above-mentioned hot air furnace, and the tube side outlet of the above-mentioned waste heat distributor is connected to the above-mentioned second bag dust collector; The airflow output end of the second bag filter, the internal circulation fan and the dryer are connected in sequence, the heat inlet of the dryer is connected to the outlet of the internal circulation fan, and the material output end of the second bag filter is used to output the second calcium oxide second finished product.

[0013] In a feasible embodiment, the temperature of the dryer is greater than or equal to 300 degrees Celsius and less than or equal to 500 degrees Celsius; and / or, The wind speed of the pipeline between the above-mentioned mixer and the above-mentioned dynamic calcining device is greater than or equal to 5 meters per second and less than or equal to 10 meters per second, and the temperature before the above-mentioned dynamic calcining device is greater than or equal to 200 degrees Celsius and less than or equal to 400 degrees Celsius.

[0014] In a feasible embodiment, the temperature in the dynamic calcining device is greater than or equal to 850 degrees Celsius and less than or equal to 1200 degrees Celsius, and the movement speed in the dynamic calcining device is greater than or equal to 7 meters per second and less than or equal to 20 meters per second; and / or, The temperature in the above-mentioned circulating constant temperature furnace is greater than or equal to 500 degrees Celsius and less than or equal to 850 degrees Celsius.

[0015] In a second aspect, the present application proposes a control method for the short-process energy-saving system for producing calcium oxide from carbide slag in the first aspect, comprising: Acquire production urgency information, current system status information and environmental information, wherein the current system status information includes temperature information, pressure information and equipment status information, and the environmental information includes external environment information and raw material supply information; The above-mentioned production urgency information, the above-mentioned current system status information and the above-mentioned environmental information are input into the production scheduling control model to obtain a quantitative belt control signal, a first rotary discharger control signal, a second rotary discharger control signal, a first proportional control valve opening signal and a second proportional control valve opening signal, wherein the first proportional control valve is used to control the above-mentioned first waste heat output airflow, and the second proportional control valve is used to control the above-mentioned second waste heat output airflow, and the above-mentioned production scheduling control model is a hybrid model based on the combination of neural network and fuzzy logic.

[0016] In a feasible implementation, the production scheduling control model includes an input layer, a processing layer and an output layer, the processing layer includes a multi-layer neural network module part and a fuzzy logic module, the multi-layer neural network module part includes a first hidden layer and a second hidden layer, and the fuzzy logic module is connected to the second hidden layer; The above production scheduling control model uses mean square error to determine the error between the predicted output and the actual control signal, and the above production scheduling control model is optimized using the Adam optimizer.

[0017] In a feasible implementation manner, the specific steps of determining the production urgency information include: The above production urgency information is determined based on the difference between the production plan and the actual progress, order delivery time, equipment status and maintenance, raw material supply, market demand fluctuations and their corresponding weight coefficients.

[0018] In summary, the present application scheme optimizes the treatment process of carbide slag, organically combines the units of feeding, drying, mixing, combustion and waste heat recovery, and constructs an efficient and energy-saving system. Compared with the traditional complex multi-stage preheating and calcination process, the simplified process can effectively reduce the energy consumption of the system and improve the overall energy efficiency. The system proposed in this application is designed with a waste heat recovery unit, which can efficiently recover the waste heat generated by the calcination unit and distribute it to the mixer and the calcination unit. By repeatedly utilizing the waste heat, energy loss is minimized, and the energy consumption of the system is further reduced. This design helps to solve the problem that the waste heat of flue gas is difficult to fully utilize in traditional processes. Through the design of the mixer, the carbide slag is fully mixed with the waste heat air flow, so that the temperature of the material entering the calcination unit is more uniform, and the suspension preheater that is prone to cause hanging, sintering, and blocking is removed, and the risk of system blocking is greatly reduced. Problems such as hanging and blocking caused by increased high-temperature viscosity are avoided. The optimized temperature and time control improves the stability of the calcination process, thereby improving the quality of calcium oxide products. Compared with the traditional fluidized calcination system, the calcination unit in the present application has been optimized to reduce problems such as uneven material dispersion and sedimentation, reduce the frequency of system blockage and shutdown, and improve the stability and operating efficiency of the system. In addition, the simplified process also reduces the complexity of system maintenance. By improving the calcination process, the present solution significantly improves the content and activity of calcium oxide produced, which can meet the needs of calcium carbide production and avoid the situation where downstream production is affected by substandard product quality.

[0019] The short-process energy-saving system for producing calcium oxide from carbide slag proposed in this application and other advantages, objectives and features of this application will be reflected in part through the following description, and will also be understood by technical personnel in this field through research and practice of this application. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] Various other advantages and benefits will become apparent to those of ordinary skill in the art by reading the detailed description of the preferred embodiments below. The accompanying drawings are only for the purpose of illustrating the preferred embodiments and are not to be considered as limiting the present specification. Also, the same reference symbols are used throughout the accompanying drawings to represent the same components. In the accompanying drawings: Figure 1 A structural schematic diagram of a short-process energy-saving system for producing calcium oxide from carbide slag provided in an embodiment of the present application; Figure 2 A structural schematic diagram of another short-process energy-saving system for producing calcium oxide from carbide slag provided in an embodiment of the present application; Figure 3 A schematic diagram of a control method process provided in an embodiment of the present application; Figure 1 and Figure 2The corresponding relationship between the reference numerals and the names of the drawings is as follows: 10 feeding unit, 20 drying unit, 30 mixer, 40 calcining unit, 50 waste heat recovery unit; 101 raw material intermediate warehouse, 102 quantitative belt, 103 iron and silicon removal device; 201 dryer, 202 drying cyclone separator, 203 first intermediate bin, 204 first rotary discharger, 205 first drying bag dust collector, 206 second intermediate bin, 207 second rotary discharger; 401 low nitrogen burner, 402 hot air furnace, 403 dynamic calcining device, 404 circulating constant temperature furnace, 405 third rotary discharger; 501 waste heat distributor, 502 blower, 503 second bag dust collector, 504 internal circulation fan; 60 system induced draft fan. DETAILED DESCRIPTION

[0021] The terms "first", "second", "third", "fourth", etc. (if any) in the specification and claims of this application and the above-mentioned drawings are used to distinguish similar objects, and are not necessarily used to describe a specific order or sequence. It should be understood that the data used in this way can be interchangeable where appropriate, so that the embodiments described herein can be implemented in an order other than that illustrated or described herein. In addition, the terms "including" and "having" and any of their variations are intended to cover non-exclusive inclusions. For example, a process, method, system, product or device that includes a series of steps or units is not necessarily limited to those steps or units that are clearly listed, but may include other steps or units that are not clearly listed or inherent to these processes, methods, products or devices. The technical solutions in the embodiments of the present application will be clearly and completely described below in conjunction with the drawings in the embodiments of the present application. Obviously, the described embodiments are only part of the embodiments of the present application, not all of the embodiments.

[0022] See also Figure 1 and Figure 2 , which is a structural schematic diagram of a short-process energy-saving system for producing calcium oxide from carbide slag provided in an embodiment of the present application, and may specifically include: A feeding unit is used to quantitatively inject a preset mass of carbide slag raw material, and remove iron and silicon from the preset mass of carbide slag to obtain primary screening carbide slag; A drying unit, wherein the material inlet of the drying unit is connected to the outlet of the feeding unit, and the drying unit is used to dry the pre-screened carbide slag to obtain dried carbide slag; A mixer, wherein the material inlet of the mixer is connected to the outlet of the drying unit, and the mixer is used to mix the dried carbide slag and the first waste heat output airflow to obtain a first mixed-flow carbide slag; A calcining unit, wherein the feed inlet of the calcining unit is connected to the discharge outlet of the mixer, the air inlet of the calcining unit is used to receive a second waste heat output airflow, the second waste heat output airflow is used to form a second mixed flow carbide slag with the first mixed flow carbide slag, and the calcining unit is used to perform calcination and heat preservation operations on the second mixed flow carbide slag to obtain a first finished calcium oxide product; A waste heat recovery unit, wherein the input end of the waste heat recovery unit is connected to the hot air flow output end of the calcining unit, the first output end of the waste heat recovery unit is connected to the mixer, the first output end of the waste heat recovery unit is used to provide the first waste heat output air flow to the mixer, the second output end of the waste heat recovery unit is connected to the air inlet of the calcining unit, and the second output end of the waste heat recovery unit is used to pass the second waste heat output air flow to the calcining unit.

[0023] Exemplarily, the feeding unit 10 is used to quantitatively inject carbide slag raw materials of a preset mass, and perform iron and silicon removal operations on the carbide slag raw materials to obtain pre-screened carbide slag. The outlet end of the feeding unit 10 is connected to the inlet end of the drying unit 20. The drying unit 20 is connected to the feeding unit 10, and is used to dry the pre-screened carbide slag to finally obtain dried carbide slag. The mixer 30 is used to mix the dried carbide slag from the drying unit 20 with the first waste heat output airflow from the waste heat recovery unit 50 to obtain a first mixed flow carbide slag. The outlet end of the mixer 30 is connected to the feed inlet of the calcining unit 40, and at the same time, the mixer 30 is connected to the first output end of the waste heat recovery unit 50 through a pipeline to obtain the first waste heat output airflow. The main task of the calcining unit 40 is to receive the first mixed-flow carbide slag output from the mixer 30 and the second waste heat output airflow from the waste heat recovery unit 50, and mix the two to form the second mixed-flow carbide slag, and then perform calcination operation and heat preservation operation in the calcining unit 40, so as to produce the first finished calcium oxide product. The feed port of the calcining unit 40 is connected to the discharge port of the mixer 30, and the air inlet is connected to the second output end of the waste heat recovery unit 50, which is used to receive the second waste heat output airflow. In addition, the hot airflow output end of the calcining unit 40 is connected to the input end of the waste heat recovery unit 50. The waste heat recovery unit 50 is used to recover the hot airflow from the calcining unit 40 and distribute it into two parts: the first part is supplied to the mixer 30 as the first waste heat output airflow; the second part is supplied to the calcining unit 40 as the second waste heat output airflow. The input end of the waste heat recovery unit 50 is connected to the hot air flow output end of the calcining unit 40, the first output end is connected to the mixer 30, for providing a first waste heat output air flow; the second output end is connected to the air inlet of the calcining unit 40, for providing a second waste heat output air flow.

[0024] In summary, the present application scheme optimizes the treatment process of carbide slag, organically combines the units of feeding, drying, mixing, combustion and waste heat recovery, and constructs an efficient and energy-saving system. Compared with the traditional complex multi-stage preheating and calcination process, the simplified process can effectively reduce the energy consumption of the system and improve the overall energy efficiency. The system proposed in this application is designed with a waste heat recovery unit, which can efficiently recover the waste heat generated by the calcination unit and distribute it to the mixer and the calcination unit. By repeatedly utilizing the waste heat, energy loss is minimized, and the energy consumption of the system is further reduced. This design helps to solve the problem that the waste heat of flue gas is difficult to fully utilize in traditional processes. Through the design of the mixer, the carbide slag is fully mixed with the waste heat air flow, so that the temperature of the material entering the calcination unit is more uniform, and the suspension preheater that is prone to hanging, sintering, and blocking is removed, and the risk of system blocking is greatly reduced, avoiding the problems of hanging and blocking caused by the increase of high-temperature viscosity. The optimized temperature and time control improves the stability of the calcination process, thereby improving the quality of the calcium oxide product. Compared with the traditional fluidized calcination system, the calcination unit in the present application has been optimized to reduce problems such as uneven material dispersion and sedimentation, reduce the frequency of system blockage and shutdown, and improve the stability and operating efficiency of the system. In addition, the simplified process also reduces the complexity of system maintenance. By improving the calcination process, the present solution significantly improves the content and activity of calcium oxide produced, which can meet the needs of calcium carbide production and avoid the situation where downstream production is affected by substandard product quality.

[0025] In some examples, the loading unit includes an intermediate bin for raw materials, a quantitative belt, and an iron and silicon removal device. The intermediate bin for raw materials, the quantitative belt, and the iron and silicon removal device are sequentially arranged on the moving path of the carbide slag raw materials, and the discharge port of the iron and silicon removal device is arranged correspondingly to the feed port of the drying unit.

[0026] Exemplarily, the feeding unit 10 includes a raw material intermediate bin 101, a quantitative belt 102 and an iron and silicon removal device 103. The raw material intermediate bin 101 is used to store carbide slag raw materials and serves as the starting point of the entire feeding process. The carbide slag raw materials enter the production process from the raw material intermediate bin 101. The carbide slag raw materials are transmitted from the raw material intermediate bin 101 through the quantitative belt 102. The function of the quantitative belt 102 is to transfer the carbide slag raw materials to the subsequent processing stage in a quantitative manner according to the preset production requirements to ensure that the quality of each batch of raw materials is consistent. After the carbide slag raw materials pass through the quantitative belt 102, they enter the iron and silicon removal device 103. The iron and silicon removal device 103 is responsible for removing iron and silicon impurities in the carbide slag raw materials to obtain high-purity primary screening carbide slag, laying the foundation for subsequent drying and calcination operations. The raw material intermediate bin 101, quantitative belt 102 and iron removal and silicon removal device 103 in the feeding unit 10 are sequentially arranged on the moving path of the carbide slag raw material to ensure that the raw material can continuously and smoothly pass through each processing link. The discharge port of the iron removal and silicon removal device 103 is arranged correspondingly to the feed port of the drying unit 20. After the iron removal and silicon removal operation is completed, the primary screened carbide slag directly enters the drying unit 20 for drying treatment. The drying unit 20 is used to dry the primary screened carbide slag from the iron removal and silicon removal device 103 to ensure that the carbide slag reaches the required moisture content when entering the subsequent processing stage. The feed port of the drying unit 20 is arranged correspondingly to the discharge port of the iron removal and silicon removal device 103 to ensure that the material can be dried immediately after the iron removal and silicon removal are completed. The raw material intermediate bin 101, quantitative belt 102 and iron and silicon removal device 103 in the feeding unit 10 are arranged in sequence on the moving path of the carbide slag raw material, ensuring an efficient and continuous operation process of the carbide slag from raw material storage to preliminary processing, and providing a reliable basis for the operation of the subsequent drying unit 20 and other processing units.

[0027] In summary, the raw material intermediate bin 101, the quantitative belt 102 and the iron and silicon removal device 103 in the feeding unit 10 are arranged in sequence on the moving path of the carbide slag raw material, ensuring an efficient and continuous operation process of the carbide slag from raw material storage to preliminary processing, and providing a reliable basis for the operation of the subsequent drying unit 20 and other processing units.

[0028] In some examples, the drying unit includes a dryer, a drying cyclone separator, a first intermediate bin, a first rotary discharger, a first drying bag filter, a second intermediate bin, and a second rotary discharger; The material inlet end of the dryer is arranged correspondingly to the material outlet end of the iron and silicon removal device; The outlet end of the dryer is connected to the inlet end of the drying cyclone separator; The outlet pipe of the above-mentioned drying cyclone separator is connected to the above-mentioned first drying bag dust collector; The flow pipe of the drying cyclone separator, the first intermediate bin and the first rotary discharger are connected in sequence; The flow pipe of the first dry bag dust collector, the second intermediate bin and the second rotary discharger are connected in sequence; The gas output end of the first dry bag filter is connected to the system induced draft fan.

[0029] Exemplarily, the dryer 201 is used to dry the pre-screened carbide slag entering from the iron and silicon removal device 103 of the loading unit 10. The dryer 201 ensures that the carbide slag has a suitable moisture content when entering the subsequent processing stage. The material inlet end of the dryer 201 is correspondingly arranged with the discharge end of the iron and silicon removal device 103, ensuring that the pre-screened carbide slag can smoothly enter the dryer 201 for drying after completing the iron and silicon removal operation.

[0030] The drying cyclone separator 202 is used to separate the dried carbide slag from the gas generated during the drying process. Through the rotating airflow, the drying cyclone separator 202 can effectively separate the fine particles in the dried carbide slag and send them to the subsequent processing unit. The outlet end of the dryer 201 is connected to the inlet end of the drying cyclone separator 202 to ensure that the material directly enters the drying cyclone separator 202 for separation operation after drying.

[0031] The first intermediate bin 203 is used to temporarily store the carbide slag separated from the drying cyclone separator 202, ensuring that the material can continue to be transported when needed. The first rotary discharger 204 is responsible for discharging the material stored in the first intermediate bin 203 to the next processing stage. The flow pipe of the drying cyclone separator 202, the first intermediate bin 203 and the first rotary discharger 204 are connected in sequence to ensure that the material can smoothly enter the first intermediate bin 203 from the drying cyclone separator 202 and be discharged through the first rotary discharger 204.

[0032] The first dry bag dust collector 205 is used to collect fine dust particles in the gas discharged from the dry cyclone separator 202 to prevent these particles from entering the subsequent processing unit or being discharged into the environment. The outlet pipe of the dry cyclone separator 202 is connected to the first dry bag dust collector 205 to ensure that the discharged gas is dust-removed.

[0033] The second intermediate bin 206 is used to temporarily store the materials processed by the first dry bag dust collector 205, and the second rotary discharger 207 is responsible for discharging these materials to the subsequent processing stage. The flow pipe of the first dry bag dust collector 205, the second intermediate bin 206 and the second rotary discharger 207 are connected in sequence to ensure that the processed materials can be smoothly transferred to the next stage.

[0034] The gas output end of the first drying bag filter 205 is connected to the system induced draft fan 60 to ensure that the gas generated during the drying process can be discharged smoothly.

[0035] The various components in the drying unit 20, including the dryer 201, the drying cyclone separator 202, the first intermediate bin 203, the first rotary discharger 204, the first drying bag dust collector 205, the second intermediate bin 206 and the second rotary discharger 207, work closely together to ensure that the calcium carbide slag can smoothly enter the next processing stage after drying, separation and dust removal, and effectively control gas emissions and material transmission in the production process.

[0036] In some examples, the calcining unit includes a low nitrogen burner, a hot air furnace, a dynamic calcining device, a circulating constant temperature furnace, and a third rotary discharger; The low nitrogen burner is connected to the first input port of the hot blast furnace, the second input port of the hot blast furnace receives the second waste heat output airflow, and the output port of the hot blast furnace is connected to the gas input port of the dynamic calcining device; The material input port of the dynamic calcining device is connected to the outlet end of the mixer, the outlet end of the dynamic calcining device is connected to the inlet end of the circulating constant temperature furnace, the material outlet end of the circulating constant temperature furnace is connected to the third rotary discharger, and the airflow outlet end of the circulating constant temperature furnace is connected to the waste heat recovery unit.

[0037] Exemplarily, the calcining unit 40 includes a low-nitrogen burner 401, a hot blast furnace 402, a dynamic calcining device 403, a circulating constant temperature furnace 404 and a third rotary discharger 405. The low-nitrogen burner 401 is used to provide a preliminary combustion heat source, reduce the emission of ammonia, and ensure that the combustion process is environmentally friendly and efficient. It provides the required heat for the hot blast furnace 402. The low-nitrogen burner 401 is connected to the first input port of the hot blast furnace 402 to ensure that the heat generated by the low-nitrogen burner 401 can be directly transported to the hot blast furnace 402.

[0038] The hot blast furnace 402 heats the gas entering the calcining unit by receiving heat from the low nitrogen burner 401 and the second waste heat output gas flow. The function of the hot blast furnace 402 is to heat these gases to the required temperature and provide sufficient thermal energy support for the subsequent dynamic calcining process. The first input port of the hot blast furnace 402 is connected to the low nitrogen burner 401, and the second input port receives the second waste heat output gas flow from the waste heat recovery unit 50. The output port of the hot blast furnace 402 is connected to the gas input port of the dynamic calcining device 403.

[0039] The dynamic calcining device 403 is the core part of the calcining unit 40, which is responsible for fully mixing the first mixed flow carbide slag from the mixer 30 with the heating gas from the hot blast furnace 402, and completing the calcination and preliminary decomposition process of the carbide slag under high temperature conditions. The material input port of the dynamic calcining device 403 is connected to the outlet end of the mixer 30 to ensure that the dried carbide slag can directly enter the dynamic calcining device 403 for calcination after mixing with the first waste heat output airflow. The outlet end of the dynamic calcining device 403 is connected to the inlet end of the circulating constant temperature furnace 404 to ensure that the calcined carbide slag can enter the next stage for insulation treatment.

[0040] The circulating constant temperature furnace 404 is used to perform heat preservation treatment on the calcium carbide slag treated by the dynamic calcining device 403, ensuring that the material continues to maintain a high temperature state after calcination to complete the final decomposition reaction, thereby obtaining high-quality calcium oxide products. The inlet end of the circulating constant temperature furnace 404 is connected to the outlet end of the dynamic calcining device 403, and the material outlet end is connected to the third rotary discharger 405 to ensure that the treated calcium oxide can be discharged smoothly. The airflow outlet end of the circulating constant temperature furnace 404 is connected to the waste heat recovery unit 50 to ensure that the waste gas can be recycled.

[0041] The third rotary discharger 405 is responsible for discharging the finished calcium oxide processed by the circulating constant temperature furnace 404 to the subsequent processing or storage stage. It ensures the continuity and stability of the material and prevents material accumulation in the production line. The third rotary discharger 405 is connected to the material outlet of the circulating constant temperature furnace 404 to ensure that the finished calcium oxide can be discharged smoothly from the circulating constant temperature furnace 404. The calcium oxide discharged by the third rotary discharger 405 can be cooled by a cooling device.

[0042] The various components of the calcining unit 40, including the low-nitrogen burner 401, the hot blast furnace 402, the dynamic calcining device 403, the circulating constant temperature furnace 404 and the third rotary discharger 405, work closely together to ensure that the carbide slag can be efficiently converted into the finished calcium oxide product during the combustion and heat preservation process, while making full use of the waste heat resources and optimizing energy efficiency. The high-temperature hot air from the hot blast furnace and the carbide slag from the mixer are mixed again and calcined in the calcining unit. The calcining unit mainly heat exchanges the carbide slag with the high-temperature hot air from the hot blast furnace and completes the decomposition of the carbide slag to obtain the finished calcium oxide product.

[0043] In some examples, the waste heat recovery unit includes a waste heat distributor, a blower, a second bag filter and an internal circulation fan; The airflow outlet end of the above-mentioned circulating constant temperature furnace is connected to the tube side inlet of the above-mentioned waste heat distributor, the output end of the above-mentioned blower is connected to the shell side inlet of the above-mentioned waste heat distributor, the shell side first outlet of the above-mentioned waste heat distributor is connected to the above-mentioned mixer, the shell side second outlet of the above-mentioned waste heat distributor is connected to the input end of the above-mentioned hot air furnace, and the tube side outlet of the above-mentioned waste heat distributor is connected to the above-mentioned second bag dust collector; The airflow output end of the second bag filter, the internal circulation fan and the dryer are connected in sequence, the heat inlet of the dryer is connected to the outlet of the internal circulation fan, and the material output end of the second bag filter is used to output the second calcium oxide second finished product.

[0044] Exemplarily, the waste heat recovery unit 50 includes a waste heat distributor 501, a blower 502, a second bag filter 503 and an internal circulation fan 504. The waste heat distributor 501 is used to receive and distribute the hot flue gas from the circulating constant temperature furnace 404 and the air flow of the blower 502. It distributes the system waste heat to the mixer 30, the hot air furnace 402 and the second bag filter 503 in the drying unit to achieve effective utilization of the waste heat.

[0045] The tube side inlet of the waste heat distributor 501 is connected to the air flow outlet end of the circulating constant temperature furnace 404 to receive the hot air flow discharged by the circulating constant temperature furnace 404. The shell side inlet of the waste heat distributor 501 is connected to the output end of the blower 502. The first shell side outlet of the waste heat distributor 501 is connected to the mixer 30 to provide the first waste heat output air flow; the second shell side outlet is connected to the hot air furnace 402 to provide the second waste heat output air flow; the tube side output end of the mixer is connected to the second bag filter 503 to ensure that the finished calcium oxide in the flue gas is further recovered.

[0046] The blower 502 is connected to the tube side inlet of the waste heat distributor 501. The blower 502 is used to provide natural wind to the waste heat distributor 501, displacing the waste heat of the hot flue gas in the tube side and transporting it to various units that need waste heat, such as the mixer 30 and the hot blast furnace 402. The output end of the blower 502 is connected to the shell side inlet of the waste heat distributor 501, which improves the kinetic energy of the shell side airflow entering the waste heat distributor 501.

[0047] The second bag filter 503 is used to purify the gas discharged from the waste heat distributor 501, recover the remaining calcium oxide product therein, and ensure that the calcined calcium oxide is completely recovered and does not enter the drying system. The pipe side outlet of the waste heat distributor 501 is connected to the second bag filter 503 to ensure that the pipe side flue gas enters the second bag filter 503 for purification. The airflow output end of the second bag filter 503 is connected to the internal circulation fan 504 to further promote the airflow circulation.

[0048] The internal circulation fan 504 is used to introduce the airflow purified by the second bag filter 503 into the interior of the drying unit 20, especially the dryer 201, to further utilize the waste heat resources of the flue gas. The outlet end of the internal circulation fan 504 is connected to the dryer 201 to ensure that the purified airflow can enter the dryer 201 for reuse.

[0049] The various components of the waste heat recovery unit 50, including the waste heat distributor 501, the blower 502, the second bag filter 503 and the internal circulation fan 504, work closely together to ensure that the waste heat from the circulating constant temperature furnace 404 is fully utilized. After the airflow is processed at multiple stages, the waste heat is efficiently recovered and used in other parts of the system, ultimately improving the energy efficiency and environmental performance of the entire system. At the same time, the second bag filter 503 further recovers the calcium oxide in the calcination flue gas to form a second calcium oxide product, further optimizing resource utilization, and recovering a higher calcium oxide product than the equivalent traditional dynamic calcination furnace. The waste heat distributor 501 is a multi-module shell-and-tube gas-to-gas heat exchanger, the input end of its tube path is connected to the flue gas output end of the calcination unit, the shell input end of the waste heat distributor is connected to the blower, and the first shell output end is connected to the mixer.

[0050] In some examples, the temperature of the dryer is greater than or equal to 300 degrees Celsius and less than or equal to 500 degrees Celsius; and / or, The wind speed of the pipeline between the above-mentioned mixer and the above-mentioned dynamic calcining device is greater than or equal to 5 meters per second and less than or equal to 10 meters per second, and the temperature before the above-mentioned dynamic calcining device is greater than or equal to 200 degrees Celsius and less than or equal to 400 degrees Celsius.

[0051] Exemplarily, the dryer 201 may be a drying machine, a flash dryer, a tubular dryer, or the like.

[0052] The temperature of the dryer 201 is between 300°C and 500°C, and the carbide slag coming out of the dryer has a moisture content of less than 1% and a temperature between 150°C and 200°C.

[0053] In the dryer 201, the drying process of carbide slag needs to be carried out at a relatively high temperature to effectively remove moisture from the material. Setting the temperature between 300 degrees Celsius and 500 degrees Celsius can ensure that the carbide slag reaches an ideal moisture content during the drying process, while avoiding thermal decomposition of the material or overheating damage to the dryer 201 due to excessive temperature.

[0054] The wind speed of the pipeline between the mixer 30 and the dynamic calcining device 403 should be controlled within a range of greater than or equal to 5 meters per second and less than or equal to 10 meters per second. The transmission speed of the material and the airflow between the mixer 30 and the dynamic calcining device 403 is crucial. Controlling the wind speed of the pipeline between 5 meters per second and 10 meters per second can ensure the stable transportation of the material in the pipeline, which can not only avoid the retention of the material in the pipeline, but also prevent the wind speed from being too high, resulting in unstable material flow or increased equipment wear.

[0055] The temperature before the dynamic calcination device 403 should be controlled within a range of greater than or equal to 200 degrees Celsius and less than or equal to 400 degrees Celsius. Before the dynamic calcination device 403 performs the calcination operation, the temperature of the material and the airflow needs to be preheated to a certain degree. Controlling the temperature between 200 degrees Celsius and 400 degrees Celsius can ensure that the material has appropriate preheating conditions when entering the dynamic calcination device 403, thereby ensuring the sufficiency and stability of the calcination process, while avoiding over-burning or under-burning due to excessively high or low temperatures.

[0056] In some examples, the temperature in the dynamic calcining device is greater than or equal to 850 degrees Celsius and less than or equal to 1200 degrees Celsius, and the movement speed in the dynamic calcining device is greater than or equal to 7 meters per second and less than or equal to 20 meters per second; and / or, The temperature in the above-mentioned circulating constant temperature furnace is greater than or equal to 500 degrees Celsius and less than or equal to 850 degrees Celsius.

[0057] Exemplarily, the carbide slag sent into the calcining furnace by the mixer 30 is mixed with the rising high-temperature flue gas (1200°C-850°C) in the calcining furnace, and is quickly heated to 1200°C-850°C. The carbide slag moves to the outlet of the dynamic calcining device 403 with the flue gas of the calcining furnace, and the movement speed is 7m / s-20s / s. It comes out of the dynamic calcining device 403 in 3S to 10S, and enters the circulating constant temperature furnace 404 through the connecting pipe to continue calcining. The circulating constant temperature furnace 404 is provided with a multi-tube cyclone separator, which separates most of the calcined calcium oxide and sends it to the circulating constant temperature furnace insulation bin. The temperature of the constant temperature furnace insulation bin is 500°C-850°C. The time of the material in the insulation bin is adjusted according to the decomposition rate of the discharged carbide slag and the calcium oxide content of the product. The time can be set to 10s-30min. The calcium oxide that is not recovered by the multi-cyclone is completely recovered along the multi-cyclone outlet connecting pipe along with the flue gas to the waste heat distributor 501 and then to the second bag dust collector 504.

[0058] It should be noted that the hot air flow process of the system is as follows: the low nitrogen burner 401 (multiple fuels) burns to generate heat, and the heat enters the hot blast furnace 402. The heat in the hot blast furnace 402 is mixed with the secondary air from the waste heat distributor 501 to generate high-temperature flue gas. The high-temperature flue gas has a temperature of 900-1250 degrees Celsius and enters the cyclone dynamic calcining device 403 through the outlet pipe of the hot blast furnace 402. The high-temperature flue gas is mixed with the carbide slag sent from the mixer 30 in the cyclone dynamic calcining device 403, and the flue gas carries the carbide slag to the outlet of the calcining device.

[0059] The flue gas with materials coming out of the dynamic calcining device 403 enters the circulating constant temperature furnace 404 through the outlet pipe of the calcining furnace. After the materials and flue gas are processed in the circulating constant temperature furnace 404, most of the calcium oxide materials are separated from the flue gas by a multi-tube cyclone separator arranged in the circulating constant temperature furnace, and the flue gas is sent to the waste heat distributor 501 through the pipe at the outlet of the multi-tube cyclone separator.

[0060] The waste heat distributor 501 is a multi-module gas-to-gas heat exchanger that converts part of the exhaust gas heat into hot air. A portion of the hot air is sent to the mixer 30 through a pipeline, and the other portion of the hot air is used as the secondary air of the hot air furnace 402 through a pipeline to enter the hot air furnace 402. The flue gas temperature passing through the waste heat distributor 501 is controlled within the heat range suitable for drying, and is sent to the second bag filter 503 through the outlet pipeline of the waste heat distributor 501.

[0061] The second bag filter 503 recovers the residual calcium oxide in the flue gas, and then the flue gas is sent to the dryer 201 through the pipeline by the internal circulation fan 504. The flue gas temperature from the dryer 201 is about 150 degrees Celsius. The flue gas after passing through the dryer 201 enters the dry cyclone separator 202 and the first dry bag filter 205 through the pipeline. After all the dry carbide slag is recovered, the flue gas is sent to the chimney through the pipeline by the system induced draft fan 60 for discharge.

[0062] In a second aspect, the present application proposes a control method for the short-process energy-saving system for producing calcium oxide from carbide slag in the first aspect, comprising: S110, obtaining production urgency information, current system status information and environmental information, wherein the current system status information includes temperature information, pressure information and equipment status information, and the environmental information includes external environment information and raw material supply information; Exemplarily, the production urgency information is used to indicate the priority and urgency of the current production task and to guide the emergency response of production scheduling.

[0063] The current system status information includes temperature information, pressure information, and device status information.

[0064] Temperature information involves the temperature parameters of key equipment and materials in the system, which is used to ensure that the production process is carried out within an appropriate temperature range.

[0065] Pressure information refers to the pressure status in production equipment and is used to monitor and control production safety and efficiency.

[0066] Equipment status information includes the equipment's operating status, fault conditions, and maintenance requirements, ensuring that system equipment operates in the best condition.

[0067] Environmental information includes external environmental information and raw material supply information. External environmental information indicates external environmental conditions such as temperature, humidity, and air pressure, which may affect parameter adjustment during the production process. Raw material supply information includes raw material inventory, supply chain stability, etc., to ensure that raw materials are sufficient and supplied smoothly during the production process.

[0068] S120. Input the above-mentioned production urgency information, the above-mentioned current system status information and the above-mentioned environmental information into the production scheduling control model to obtain a quantitative belt control signal, a first rotary discharger control signal, a second rotary discharger control signal, a first proportional control valve opening signal and a second proportional control valve opening signal, wherein the first proportional control valve is used to control the above-mentioned first waste heat output airflow, and the second proportional control valve is used to control the above-mentioned second waste heat output airflow, and the above-mentioned production scheduling control model is a hybrid model based on the combination of neural network and fuzzy logic.

[0069] Exemplarily, the production scheduling control model is based on a hybrid model combining neural network and fuzzy logic. Neural network is used to process complex nonlinear relationships, and fuzzy logic is used to process uncertainty and ambiguity in information. After receiving input information, the model generates the following control signals: Quantitative belt control signal: used to adjust the conveying speed of raw materials to ensure a stable supply of raw materials according to production needs.

[0070] The first rotary discharger control signal is used to control the discharge rate of materials from the first intermediate bin 203 to ensure the continuity and stability of material processing.

[0071] The second rotary discharger control signal is used to control the discharge rate of the material from the second intermediate bin 206 and coordinate the material flow in the subsequent processing stage.

[0072] The first proportional regulating valve opening signal is used to control the flow rate of the first waste heat output airflow to ensure that the preheating process in the mixer 30 is carried out efficiently.

[0073] The second proportional regulating valve opening signal is used to control the flow rate of the second waste heat output airflow to ensure that the heat supply of the hot blast furnace 402 and the dynamic calcining device 403 meets the production requirements.

[0074] In summary, the embodiment of the present application obtains production urgency information, current system status information and environmental information, and inputs this information into the production scheduling control model, so that the system can adjust the production parameters in real time to ensure that the raw material transportation, material handling and heat management in the production process are optimally configured, thereby improving the overall production efficiency. The production scheduling control model combines neural network and fuzzy logic technology, and can handle complex nonlinear relationships and uncertainty information, so that the system can quickly respond to changes in the production environment, such as the urgency of production tasks, equipment status changes and raw material supply fluctuations, to ensure the continuity and stability of the production process. By accurately controlling the operation of quantitative belts, rotary unloaders and proportional control valves, this solution can optimize the utilization of raw materials, energy and equipment and reduce unnecessary waste. For example, by controlling the flow rate of waste heat output airflow, the waste heat resources in the system are fully utilized to reduce energy consumption. By monitoring temperature information, pressure information and equipment status information, the production scheduling control model can prevent and promptly deal with potential safety hazards, ensure that production equipment operates in the best state, and reduce the incidence of failures and accidents. This solution takes into account external environmental information (such as temperature, humidity, air pressure) and raw material supply information. By dynamically adjusting production parameters, the system can maintain a stable production state under different environmental conditions to ensure the consistency of product quality. The production scheduling control model in this solution can flexibly adjust the production strategy according to the production urgency information, so that the system can quickly switch when facing a variety of production tasks to meet the needs of different production goals. Through the effective recovery and utilization of waste heat and the optimization and control of various production parameters, the system can significantly reduce energy consumption and emissions, meet the requirements of energy conservation and emission reduction, and improve environmental protection benefits.

[0075] In some examples, the production scheduling control model includes an input layer, a processing layer and an output layer, the processing layer includes a multi-layer neural network module part and a fuzzy logic module, the multi-layer neural network module part includes a first hidden layer and a second hidden layer, and the fuzzy logic module is connected to the second hidden layer; The above production scheduling control model uses mean square error to determine the error between the predicted output and the actual control signal, and the above production scheduling control model is optimized using the Adam optimizer.

[0076] Exemplarily, the production scheduling control model is divided into three main parts: an input layer, a processing layer, and an output layer.

[0077] The input layer is responsible for receiving various key information in the production process, including production urgency information, current system status information (such as temperature information, pressure information, equipment status information) and environmental information (such as external environment information, raw material supply information).

[0078] The input data of the input layer directly affects the processing results of the model and is the basis for the model to make scheduling decisions.

[0079] The processing layer is the core part of the model, which consists of a multi-layer neural network module and a fuzzy logic module.

[0080] The first hidden layer is used to perform preliminary feature extraction and processing on the data received by the input layer. It identifies key patterns that affect production scheduling by modeling the complex nonlinear relationships of the input data. The first hidden layer consists of several neurons, each of which uses an activation function to process input information, usually using the ReLU activation function to improve the training efficiency and performance of the model.

[0081] The second hidden layer further extracts and processes the feature information passed from the first hidden layer. Through multi-level processing, the second hidden layer can capture deeper features, allowing the model to have a more comprehensive understanding of complex production scheduling problems. The structure of the second hidden layer is similar to that of the first hidden layer, and is also composed of several neurons, continuing to use the ReLU activation function for information processing.

[0082] The fuzzy logic module is connected after the second hidden layer and is specifically used to process production information with uncertainty or ambiguity. It can generate reasonable scheduling strategies based on fuzzy rules in production (such as "if the production urgency is high and the equipment status is unstable, the production rate should be reduced").

[0083] The operation process of the fuzzy logic module includes: Fuzzification: Convert the precise numerical information transmitted by the neural network into a fuzzy set.

[0084] Rule reasoning: Reasoning based on the preset fuzzy logic rule base to generate fuzzy output.

[0085] Defuzzification: Convert the fuzzy output into an accurate control signal value and pass it to the output layer.

[0086] The output layer receives the final processing results of the processing layer and generates specific control signals. These control signals include: Quantitative belt control signal: adjust the conveying speed of raw materials.

[0087] First rotary discharger control signal: controls the discharge rate of materials from the first intermediate bin 203 .

[0088] Second rotary discharger control signal: controls the discharge rate of materials from the second intermediate bin 206 .

[0089] The first proportional regulating valve opening signal controls the flow rate of the first waste heat output airflow.

[0090] The second proportional control valve opening signal: controls the flow rate of the second waste heat output airflow.

[0091] The production scheduling control model uses mean square error (MSE) to measure the difference between the predicted output and the actual control signal. Mean square error is a commonly used regression model loss function that evaluates the performance of the model by calculating the average of the squared difference between the predicted value and the actual value. The formula for MSE is: ; Among them, yi is the actual control signal, is the predicted output of the model and n is the total number of data points.

[0092] The model is optimized using the Adam optimizer. The Adam optimizer is an optimization algorithm widely used in deep learning. It has the ability to adjust the learning rate adaptively and dynamically adjust the learning rate during training to improve the convergence speed and model accuracy. The Adam optimizer combines the advantages of momentum and RMSProp to more effectively find the minimum value of the loss function during the gradient descent process.

[0093] In the embodiment of the present application, the processing layer combining neural network and fuzzy logic can quickly and efficiently process complex production scheduling information and generate accurate control signals. The fuzzy logic module processes the uncertainty in the information, making the model more robust when facing uncertain factors in actual production. Using mean square error as the error measurement standard and optimizing it through Adam optimizer, the model can converge quickly and accurately predict control signals. The model can flexibly adjust the production scheduling strategy according to different production information and adapt to the changing production environment.

[0094] In some examples, the specific steps of determining the production urgency information include: The above production urgency information is determined based on the difference between the production plan and the actual progress, order delivery time, equipment status and maintenance, raw material supply, market demand fluctuations and their corresponding weight coefficients.

[0095] For example, an important time indicator of urgency. If the order delivery time is approaching, it indicates that the production task is urgent and needs to be prioritized to ensure the production of these orders. Calculate the difference between the current time and the order delivery time, usually measured in days or hours.

[0096] Equipment status and maintenance directly affect production capacity. If key equipment fails or requires emergency maintenance, the urgency of production tasks will increase significantly. Evaluate equipment status based on equipment health indexes (such as failure rate, usage time, maintenance records, etc.). If the equipment is in poor condition, the production urgency will increase.

[0097] The availability of raw materials is the basis for the smooth progress of the production process. If the raw materials are insufficient or there are fluctuations in the supply chain, the production urgency will increase. Assess the risk of raw material supply by monitoring the raw material inventory level and supply chain stability (such as transportation delays, supplier availability, etc.).

[0098] Changes in market demand (such as sudden increase in orders or seasonal demand peaks) will also affect production urgency. If market demand fluctuates greatly, production urgency will increase. Through market analysis and sales forecasting, determine the changing trend of current market demand and evaluate its impact on production urgency based on the magnitude of the change.

[0099] Each of the above key evaluation factors has a different impact on production urgency, so it is necessary to assign a corresponding weight coefficient to each factor. These weight coefficients reflect the relative importance of each factor in the final production urgency information.

[0100] Weight coefficient setting: The weight coefficient can be determined based on historical data, experience or through expert scoring. The following is an exemplary weight allocation: The difference between production plan and actual progress: weight coefficient w1 Order delivery time: weight coefficient w2 Equipment status and maintenance: weight coefficient w3 Raw material supply: weight coefficient w4 Market demand fluctuations: weight coefficient w5 The final production urgency information is calculated by the weighted average method. The value of each key evaluation factor is multiplied by its corresponding weight coefficient, and then the sum is obtained to obtain the comprehensive evaluation result: Production urgency information = w1×progress difference + w2×order delivery time + w3×equipment status assessment + w4×raw material supply + w5×market demand fluctuation Through comprehensive evaluation of multiple factors and adjustment of weight coefficients, the urgency of the current production task can be accurately reflected. The production urgency information can be dynamically adjusted according to the real-time changing production data to ensure that the production scheduling model can respond flexibly in complex environments. Optimize resource allocation: This step helps the production scheduling system to reasonably allocate production resources and give priority to the most urgent production tasks when resources are limited.

[0101] The above embodiments are only used to illustrate the technical solutions of the present application, rather than to limit them. Although the present application has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that they can still modify the technical solutions described in the aforementioned embodiments, or make equivalent replacements for some of the technical features therein. However, these modifications or replacements do not deviate the essence of the corresponding technical solutions from the spirit and scope of the technical solutions of the embodiments of the present application.

Claims

1. A short-process energy-saving system for producing calcium oxide from carbide slag, characterized in that: include: A feeding unit is used to quantitatively inject a preset mass of carbide slag raw material, and remove iron and silicon from the preset mass of carbide slag to obtain primary screening carbide slag; A drying unit, wherein the material inlet of the drying unit is connected to the outlet of the feeding unit, and the drying unit is used to dry the pre-screened carbide slag to obtain dried carbide slag; A mixer, wherein the material inlet of the mixer is connected to the outlet end of the drying unit, and the mixer is used to mix the dried carbide slag and the first waste heat output airflow to obtain a first mixed-flow carbide slag; A calcining unit, wherein the feed inlet of the calcining unit is connected to the discharge outlet of the mixer, the air inlet of the calcining unit is used to receive a second waste heat output airflow, the second waste heat output airflow is used to form a second mixed flow carbide slag with the first mixed flow carbide slag, and the calcining unit is used to perform calcination operations and heat preservation operations on the second mixed flow carbide slag to obtain a first finished calcium oxide product; A waste heat recovery unit, wherein the input end of the waste heat recovery unit is connected to the hot air flow output end of the calcining unit, the first output end of the waste heat recovery unit is connected to the mixer, the first output end of the waste heat recovery unit is used to provide the first waste heat output air flow to the mixer, the second output end of the waste heat recovery unit is connected to the air inlet of the calcining unit, and the second output end of the waste heat recovery unit is used to pass the second waste heat output air flow to the calcining unit.

2. The short-process energy-saving system for producing calcium oxide from carbide slag according to claim 1 is characterized in that: The feeding unit includes an intermediate bin for raw materials, a quantitative belt and an iron and silicon removal device. The intermediate bin for raw materials, the quantitative belt and the iron and silicon removal device are arranged in sequence on the moving path of the carbide slag raw materials. The discharge port of the iron and silicon removal device is arranged corresponding to the feed port of the drying unit.

3. The short-process energy-saving system for producing calcium oxide from carbide slag according to claim 2 is characterized in that: The drying unit comprises a dryer, a drying cyclone separator, a first intermediate bin, a first rotary discharger, a first drying bag dust collector, a second intermediate bin and a second rotary discharger; The material inlet end of the dryer is arranged correspondingly to the material outlet end of the iron and silicon removal device; The outlet end of the dryer is connected to the inlet end of the drying cyclone separator; The outlet pipe of the drying cyclone separator is connected to the first drying bag filter; The flow pipe of the drying cyclone separator, the first intermediate bin and the first rotary discharger are connected in sequence; The material flow pipe of the first dry bag filter, the second intermediate bin and the second rotary discharger are connected in sequence; The gas output end of the first drying bag filter is connected to the system induced draft fan.

4. The short-process energy-saving system for producing calcium oxide from carbide slag according to claim 3 is characterized in that: The calcining unit includes a low-nitrogen burner, a hot blast furnace, a dynamic calcining device, a circulating constant temperature furnace and a third rotary discharger; The low nitrogen burner is connected to the first input port of the hot blast furnace, the second input port of the hot blast furnace receives the second waste heat output airflow, and the output port of the hot blast furnace is connected to the gas input port of the dynamic calcining device; The material input port of the dynamic calcining device is connected to the outlet end of the mixer, the outlet end of the dynamic calcining device is connected to the inlet end of the circulating constant temperature furnace, the material outlet end of the circulating constant temperature furnace is connected to the third rotary discharger, and the airflow outlet end of the circulating constant temperature furnace is connected to the waste heat recovery unit.

5. The short-process energy-saving system for producing calcium oxide from carbide slag according to claim 4 is characterized in that: The waste heat recovery unit includes a waste heat distributor, a blower, a second bag filter and an internal circulation fan; The airflow outlet end of the circulating constant temperature furnace is connected to the tube side inlet of the waste heat distributor, the output end of the blower is connected to the shell side inlet of the waste heat distributor, the shell side first outlet of the waste heat distributor is connected to the mixer, the shell side second outlet of the waste heat distributor is connected to the input end of the hot blast furnace, and the tube side outlet of the waste heat distributor is connected to the second bag filter; The airflow output end of the second bag dust collector, the internal circulation fan and the dryer are connected in sequence, the heat inlet of the dryer is connected to the outlet of the internal circulation fan, and the material output end of the second bag dust collector is used to output the second calcium oxide second finished product.

6. The short-process energy-saving system for producing calcium oxide from carbide slag according to claim 5 is characterized in that: The temperature of the dryer is greater than or equal to 300 degrees Celsius and less than or equal to 500 degrees Celsius; and / or, The wind speed of the pipeline between the mixer and the dynamic calcining device is greater than or equal to 5 meters per second and less than or equal to 10 meters per second, and the temperature before the dynamic calcining device is greater than or equal to 200 degrees Celsius and less than or equal to 400 degrees Celsius.

7. The short-process energy-saving system for producing calcium oxide from carbide slag according to claim 5 is characterized in that: The temperature in the dynamic calcining device is greater than or equal to 850 degrees Celsius and less than or equal to 1200 degrees Celsius, and the movement speed in the dynamic calcining device is greater than or equal to 7 meters per second and less than or equal to 20 meters per second; and / or, The temperature in the circulating constant temperature furnace is greater than or equal to 500 degrees Celsius and less than or equal to 850 degrees Celsius.

8. A control method for a short-process energy-saving system for producing calcium oxide from carbide slag according to any one of claims 5 to 7, characterized in that: include: Acquire production urgency information, current system status information and environmental information, wherein the current system status information includes temperature information, pressure information and equipment status information, and the environmental information includes external environment information and raw material supply information; The production urgency information, the current system status information and the environmental information are input into the production scheduling control model to obtain a quantitative belt control signal, a first rotary discharger control signal, a second rotary discharger control signal, a first proportional regulating valve opening signal and a second proportional regulating valve opening signal, wherein the first proportional regulating valve is used to control the first waste heat output airflow, and the second proportional regulating valve is used to control the second waste heat output airflow, and the production scheduling control model is a hybrid model based on a combination of neural network and fuzzy logic.

9. The control method according to claim 8, characterized in that: The production scheduling control model includes an input layer, a processing layer and an output layer, the processing layer includes a multi-layer neural network module part and a fuzzy logic module, the multi-layer neural network module part includes a first hidden layer and a second hidden layer, and the fuzzy logic module is connected to the second hidden layer; The production scheduling control model uses mean square error to determine the error between the predicted output and the actual control signal, and the production scheduling control model uses Adam optimizer for optimization.

10. The control method according to claim 8, characterized in that: The specific steps of determining the production urgency information include: The production urgency information is determined based on the difference between the production plan and the actual progress, order delivery time, equipment status and maintenance, raw material supply, market demand fluctuations and their corresponding weight coefficients.

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