A supercritical CO2 vulcanizing press hydraulic station heat dissipation and heat recovery system

Abstract

The present invention discloses a heat dissipation and heat recovery system for a supercritical CO2 vulcanizing press hydraulic station, which relates to the technical field of hydraulic systems and comprises: a hydraulic oil tank unit, a vaporizing coil arranged inside the hydraulic oil tank; a temperature sensor for real-time monitoring of the temperature of the hydraulic oil; a flow regulating valve connected to the vaporizing coil; wherein the temperature control system comprises a PLC controller and a host computer, the PLC controller is used to receive data collected by the temperature sensor, and transmit the collected data to the host computer for data processing through a modbus protocol to execute heat dissipation control; a dynamic temperature prediction module, a supercritical CO2 generating unit, and the supercritical CO2 generating unit and the hydraulic oil tank unit are connected by a pipeline; a heat energy recovery and utilization unit, comprising a high-pressure coil and a heat storage medium for absorbing and storing heat transferred by the high-pressure coil, thereby facilitating centralized monitoring and management of equipment and improving the efficiency and scale benefits of centralized heat energy recovery.

Description

Technical Field

[0001] The present invention belongs to the technical field of hydraulic systems, and in particular relates to a heat dissipation and heat recovery system for a supercritical CO2 vulcanizing press hydraulic station. Background Art

[0002] The vulcanizer hydraulic station is the core equipment in the rubber vulcanization process, responsible for providing the necessary pressure and power. Because the vulcanization process operates under high temperature and pressure, a significant amount of heat is generated within the equipment. The hydraulic system also generates heat during operation. If this heat is not dissipated promptly, the hydraulic oil temperature will rise, affecting the performance and lifespan of the hydraulic system. Excessively high hydraulic oil temperature reduces oil viscosity, increases the likelihood of leakage, and reduces system efficiency. The necessity of heat dissipation technology affects the performance and lifespan of the hydraulic system. Therefore, effective heat dissipation technology is crucial to ensuring the proper operation of the vulcanizer hydraulic station.

[0003] The current mainstream heat dissipation method is water circulation. For a hydraulic system like a vulcanizer that generates a lot of heat, a high-powered water pump is required to circulate the water, and a large water tower is needed to dissipate the heat naturally. However, in summer, due to the small temperature difference, the natural heat dissipation efficiency of water is low, making it difficult for this cooling system to maintain a stable temperature in the hydraulic system. In this case, either the design margin of the water tower is increased or the water pump power is increased to increase the circulation volume, which significantly increases the heat dissipation cost. Furthermore, this system cannot precisely control the oil temperature, causing the hydraulic oil to operate in an abnormal operating range, which can also lead to hydraulic oil deterioration and shorten its service life. The heat generated by the system can also be considered as a form of energy. The input power of the vulcanizer hydraulic system is almost entirely converted into internal energy of the hydraulic system, that is, the input electrical energy is almost entirely converted into heat. Current heat dissipation methods dissipate this energy into the environment, resulting in a waste of this energy. To address the current heat dissipation and energy recovery issues in hydraulic systems, we propose a heat dissipation and heat recovery system for the vulcanizer hydraulic station using supercritical carbon dioxide. Summary of the Invention

[0004] In view of the problems mentioned in the background technology, the purpose of the present invention is to provide a supercritical CO2 vulcanizer hydraulic station heat dissipation and heat recovery system to solve the problems raised in the background technology.

[0005] The above technical objectives of the present invention are achieved through the following technical solutions:

[0006] A heat dissipation and heat recovery system for a supercritical CO2 vulcanizing press hydraulic station includes: a hydraulic oil tank unit, the hydraulic oil tank unit including a hydraulic oil tank for containing hydraulic oil; a vaporization coil disposed within the hydraulic oil tank for removing heat from the hydraulic oil by absorbing heat through supercritical CO2 phase change; a temperature sensor for real-time monitoring of the hydraulic oil temperature and transmitting the temperature data to a temperature control system; and a flow control valve connected to the vaporization coil for receiving instructions from the temperature control system and regulating the flow of supercritical CO2 entering the vaporization coil.

[0007] The temperature control system includes a PLC controller and a host computer. The PLC controller is used to receive data collected by the temperature sensor and transmit the collected data to the host computer for data processing through the Modbus protocol to perform heat dissipation control.

[0008] A dynamic temperature prediction module, provided in the temperature control system, for predicting the future temperature trend of the hydraulic oil based on historical temperature data and generating parameters for adjusting heat dissipation control;

[0009] A supercritical CO2 generation unit, comprising a CO2 compressor for compressing gaseous CO2 to a supercritical state and a supercritical CO2 storage tank connected to the CO2 compressor via a high-pressure pipeline;

[0010] The supercritical CO2 generating unit and the hydraulic oil tank unit are connected via a pipeline;

[0011] The heat energy recovery and utilization unit includes a high-pressure coil connected to the CO2 compressor and a heat storage medium for absorbing and storing heat transferred by the high-pressure coil, and the heat storage medium is used for domestic heat, heating or industrial production.

[0012] Preferably, the data processing of the temperature control system includes:

[0013] The temperature setting module is used to set the target operating temperature range of the hydraulic oil. The upper limit of the operating temperature range is Tmax, and the lower limit is Tmin;

[0014] The temperature comparison module is used to compare the real-time temperature T of the hydraulic oil detected by the temperature sensor with the target working temperature range;

[0015] The heat dissipation calculation module is used to calculate the heat Q that needs to be removed from the hydraulic oil according to the following formula when T>Tmax:

[0016] Q = c × m × (T - Tn)

[0017] Where c is the specific heat capacity of the hydraulic oil, m is the mass of the hydraulic oil, T is the current hydraulic oil temperature, and Tn is the target cooling temperature;

[0018] The hydraulic oil mass m is calculated by m=ρ×V, where ρ is the hydraulic oil density and V is the hydraulic oil volume; c and ρ are updated according to the hydraulic oil type and temperature;

[0019] The CO2 flow calculation module is used to calculate the required CO2 mass M2 based on the required heat dissipation Q and the unit mass enthalpy change Δh of CO2 in the gasification coil:

[0020] M2=Q / Δh

[0021] The flow control instruction generation module is used to generate an instruction signal for controlling the opening degree or opening time of the flow control valve according to the calculated required CO2 mass M2.

[0022] Preferably, the dynamic temperature prediction module is used to:

[0023] Collect and store historical hydraulic oil temperature change data and establish a temperature change trend model;

[0024] Based on historical data and current status, predict the temperature change trend ΔT in the future;

[0025] Calculate the pre-adjustment coefficient α based on the predicted temperature change trend ΔT

[0026] α=f(ΔT)

[0027] Where f is a preset function used to increase the α value when the temperature is predicted to rise rapidly;

[0028] The temperature control system uses a pre-adjustment coefficient α to correct the required CO2 quality;

[0029] M2'=α×M2

[0030] And generate flow regulation instructions based on the correction.

[0031] The temperature control system further comprises:

[0032] Data communication module, used to communicate with temperature sensors and flow control valves via RS-485, CAN bus or analog signals;

[0033] The algorithm correction module is used to record the actual cooling amplitude ΔTr of each cooling process, compare it with the theoretically calculated cooling amplitude ΔTc, and determine the correction coefficient K according to the formula:

[0034] K=ΔTr / ΔTc

[0035] The correction factor K is applied to subsequent heat dissipation calculations or CO2 flow calculations to compensate for the temperature change trend model error.

[0036] Preferably, the hydraulic oil tank unit further comprises a stirring blade arranged inside the hydraulic oil tank for increasing the circulation of the hydraulic oil and making the oil temperature uniform.

[0037] Preferably, the pipeline includes a supercritical transport pipe and a high-pressure and high-temperature gasification CO2 pipeline;

[0038] Among them, the supercritical CO2 storage tank is connected to the flow regulating valve through a supercritical transport pipe;

[0039] The CO2 compressor is connected to the gasification coil through a high-pressure and high-temperature gasification CO2 pipeline;

[0040] The supercritical transport pipe and the high-pressure and high-temperature gasification CO2 pipeline are provided with heating belts on the outside to adjust the CO2 state or prevent abnormal phase change as needed.

[0041] Preferably, the system can be applied to a single vulcanizing press hydraulic station, or applied to a clustered vulcanizing press hydraulic station by duplicating the hydraulic oil tank unit and adjusting the corresponding control logic.

[0042] Preferably, the heat storage medium in the heat energy recovery and utilization unit is water or thermal oil, and the recovered heat energy is used for domestic heating, heating or industrial preheating.

[0043] The present application also discloses a control method for a heat dissipation and heat recovery system of a supercritical CO2 vulcanizing press hydraulic station, comprising the following steps:

[0044] S1: Continuously or periodically obtain the real-time temperature T of the hydraulic oil through the temperature sensor and transmit the collected data to the PLC controller;

[0045] S2: The PLC controller compares the real-time temperature T with the preset operating temperature range [Tmin, Tmax];

[0046] S3: If T>Tmax, perform the following heat dissipation calculation:

[0047] Calculate the heat that needs to be taken away using the formula: Q=c×m×(T-Tn);

[0048] Calculate the initial required CO2 mass using the formula: M2=Q / Δh;

[0049] S4: Call the dynamic temperature prediction module to predict the future temperature trend ΔT, calculate the pre-adjustment coefficient α, and correct the CO2 mass M2'=α×M2;

[0050] S5: Apply the learned correction factor K to adjust the heat dissipation calculation or CO2 flow calculation;

[0051] S6: Based on the final calculated CO2 demand (M2, M2' or the value corrected by K), a command signal is generated and sent to the flow control valve to control the opening degree or opening time of the flow control valve to inject an appropriate amount of CO2 into the gasification coil;

[0052] S7: Start the stirring blade and run it for a preset time tmix to promote uniform oil temperature;

[0053] S8: Return to step S1 and continue monitoring and controlling.

[0054] As a preference, the method further includes the following steps of controlling the CO2 compressor:

[0055] Monitoring the pressure P in the supercritical CO2 storage tank;

[0056] When P is lower than the preset starting pressure threshold P_low, the CO2 compressor is started;

[0057] When P is higher than the preset stop pressure threshold P_high, the CO2 compressor is stopped.

[0058] In summary, the present invention mainly has the following beneficial effects:

[0059] 1. This system places the vaporizer coil directly inside the hydraulic oil tank, causing the supercritical CO2 to undergo a phase change at the heat source, directly absorbing the heat from the hydraulic oil. Compared to traditional external coolers (such as air and water cooling), this eliminates the thermal resistance of intermediate heat transfer media and long-distance piping, minimizing the heat exchange path and achieving high heat transfer efficiency. Furthermore, by leveraging the high latent heat of supercritical CO2 phase change, more heat can be removed per unit mass of working fluid, further enhancing heat dissipation capacity and ensuring rapid cooling of the hydraulic system, even under high-load conditions, to maintain the optimal operating temperature.

[0060] 2. This application combines real-time temperature monitoring, dynamic temperature prediction, and algorithm self-correction. A high-precision temperature sensor measures oil temperature, and a flow control valve precisely controls the amount of CO2 injected. The dynamic prediction module anticipates temperature trends and adjusts cooling capacity in advance, effectively suppressing temperature overshoots and fluctuations.

[0061] 3. This system not only solves the heat dissipation problem of the hydraulic station, but also utilizes a heat recovery unit. The CO2 compressor releases a large amount of compression heat while producing supercritical CO2. This waste heat, which would otherwise require additional cooling and dissipation, is effectively recovered through the high-pressure coil installed in the high-pressure CO2 pipeline. The recovered heat energy can be used to heat media such as water or thermal oil, providing the factory with domestic hot water, winter heating, or industrial preheating. This achieves cascade energy utilization, significantly reducing the factory's overall energy consumption and operating costs, and improving economic benefits.

[0062] 4. This application uses CO2 as the refrigerant for cooling and heat transfer. CO2 is chemically stable, non-flammable, and non-toxic, making it safer to use than traditional Freon refrigerants or flammable hydrocarbons, making it particularly suitable for high-temperature, high-pressure industrial production environments. Furthermore, the heating belt ensures the stability of the CO2 in the pipeline, and the stirring blades ensure uniform oil temperature, improving the reliability and stability of system operation.

[0063] 5. For a single vulcanizer, an independent heat dissipation and heat recovery system can be configured. For factories with multiple vulcanizers, a cluster model can be adopted, with a centralized supercritical CO2 generation unit and heat recovery unit serving multiple independent hydraulic oil tank units. The modular and scalable design reduces the initial investment and maintenance complexity in large-scale applications, facilitates centralized monitoring and management of equipment, and also improves the efficiency and scale benefits of centralized heat recovery. BRIEF DESCRIPTION OF THE DRAWINGS

[0064] Figure 1 This is a schematic diagram of the system flow of a single supercritical CO2 vulcanizing press hydraulic station according to embodiment 1 of the present invention;

[0065] Figure 2 This is a schematic diagram of the flow chart of a hydraulic station system for multiple supercritical CO2 vulcanizers according to embodiment 2 of the present invention;

[0066] Figure 3 This is a flow chart of Example 4 of the present invention. DETAILED DESCRIPTION

[0067] The invention of this application is further described in detail below with reference to the accompanying drawings and specific embodiments. In order to clearly and completely describe the technical solution, the following embodiments are selected for illustration; other embodiments obtained based on the contents recorded in this application without creative work are all within the scope of protection of this invention.

[0068] In the following embodiments, it should be noted that the terms "upper", "lower", "left", "right", "inside", "outside", "top / bottom", etc., or the like, are based on the terms or the like as shown in the accompanying drawings. They are only for the purpose of clearly describing the present embodiment, and do not indicate or imply that the device or element referred to must have a specific orientation. Therefore, they should not be understood as limiting the present application.

[0069] Example 1: This example provides a heat dissipation and heat recovery system for a single supercritical CO2 vulcanizing press hydraulic station, comprising a hydraulic oil tank unit, a temperature control system, a supercritical CO2 generating unit, and a heat recovery and utilization unit;

[0070] Among them, the hydraulic oil tank unit is the core oil storage and initial heat exchange place of the hydraulic system, including:

[0071] Hydraulic oil tank: a standard or customized container used to hold the hydraulic oil required for the operation of the vulcanizer. Its volume is determined according to the requirements of the hydraulic system of the vulcanizer.

[0072] The vaporizer coil is located inside the hydraulic oil tank and is completely immersed in the hydraulic fluid. It is preferably made of a pressure-resistant and thermally conductive material (such as copper or stainless steel), with a large surface area, spiral or serpentine piping structure to maximize contact with the hydraulic fluid. The inlet of the vaporizer coil is connected to the supercritical CO2 line from the flow control valve, while the outlet is connected to the high-pressure, high-temperature vaporized CO2 pipeline, which returns to the low-pressure side of the CO2 compressor. The purpose is to utilize the phase change of supercritical CO2 flowing into the vaporizer coil to absorb heat from the hydraulic fluid, achieving efficient heat dissipation. Cooling is performed directly at the heat source, resulting in high heat exchange efficiency. The use of CO2 as a refrigerant is environmentally friendly and non-flammable.

[0073] Temperature sensor: Installed in the middle of the hydraulic oil tank or near the oil return port, it can reflect the overall or highest oil temperature point and is used to monitor the hydraulic oil temperature T in real time. The temperature sensor can be a Pt100 thermal resistor or thermocouple, which transmits the detected temperature signal to the PLC controller in the temperature control system, providing a real-time data foundation for precise control.

[0074] Flow Control Valve: Installed on the supercritical CO2 transport pipe entering the vaporizer coil. Using a proportional control valve or a fast-acting solenoid valve, based on command signals from the PLC controller, this valve precisely regulates the flow rate or total injection volume of supercritical CO2 entering the vaporizer coil, achieving on-demand cooling, preventing overcooling or undercooling, and maintaining a stable oil temperature.

[0075] The stirring blade is located inside the hydraulic oil tank and driven by a small motor. Its function is to stir the hydraulic oil during the cooling process or periodically to evenly distribute the oil temperature within the tank, avoiding local overheating or overcooling. This improves the overall heat transfer efficiency of the vaporizer coil, enhances heat transfer, improves cooling uniformity and efficiency, and ensures representative temperature sensor readings.

[0076] The supercritical CO2 generation unit is responsible for providing supercritical CO2 medium for heat dissipation, including:

[0077] CO2 compressor: It is a multi-stage compressor that can compress normal temperature and pressure or recycled low-pressure gaseous CO2 to a supercritical state with a pressure higher than 7.38MPa and a temperature higher than 31.1°C. The outlet of the CO2 compressor is connected to a high-pressure pipeline.

[0078] Supercritical CO2 storage tank: connected to the CO2 compressor through a high-pressure pipeline, used to store compressed supercritical CO2. The supercritical CO2 storage tank acts as a buffer to ensure a stable supply of supercritical CO2 even during the start-up and shutdown of the CO2 compressor. The supercritical CO2 storage tank is equipped with a pressure sensor and a safety valve.

[0079] The pipeline system includes: Supercritical transport pipe: connecting the supercritical CO2 storage tank and the flow regulating valve. The pipeline needs to withstand high pressure and requires insulation treatment to maintain the supercritical state of CO2.

[0080] High-pressure and high-temperature gasification CO2 pipeline: The CO2 after the gasification coil absorbs heat is discharged into the CO2 compressor. Among them, the high-pressure coil for heat recovery is connected between the CO2 compressor outlet and the supercritical CO2 storage tank inlet.

[0081] Heating belts: These are installed on the outside of supercritical transport pipes and high-pressure, high-temperature CO2 gasification pipelines. These belts can be activated as needed to prevent phase change of the CO2 in the pipeline due to rapid heat dissipation. They can also be used to precisely adjust the CO2 state before entering the gasification coil, ensuring a stable working medium and improving system reliability and controllability.

[0082] The temperature control system includes a PLC controller and a host computer. The PLC controller is used to receive data collected by the temperature sensor and transmit the collected data to the host computer for data processing through the Modbus protocol to perform heat dissipation control.

[0083] A dynamic temperature prediction module, provided in the temperature control system, for predicting the future temperature trend of the hydraulic oil based on historical temperature data and generating parameters for adjusting heat dissipation control;

[0084] Data processing of the temperature control system includes:

[0085] The temperature setting module is used to set the target operating temperature range of the hydraulic oil. The upper limit of the operating temperature range is Tmax, and the lower limit is Tmin;

[0086] The temperature comparison module is used to compare the real-time temperature T of the hydraulic oil detected by the temperature sensor with the target working temperature range;

[0087] The heat dissipation calculation module is used to calculate the heat Q that needs to be removed from the hydraulic oil according to the following formula when T>Tmax:

[0088] Q = c × m × (T - Tn)

[0089] Where c is the specific heat capacity of the hydraulic oil, m is the mass of the hydraulic oil, T is the current hydraulic oil temperature, and Tn is the target cooling temperature;

[0090] The hydraulic oil mass m is calculated by m=ρ×V, where ρ is the hydraulic oil density and V is the hydraulic oil volume. c and ρ can be obtained and updated from a database or a lookup table based on the current oil temperature or a preset oil type to improve calculation accuracy.

[0091] The CO2 flow calculation module is used to calculate the required CO2 mass M2 based on the required heat dissipation Q and the unit mass enthalpy change Δh of CO2 during evaporation / expansion in the gasification coil:

[0092] M2=Q / Δh

[0093] The flow control command generation module converts the calculated M2 into a specific control signal for the flow control valve. For example, for a proportional valve, it outputs an analog signal proportional to M2 to control the valve opening; for an on-off valve, it calculates an opening time so that the total amount of CO2 flowing in during this time is approximately equal to M2.

[0094] The dynamic temperature prediction module, which is implemented by a PLC controller or a host computer, collects and stores historical hydraulic oil temperature change data and establishes a temperature change trend model, for example, based on time series analysis or a more complex machine learning model;

[0095] Based on historical data and current status (current temperature, equipment operating status), predict the temperature change trend ΔT in the future;

[0096] Calculate the pre-adjustment coefficient α based on the predicted temperature change trend ΔT

[0097] α=f(ΔT)

[0098] Wherein, f is a preset function, for example, a piecewise function or an exponential function, which outputs a larger value when the predicted heating rate is fast, and is used to increase the α value when the predicted temperature will rise rapidly;

[0099] An example of an exponential function is: α = exp(β × ΔT);

[0100] Where β is the positive adjustment coefficient;

[0101] When ΔT=0, α=exp(0)=1;

[0102] When ΔT>0, α>1, and increases exponentially with the increase of ΔT;

[0103] When ΔT<0, 0<α<1.

[0104] The temperature control system uses a pre-adjustment coefficient α to correct the required CO2 quality;

[0105] M2'=α×M2

[0106] If the temperature is predicted to rise rapidly, α>1, and the CO2 injection rate is increased in advance; if the temperature is predicted to stabilize or decrease, α≤1, and the CO2 injection rate is reduced or maintained;

[0107] Finally, the modified M2' is used to generate flow control commands. This enables faster response to temperature changes, effectively suppresses temperature overshoot, and improves the stability and accuracy of temperature control, making it particularly suitable for vulcanization operations with large fluctuations in operating conditions.

[0108] The temperature control system also includes:

[0109] Data communication module, used to communicate with temperature sensors and flow control valves via RS-485, CAN bus or analog signals;

[0110] The algorithm correction module is used to record the actual cooling amplitude ΔTr of each cooling process and compare it with the theoretically calculated cooling amplitude ΔTc. ΔTc = (M2' × Δh) / (c × m). The correction coefficient K is determined according to the following formula:

[0111] K=ΔTr / ΔTc

[0112] The correction factor K is applied to subsequent heat dissipation calculations or CO2 flow calculations to compensate for the temperature change trend model error.

[0113] In Example 2, the system can be applied to a single vulcanizing press hydraulic station, or applied to a clustered vulcanizing press hydraulic station by duplicating the hydraulic oil tank unit and adjusting the corresponding control logic.

[0114] In this application scenario:

[0115] The supercritical CO2 generation unit and the heat recovery and utilization unit can be designed to be centralized to serve multiple vulcanizers, using larger capacity compressors, storage tanks and heat recovery systems to achieve economies of scale.

[0116] The hydraulic oil tank unit of each vulcanizer (including oil tank, vaporizing coil, temperature sensor, flow control valve, optional stirring blade) is independently set up for its own hydraulic station.

[0117] The PLC controller in the temperature control system needs to have sufficient processing power and I / O points to simultaneously monitor and control all hydraulic tank units. The control logic is replicated and applied to each unit, but the control parameters (such as Tmax, Tmin, Tn, c, m, V, Δh) can be set independently for each unit. The PLC controller will independently calculate and control the opening degree / time of the corresponding flow control valve based on the temperature conditions of each unit.

[0118] The upper computer interface will be able to centrally display the status of all hydraulic stations and allow each station to be independently set up and managed. For factories with multiple vulcanizing presses, cluster control can reduce initial investment and maintenance costs, and centralized management of heat recovery is also more efficient.

[0119] Example 3: This example describes in detail the working mode of the heat energy recovery and utilization unit, aiming to illustrate how to effectively recover and utilize the heat generated during the CO2 compression process.

[0120] In the heat dissipation and heat recovery system of a supercritical CO2 curing press's hydraulic station, the CO2 compressor is a component that generates a significant amount of heat. During the process of compressing low-pressure gaseous CO2 to a supercritical state (high pressure and high temperature), most of the mechanical energy input is converted into the CO2's internal energy and heat of compression. If not utilized, this heat would be dissipated into the environment through additional cooling equipment (such as air- or water-cooled condensers), resulting in energy waste.

[0121] To address these issues, a heat recovery and utilization unit includes a high-pressure coil connected to the CO2 compressor and a heat storage medium that absorbs and stores the heat transferred by the high-pressure coil. The heat storage medium is water or thermal oil, and the recovered heat is used for domestic heating, heating, or industrial preheating.

[0122] A high-pressure coil is installed between the CO2 compressor outlet and the supercritical CO2 storage tank, acting like a heat exchanger. After exiting the compressor, the high-temperature, high-pressure supercritical CO2 first flows through the coil. The coil is preferably made of a material with high pressure resistance and good thermal conductivity, and is designed with fins to increase the heat exchange area. The coil is housed in a container and surrounded by an independent fluid circuit, which contains a heat storage medium. This medium is preferably thermal oil or water.

[0123] If water is chosen as the heat storage medium, when the high-temperature CO2 flows through the high-pressure coil, heat is transferred through the pipe walls to the water in the tank, raising its temperature. The heated water can be directly piped out and used for domestic heating in the factory or nearby community water storage tanks (for example, providing water for employee showers and cafeterias), or incorporated into the factory (for example, heating factory buildings and offices through radiators, fan heaters, or floor heating systems).

[0124] If thermal oil is selected as the heat storage medium, the high-pressure coil will be coupled to a thermal oil circulation loop. The high-temperature CO2 will heat the thermal oil, and then the high-temperature thermal oil will be transported through pumps and pipelines to industrial equipment that needs heat. For example, it can provide hot air for drying equipment, or be used in industrial production links such as mold heating and shaping.

[0125] Embodiment 4. The present application also discloses a control method for the heat dissipation and heat recovery system of the hydraulic station of a vulcanizer using supercritical CO2, including the following steps:

[0126] S1: Continuously or at a set sampling period (such as once per second) through a temperature sensor, measure the real-time temperature T of the hydraulic oil, and send the data to the PLC controller;

[0127] S2: The PLC controller compares the real-time temperature T with the preset working temperature range [Tmin, Tmax];

[0128] S3: If T > Tmax, it indicates that the hydraulic oil is overheated and heat dissipation needs to be started. The PLC controller executes:

[0129] Call the heat dissipation calculation module to calculate the heat Q that needs to be taken away, Q = c × m × (T - Tn);

[0130] Call the CO2 flow calculation module to calculate the initial required CO2 mass M2 = Q / Δh;

[0131] S4: If the dynamic temperature prediction function is enabled, call the dynamic temperature prediction module, predict the future temperature trend ΔT based on historical data and the current state, calculate the pre-adjustment coefficient α, and correct the required CO2 mass M2' = α × M2;

[0132] S5: If the algorithm correction function is enabled, apply the previously learned correction coefficient K to adjust the heat dissipation calculation or directly adjust the CO2 flow calculation;

[0133] S6: According to the finally calculated CO2 demand (M2, M2' or the value corrected by K), generate an instruction signal and send it to the flow regulating valve to control the opening degree or opening time of the flow regulating valve, and inject an appropriate amount of CO2 into the vaporization coil;

[0134] S7: Start the stirring paddle to run for a preset time tmix to promote uniform oil temperature;

[0135] After completing one control action, the system returns to step S1, continuously monitors the temperature and controls as needed. If T ≤ Tmax, stop injecting CO2. If T < Tmin, the system can remain in the stopped state or enter the heat preservation logic.

[0136] To ensure the stable supply of supercritical CO2, the system also includes the start-stop control of the CO2 compressor:

[0137] Monitor the pressure P in the tank through a pressure sensor installed on the supercritical CO2 storage tank.

[0138] The PLC controller compares the real-time pressure P with the preset start pressure threshold P_low and stop pressure threshold P_high.

[0139] When P < P_low, it indicates that the CO2 pressure in the storage tank is insufficient. The PLC controller sends a start signal to the CO2 compressor to start compressing and supplementing CO2.

[0140] When P ≥ P_high, it indicates that the CO2 pressure in the storage tank is sufficient. The PLC controller sends a stop signal to the CO2 compressor to stop compressing, so as to save energy and prevent overpressure.

[0141] Ensure that the system always has enough working medium for heat dissipation, and at the same time achieve the on-demand operation of the compressor to reduce energy consumption.

[0142] As described above, it is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any minor modifications, equivalent replacements, and improvements made to the above embodiments based on the technical essence of the present invention shall be included within the protection scope of the technical solution of the present invention.

Claims

1. A supercritical CO2 vulcanizing press hydraulic station heat dissipation and heat recovery system, characterized in that: include: The hydraulic oil tank unit includes a hydraulic oil tank for containing hydraulic oil; a vaporizing coil disposed inside the hydraulic oil tank for removing heat from the hydraulic oil by absorbing heat through supercritical CO2 phase change; a temperature sensor for real-time monitoring of the hydraulic oil temperature and transmitting the temperature data to a temperature control system; and a flow regulating valve connected to the vaporizing coil for receiving instructions from the temperature control system and regulating the flow of supercritical CO2 entering the vaporizing coil. The temperature control system includes a PLC controller and a host computer. The PLC controller is used to receive data collected by the temperature sensor and transmit the collected data to the host computer for data processing through the Modbus protocol to perform heat dissipation control. A dynamic temperature prediction module, provided in the temperature control system, for predicting the future temperature trend of the hydraulic oil based on historical temperature data and generating parameters for adjusting heat dissipation control; A supercritical CO2 generation unit, comprising a CO2 compressor for compressing gaseous CO2 to a supercritical state and a supercritical CO2 storage tank connected to the CO2 compressor via a high-pressure pipeline; The supercritical CO2 generating unit and the hydraulic oil tank unit are connected via a pipeline; A heat energy recovery and utilization unit, comprising a high-pressure coil connected to a CO2 compressor and a heat storage medium for absorbing and storing heat transferred by the high-pressure coil, and using the heat storage medium for domestic heat, heating, or industrial production; Data processing of the temperature control system includes: The temperature setting module is used to set the target operating temperature range of the hydraulic oil. The upper limit of the operating temperature range is Tmax, and the lower limit is Tmin; The temperature comparison module is used to compare the real-time temperature T of the hydraulic oil detected by the temperature sensor with the target working temperature range; The heat dissipation calculation module is used to calculate the heat Q that needs to be removed from the hydraulic oil according to the following formula when T>Tmax: Q = c × m × (T - Tn) Where c is the specific heat capacity of the hydraulic oil, m is the mass of the hydraulic oil, T is the current hydraulic oil temperature, and Tn is the target cooling temperature; The hydraulic oil mass m is calculated by m=ρ×V, where ρ is the hydraulic oil density and V is the hydraulic oil volume; c and ρ are updated according to the hydraulic oil type and temperature; The CO2 flow calculation module is used to calculate the required CO2 mass M2 based on the required heat dissipation Q and the unit mass enthalpy change Δh of CO2 in the gasification coil: M2=Q / Δh A flow control instruction generation module is used to generate an instruction signal for controlling the opening degree or opening time of the flow control valve according to the calculated required CO2 mass M2; The dynamic temperature prediction module is used to: Collect and store historical hydraulic oil temperature change data and establish a temperature change trend model; Based on historical data and current status, predict the temperature change trend ΔT in the future; According to the predicted temperature change trend ΔT, calculate the pre-adjustment coefficient α: α=f(ΔT) Where f is a preset function used to increase the α value when the temperature is predicted to rise rapidly; The temperature control system uses a pre-adjustment coefficient α to correct the required CO2 quality; M2'=α×M2 And generate flow regulation instructions based on the correction.

2. A supercritical CO2 vulcanizing press hydraulic station heat dissipation and heat recovery system according to claim 1, characterized in that: The temperature control system also includes: Data communication module, used to communicate with temperature sensors and flow control valves via RS-485, CAN bus or analog signals; The algorithm correction module is used to record the actual cooling amplitude ΔTr of each cooling process, compare it with the theoretically calculated cooling amplitude ΔTc, and determine the correction coefficient K according to the formula: K=ΔTr / ΔTc The correction factor K is applied to subsequent heat dissipation calculations or CO2 flow calculations to compensate for the temperature change trend model error.

3. A supercritical CO2 vulcanizing press hydraulic station heat dissipation and heat recovery system according to claim 1, characterized in that: The hydraulic oil tank unit also includes a stirring blade arranged inside the hydraulic oil tank for increasing the circulation of the hydraulic oil and making the oil temperature uniform.

4. A supercritical CO2 vulcanizing press hydraulic station heat dissipation and heat recovery system according to claim 1, characterized in that: The pipeline includes a supercritical transport pipe and a high-pressure and high-temperature gasification CO2 pipeline; Among them, the supercritical CO2 storage tank is connected to the flow regulating valve through a supercritical transport pipe; The CO2 compressor is connected to the gasification coil through a high-pressure and high-temperature gasification CO2 pipeline; The supercritical transport pipe and the high-pressure and high-temperature gasification CO2 pipeline are provided with heating belts on the outside to adjust the CO2 state or prevent abnormal phase change as needed.

5. A supercritical CO2 vulcanizing press hydraulic station heat dissipation and heat recovery system according to any one of claims 1 to 4, characterized in that: The system can be applied to a single vulcanizing press hydraulic station, or applied to a clustered vulcanizing press hydraulic station by duplicating the hydraulic oil tank unit and adjusting the corresponding control logic.

6. A supercritical CO2 vulcanizing press hydraulic station heat dissipation and heat recovery system according to claim 1, characterized in that: The heat storage medium in the heat energy recovery and utilization unit is water or thermal oil, and the recovered heat energy is used for domestic heating, heating or industrial preheating.

7. A control method for the heat dissipation and heat recovery system of a vulcanizing press hydraulic station based on the supercritical CO2 according to any one of claims 1 to 6, characterized in that: The following steps are involved: S1: Continuously or periodically obtain the real-time temperature T of the hydraulic oil through the temperature sensor and transmit the collected data to the PLC controller; S2: The PLC controller compares the real-time temperature T with the preset operating temperature range [Tmin, Tmax]; S3: If T>Tmax, perform the following heat dissipation calculation: Calculate the heat that needs to be taken away using the formula: Q=c×m×(T-Tn); Calculate the initial required CO2 mass using the formula: M2=Q / Δh; S4: Call the dynamic temperature prediction module to predict the future temperature trend ΔT, calculate the pre-adjustment coefficient α, and correct the CO2 mass M2'=α×M2; S5: Apply the learned correction factor K to adjust the heat dissipation calculation or CO2 flow calculation; S6: Based on the final calculated CO2 demand, a command signal is generated and sent to the flow control valve to control the opening degree or opening time of the flow control valve to inject an appropriate amount of CO2 into the gasification coil; S7: Start the stirring blade and run it for a preset time tmix to promote uniform oil temperature; S8: Return to step S1 and continue monitoring and controlling.

8. A control method for a heat dissipation and heat recovery system of a supercritical CO2 vulcanizing press hydraulic station according to claim 7, characterized in that: It also includes the control steps for the CO2 compressor: Monitoring the pressure P in the supercritical CO2 storage tank; When P is lower than the preset starting pressure threshold P_low, the CO2 compressor is started; When P is higher than the preset stop pressure threshold P_high, the CO2 compressor is stopped.

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