Ultrathin glass mixture temperature control system and ultrathin glass mixture temperature control method

Abstract

The invention provides an ultra-thin glass mixture temperature control system and an ultra-thin glass mixture temperature control method. The ultra-thin glass mixture temperature control system comprises a steam generator, a main adjusting valve, a raw material mixing bin, a mixing bin temperature sensor and a PLC, steam generated by the steam generator flows through the main adjusting valve on a steam pipeline and enters the raw material mixing bin, and the main adjusting valve and the mixing bin temperature sensor are electrically connected with the PLC. The mixing bin temperature sensor is used for monitoring the temperature of a mixture in the raw material mixing bin in real time and sending the temperature to the PLC, and the PLC is used for dynamically adjusting the opening degree of the main adjusting valve according to the temperature of the mixture so as to control the flow of steam entering the raw material mixing bin, so that the difference between the temperature of the mixture and the target temperature is stabilized within a preset allowable fluctuation range. The temperature of the ultra-thin glass mixture can be accurately regulated and controlled, and the problem that the waviness of ultra-thin glass exceeds the standard is effectively solved.

Description

Technical Field

[0001] This disclosure relates to a temperature control system and method for ultrathin glass mixtures. Background Technology

[0002] The production of ultra-thin glass places extremely stringent requirements on the raw material mixing process. The smoothness and waviness of the mixture are core indicators that directly affect the surface quality of the final glass product. During the raw material mixing process, the mixture needs to possess excellent fluidity to ensure uniform distribution during the forming stage, thereby avoiding microscopic defects caused by local density or compositional differences, such as excessive surface waviness. The initial temperature of the raw materials is a key physical parameter that determines the fluidity and uniformity of the mixture.

[0003] In low-temperature environments, such as winters in northern regions, ambient temperatures often drop below -10°C. Under these conditions, the initial temperatures of raw materials such as quartz sand, soda ash, and limestone will be significantly lower. Low temperatures increase the cohesive and frictional forces between particles in the mixture, severely weakening its flow properties. This makes it difficult to achieve uniform spreading of the mixture during transportation and distribution. This non-uniformity is amplified in subsequent high-temperature melting and molding processes, ultimately manifesting as visible or instrumental corrugated defects on ultra-thin glass sheets that fail to meet quality standards, severely reducing product yield and grade.

[0004] Currently, the main method for raising the temperature of the mixture is through direct or indirect steam heating. However, these steam heating technologies often rely on manual valve regulation, which suffers from problems such as temperature control lag. They cannot respond quickly and accurately to instantaneous changes in raw material temperature, and are prone to overheating or underheating, resulting in large temperature fluctuations and poor stability in the mixture. Therefore, a new temperature control solution for ultra-thin glass mixtures is urgently needed to address the aforementioned issues of temperature control lag, uncontrollable steam introduction time, and low automation. This would improve the flowability and uniformity of the mixture, effectively solve the problem of excessive surface waviness in glass, and ensure the yield and grade of ultra-thin glass products. Summary of the Invention

[0005] In view of this, the present disclosure provides a temperature control system and a method for ultrathin glass mixture.

[0006] According to a first aspect of this disclosure, an ultra-thin glass mixing material temperature control system is provided, the ultra-thin glass raw material mixing system comprising: a steam generator, a main shut-off valve, a main regulating valve, a raw material mixing chamber, a mixing chamber temperature sensor, and a PLC controller; Steam generated by the steam generator enters the steam pipeline and flows sequentially through the main shut-off valve and the main regulating valve on the steam pipeline into the raw material mixing chamber; the main shut-off valve is used to start and stop the steam pipeline; the mixing chamber temperature sensor is fixed on the raw material mixing chamber, and the main regulating valve and the mixing chamber temperature sensor are electrically connected to the PLC controller respectively; The mixing chamber temperature sensor is used to monitor the temperature of the mixture in the raw material mixing chamber in real time and send the data to the PLC controller; The PLC controller is used to dynamically adjust the opening of the main regulating valve according to the temperature of the mixture to control the steam flow rate entering the raw material mixing chamber, so that the temperature difference between the mixture and the target temperature is stabilized within a preset allowable fluctuation range.

[0007] In some embodiments of the first aspect of this disclosure, the system further includes: a distribution cylinder, a preheating regulating valve, a steam flow stabilizing chamber, a drain valve, a flow stabilizing chamber temperature sensor, a pressure transmitter, and a branch isolation valve. The distribution cylinder has an inlet, a first outlet, and a second outlet. The steam flow stabilizing chamber has an inlet and a liquid outlet. The steam pipeline includes a first steam pipeline, a second steam pipeline, and a third steam pipeline. The outlet of the steam generator is connected to the inlet of the distribution cylinder through the first steam pipeline. The main shut-off valve is disposed on the first steam pipeline and located at... The steam generator's outlet is located between the steam distribution cylinder's inlet and the main shut-off valve, which is used to start and stop the first steam pipeline. The first outlet of the steam distribution cylinder is connected to the inlet of the steam stabilizing chamber via the second steam pipeline. The outlet of the steam stabilizing chamber is connected to the steam trap, which is used to drain the condensate generated in the steam stabilizing chamber. The preheating regulating valve is located on the second steam pipeline between the first outlet of the steam distribution cylinder and the inlet of the steam stabilizing chamber. The second outlet of the steam distribution cylinder is connected to the third steam pipeline. A steam inlet is connected to the raw material mixing chamber. A branch isolation valve and a main regulating valve are installed on the third steam pipeline. The branch isolation valve is located between the second outlet of the gas distribution cylinder and the main regulating valve. The main regulating valve is located between the branch isolation valve and the steam inlet of the raw material mixing chamber. The branch isolation valve is used to start and stop the third steam pipeline. The preheating regulating valve is electrically connected to the PLC controller. The pressure transmitter and the stabilizing chamber temperature sensor are respectively fixed on the steam stabilizing chamber and electrically connected to the PLC controller. The stabilizing chamber temperature sensor is used to monitor the internal temperature of the steam stabilizing chamber in real time and send the data to the PLC controller. The pressure transmitter is used to measure the real-time pressure of the steam stabilizing chamber and send the data to the PLC controller. The PLC controller is also used to close the preheating regulating valve and open the main regulating valve when the steam superheat meets the requirements, based on the internal temperature and real-time pressure of the steam stabilizing chamber, so that the steam generated by the steam generator enters the raw material mixing chamber through the first steam pipeline and the third steam pipeline. In some embodiments of the first aspect of this disclosure, the system further includes: a control terminal, wherein the PLC controller is communicatively connected to the control terminal; the control terminal is configured to provide a human-machine interface and receive a user duration setting instruction through the human-machine interface and transmit it to the PLC controller, wherein the user duration setting instruction carries a first steam inlet duration set by the operator; the PLC controller is further configured to control the opening duration of the main regulating valve according to the user duration setting instruction so that the steam inlet duration of the raw material mixing chamber is the first steam inlet duration.

[0008] According to a second aspect of this disclosure, a method for temperature control of an ultra-thin glass mixture is provided, wherein the method is executed by a PLC controller in the aforementioned ultra-thin glass mixture temperature control system, the method comprising: After the main regulating valve is opened, the current temperature of the mixture in the raw material mixing chamber is obtained as monitored by the mixing chamber temperature sensor; A control signal is generated based on the current mixture temperature, the target temperature, and the preset allowable fluctuation range and sent to the main regulating valve. The main regulating valve adjusts its opening according to the control signal to control the steam flow rate entering the raw material mixing chamber, so that the difference between the mixture temperature and the target temperature is stabilized within the preset allowable fluctuation range.

[0009] In some embodiments of the second aspect of this disclosure, the step of generating a control signal based on the current mixture temperature, the target temperature, and a preset allowable fluctuation range and sending it to the main regulating valve includes: determining a temperature error and a temperature error change rate based on the current mixture temperature and the target temperature; determining a current coefficient correction amount based on the temperature error, the temperature error change rate, the target temperature, and the preset allowable fluctuation range using a fuzzy algorithm, wherein the current coefficient correction amount includes a proportional coefficient correction amount, an integral coefficient correction amount, and a derivative coefficient correction amount; calculating a current control amount based on the proportional coefficient correction amount, the integral coefficient correction amount, and the derivative coefficient correction amount, wherein the current control amount represents the desired opening ratio of the main regulating valve; and converting the current control amount into a control signal and sending it to the main regulating valve.

[0010] In some embodiments of the second aspect of this disclosure, the step of using a fuzzy algorithm to determine the current coefficient correction amount based on the temperature error, the rate of change of the temperature error, the target temperature, and a preset allowable fluctuation range includes: obtaining a fuzzy language description of the temperature error and a fuzzy language description of the rate of change of the temperature error using a pre-set first membership function based on a first fuzzy language label and a second fuzzy language label, wherein the first fuzzy language label and the second fuzzy language label are pre-configured based on the target temperature and the allowable fluctuation range; and performing fuzzy inference using the fuzzy language description of the temperature error and the fuzzy language description of the rate of change of the temperature error based on a pre-configured fuzzy rule base for proportional coefficients, a fuzzy rule base for integral coefficients, and a fuzzy rule base for differential coefficients to obtain the proportional coefficient correction amount, the integral coefficient correction amount, and the differential coefficient correction amount.

[0011] In some embodiments of the second aspect of this disclosure, calculating the current valve opening based on the proportional coefficient correction, integral coefficient correction, and derivative coefficient correction includes: The current proportional coefficient, current integral coefficient, and current differential coefficient are determined based on the aforementioned proportional coefficient correction, integral coefficient correction, and differential coefficient correction. The current control quantity is calculated based on the following formula:

[0012] in, This represents the control quantity at the current time t, which indicates the desired opening ratio of the main control valve at the current time t. This indicates the current scaling factor. Indicates the current integral coefficient. Indicates the current differential coefficient. Represents the current time t This represents the integral of the temperature error from the initial time in the past to the current time t.

[0013] In some embodiments of the second aspect of this disclosure, the method further includes: after receiving a stirring start signal, opening a preheating regulating valve to preheat steam; and after determining that the superheat of the steam meets the requirements based on the internal temperature and real-time pressure of the steam stabilizing chamber, closing the preheating regulating valve and opening the main regulating valve.

[0014] In some embodiments of the second aspect of this disclosure, the step of closing the preheating regulating valve and opening the main regulating valve after determining that the superheat of the steam meets the requirements based on the internal temperature and real-time pressure of the steam flow stabilizing chamber includes: The internal temperature of the steam flow stabilizing chamber and the real-time pressure of the steam flow stabilizing chamber are obtained from the temperature sensor of the flow stabilizing chamber and the pressure transmitter. The current saturation temperature is calculated based on the real-time pressure of the steam flow stabilization chamber; If the temperature difference between the steam stabilizing chamber and the current saturation temperature is within a predetermined range, then the superheat of the steam is determined to meet the requirements, the preheating regulating valve is closed, and the main regulating valve is opened. If the difference between the internal temperature of the steam stabilizing chamber and the current saturation temperature is not within the predetermined range, it is determined that the superheat of the steam does not meet the requirements, and the opening of the preheating regulating valve remains unchanged and the main regulating valve remains closed.

[0015] In some embodiments of the second aspect of this disclosure, the method further includes: receiving a user duration setting instruction from a control terminal, the user duration setting instruction including a first steam inlet duration set by an operator; simultaneously opening the main regulating valve and controlling a preset timer to start timing; and closing the main regulating valve when the timing duration of the preset timer reaches the first steam inlet duration to stop the steam inlet to the raw material mixing chamber.

[0016] The embodiments disclosed herein can achieve precise control of the temperature of ultra-thin glass mixtures, reduce temperature fluctuations in the mixtures, improve temperature stability of the mixtures, and solve problems such as excessive waviness in ultra-thin glass caused by large temperature fluctuations and poor stability of the mixtures. Attached Figure Description

[0017] To more clearly illustrate the technical solutions in the embodiments of this disclosure or the prior art, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this disclosure. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0018] Figure 1 A schematic diagram of the structure of the ultrathin glass mixture temperature control system provided in the embodiments of this disclosure; Figure 2 This is another structural schematic diagram of the ultrathin glass mixture temperature control system provided in the embodiments of this disclosure; Figure 3 This is a schematic flowchart of the temperature control method for ultrathin glass mixtures provided in an embodiment of this disclosure.

[0019] Figure 4 A schematic diagram of the structure of the PLC controller in the ultrathin glass mixing temperature control system provided in the embodiments of this disclosure.

[0020] Explanation of reference numerals in the attached figures: 101. Steam generator; 102. Raw material mixing chamber; 103. Main shut-off valve; 104. Main regulating valve; 105. PLC controller; 106. Mixing chamber temperature sensor; 107. Control terminal; 108. Steam distribution cylinder; 109. Preheating regulating valve; 110. Steam flow stabilizing chamber; 111. Drain valve; 112. Pressure transmitter; 113. Flow stabilizing chamber temperature sensor; 114. Branch isolation valve. Detailed Implementation

[0021] The technical solutions of the embodiments of this disclosure will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this disclosure, and not all embodiments. Based on the embodiments of this disclosure, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this disclosure.

[0022] The terminology used in the embodiments of this disclosure is for the purpose of describing particular embodiments only and is not intended to be limiting of this disclosure. The singular forms “a,” “the,” and “the” as used in the embodiments of this disclosure and the appended claims are also intended to include the plural forms unless the context clearly indicates otherwise.

[0023] Depending on the context, words such as "if," "when," etc., used here can be interpreted as "when," "when," "in response to determination," or "in response to detection." Similarly, depending on the context, the phrases "if determination" or "if detection (of the stated condition or event)" can be interpreted as "when determination," "in response to determination," "when detection (of the stated condition or event)," or "in response to detection (of the stated condition or event)."

[0024] Ultra-thin glass refers to glass with a thickness between 0.1 mm and 1.1 mm. It has a light transmittance of over 90% and extremely low refractive index inhomogeneity. Furthermore, ultra-thin glass has significantly higher mechanical strength than ordinary glass, exhibiting excellent impact resistance, scratch resistance, and bending resistance. In addition, ultra-thin glass has an extremely low coefficient of thermal expansion and high thermal stability. Ultra-thin glass also boasts advantages such as ultra-cleanliness, ultra-flatness, and surface roughness at the nanometer level. However, besides the aforementioned temperature control lag issue, related technologies also suffer from problems such as a lack of coordination between automated and manual modes and uncontrollable steam introduction time. These issues can also lead to large temperature fluctuations and poor stability of the mixture, resulting in excessive waviness in the ultra-thin glass.

[0025] In view of this, the present disclosure provides the following ultra-thin glass mixture temperature control system and ultra-thin glass mixture temperature control method, which can achieve precise control of the temperature of ultra-thin glass mixture, reduce temperature fluctuation of mixture, improve temperature stability of mixture, and solve problems such as excessive waviness of ultra-thin glass caused by large temperature fluctuation and poor stability of mixture.

[0026] Figure 1 A schematic diagram of the structure of the ultrathin glass mixture temperature control system provided in an embodiment of this disclosure is shown. See also Figure 1 The ultrathin glass mixing temperature control system of this disclosure includes: a steam generator 101, a main shut-off valve 103, a main regulating valve 104, a raw material mixing chamber 102, a mixing chamber temperature sensor 106, and a PLC controller 105.

[0027] See Figure 1 Steam generated by steam generator 101 enters the steam pipeline and flows sequentially through the main shut-off valve 103 and the main regulating valve 104 into the raw material mixing chamber 102. A mixing chamber temperature sensor 106 is fixed to the raw material mixing chamber 102. The main regulating valve 104 and the mixing chamber temperature sensor 106 are electrically connected to the PLC controller 105. The mixing chamber temperature sensor 106 can monitor the temperature of the mixture in the raw material mixing chamber 102 in real time and send the data to the PLC controller 105. The PLC controller 105 can dynamically adjust the opening of the main regulating valve 104 according to the mixture temperature to control the steam flow rate into the raw material mixing chamber 102, thereby maintaining the mixture temperature at a preset target temperature.

[0028] In practical applications, the main regulating valve 104 can be selected as a regulating valve with equal percentage flow characteristics. Under the control of the PLC controller 105, the main regulating valve 104 can adjust its own opening to control the steam flow rate entering the raw material mixing chamber 102. The specific implementation process of the PLC controller 105 dynamically adjusting the opening of the main regulating valve 104 according to the temperature of the mixture to control the steam flow rate entering the raw material mixing chamber 102 can be found in the method section below, and will not be repeated here.

[0029] In specific applications, the mixing chamber temperature sensor 106 can be a thermocouple, such as a PT100 resistance temperature detector.

[0030] See Figure 1 The ultra-thin glass mixture temperature control system of this embodiment may further include: a control terminal 107, which is communicatively connected to a PLC controller 105. The control terminal 107 can provide a human-machine interface and receive user duration setting instructions through the interface, transmitting them to the PLC controller 105. The user duration setting instructions carry the first steam inlet duration set by the operator. The PLC controller 105 can also control the opening duration of the main regulating valve 104 according to the user duration setting instructions so that the steam inlet duration of the raw material mixing chamber 102 is the first steam inlet duration. Thus, the steam inlet duration can be dynamically adjusted by the operator, thereby avoiding excessively long or short steam inlet durations and further improving the fluidity and distribution uniformity of the ultra-thin glass mixture.

[0031] In specific applications, the control terminal 107 can be, but is not limited to, an electronic device with a touch screen, such as a computer or host computer, that can be operated by an operator.

[0032] Figure 2 Another structural schematic diagram of the ultrathin glass mixture temperature control system provided in this disclosure embodiment is shown. See also Figure 2 The ultrathin glass mixture temperature control system of this embodiment may further include: a gas distribution cylinder 108, a preheating regulating valve 109, a steam stabilizing chamber 110, a drain valve 111, a stabilizing chamber temperature sensor 113, a pressure transmitter 112, and a branch isolation valve 114. The gas distribution cylinder 108 has an air inlet, a first air outlet, and a second air outlet. The steam stabilizing chamber 110 has an air inlet and a liquid outlet. The steam pipeline includes a first steam pipeline, a second steam pipeline, and a third steam pipeline. The first steam pipeline is divided into a second steam pipeline and a third steam pipeline by the gas distribution cylinder 108.

[0033] See Figure 2The outlet of the steam generator 101 is connected to the inlet of the distribution cylinder 108 through the first steam pipeline. The main shut-off valve 103 is installed on the first steam pipeline and located between the outlet of the steam generator 101 and the inlet of the distribution cylinder 108. The main shut-off valve 103 can be used to start and stop the first steam pipeline.

[0034] See Figure 2 The first outlet of the gas distribution cylinder 108 is connected to the inlet of the steam stabilizing chamber 110 through the second steam pipeline. The outlet of the steam stabilizing chamber 110 is connected to the drain valve 111. The drain valve 111 is used to discharge the condensate generated by the steam stabilizing chamber 110. The preheating regulating valve 109 is set on the second steam pipeline and located between the first outlet of the gas distribution cylinder 108 and the inlet of the steam stabilizing chamber 110. See Figure 2 The second outlet of the gas distribution cylinder 108 is connected to the steam inlet of the raw material mixing chamber 102 through the third steam pipeline. The branch isolation valve 114 and the main regulating valve 104 are installed on the third steam pipeline. The branch isolation valve 114 is located between the second outlet of the gas distribution cylinder 108 and the main regulating valve 104. The main regulating valve 104 is located between the branch isolation valve 114 and the steam inlet of the raw material mixing chamber 102. The branch isolation valve 114 is used to start and stop the third steam pipeline.

[0035] See Figure 2 The preheating regulating valve 109 is electrically connected to the PLC controller 105. The pressure transmitter 112 and the stabilizing chamber temperature sensor 113 are respectively fixed on the steam stabilizing chamber 110 and electrically connected to the PLC controller 105. The stabilizing chamber temperature sensor 113 is used to monitor the internal temperature of the steam stabilizing chamber 110 in real time and send it to the PLC controller 105. The pressure transmitter 112 is used to measure the real-time pressure of the steam stabilizing chamber 110 and send it to the PLC controller 105.

[0036] See Figure 2 The PLC controller 105 can also be used to control the preheating regulating valve 109 to close and the main regulating valve 104 to open when the steam superheat meets the requirements based on the internal temperature and real-time pressure of the steam stabilizing chamber 110. This allows the steam generated by the steam generator 101 to enter the raw material mixing chamber 102 through the first steam pipeline and the third steam pipeline.

[0037] The specific implementation process of the PLC controller 105 controlling the preheating regulating valve 109 and the main regulating valve 104 according to the internal temperature and real-time pressure of the steam stabilizing chamber 110 can be found in the method section below, and will not be repeated here.

[0038] Therefore, by setting up a gas distribution structure and a steam preheating structure in the ultra-thin glass mixture temperature control system, the interference of condensate can be effectively avoided, ensuring that the steam entering the raw material mixing chamber 102 is dried to saturation, thereby further improving the uniformity of the distribution of the ultra-thin glass mixture.

[0039] The main shut-off valve 103 can be a manual valve, with both fully open and fully closed states. When the main shut-off valve 103 is in the fully open state, the first steam pipeline is started; when the main shut-off valve 103 is in the fully closed state, the first steam pipeline is stopped.

[0040] Branch isolation valve 114 can be a manual valve with two states: fully open and fully closed. When branch isolation valve 114 is in the fully open state, the third steam pipeline is started; when branch isolation valve 114 is in the fully closed state, the third steam pipeline is stopped.

[0041] The main shut-off valve 103 and the branch isolation valve 114 can also be remotely controlled. For example, the main shut-off valve 103 and the branch isolation valve 114 can also be electrically connected to the PLC controller 105 respectively. The PLC controller 105 can be used to control the opening and closing of the main shut-off valve 103 and / or the branch isolation valve 114 according to the user start and stop commands from the control terminal 107, so as to realize the remote control of the main shut-off valve 103 and the branch isolation valve 114.

[0042] In practical applications, the main shut-off valve 103 and the branch isolation valve 114 can be normally open. In cases such as fault detection or equipment maintenance requiring shutdown, the main shut-off valve 103 can be manually closed or remotely controlled to ensure safety. Similarly, if the main regulating valve 104 on the third steam pipeline malfunctions or requires maintenance, the branch isolation valve 114 can be manually closed or remotely controlled to ensure safety.

[0043] The steam flow stabilizing chamber 110 is a pressure vessel with an insulation layer, which provides a place for the flowing steam to release heat and maintain a stable state. The steam trap 111 can be installed in the steam flow stabilizing chamber 110 and at the lowest point of the second steam pipeline. It can include a thermostatic steam trap, which can automatically and continuously discharge condensate while preventing steam loss.

[0044] The preheating regulating valve 109 can be selected as an on / off valve, a small-diameter regulating valve, or a regulating valve with equal percentage flow characteristics, and is used to control the steam flow rate entering the second steam pipeline during the steam preheating stage. The opening degree of the preheating regulating valve 109 can be set to a fixed value, or it can be flexibly controlled by the PLC controller 105 based on the internal temperature of the steam stabilizing chamber 110.

[0045] The temperature sensor 113 of the steam flow stabilization chamber can be installed on the upper cavity sidewall near the air inlet of the steam flow stabilization chamber 110. This location offers good steam flow, avoiding direct impact and excessive condensation at the inlet, while also representing the temperature of the steam about to enter the main pipeline. This allows for rapid and accurate measurement of the true temperature of the steam within the steam flow stabilization chamber 110. For example, the temperature sensor 113 can be inserted into a mounting sleeve, which is fixed to the upper cavity sidewall near the air inlet of the steam flow stabilization chamber 110 by threads or flanges, facilitating future maintenance or replacement. In some examples, the sensing end of the temperature sensor 113 extends a predetermined length into the cavity of the steam flow stabilization chamber 110, for example, exceeding the sleeve diameter by 8-10 times, to ensure that the temperature sensor 113 accurately senses the temperature of the medium inside the steam flow stabilization chamber 110, rather than the temperature cooled by the cavity wall.

[0046] The pressure transmitter 112 can be installed on the upper cavity sidewall or top near the steam outlet of the steam stabilizing cavity 110 to prevent condensate from accumulating in the pressure tapping pipe, while ensuring that the pressure transmitter 112 can measure the steam pressure inside the steam stabilizing cavity 110 rather than the water pressure.

[0047] In specific applications, the temperature sensor 113 of the steady flow cavity can be selected from, but is not limited to, a vibration-resistant and stable sensor such as Pt100 platinum resistance thermometer, and the pressure transmitter 112 can be an industrial-grade pressure transmitter 112.

[0048] The steam pipeline is divided into a second steam pipeline for steam preheating and a third steam pipeline for supplying steam to the raw material mixing chamber 102 by the steam distribution cylinder 108. After the preheating regulating valve 109 on the second steam pipeline is opened, a small amount of steam is introduced into the second steam pipeline. The steam enters the steam stabilizing chamber 110 through the second steam pipeline. The low temperature chamber of the steam stabilizing chamber 110 and the low temperature preheating pipeline will cause this part of the steam to condense rapidly. The condensate is automatically discharged through the drain valve 111. Steam is introduced into the raw material mixing chamber 102 only after the superheat of the steam in the entire steam pipeline meets the requirements. In this way, condensate can be prevented from entering the third steam pipeline and the raw material mixing chamber 102 from the source, ensuring that the steam supplied to the raw material mixing chamber 102 is stable, dry (i.e., without water droplets) high-quality saturated steam, thereby further improving the uniformity of the mixture distribution.

[0049] In practical applications, steam output from steam generator 101 may travel a long distance to reach the raw material mixing chamber. In cold environments such as northern winters, the temperature of the steam pipeline is far below the steam saturation temperature, causing a large amount of steam to condense into water upon contact with the pipe wall. This leads to the following problems: 1) The steam entering the raw material mixing chamber is wet steam carrying condensate, resulting in a low effective heating enthalpy and low thermal efficiency; 2) The condensate impacts the mixture, potentially causing localized over-wetting or sudden temperature changes, leading to inaccurate control; 3) Condensate accumulation can easily cause water hammer, damaging valves and pipelines and exacerbating corrosion. The embodiments of this disclosure, through the aforementioned second steam pipeline and the steam preheating structure formed thereon, can effectively solve these problems.

[0050] Upon receiving the stirring start signal, the PLC controller 105 first opens the preheating regulating valve 109. Steam generated by the steam generator 101 flows through the first and second steam pipelines into the preheating stabilizing chamber. The stabilizing chamber temperature sensor 113 continuously monitors the internal temperature of the steam stabilizing chamber 110 until the temperature reaches the target. Once the internal temperature of the steam stabilizing chamber 110 reaches the target, the PLC controller 105 opens the main regulating valve 104. Steam from the steam generator 101 then flows through the first and third steam pipelines into the raw material mixing chamber 102. Simultaneously, based on the temperature of the mixture in the raw material mixing chamber 102 fed back by the mixing chamber temperature sensor 106, the PLC controller dynamically controls the opening of the main regulating valve 104 using a fuzzy PID algorithm to control the steam flow rate into the raw material mixing chamber 102, thereby achieving precise temperature control of the raw material mixing chamber 102.

[0051] Figure 3 This diagram illustrates a flow chart of a temperature control method for ultrathin glass mixtures provided in an embodiment of this disclosure. This temperature control method for ultrathin glass mixtures can be achieved through the aforementioned... Figure 1 and Figure 2 The PLC controller 105 of the ultra-thin glass mixture temperature control system shown is executed.

[0052] See Figure 3 The temperature control method for ultrathin glass mixtures according to embodiments of this disclosure may include the following steps: Step 301: After the main regulating valve 104 is opened, the current temperature of the mixture in the raw material mixing chamber 102 is obtained by the temperature sensor 106 of the mixing chamber. Step 302: A control signal is generated based on the current mixture temperature and the target temperature and sent to the main regulating valve 104. The main regulating valve 104 adjusts its opening according to the control signal to control the steam flow rate entering the raw material mixing chamber 102 so that the temperature difference between the mixture and the target temperature is stabilized within the preset allowable fluctuation range.

[0053] In practical applications, the target temperature can be, but is not limited to, 30℃~40℃. For example, the target temperature can be set to 30℃, 35℃, 40℃, etc. The allowable fluctuation range of the target temperature can be preset as needed. For example, the allowable fluctuation range can be set to ±10℃, ±5℃, ±3℃, etc.

[0054] See Figure 3 In addition to the aforementioned steps 301 to 302, the ultrathin glass mixture temperature control method of this disclosure may also include: step 300, after receiving the stirring start signal, opening the preheating regulating valve 109 to preheat the steam, and after determining that the superheat of the steam meets the requirements based on the internal temperature and real-time pressure of the steam stabilizing chamber 110, closing the preheating regulating valve 109 and opening the main regulating valve 104.

[0055] Specifically, step 300 may include: after opening the preheating regulating valve 109, acquiring the internal temperature and real-time pressure of the steam stabilizing chamber 110 from the stabilizing chamber temperature sensor 113 and the pressure transmitter 112; calculating the current saturation temperature based on the real-time pressure of the steam stabilizing chamber 110; if the difference between the internal temperature of the steam stabilizing chamber 110 and the current saturation temperature is within a predetermined range, the superheat of the steam meets the requirements, and the inner wall of the entire steam pipeline from the steam distributor to the inlet of the raw material mixing chamber 102 has been fully preheated, and the steam will no longer condense in large quantities during transportation, that is, the system is in a "steam ready" state, at which time the preheating regulating valve 109 can be closed and the main regulating valve 104 can be opened; if the difference between the internal temperature of the steam stabilizing chamber 110 and the current saturation temperature is not within a predetermined range, the superheat of the steam does not meet the requirements, and the opening of the preheating regulating valve 109 remains unchanged and the main regulating valve 104 remains closed. Thus, steam preheating can ensure that the steam entering the raw material mixing chamber 102 is stable, dry, and of high quality.

[0056] Furthermore, if the temperature difference between the steam stabilizing chamber 110 and the current saturation temperature remains stable within the aforementioned predetermined range for a predetermined period of time, the steam superheat is considered to meet the requirements. The preheating regulating valve 109 is then closed, and the main regulating valve 104 is opened. If the temperature difference between the steam stabilizing chamber 110 and the current saturation temperature fails to remain stable within the aforementioned predetermined range for a predetermined period of time, the steam superheat is considered not to meet the requirements. The opening of the preheating regulating valve 109 remains unchanged, and the main regulating valve 104 remains closed. Steam preheating continues until the steam superheat meets the requirements. Thus, by incorporating a time-based condition, the steam superheat can be precisely controlled, further improving the quality of the steam entering the raw material mixing chamber 102.

[0057] In practical applications, the aforementioned predetermined range can be flexibly set according to actual needs. For example, the predetermined range can be set to ±1℃ to ±4℃. In scenarios where high quality requirements for ultra-thin glass are necessary, the predetermined range can be set to ±1℃ to ±2℃.

[0058] Steam preheating avoids the risk of sudden localized temperature changes and raw material agglomeration caused by condensate entering the raw material mixing chamber 102, ensuring the mixing uniformity of the raw material mixing chamber 102. Simultaneously, the heating efficiency of dry saturated steam is far higher than that of wet steam, making the relationship between the valve opening of the main regulating valve 104 and the heat input to the raw material mixing chamber 102 more precise, fundamentally improving the controllability of the ultra-thin glass mixture temperature. Furthermore, the steam preheating and condensation functions protect the main regulating valve 104 and the actuator from water hammer impact and corrosion, extending their service life.

[0059] Furthermore, the method in this embodiment may also include: the PLC controller 105 records the internal temperature of the steam stabilizing chamber 110 collected by the temperature sensor 113, performs energy efficiency analysis and fault warning based on the previously recorded historical internal temperature of the steam stabilizing chamber 110, thereby timely detecting and warning of conditions such as abnormally long preheating time that may indicate a fault in the steam trap 111 or insulation damage.

[0060] Further, in step 302, the temperature error and the rate of change of temperature error can be determined based on the current mixture temperature and the target temperature. A fuzzy algorithm is used to determine the current coefficient correction amount based on the temperature error, the rate of change of temperature error, the target temperature and the preset allowable fluctuation range. The current coefficient correction amount includes the proportional coefficient correction amount, the integral coefficient correction amount and the derivative coefficient correction amount. Then, the current control amount is calculated based on the proportional coefficient correction amount, the integral coefficient correction amount and the derivative coefficient correction amount. The current control amount represents the opening ratio that the main regulating valve 104 is expected to achieve. Finally, the current control amount is converted into a control signal and sent to the main regulating valve 104.

[0061] The temperature error is the difference between the current mixture temperature and the target temperature. A positive temperature error indicates that the current mixture temperature is higher than the target temperature, while a negative temperature error indicates that the current mixture temperature is lower than the target temperature. The rate of change of temperature error is the difference between the current temperature error and the temperature error at the previous moment, representing the trend and speed of temperature change in the mixture.

[0062] In some examples, fuzzy rule bases can be configured for proportional coefficients, integral coefficients, and differential coefficients respectively, and fuzzy inference can be performed separately to determine the corresponding coefficient correction amounts.

[0063] Specifically, determining the current coefficient correction amount using a fuzzy algorithm based on temperature error, temperature error change rate, target temperature, and a preset allowable fluctuation range may include: obtaining a fuzzy linguistic description of the temperature error and a fuzzy linguistic description of the temperature error change rate using a pre-set first membership function based on a first fuzzy linguistic label and a second fuzzy linguistic label, wherein the first fuzzy linguistic label and the second fuzzy linguistic label are pre-configured based on the target temperature and the allowable fluctuation range; and performing fuzzy inference using the fuzzy linguistic description of the temperature error and the fuzzy linguistic description of the temperature error change rate based on a pre-configured fuzzy rule base for the proportional coefficient, the integral coefficient, and the differential coefficient, to obtain the proportional coefficient correction amount, the integral coefficient correction amount, and the differential coefficient correction amount.

[0064] The system allows for pre-configuration of fuzzy rule bases for proportional coefficients, integral coefficients, and differential coefficients. Each fuzzy rule base is an "if...then..." rule base based on expert experience. Each fuzzy rule base includes multiple fuzzy rules configured based on expert experience. Each fuzzy rule includes a condition and a conclusion. Each conclusion can correspond to a fuzzy set, which is a fuzzy subset of the corresponding coefficient correction amount. This fuzzy subset is defined by a second membership function on the universe of discourse of the corresponding coefficient correction amount. The universe of discourse for the correction amount of each of the proportional, integral, and differential coefficients can be pre-configured.

[0065] The temperature error domain and the temperature error rate of change domain can be pre-determined based on the target temperature and its allowable fluctuation range. Semantic partitioning of the temperature error domain yields a first fuzzy linguistic label, and semantic partitioning of the temperature error rate of change domain yields a second fuzzy linguistic label. Both the first and second fuzzy linguistic labels are linguistic values. Each first fuzzy linguistic label corresponds to a temperature error value interval, which is a subinterval of the temperature error domain. Each second fuzzy linguistic label corresponds to a temperature error rate of change value interval, which is a subinterval of the temperature error rate of change domain.

[0066] For example, the first fuzzy language label may include, but is not limited to, negative large (current mixture temperature is much lower than the target temperature), negative small (current mixture temperature is slightly lower than the target temperature), zero (current mixture temperature is near the target temperature), positive small (current mixture temperature is slightly higher than the target temperature), and positive large (current mixture temperature is much higher than the target temperature). For example, the second fuzzy language label may include: "rapidly decreasing", "slowly decreasing", "unchanged", "slowly increasing", and "rapidly increasing".

[0067] For example, if the target temperature is 35°C and the allowable fluctuation range is ±2°C, considering that the ultra-thin glass mixture temperature control system starts from ambient temperature, the maximum possible error could reach approximately ±10°C. To allow for this margin, the temperature error domain can be set to [-15, +15] °C. In practical applications, the temperature error domain can cover all possible operating conditions.

[0068] The membership degree of temperature error to each first fuzzy language tag is calculated using a pre-configured first membership function. The membership degree of temperature error change rate to each second fuzzy language tag is also calculated using the same first membership function. The membership degree of temperature error to each first fuzzy language tag indicates the degree to which the temperature error belongs to that first fuzzy language tag, and the membership degree of temperature error change rate to each second fuzzy language tag indicates the degree to which the temperature error change rate belongs to that second fuzzy language tag. The combination of the membership degree of temperature error to each first fuzzy language tag and the corresponding first fuzzy language tag can serve as a fuzzy linguistic description of the temperature error, and the combination of the membership degree of temperature error change rate to each second fuzzy language tag and the corresponding second fuzzy language tag can serve as a fuzzy linguistic description of the temperature error change rate.

[0069] For example, if the first fuzzy language label includes negative large, negative small, zero, positive small, and positive large, the membership degree of the temperature error to "positive small" can be calculated using the first membership function as follows: 0.72; 0.28; 0; 0; 0; and 0.0. The fuzzy language description of the temperature error can be: {(positive large, 0);(positive small, 0.72);(zero, 0.28);(negative small, 0);(negative large, 0)}. This indicates that the current temperature error can be described as "positive small" to a certain extent, "zero" to a certain extent, and does not belong to any other description.

[0070] In practical applications, the first membership function and the second membership function can be, but are not limited to, triangular membership functions, trapezoidal membership functions, Gaussian membership functions, etc.

[0071] The process iterates through each fuzzy rule in the pre-configured proportional coefficient fuzzy rule library: Calculate the activation strength of the fuzzy rule, taking the minimum membership degree among the conditions of the fuzzy rule as the activation strength, and using this activation strength to trim the fuzzy set of the conclusion of the fuzzy rule to obtain the trimmed fuzzy set of the fuzzy rule. After obtaining the trimmed fuzzy set of each fuzzy rule, the trimmed fuzzy sets of all fuzzy rules in the proportional coefficient fuzzy rule library are synthesized to obtain the comprehensive output fuzzy set of the proportional coefficient. The comprehensive output fuzzy set of the proportional coefficient is then defuzzified to obtain the proportional coefficient correction amount.

[0072] The scaling-summing method can be used to synthesize the cropped fuzzy sets of all fuzzy rules in the proportional coefficient fuzzy rule base to obtain the comprehensive output fuzzy set of the proportional coefficient. The comprehensive output fuzzy set of the proportional coefficient includes all possible values ​​of the proportional coefficient and the membership degree of each possible value. The membership degree of each possible value indicates the credibility of the possible value being recommended by all fuzzy rules.

[0073] The comprehensive output fuzzy set of the scaling factor is defuzzified to obtain the numerical value of the scaling factor correction. For example, the centroid method can be used to calculate the abscissa value corresponding to the centroid of the data distribution corresponding to the comprehensive output fuzzy set of the scaling factor; this abscissa value is the numerical value of the scaling factor correction. That is, the numerical value of the scaling factor correction is obtained by weighting all possible values ​​in the comprehensive output fuzzy set of the scaling factor according to their membership degrees.

[0074] The correction amounts for integral coefficients and differential coefficients are obtained in the same way as the correction amounts for proportional coefficients mentioned above, and will not be repeated here.

[0075] By using a fuzzy algorithm, the proportional, integral, and derivative coefficients can be dynamically adjusted based on real-time temperature errors and their rate of change, achieving optimal coordination among these coefficients under the current operating conditions. Adjusting these coefficients allows for smoother output from the PLC controller 105, further reducing fluctuations in steam flow and temperature within the raw material mixing chamber 102, and ultimately improving the uniformity of the ultra-thin glass mixture.

[0076] After adding steam preheating in subsequent step 300, the steam drying process becomes stable, and the relationship between the valve opening of the main regulating valve 104 and the actual enthalpy value entering the raw material mixing chamber 102 becomes more linear and predictable, effectively improving control accuracy. Furthermore, by adding steam preheating and simultaneously adjusting minute parameters using a fuzzy algorithm, the accuracy and stability of the ultra-thin glass mixture temperature control can be further improved.

[0077] In step 302, the current proportional coefficient, current integral coefficient, and current derivative coefficient can be determined based on the proportional coefficient correction amount, integral coefficient correction amount, and derivative coefficient correction amount. Then, the current control quantity is obtained through PID calculation. The current control quantity obtained in this way is smoother, which can effectively reduce steam fluctuations and achieve more stable temperature control of the mixture.

[0078] Specifically, the current proportional coefficient can be obtained by adding the proportional coefficient correction amount of the previous time step to the proportional coefficient correction amount of the current time step, the current integral coefficient can be obtained by adding the integral coefficient correction amount of the previous time step to the integral coefficient correction amount of the current time step, and the current differential coefficient can be obtained by adding the differential coefficient correction amount of the previous time step to the differential coefficient correction amount of the current time step.

[0079] Specifically, obtaining the current control quantity through PID calculation can include: calculating the current control quantity based on the following formula.

[0080]

[0081] in, This represents the control quantity at the current time t. This indicates the current temperature error.

[0082] in, This represents the proportionality coefficient, indicating the strength of the response to the current temperature error. This is a proportional term, representing the immediate response to the current temperature error. The larger the temperature error, the larger the proportional term output, and the wider the main regulating valve 104 opens.

[0083] Let be the integral variable, representing any point in time from the initial moment in the past to the current moment t. This represents the integral of the temperature error, that is, the cumulative sum of the temperature error from the initial time in the past to the current time t. For example, if the temperature error has existed for the past 2 minutes... The value will increase over time.

[0084] The integral coefficient represents the strength of the correction for "cumulative error" and determines the system's tolerance for "long-term failure to meet standards". This is the integral term, specifically used to eliminate residual small errors that the proportional term cannot eliminate. For example, when the temperature adjusted by the proportional term has a steady-state error compared to the target temperature, it can be eliminated by... The valve of the main regulating valve 104 can be opened slowly and continuously until the steady-state error is completely eliminated.

[0085] The differential of the temperature error, also known as the rate of change of the temperature error, represents the trend and speed of temperature change. The differential coefficient represents the prediction and suppression of the "trend of change," and can determine whether to suppress the "rapidly rising" trend in advance. This represents the differential term, used to predict future error trends and suppress potential overshoot or oscillations. For example, when a rapid rise in the mixture temperature is detected, the differential term will output a command to "close the main regulating valve 104" to prevent the mixture temperature from exceeding the target temperature in advance.

[0086] The current control quantity is a percentage value, which represents the expected opening ratio of the main regulating valve 104. This current control quantity can be converted into a control signal in the form of, for example, current signal or voltage signal, and sent to the main regulating valve 104. After receiving the control signal, the main regulating valve 104 adjusts its own valve opening according to the expected opening ratio and returns a feedback signal to the PLC control after adjustment. The feedback signal indicates the actual valve opening after adjustment.

[0087] In practical applications, after the stirring start signal triggers the mixture temperature control program, the PLC control can first perform parameter initialization, that is, load a set of default proportional coefficients, integral coefficients and derivative coefficients. Initially, the valve opening of the main regulating valve 104 is controlled using the default proportional coefficients, integral coefficients and derivative coefficients to ensure safety and stability in the initial stage of startup.

[0088] Furthermore, the method in this embodiment may further include: receiving a user duration setting instruction from a control terminal 107, the user duration setting instruction including a first steam supply duration set by the operator; simultaneously opening the main regulating valve 104 and controlling a preset timer to start timing; and closing the main regulating valve 104 when the preset timer reaches the first steam supply duration to stop supplying steam to the raw material mixing chamber 102. This allows the operator to easily control the steam supply duration to the raw material mixing chamber 102 manually.

[0089] The control terminal 107 can provide a human-machine interface, which can provide start / stop buttons for the preheating regulating valve 109 and the main shut-off valve 103. It can also provide input boxes for parameters such as steam introduction time, target temperature, heating rate, and initial valve opening of the main regulating valve 104, so as to facilitate the operator to manually control the temperature control of the ultra-thin glass mixture.

[0090] Furthermore, the human-machine interface can also provide mode selection buttons, system start / stop buttons, etc. Operators can switch between manual mode, automatic mode, and stop mode using the mode selection buttons, and can start or stop the ultra-thin glass mixing temperature control system using the system start / stop buttons. Therefore, this embodiment supports multiple operating modes, balancing automation and manual intervention requirements, and can better adapt to the needs of industrialized ultra-thin glass production.

[0091] In automatic mode, the PLC controller 105 can control the steam supply duration of the raw material mixing chamber 102 according to the pre-configured second steam supply duration. Specifically, after starting the main regulating valve 104, the PLC controller 105 can start a timer. If the timer duration has not reached the second steam supply duration, the aforementioned temperature control will be executed normally. When the timer duration reaches the second steam supply duration, the main regulating valve 104 will be forcibly closed to stop the steam supply to the raw material mixing chamber 102.

[0092] In manual mode, the PLC controller 105 can control the steam introduction duration of the raw material mixing chamber 102 according to the first steam introduction duration in the user duration setting instruction.

[0093] The emergency stop button on the human-machine interface should be directly connected to the hardware interrupt input point of the PLC controller 105 or used as the highest priority logic signal. When triggered, it should immediately close all valves regardless of the mode of the PLC controller 105, and the ultra-thin glass mixing temperature control system should stop working.

[0094] Furthermore, the human-machine interface can also display the current mixture temperature, the mixture temperature change curve, the actual valve opening of the main regulating valve 104, the current PID parameters (i.e., proportional coefficient, integral coefficient, and derivative coefficient), alarm information, etc., in real time, so that the operator can understand the status of the ultra-thin glass mixture temperature control system in real time.

[0095] The embodiments disclosed herein can achieve precise temperature control of ultra-thin glass mixtures, effectively solving the problem of excessive waviness in ultra-thin glass caused by low raw material temperatures in northern winters, and improving product yield. Experimental data show that the method of the embodiments disclosed herein can increase the product yield of ultra-thin glass from 82% to 95%, and the operation is flexible and adaptable to different working conditions.

[0096] Furthermore, the embodiments disclosed herein can effectively solve the problem that the low winter temperatures in northern regions cause steam to easily form condensate, thus affecting the temperature control efficiency of ultrathin glass mixtures.

[0097] Meanwhile, the embodiments of this disclosure use a combination of fuzzy control and PID calculation to achieve precise control of the mixture temperature, which can effectively reduce the impact of steam inlet fluctuations on the temperature fluctuation and stability of the mixture, improve the fluidity and distribution uniformity of the mixture, thereby further improving the yield of ultra-thin glass products and reducing problems such as excessive waviness of ultra-thin glass.

[0098] Figure 4 A structural example diagram of the PLC controller 105 in the ultrathin glass mixing temperature control system provided in this embodiment of the disclosure is shown. See also Figure 4 The PLC controller 105 may include a processor 401 and a memory 402. The memory 402 stores a computer program. When the computer program is run by the processor 401, it causes the processor 401 to execute the above-mentioned ultra-thin glass mixture temperature control method.

[0099] The processor 401 may be a central processing unit (CPU) or other form of processing unit with data processing capabilities and / or instruction execution capabilities.

[0100] The memory 402 may include one or more computer program products, which may include various forms of computer-readable storage media, such as volatile memory and / or non-volatile memory. The volatile memory may include, for example, random access memory (RAM) and / or cache memory. The non-volatile memory may include, for example, read-only memory (ROM), hard disk, flash memory, etc. One or more computer programs may be stored on the computer-readable storage medium, and the processor 401 may run the programs to implement the ultrathin glass mixture temperature control method described in this embodiment of the present disclosure.

[0101] In addition to the methods and devices described above, embodiments of this disclosure may also be computer program products, including computer program instructions that, when executed by a processor, cause the processor to perform the steps in the ultrathin glass mixture temperature control method of embodiments of this disclosure.

[0102] The computer program product can be written in any combination of one or more programming languages ​​to perform the operations of the embodiments of this disclosure. The programming languages ​​include object-oriented programming languages ​​such as Java and C++, as well as conventional procedural programming languages ​​such as C or similar languages. The program code can be executed entirely on a user's computing device, partially on a user's computing device, as a standalone software package, partially on a user's computing device and partially on a remote computing device, or entirely on a remote computing device or server.

[0103] Furthermore, embodiments of this disclosure may also be computer-readable storage media storing computer program instructions that, when executed by a processor, cause the processor to perform the steps in the ultrathin glass mixture temperature control method provided in embodiments of this disclosure.

[0104] The computer-readable storage medium may be any combination of one or more readable media. A readable medium may be a readable signal medium or a readable storage medium. A readable storage medium may be, for example, an electrical, magnetic, optical, electromagnetic, infrared, or semiconductor system, apparatus, or device, or any combination thereof. More specific examples of readable storage media (a non-exhaustive list) include: an electrical connection having one or more wires, a portable disk, a hard disk, random access memory (RAM), read-only memory (ROM), erasable programmable read-only memory (EPROM or flash memory), optical fiber, portable compact disk read-only memory (CD-ROM), optical storage device, magnetic storage device, or any suitable combination thereof.

[0105] The technical solutions provided in this disclosure have been described in detail above. Specific examples have been used to illustrate the principles and implementation methods of this disclosure. The descriptions of the embodiments above are only for the purpose of helping to understand the methods and core ideas of this disclosure. Furthermore, those skilled in the art will recognize that, based on the ideas of this disclosure, there will be changes in the specific implementation methods and application scope. Therefore, the content of this specification should not be construed as a limitation of this disclosure.

[0106] The above description is merely a preferred embodiment of this disclosure and is not intended to limit this disclosure. Any modifications or equivalent substitutions made within the spirit and principles of this disclosure should be included within the scope of protection of this disclosure.

Claims

1. A temperature control system for an ultra-thin glass mixture, characterized in that, The ultra-thin glass raw material mixing system includes: a steam generator, a main shut-off valve, a main regulating valve, a raw material mixing chamber, a mixing chamber temperature sensor, and a PLC controller; Steam generated by the steam generator enters the steam pipeline and flows sequentially through the main shut-off valve and the main regulating valve on the steam pipeline into the raw material mixing chamber; the main shut-off valve is used to start and stop the steam pipeline; the mixing chamber temperature sensor is fixed on the raw material mixing chamber, and the main regulating valve and the mixing chamber temperature sensor are electrically connected to the PLC controller respectively; The mixing chamber temperature sensor is used to monitor the temperature of the mixture in the raw material mixing chamber in real time and send the data to the PLC controller; The PLC controller is used to dynamically adjust the opening of the main regulating valve according to the temperature of the mixture to control the steam flow rate entering the raw material mixing chamber, so that the temperature difference between the mixture and the target temperature is stabilized within a preset allowable fluctuation range.

2. The system according to claim 1, characterized in that, The system also includes: a gas distribution cylinder, a preheating regulating valve, a steam flow stabilizing chamber, a drain valve, a flow stabilizing chamber temperature sensor, a pressure transmitter, and a branch isolation valve. The gas distribution cylinder has an air inlet, a first air outlet, and a second air outlet. The steam flow stabilizing chamber has an air inlet and a liquid outlet. The steam pipeline includes a first steam pipeline, a second steam pipeline, and a third steam pipeline. The outlet of the steam generator is connected to the inlet of the gas distribution cylinder through the first steam pipeline. The main shut-off valve is installed on the first steam pipeline and located between the outlet of the steam generator and the inlet of the gas distribution cylinder. The main shut-off valve is used to start and stop the first steam pipeline. The first outlet of the gas distribution cylinder is connected to the inlet of the steam stabilizing chamber through the second steam pipeline. The outlet of the steam stabilizing chamber is connected to the steam trap. The steam trap is used to discharge the condensate generated by the steam stabilizing chamber. The preheating regulating valve is installed on the second steam pipeline and located between the first outlet of the gas distribution cylinder and the inlet of the steam stabilizing chamber. The second outlet of the gas distribution cylinder is connected to the steam inlet of the raw material mixing chamber through the third steam pipeline. The branch isolation valve and the main regulating valve are installed on the third steam pipeline. The branch isolation valve is located between the second outlet of the gas distribution cylinder and the main regulating valve. The main regulating valve is located between the branch isolation valve and the steam inlet of the raw material mixing chamber. The branch isolation valve is used to start and stop the third steam pipeline. The preheating regulating valve is electrically connected to the PLC controller. The pressure transmitter and the steam stabilizing chamber temperature sensor are respectively fixed on the steam stabilizing chamber and electrically connected to the PLC controller. The steam stabilizing chamber temperature sensor is used to monitor the internal temperature of the steam stabilizing chamber in real time and send it to the PLC controller. The pressure transmitter is used to measure the real-time pressure of the steam stabilizing chamber and send it to the PLC controller. The PLC controller is also used to close the preheating regulating valve and open the main regulating valve when the steam superheat meets the requirements based on the internal temperature and real-time pressure of the steam stabilizing chamber. This allows the steam generated by the steam generator to enter the raw material mixing chamber through the first steam pipeline and the third steam pipeline.

3. The system according to claim 1, characterized in that, The system further includes a control terminal, and the PLC controller is communicatively connected to the control terminal; The control terminal is used to provide a human-machine interface and receive user duration setting instructions through the human-machine interface and transmit them to the PLC controller. The user duration setting instructions carry the first steam inlet duration set by the operator. The PLC controller is also used to control the opening duration of the main regulating valve according to the user duration setting instruction so that the steam introduction duration of the raw material mixing chamber is the first steam introduction duration.

4. A method for temperature control of an ultrathin glass mixture, characterized in that, The ultrathin glass mixture temperature control method is executed by a PLC controller in the ultrathin glass mixture temperature control system according to any one of claims 1 to 3, the method comprising: After the main regulating valve is opened, the current temperature of the mixture in the raw material mixing chamber is obtained as monitored by the mixing chamber temperature sensor; A control signal is generated based on the current mixture temperature, the target temperature, and the preset allowable fluctuation range and sent to the main regulating valve. The main regulating valve adjusts its opening according to the control signal to control the steam flow rate entering the raw material mixing chamber, so that the difference between the mixture temperature and the target temperature is stabilized within the preset allowable fluctuation range.

5. The method according to claim 4, characterized in that, The step of generating a control signal based on the current mixture temperature, the target temperature, and the preset allowable fluctuation range, and sending it to the main regulating valve, includes: The temperature error and the rate of change of temperature error are determined based on the current mixture temperature and the target temperature. A fuzzy algorithm is used to determine the current coefficient correction amount based on the temperature error, the rate of change of the temperature error, the target temperature, and the preset allowable fluctuation range. The current coefficient correction amount includes the proportional coefficient correction amount, the integral coefficient correction amount, and the derivative coefficient correction amount. The current control quantity is calculated based on the proportional coefficient correction, integral coefficient correction, and derivative coefficient correction. The current control quantity represents the desired opening ratio of the main control valve. The current control quantity is converted into a control signal and sent to the main regulating valve.

6. The method according to claim 5, characterized in that, The step of using a fuzzy algorithm to determine the current coefficient correction amount based on the temperature error, the rate of change of the temperature error, the target temperature, and a preset allowable fluctuation range includes: Based on the first fuzzy language label and the second fuzzy language label, a fuzzy language description of the temperature error and a fuzzy language description of the temperature error change rate are obtained using a pre-set first membership function. The first fuzzy language label and the second fuzzy language label are pre-configured based on the target temperature and the allowable fluctuation range. Based on the pre-configured fuzzy rule bases for proportional coefficients, integral coefficients, and differential coefficients, fuzzy inference is performed using the fuzzy language description of the temperature error and the fuzzy language description of the temperature error change rate to obtain the proportional coefficient correction, integral coefficient correction, and differential coefficient correction.

7. The method according to claim 5, characterized in that, The calculation of the current valve opening based on the proportional coefficient correction, integral coefficient correction, and derivative coefficient correction includes: The current proportional coefficient, current integral coefficient, and current differential coefficient are determined based on the aforementioned proportional coefficient correction, integral coefficient correction, and differential coefficient correction. The current control quantity is calculated based on the following formula: in, This represents the control quantity at the current time t, which indicates the desired opening ratio of the main control valve at the current time t. This indicates the current scaling factor. Indicates the current integral coefficient. Indicates the current differential coefficient. Represents the current time t This represents the integral of the temperature error from the initial time in the past to the current time t.

8. The method according to claim 4, characterized in that, The method further includes: after receiving the stirring start signal, opening the preheating regulating valve to preheat the steam; after determining that the superheat of the steam meets the requirements based on the internal temperature and real-time pressure of the steam stabilizing chamber, closing the preheating regulating valve and opening the main regulating valve.

9. The method according to claim 8, characterized in that, The step of determining that the superheat of the steam meets the requirements based on the internal temperature and real-time pressure of the steam flow stabilizing chamber, and then closing the preheating regulating valve and opening the main regulating valve, includes: The internal temperature of the steam flow stabilizing chamber and the real-time pressure of the steam flow stabilizing chamber are obtained from the temperature sensor of the flow stabilizing chamber and the pressure transmitter. The current saturation temperature is calculated based on the real-time pressure of the steam flow stabilization chamber; If the temperature difference between the steam stabilizing chamber and the current saturation temperature is within a predetermined range, then the superheat of the steam is determined to meet the requirements, the preheating regulating valve is closed, and the main regulating valve is opened. If the difference between the internal temperature of the steam stabilizing chamber and the current saturation temperature is not within the predetermined range, it is determined that the superheat of the steam does not meet the requirements, and the opening of the preheating regulating valve remains unchanged and the main regulating valve remains closed.

10. The method according to claim 4, characterized in that, The method further includes: Receive a user duration setting instruction from the control terminal, the user duration setting instruction including a first steam inlet duration set by the operator; Simultaneously with opening the main regulating valve, the preset timer is controlled to start counting. When the preset timer reaches the first steam supply duration, the main regulating valve is closed to stop the steam supply to the raw material mixing chamber.

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