A high-viscosity resin dispensing fluid field dynamic compensation control method and system

Abstract

The application relates to the technical field of automatic control, and particularly discloses a high-viscosity resin dispensing fluid field dynamic compensation control method and system. The application calculates the consumed resin volume through integration, dynamically adjusts the equivalent driving pressure based on a thermodynamic equation to realize constant work, deduces the internal fluid heating and real-time dynamic viscosity based on operation parameters, uses the same as an adaptive variable to accurately compensate the dispensing valve opening pulse width, generates a pre-shearing non-dispensing pulse and a stepped back-suction negative pressure waveform in combination with the pause time, and jointly controls the dispensing operation. The application realizes coupling calibration of pressure and flow, effectively overcomes the interference of changes of a glue cylinder air chamber and the fluid shear thinning characteristics, effectively overcomes the first drop delay and the broken glue wire phenomenon, and greatly improves the long-term volume consistency and coating precision of high-viscosity dispensing.

Description

Technical Field

[0001] This invention belongs to the field of automatic control technology and relates to a method and system for dynamic compensation control of the fluid field in high-viscosity resin dispensing. Background Technology

[0002] High-viscosity resin dispensing is a critical process in industrial production such as electronic packaging, new energy battery manufacturing, and high-end equipment assembly. Its core task is to apply high-molecular-weight polymer fluids at high speed and in a predetermined form in a precise volume and repeatable manner to designated locations. The stability of dispensing quality directly affects the electrical performance, structural strength, and long-term reliability of the product, thus placing extremely high demands on the control precision of the dispensing process.

[0003] In existing technologies, time-pressure control is commonly used to achieve high-viscosity resin dispensing. This method applies a constant driving air pressure to a sealed glue reservoir and adjusts the dispensing volume per batch by precisely controlling the opening time of the dispensing valve. Before production, operators set a set of fixed air pressure and time parameters based on experience. Throughout the production batch, the control system simply repeats these preset parameters, which is an open-loop or fixed-parameter control mode.

[0004] However, the fixed-parameter control method has revealed several technical defects in actual production. As the resin in the glue cartridge is continuously consumed, the volume of the air cavity above it gradually increases, leading to a decrease in the efficiency of compressed air expansion during each dispensing operation. This, in turn, reduces the actual thrust applied to the resin, resulting in a decrease in the dispensing volume over time. Furthermore, under high-frequency continuous dispensing conditions, the fluid inside the valve body generates heat due to intense shear friction, causing localized temperature increases and a decrease in resin viscosity, which in turn leads to a gradual increase in the dispensing volume. Simultaneously, the inherent thixotropic nature of high-viscosity resin results in a delayed response to the first dispensing after settling, and incomplete fluid retraction at the end of dispensing easily leads to undesirable phenomena such as stringing and dripping. Summary of the Invention

[0005] In view of this, in order to solve the problems mentioned in the background art, a dynamic compensation control method and system for the dispensing fluid field of high viscosity resin is proposed.

[0006] The objective of this invention can be achieved through the following technical solution: The first aspect of this invention provides a dynamic compensation control method for the dispensing fluid field of high viscosity resin, including: S1, obtaining the historical cumulative valve opening time parameter of the dispensing valve and the single theoretical extrusion rate parameter, performing integral calculation to generate the current consumed resin volume parameter.

[0007] S2. Map the dynamic volume parameters of the air column above the glue tube according to the current consumed resin volume parameters, and calculate the equivalent driving pressure parameters under constant work conditions by combining the gas multivariate expansion thermodynamic equation.

[0008] S3. Convert the equivalent driving pressure parameters into a continuous analog control signal and output it to the electronic proportional pressure regulating valve for air pressure regulation. At the same time, obtain the motion frequency parameters, valve core stroke parameters and fluid back pressure parameters of the dispensing valve.

[0009] S4. Based on the motion frequency parameters, valve core stroke parameters and fluid back pressure parameters, the transient heat accumulation parameters inside the fluid are calculated through the fluid shear friction work equation, and the real-time virtual temperature parameters of the fluid are deduced by combining the valve body heat dissipation model.

[0010] S5. Input the real-time virtual temperature parameters of the fluid into the viscosity-temperature curve equation of the high-viscosity resin for calculation to generate the dynamic viscosity parameters of the fluid.

[0011] S6. Calculate the opening pulse width compensation parameter of the dispensing valve using the fluid dynamic viscosity parameter as an adaptive variable, and obtain the pause time parameter between two dispensing actions.

[0012] S7. Input the pause time parameter into the thixotropic recovery time function to calculate the initial yield stress parameter, and generate a pre-shear non-exploding pulse signal and a stepped back suction negative pressure waveform signal that match the initial yield stress parameter.

[0013] S8 combines the opening pulse width compensation parameter, the pre-shear non-dispensing pulse signal and the stepped back suction negative pressure waveform signal to control the dispensing valve actuator and vacuum generator to perform dispensing operations.

[0014] A second aspect of the present invention provides a dynamic compensation control system for the fluid field of high viscosity resin dispensing, comprising: a consumed resin volume generation module, used to obtain the historical cumulative valve opening time parameter of the dispensing valve and the single theoretical extrusion rate parameter, perform integral calculation, and generate the current consumed resin volume parameter.

[0015] The equivalent driving pressure parameter calculation module is used to map the dynamic volume parameter of the air column above the glue tube according to the current consumed resin volume parameter, and calculate the equivalent driving pressure parameter under constant work conditions by combining the gas multivariate expansion thermodynamic equation.

[0016] The dispensing valve parameter acquisition module is used to convert the equivalent driving pressure parameters into continuous analog control signals and output them to the electronic proportional pressure regulating valve for air pressure regulation. At the same time, it acquires the dispensing valve's motion frequency parameters, valve core stroke parameters, and fluid back pressure parameters.

[0017] The real-time virtual temperature deduction module for fluids is used to calculate the transient heat accumulation parameters inside the fluid based on the motion frequency parameters, valve core stroke parameters, and fluid back pressure parameters through the fluid shear friction work equation, and to deduce the real-time virtual temperature parameters of the fluid in combination with the valve body heat dissipation model.

[0018] The fluid dynamic viscosity parameter generation module is used to input the real-time virtual temperature parameters of the fluid into the viscosity-temperature curve equation of the high-viscosity resin for calculation, and generate the fluid dynamic viscosity parameters.

[0019] Enable the pulse width compensation parameter calculation module, which is used to calculate the opening pulse width compensation parameter of the dispensing valve using the fluid dynamic viscosity parameter as an adaptive variable, and to obtain the pause time parameter between two dispensing actions.

[0020] The waveform pulse signal matching module is used to input the pause time parameter into the thixotropic recovery time function to calculate the initial yield stress parameter, and generate a pre-shear non-exploding pulse signal and a stepped back suction negative pressure waveform signal that match the initial yield stress parameter.

[0021] The dispensing operation execution module is used to control the dispensing valve actuator and vacuum generator to perform dispensing operations by combining the opening pulse width compensation parameter, the pre-shear non-dispensing pulse signal and the stepped back suction negative pressure waveform signal.

[0022] Compared to existing technologies, the embodiments of the present invention have at least the following advantages or beneficial effects: The present invention accurately maps the dynamic volume change of the air column above the glue canister by integrating the historical cumulative valve opening time with the theoretical single extrusion rate. Based on this, it innovatively combines the gas multivariate expansion thermodynamic equation to calculate the equivalent driving pressure and outputs it to the electronic proportional pressure regulating valve for real-time air pressure adjustment. This mechanism effectively overcomes the problem in existing technologies where the efficiency of compressed air expansion decreases due to resin consumption and increased air cavity volume, ensuring a constant work done by the driving gas on the resin throughout the entire glue canister's service life and improving the long-term consistency of the single glue dispensing volume.

[0023] This invention collects data on motion frequency, valve core stroke, and fluid back pressure. Utilizing the fluid shear friction work equation and valve body heat dissipation model, it extrapolates the transient heat accumulation and virtual temperature within the fluid in real time. Furthermore, it combines this with the viscosity-temperature curve equation to calculate the fluid's dynamic viscosity, using this as an adaptive variable to precisely feedforward and feedback compensate for the dispensing valve's opening pulse width. This method completely eliminates the interference of temperature and viscosity fluctuations on flow rate, preventing the dispensing volume from gradually increasing with the production cycle.

[0024] This invention accurately calculates the initial yield stress by substituting the pause time between two dispensing operations into a thixotropic recovery time function, and generates a matching "pre-shear non-dispensing pulse signal." Before the actual dispensing, the valve core is slightly moved, prematurely disrupting the network structure formed inside the resin during static dispensing and restoring its fluidity. Simultaneously, a "starting flow resistance compensation coefficient" superimposed on the rising edge of the drive command provides additional driving force to overcome residual flow resistance at the moment of dispensing initiation, achieving uniformity between the initial dispensing volume and subsequent continuous dispensing volumes.

[0025] This invention constructs a refined, stepped negative pressure back-suction strategy. The system integrates the current residual stress in the pipeline with the real-time dynamic viscosity of the fluid to generate a high-suction "first-step cut-off negative pressure" to overcome fluid viscous resistance and quickly break the adhesive line. Subsequently, combined with the stress release decay time, it seamlessly switches to a lower-suction "second-step pressure-holding negative pressure" to maintain a micro-negative pressure balance at the nozzle interface. This waveform control strategy ensures clean adhesive breakage and eliminates stringing and tailing, while effectively preventing leakage and air intake during prolonged pauses, greatly improving the appearance quality of the dispensing and product yield.

[0026] The system provided by this invention, through the coordinated work of its various modules, not only achieves coupled calibration of pressure and flow rate but also takes into account complex rheological properties such as the "shear thinning" of non-Newtonian fluids. It eliminates the need for operators to frequently stop and adjust parameters based on experience, significantly reducing reliance on manual expertise and meeting the extremely stringent coating precision requirements for high-viscosity fluids in high-end applications such as electronic packaging and new energy battery manufacturing. Attached Figure Description

[0027] To more clearly illustrate the technical solutions of the embodiments of the present invention, the accompanying drawings used in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0028] Figure 1 This is a schematic diagram of the method steps of the present invention.

[0029] Figure 2 This is a three-dimensional coupling diagram of the valve body heat dissipation model derivation and fluid dynamic viscosity according to the present invention.

[0030] Figure 3 The diagram shows the dynamic waveform of thixotropic property recovery and unsteady stepped negative pressure reabsorption in this invention.

[0031] Figure 4 This is a schematic diagram of the system structure connection of the present invention. Detailed Implementation

[0032] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0033] Please see Figure 1 The first aspect of the present invention provides a dynamic compensation control method for the dispensing fluid field of high viscosity resin, comprising: S1, acquiring the historical cumulative valve opening time parameter of the dispensing valve and the single theoretical extrusion rate parameter, performing integral calculation to generate the current consumed resin volume parameter.

[0034] In a specific embodiment of the present invention, generating the current consumed resin volume parameter includes: acquiring multiple dispensing operation records since the last reset or replacement of the resin cartridge of the dispensing valve, extracting the valve opening duration of each dispensing action and accumulating them to generate a historical cumulative valve opening time parameter.

[0035] The system obtains the current driving air pressure parameters, fluid temperature parameters, and resin viscosity parameters of the dispensing valve, and calculates the resin extrusion volume per unit time based on a preset fluid dynamics model, which is used as the theoretical extrusion rate parameter for a single pass.

[0036] Using time as the integration variable, the single theoretical extrusion rate parameter is integrated over the range of historical cumulative valve opening time parameters to obtain the cumulative extrusion volume.

[0037] The cumulative extrusion volume is summed with the preset system pipeline loss compensation value to generate the current resin consumption volume parameter.

[0038] Specifically, this step aims to accurately calculate the total amount of resin consumed from the dispensing cartridge since the dispensing system started operating or a new cartridge was replaced. To achieve this, the system first needs to obtain two basic operating parameters. The first is the historical cumulative valve opening time parameter of the dispensing valve, and the second is the theoretical extrusion rate parameter per cycle. By performing an integral calculation on these two parameters, the current resin volume parameter is finally generated.

[0039] The historical cumulative valve opening time parameter refers to the sum of all time periods during which resin is allowed to flow out when the valve core of the dispensing valve switches from the closed state to the open state. This parameter is continuously recorded and accumulated by a timer inside the controller, reflecting the total duration of resin flow.

[0040] The theoretical extrusion rate parameter represents the volume of resin extruded from the nozzle per unit time under ideal and constant operating conditions. This parameter is typically determined through a standardized calibration process after the initial installation of the equipment or replacement of key components. It serves as a baseline value characterizing the basic dispensing capacity of the dispensing system.

[0041] The integral operation is simplified to a multiplication operation in this step because the theoretical extrusion rate parameter for a single run is set as a constant that remains unchanged at the theoretical calculation level. Therefore, multiplying this constant extrusion rate by the total extrusion time yields the total extrusion volume. This calculation method provides the basic data for subsequent more complex dynamic compensation.

[0042] The relationship between these four parameters can be expressed by the following formula:

[0043] The explanations of the symbols in the formula are as follows: : Current resin volume consumed, in cubic millimeters (mm³). This parameter is the final output of this step and is used to characterize the total volume of resin that has been extruded from the cartridge. The theoretical extrusion rate parameter for a single pass, expressed in cubic millimeters per second (mm³ / s). This parameter is set based on multiple (e.g., 100) repetitive dispensing tests conducted on a specific type of high-viscosity resin under standard testing conditions (e.g., temperature 25℃, driving air pressure 0.4MPa). The weight of the dispensed resin is measured using a precision balance, converted to volume based on resin density, and finally divided by the dispensing time to calculate the average extrusion rate. Based on 100 sets of measured data for a certain type of high-viscosity epoxy resin, this parameter is set to 20 mm³ / s. Historical cumulative valve opening time parameter, in seconds (s). This parameter is accumulated in real time by the system control software. Every time the dispensing valve executes an opening command, the pulse width time of its opening is added to the total value of this parameter. : System pipeline loss compensation value, in cubic millimeters (mm³). This parameter represents the irreversible volumetric residue or loss of resin as it flows through dead zones inside the system pipelines, joints, and dispensing valves. It is usually obtained through pipeline volume measurement or preset empirical calibration.

[0044] For example, suppose a dispensing system starts production after a new 30 ml cartridge is replaced. After running for a period of time, it is necessary to calculate the current volume of resin consumed.

[0045] According to the implementation process of this step, the system first obtains the single-batch theoretical extrusion rate parameter, which was set during equipment calibration. Based on the calibration test of the high-viscosity epoxy resin used, the single-batch theoretical extrusion rate parameter is set. It is 20 mm³ / s.

[0046] Simultaneously, the system reads the historical cumulative valve opening time parameter from the internal controller. Assuming that the total valve opening time for all dispensing actions since the new glue cartridge was first used is 1800 seconds, the historical cumulative valve opening time parameter... It is 1800s.

[0047] Next, the obtained parameters are substituted into the formula for calculation to generate the current resin volume parameters. Assuming that in this specific calibration condition for replacing the glue cartridge, the preset system pipeline loss compensation value... The value is 0 mm³. The calculation process is as follows: The calculations above show that the current resin volume consumed is 36,000 mm³. This result indicates that 36,000 cubic millimeters (36 ml) of resin has been consumed since the new dispensing cartridge was first used. This parameter will serve as a direct input for subsequent steps to calculate the air column volume within the cartridge and for pressure compensation, providing crucial initial data for achieving high-precision and high-consistency dispensing control.

[0048] S2. Map the dynamic volume parameters of the air column above the glue tube according to the current consumed resin volume parameters, and calculate the equivalent driving pressure parameters under constant work conditions by combining the gas multivariate expansion thermodynamic equation.

[0049] In a specific embodiment of the present invention, the equivalent driving pressure parameters under constant work conditions are calculated by combining the gas multi-directional expansion thermodynamic equation, including: obtaining the dynamic volume parameters and calculating the difference between the initial cavity volume parameters of the rubber tube to generate real-time gas phase volume parameters.

[0050] Substitute the real-time gas phase volume parameters and the basic driving gas pressure parameters into the gas multivariate expansion thermodynamic equation to solve for energy conservation, and generate a single pulse as the energy quantity parameter.

[0051] Based on the single pulse function parameters and real-time gas phase volume parameters, inverse pressure compensation deduction is performed to generate equivalent driving pressure parameters.

[0052] Specifically, after obtaining the current consumed resin volume parameter in step S1, this step aims to calculate a dynamically adjusted driving pressure to compensate for the changes in dispensing force caused by the reduction of resin and the increase in air volume within the cartridge. The core objective is to ensure that the work done by compressed air on the resin remains constant during each dispensing action, thereby maintaining consistent dispensing volume. This process first maps the consumed resin volume to the real-time volume of the air column within the cartridge, and then uses the thermodynamic principle of gas expansion in multiple directions to solve for the equivalent driving pressure parameter required to achieve constant work.

[0053] The first step in this process is to calculate the real-time gas phase volume parameter. The system acquires the currently consumed resin volume parameter generated in step S1 and combines it with a preset initial cavity volume parameter of the cartridge. The initial cavity volume parameter of the cartridge refers to the volume of a tiny air layer between the piston and the resin surface after a brand-new, fully loaded cartridge is installed in the equipment; this volume is unavoidable. The real-time gas phase volume parameter is the sum of these two volumes, accurately reflecting the total volume of the air column in the cartridge. Here, the dynamic volume parameter is understood as the currently consumed resin volume parameter because it directly reflects the dynamic change in gas phase volume.

[0054]

[0055] The explanations of the symbols in the formula are as follows: Real-time gas phase volume parameter, in cubic millimeters (mm³). It represents the actual volume of the air column inside the cartridge at the current moment. : Initial cavity volume parameter of the rubber cartridge, in cubic millimeters (mm³). This parameter is determined based on the specifications of the rubber cartridge used. For example, for a standard 30 ml rubber cartridge, its initial cavity volume at the top can be set through geometric measurements or empirical data. Based on the statistical measurement of 200 sets of industrial 30 ml rubber cartridges, this parameter is set to 5000 mm³. : Current resin volume consumed, in cubic millimeters (mm³). This parameter is calculated in step S1.

[0056] Next, based on the principle of energy conservation, the system calculates a baseline single-pulse work parameter. This parameter represents the work required to complete one standard dispensing action under ideal initial conditions. The calculation uses the gas multivariate expansion thermodynamic equation, which describes the pressure-volume relationship of a gas during a non-adiabatic, non-isothermal rapid expansion process. Simultaneously, a basic driving gas pressure parameter is introduced, which is the standard working gas pressure set for the new glue cartridge.

[0057]

[0058] The explanations of the symbols in the formula are as follows: The single-pulse work quantity parameter is expressed in Newton-millimeter (N·mm). It represents the work done by the gas to expand and expel the resin volume in a single pulse under initial conditions, serving as a constant target energy value. : Basic driving air pressure parameter, in megapascals (MPa). This is the initial driving air pressure calibrated for the system, set to ensure ideal dispensing results with brand new glue cartridges. Based on process requirements, it is set to 0.4 MPa. The gas multivariable expansion index (VMI) is dimensionless. It describes the thermodynamic characteristics of gas expansion. For the rapid expansion of air, its value ranges between 1 (isothermal) and 1.4 (adiabatic). Based on the actual conditions of compressed air in industrial settings, this value is set to 1.2. : Single pulse extrusion volume parameter, in cubic millimeters (mm³). This is the theoretically required volume of resin to be extruded in a single dispensing action, which can be obtained by multiplying the theoretical single-pulse extrusion rate parameter by the single pulse time.

[0059] Finally, the system performs a reverse pressure compensation simulation to generate equivalent driving pressure parameters. The goal of this step is to determine the initial driving pressure required to generate work equal to the single-pulse work parameters under the current real-time gas phase volume parameters. This compensated pressure value can be calculated by inversely solving the gas multivariate expansion work equation.

[0060]

[0061] The explanations of the symbols in the formula are as follows: : Equivalent driving pressure parameter, in megapascals (MPa). This is the final output of this step, a dynamically compensated pressure setpoint used to offset the effects of changes in air volume.

[0062] For example, following the example of step S1, the currently consumed resin volume parameter The value is 36000 mm³. Now, it is necessary to calculate the equivalent driving pressure parameters required to achieve constant work.

[0063] First, real-time gas phase volume parameters are generated. The system acquires the initial cavity volume parameters of the rubber cartridge and sets them as follows. The calculation process is as follows: The real-time gas phase volume parameter was obtained as 41000 mm³.

[0064] Next, a single pulse is generated as the functional parameter. The system acquires the basic driving air pressure parameters. Gas polytropic expansion index At the same time, it is necessary to determine the single-pulse extrusion volume parameters. Assuming the pulse time for a single dispensing cycle is 0.05 seconds, and considering the theoretical extrusion rate parameter set in step S1... , can be obtained The calculation process is as follows:

[0065] The functional parameters of a single pulse are 0.39992 N·mm.

[0066] Finally, equivalent driving pressure parameters are generated based on the obtained parameters. Substituting the relevant parameters, a precise algebraic derivation is performed. The calculation process is as follows:

[0067] Calculations yielded an equivalent driving pressure parameter of 0.39993 MPa. This result indicates that after 36,000 mm³ of resin has been consumed in the glue cartridge, the driving air pressure needs to be finely adjusted from the initial 0.4 MPa to 0.39993 MPa to maintain a constant dispensing work per cycle. This compensated pressure value will be used for subsequent pressure regulation and control.

[0068] S3. Convert the equivalent driving pressure parameters into a continuous analog control signal and output it to the electronic proportional pressure regulating valve for air pressure regulation. At the same time, obtain the motion frequency parameters, valve core stroke parameters and fluid back pressure parameters of the dispensing valve.

[0069] Specifically, the equivalent driving pressure parameters are converted into continuous analog control signals and output to the electronic proportional pressure regulating valve for air pressure adjustment. Simultaneously, the system acquires the dispensing valve's motion frequency parameters, valve core stroke parameters, and fluid back pressure parameters. The aim is to achieve high-precision dynamic control of the dispensing process through the synergy of electromechanical and hydraulic multi-source data. The detailed process is as follows: First, after calculating the required equivalent driving pressure parameters, which are typically in digital form, the system's analog-to-digital converter (D / A converter) converts these digital equivalent driving pressure parameters into industry-standard continuous analog control signals (e.g., 0-10V voltage signals or 4-20mA current signals) to drive the underlying pneumatic actuators. This analog signal is then directly output to the electronic proportional pressure regulating valve. The electronic proportional pressure regulating valve can linearly and steplessly adjust its output driving air pressure according to the strength of the received analog signal, thus replacing the traditional manual pressure regulating valve and achieving real-time, automated, and high-precision adjustment of the dispensing driving air pressure.

[0070] Meanwhile, to monitor the actual response status of the system after pressure adjustment and provide basic data for subsequent feedback compensation, the system simultaneously acquires three key status parameters of the dispensing valve's current operation: First, the motion frequency parameter: through the underlying pulse transmission recorder of the dispensing controller or a Hall sensor installed on the actuator, the number of times the dispensing valve opens and closes per unit time (i.e., dispensing frequency, such as 200Hz) is acquired. This parameter directly determines the number of dispensing points per unit time and the air filling and discharging response time of the air chamber inside the valve body. Second, the valve core stroke parameter: through the calibration data of a displacement sensor or micrometer, the maximum upward distance of the valve core (dispensing pin) when it is open is read or extracted in real time. The size of the valve core stroke determines the instantaneous cross-sectional area of ​​the fluid channel at the nozzle of the dispensing valve, directly affecting the volume of glue extruded in a single operation. Third, the fluid back pressure parameter: using a miniature pressure transmitter installed inside the fluid pipeline or glue reservoir, the back pressure generated by the glue (resin) and other fluids on the internal channel of the dispensing valve is collected in real time. As the dispensing process progresses, the liquid level in the cartridge decreases or the fluid viscosity changes with temperature and curing time, causing dynamic fluctuations in fluid back pressure. This parameter is a key indicator for evaluating the actual fluid extrusion resistance.

[0071] See Figure 2 S4. Based on the motion frequency parameters, valve core stroke parameters and fluid back pressure parameters, the transient heat accumulation parameters inside the fluid are calculated through the fluid shear friction work equation, and the real-time virtual temperature parameters of the fluid are deduced by combining the valve body heat dissipation model.

[0072] In a specific embodiment of the present invention, the real-time virtual temperature parameters of the fluid are derived by combining the valve body heat dissipation model, including: obtaining the motion frequency parameters and valve core stroke parameters to calculate the valve core motion speed parameters, and substituting the valve core motion speed parameters and fluid back pressure parameters into the fluid shear friction work equation to generate shear work parameters per unit time.

[0073] By integrating the shear work done per unit time in the time domain, the transient heat accumulation parameters inside the fluid are generated.

[0074] The transient heat accumulation parameters inside the fluid are obtained and combined with the heat dissipation model of the valve body to calculate the heat conduction attenuation, thereby generating real-time virtual temperature parameters of the fluid.

[0075] Specifically, after receiving the equivalent driving pressure parameters calculated in step S2, this step, based on the motion frequency parameters, valve core stroke parameters, and fluid back pressure parameters, calculates the heat generated by the work done on the fluid by the valve core motion using a fluid shear friction work equation. The first step is to calculate the valve core motion velocity parameters, which are jointly determined by the motion frequency parameters and valve core stroke parameters, reflecting the intensity of the valve core motion. Subsequently, the valve core motion velocity parameters and fluid back pressure parameters are substituted into the fluid shear friction work equation to generate the shear work parameter per unit time. This parameter is physically equivalent to the heat power generated by friction within the fluid.

[0076]

[0077] The explanations of the symbols in the formula are as follows: Shear work done per unit time, measured in Newton-millimeter-seconds (N·mm / s), or milliwatts (mW). It represents the heat energy converted into thermal energy per second due to shear friction. : Fluid back pressure parameter, measured in megapascals (MPa), or Newtons per square millimeter (N / mm²). This parameter can be measured in real time by a pressure sensor installed near the dispensing valve inlet, or estimated based on a fluid dynamics model. Based on 50 sets of measured data on the flow of a high-viscosity resin in a specific pipeline, this parameter is set to 0.2 MPa. : Valve core cross-sectional area parameter, in square millimeters (mm²). This is a fixed parameter related to the structure of the dispensing valve, determined according to the design drawings of the dispensing valve used. Set to 5mm². : Valve spool stroke parameter, in millimeters (mm). This parameter is set by the dispensing process and is typically between 0.1 and 1.0 mm. Set to 0.5 mm. : Motion frequency parameter, in Hertz (Hz). This parameter is determined by the production cycle time. Set to 10Hz. A coefficient of 2 indicates that the valve core opens and closes once per working cycle, with work being done on the fluid in both strokes.

[0078] After obtaining the shear work parameters per unit time, the system performs thermal equilibrium integration with the structural heat capacity parameters of the dispensing valve to generate transient heat accumulation parameters within the fluid. This step essentially calculates the newly generated heat within an extremely short time step.

[0079]

[0080] The explanations of the symbols in the formula are as follows: : The transient heat accumulation parameter inside the fluid, measured in Newton-millimeter (N·mm), or millijoule (mJ). It represents the new heat energy accumulated inside the fluid within one calculation cycle. : Calculation time step, in seconds (s). This is the time interval for the control system to perform iterative calculations, set to 1 second.

[0081] Finally, the system acquires the transient heat accumulation parameters inside the fluid and introduces a valve body heat dissipation model to calculate heat conduction attenuation, ultimately deriving the real-time virtual temperature parameters of the fluid. This model considers that the generated heat will dissipate to the surrounding environment through the valve body. Using a discrete-time heat balance equation, the virtual temperature of the fluid at any given time can be iteratively calculated.

[0082]

[0083] The explanations of the symbols in the formula are as follows: : The current real-time virtual temperature parameter of the fluid, in degrees Celsius (°C). This is the final output of this step. : The real-time virtual temperature parameter of the fluid at the previous moment, in degrees Celsius (°C). : Structural heat capacity parameter of the dispensing valve, in Newton-millimeter per degree Celsius (N·mm / °C). It characterizes the energy absorbed required to raise the overall temperature of the valve body and internal fluid by 1 degree Celsius, obtained through finite element thermal analysis or experimental calibration of the valve body material and structure. Set to 500 N·mm / °C. : Valve body heat dissipation coefficient, measured in seconds (s⁻¹). This coefficient integrates heat dissipation effects from conduction, convection, and radiation, and is determined experimentally by measuring the final steady-state temperature rise of the valve body under stable heating power. It is set to 0.1 s⁻¹. Ambient temperature parameter, in degrees Celsius (°C). Acquired by a temperature sensor mounted on the equipment rack. Set to 25°C.

[0084] For example, following the example from step S2, the system has calculated the equivalent driving pressure parameters. The pressure is set to 0.39993 MPa, which is then converted into a continuous analog control signal and output to the electronic proportional pressure regulating valve. Simultaneously, the system begins calculating the real-time virtual temperature parameters of the fluid.

[0085] The system obtained the following operating parameters: motion frequency parameters Valve core stroke parameters Fluid back pressure parameters First, the shear work parameters per unit time are generated. The fixed parameter used in the calculation is the valve core cross-sectional area parameter. The calculation process is as follows: The shear work per unit time was obtained as 10 N·mm / s. Next, the transient heat accumulation parameters inside the fluid were generated. The fixed parameters used in the calculation were: calculation time step... The calculation process is as follows: The transient heat accumulation parameter inside the fluid was obtained as 10 N·mm.

[0086] Finally, the real-time virtual temperature parameters of the fluid are generated. Assume this is the first calculation cycle after system startup, with the initial temperature equal to the ambient temperature. The parameters used in the calculation are: the real-time virtual temperature parameters of the fluid from the previous moment. Structural heat capacity parameters of dispensing valve Valve body heat dissipation coefficient Ambient temperature parameters The calculation process is as follows: After the first calculation cycle, the real-time virtual temperature parameter of the fluid increased from 25°C to 25.02°C.

[0087] To demonstrate the model's dynamics, a second cycle is calculated. At this point, Other parameters remain unchanged. After the second calculation cycle, the real-time virtual temperature parameter of the fluid was updated to 25.038°C.

[0088] S5. Input the real-time virtual temperature parameters of the fluid into the viscosity-temperature curve equation of the high-viscosity resin for calculation to generate the dynamic viscosity parameters of the fluid.

[0089] In a specific embodiment of the present invention, generating fluid dynamic viscosity parameters includes: obtaining the activation energy parameters and general gas constant parameters of high viscosity resin, and performing exponential calculations in combination with the real-time virtual temperature parameters of the fluid to generate temperature influence factor parameters.

[0090] The reference temperature viscosity parameters of the high-viscosity resin are obtained, and the reference temperature viscosity parameters are multiplied with the temperature influence factor parameters to generate the theoretical viscosity parameters.

[0091] The current shear rate parameter of the dispensing valve is obtained, and the theoretical viscosity parameter is corrected for non-Newtonian fluid shear thinning to generate the fluid dynamic viscosity parameter.

[0092] Specifically, the core task of this step is to accurately calculate the actual flow viscosity of the high-viscosity resin under the current operating conditions using the real-time virtual temperature parameters of the fluid derived in step S4. The viscosity of the resin is not only drastically affected by temperature but also by the shear forces it experiences while flowing within the valve. Therefore, this step uses a viscosity-temperature curve equation that integrates both temperature and shear effects to ultimately generate a dynamic viscosity parameter that accurately reflects the true state of the fluid.

[0093] The process first addresses the effect of temperature on viscosity. The system acquires the activation energy parameter and universal gas constant parameter of the high-viscosity resin; these two parameters together describe the energy required for resin molecules to overcome internal resistance and begin flowing. Combined with the real-time virtual temperature parameter of the fluid input from step S3, a dimensionless temperature influence factor parameter is generated through exponential calculation. This calculation is based on the Arrhenius equation, a classic model describing the relationship between chemical reaction rates or material physical properties and temperature.

[0094]

[0095] The explanations of the symbols in the formula are as follows: Temperature effect factor parameter, dimensionless. It quantifies the degree to which the current temperature affects viscosity relative to the reference temperature. : Activation energy parameter of high-viscosity resin, expressed in joules per mole (J / mol). This parameter is an inherent material property of the resin, characterizing its viscosity sensitivity to temperature. It is obtained by testing the resin viscosity at different temperatures using a rotational rheometer and fitting the data. For a specific epoxy resin, this parameter was set to 50,000 J / mol by fitting viscosity test data from 50 sets of different temperatures. The universal gas constant parameter, with a value of 8.314 J / (mol·K), is a physical constant. The fluid's real-time virtual absolute temperature is expressed in Kelvin (K). It is derived by adding 273.15 to the fluid's real-time virtual temperature parameter (in degrees Celsius) generated in step S4. Reference absolute temperature, in Kelvin (K). This is the reference temperature for defining the reference viscosity, usually set to standard room temperature of 25°C, or 298.15K.

[0096] After obtaining the temperature influence factor parameters, the system acquires the reference temperature viscosity parameters of the high-viscosity resin and multiplies them with the temperature influence factor parameters to generate the theoretical viscosity parameters. The reference temperature viscosity parameters are the resin viscosity values ​​measured at a standard reference temperature.

[0097]

[0098] The explanations of the symbols in the formula are as follows: Theoretical viscosity parameter, measured in Pascal-seconds (Pa·s). It represents the resin viscosity determined solely by the current temperature, without considering shear effects. : The reference temperature viscosity parameter of the high-viscosity resin, in Pascal-seconds (Pa·s). This parameter is measured by a rheometer at a reference temperature (e.g., 25°C). Based on measurements of the resin used, this parameter is set to 100 Pa·s.

[0099] Finally, since high-viscosity resins are mostly non-Newtonian fluids, their viscosity decreases with increasing shear rate, a phenomenon known as "shear thinning." Therefore, the system obtains the current shear rate parameter of the dispensing valve and applies a non-Newtonian shear thinning correction to the theoretical viscosity parameter calculated in the previous step, thereby generating the final dynamic viscosity parameter of the fluid. This correction is typically described using a power-law model.

[0100]

[0101] The explanations of the symbols in the formula are as follows: : Dynamic viscosity parameter of the fluid, in Pascal-seconds (Pa·s). This is the final output of this step, taking into account the effects of temperature and shear rate, and represents the actual viscosity of the resin flowing within the valve. : The current shear rate parameter of the dispensing valve, in seconds (s⁻¹). This parameter is estimated based on the gap between the valve core and the valve body, the valve core movement speed, and the fluid flow rate. For typical dispensing conditions, this parameter is set to 100 s⁻¹. : Reference shear rate parameter, in seconds (s⁻¹). This is a baseline value in the power-law model, usually set to 1 s⁻¹. Power-law exponent, dimensionless. This is also an inherent material property of the resin, characterizing its shear-thinning degree, and is also obtained through rheometer testing. For shear-thinning fluids, this value is less than 1. Based on the rheological curve analysis of the resin used, this parameter is set to 0.5.

[0102] For example, following the example from step S4, the system calculates the real-time virtual temperature parameter of the fluid to be 25.038°C. Now, it is necessary to calculate the dynamic viscosity of the fluid based on this temperature.

[0103] First, the temperature influence factor parameters are generated. The parameters obtained by the system are as follows: activation energy parameters of high viscosity resin. General gas constant parameters J / (mol·K), reference absolute temperature The input fluid real-time virtual temperature parameter is 25.038°C, converted to absolute temperature: The calculation process is as follows:

[0104] The temperature influence factor parameter was found to be 0.99743.

[0105] Next, theoretical viscosity parameters are generated. The system obtains the reference temperature viscosity parameters for high-viscosity resins. The calculation process is as follows: The theoretical viscosity parameter was obtained as 99.743 Pa·s. Finally, a non-Newtonian fluid shear thinning correction was applied to the theoretical viscosity parameter. The parameters obtained by the system are as follows: the current shear rate parameter of the dispensing valve. Reference shear rate parameter Power Law Index The calculation process is as follows: Calculations yielded a final fluid dynamic viscosity parameter of 9.9743 Pa·s. This parameter represents a significant decrease compared to the baseline viscosity of 100 Pa·s and the theoretical viscosity of 99.743 Pa·s, accurately reflecting the fluid behavior under high shear rates and serving as the core basis for subsequent dispensing pulse width compensation.

[0106] S6. Calculate the opening pulse width compensation parameter of the dispensing valve using the fluid dynamic viscosity parameter as an adaptive variable, and obtain the pause time parameter between two dispensing actions.

[0107] In a specific embodiment of the present invention, the opening pulse width compensation parameter of the dispensing valve is calculated using the fluid dynamic viscosity parameter as an adaptive variable, including: obtaining the fluid dynamic viscosity parameter and performing a ratio calculation with the initial calibrated viscosity parameter to generate a viscosity drift coefficient parameter.

[0108] The viscosity drift coefficient parameter is multiplied by the reference valve opening time parameter to generate the initial pulse width adjustment parameter.

[0109] The current equivalent driving pressure parameters of the electronic proportional pressure regulating valve are obtained, and the initial pulse width adjustment parameters are calibrated by pressure-flow coupling to generate the activation pulse width compensation parameters.

[0110] Specifically, after accurately calculating the fluid dynamic viscosity parameters in step S5, the core objective of this step is to adaptively adjust the opening time of the dispensing valve using this dynamically changing viscosity value to ensure that the dispensing volume remains constant even under viscosity fluctuations. This process ultimately generates a fully compensated opening pulse width compensation parameter. Furthermore, this step also acquires the pause time parameter between two dispensing actions. Although this parameter is not included in the calculation in this step, it is passed as input to step S7 to address the thixotropic recovery issue of the resin.

[0111] The first step in this process is to quantify the degree of deviation of the current viscosity from the initial calibration state. The system acquires the fluid dynamic viscosity parameter generated in step S5 and performs a ratio calculation with a preset initial calibration viscosity parameter to generate a dimensionless viscosity drift coefficient parameter.

[0112]

[0113] The explanations of the symbols in the formula are as follows: Viscosity drift coefficient: A dimensionless parameter. It reflects the proportion of change in the current fluid viscosity relative to the initial calibration viscosity. : Fluid dynamic viscosity parameter, in Pascal-seconds (Pa·s). This parameter is calculated in step S5. Initial calibration viscosity parameter, in Pascal-seconds (Pa·s). This parameter is the resin viscosity value measured or calculated during the initial commissioning and calibration phase of the equipment at a reference temperature, reference pressure, and typical shear rate. It represents the reference viscosity under ideal operating conditions. Based on rheological tests of the resin used at 25°C and a shear rate of 100 s⁻¹, this parameter is set to 10 Pa·s.

[0114] After obtaining the viscosity drift coefficient parameter, the system performs initial time adjustments. The viscosity drift coefficient parameter is multiplied by a preset baseline valve opening time parameter to generate the initial pulse width adjustment parameter. The baseline valve opening time parameter is the valve opening time required to extrude the target volume of resin under initial calibration conditions. The basic logic of this calculation is that, under constant driving pressure, fluid flow rate is inversely proportional to viscosity; therefore, to maintain a constant extrusion volume, the valve opening time should be directly proportional to the viscosity.

[0115]

[0116] The explanations of the symbols in the formula are as follows: : Initial pulse width adjustment parameter, in seconds (s). This is an initial compensation time that only considers viscosity changes. : Reference valve opening time parameter, in seconds (s). This parameter was determined through process experiments and is the basic setting value for achieving the target dispensing amount per cycle. It is set to 0.05 seconds.

[0117] However, considering only viscosity changes is insufficient because in step S2, the driving pressure (equivalent driving pressure parameter) itself is also dynamically adjusted to compensate for changes in air volume within the cartridge. Fluid flow rate is affected by both pressure and viscosity. Therefore, the final step is to perform pressure-flow coupling calibration. The system acquires the equivalent driving pressure parameter, currently set by the electronic proportional pressure regulator and derived from step S2, and uses it to calibrate the initial pulse width adjustment parameter obtained in the previous step, ultimately generating the opening pulse width compensation parameter. This calibration is based on a simplified relationship of the Hagen-Poiseuille law, i.e., flow rate is directly proportional to pressure, therefore the valve opening time should be inversely proportional to pressure.

[0118]

[0119] The explanations of the symbols in the formula are as follows: Enable pulse width compensation parameter, in seconds (s). This is the final output of this step, a precise valve opening time that takes into account both viscosity and pressure changes. : Basic driving air pressure parameter, in megapascals (MPa). This parameter has been defined in step S2 and is the driving pressure used during the initial calibration of the system. : Equivalent driving pressure parameter, in megapascals (MPa). This parameter is calculated in step S2 and is the driving pressure that is currently being adjusted in real time.

[0120] For example, following the previous steps, the system needs to calculate the opening pulse width compensation parameters of the dispensing valve. The fluid dynamic viscosity parameters obtained from step S5... The equivalent driving pressure parameter obtained from step S2 is 9.9743 Pa·s. It is 0.39993 MPa.

[0121] First, the viscosity drift coefficient parameters are generated. The system obtains the initial calibration viscosity parameters. The value is 10 Pa·s. The calculation process is as follows: The viscosity drift coefficient was found to be 0.99743.

[0122] Next, the initial pulse width adjustment parameters are generated. The system acquires the reference valve opening time parameters. The value is 0.05s. The calculation process is as follows: The initial pulse width adjustment parameter was obtained as 0.0498715 seconds. This indicates that due to the slight decrease in viscosity, the required valve opening time is correspondingly shortened.

[0123] Finally, pressure-flow coupling calibration was performed on the initial pulse width adjustment parameters. The system acquired the basic driving gas pressure parameters. The value is 0.4 MPa. The calculation process is as follows: Through calculation, the final opening pulse width compensation parameter was obtained as 0.049880 seconds (i.e., 49.880 milliseconds). This result integrates the dual effects of the fluid viscosity decreasing from 10 Pa·s to 9.9743 Pa·s and the driving pressure being fine-tuned from 0.4 MPa to 0.39993 MPa, calculating a precise valve opening time for actual dispensing control. Simultaneously, the system records the pause time parameter between the current dispensing and the next dispensing, for example, 0.5 seconds, and transmits it to subsequent steps.

[0124] See Figure 3 S7. Input the pause time parameter into the thixotropic recovery time function to calculate the initial yield stress parameter, and generate a pre-shear non-gluing pulse signal and a stepped back suction negative pressure waveform signal that match the initial yield stress parameter.

[0125] In a specific embodiment of the present invention, generating a pre-shear non-gluing pulse signal and a stepped back suction negative pressure waveform signal that match the initial yield stress parameter includes: obtaining the pause time parameter and substituting it into the thixotropic recovery time function for exponential growth fitting to generate the initial yield stress parameter.

[0126] The critical driving force parameter for glue breaking is generated by multiplying the initial yield stress parameter with the valve core cross-sectional area parameter of the dispensing valve.

[0127] Based on the critical driving force parameter for breaking the glue, a micro-motion control pulse signal with a duration shorter than the critical time for fluid extrusion is generated to obtain the pre-shear non-glue pulse signal.

[0128] The residual stress parameters of the pipeline at the end of dispensing by the dispensing valve are weighted and calculated with the dynamic viscosity parameters of the fluid to generate the first-step cut-off negative pressure parameters.

[0129] The stress release attenuation time is calculated based on the first-step cut-off negative pressure parameters and the pipeline cross-sectional dimensions, and the second-step pressure-holding negative pressure parameters are generated.

[0130] The first-step cut-off negative pressure parameter, the second-step pressure holding negative pressure parameter, and the stress release decay time are sequentially spliced ​​together to generate a stepped back suction negative pressure waveform signal.

[0131] Specifically, this step aims to address two key issues in the dispensing process of high-viscosity resins: lag at the start of dispensing and stringing at the end. To this end, the system generates two distinct control signals based on the pause time between two dispensing operations. The first is a pre-shear non-dispensing pulse signal used to overcome the viscosity rebound (i.e., thixotropy) after the resin has settled; the second is a stepped back suction negative pressure waveform signal used to achieve clean dispensing.

[0132] First, the system addresses the thixotropic issue. When high-viscosity resins are left to stand, a microscopic network structure forms inside, leading to reduced flowability. An initial driving force (i.e., yield stress) is required to restore its flow. This yield stress increases with the standing time. The system obtains the dwell time parameter from step S6 and substitutes it into a preset thixotropic recovery time function for calculation. This function simulates the recovery process of the initial yield stress parameter over time through exponential growth fitting.

[0133]

[0134] The explanations of the symbols in the formula are as follows: Initial yield stress parameter, in megapascals (MPa). It represents the minimum shear stress required for the resin to begin flowing after a certain period of inactivity. Maximum yield stress parameter, in megapascals (MPa). This is the maximum yield stress that the resin can reach after full recovery, and is an inherent property of the material. Based on rheological tests of the epoxy resin used after a long period of static rest, this parameter was set to 0.05 MPa. : Residual yield stress parameter, in megapascals (MPa). This is the yield stress measured immediately after the last dispensing and shearing, representing the lowest state after the mesh structure is destroyed. Set to 0.001 MPa. : Pause time parameter, in seconds (s). Obtained from step S6. : Thixotropic recovery time constant, in seconds (s). This parameter characterizes the rate of yield stress recovery, obtained by testing the yield stress of the resin at different resting times and fitting an exponential curve. It is set to 0.8 s.

[0135] After calculating the initial yield stress parameter, the system multiplies it with the valve core cross-sectional area parameter of the dispensing valve to obtain the critical driving force parameter for breaking the adhesive required to start the fluid.

[0136]

[0137] The explanations of the symbols in the formula are as follows: Critical driving force parameter for resin breaking, measured in Newtons (N). It represents the minimum thrust that the actuator needs to apply to the valve core to make the resin flow at the valve core. : Valve core cross-sectional area parameter, in square millimeters (mm²). This parameter has been defined in step S4 and set to 5mm².

[0138] Based on this force, the system generates a pre-shear non-exploding pulse signal. This is a micro-motion control pulse signal with an amplitude sufficient to generate a value greater than the critical driving force parameter for breaking the resin, but its duration is strictly controlled and must be less than the critical fluid extrusion time. The critical fluid extrusion time refers to the shortest time from the start of the valve core's movement to the actual extrusion of the resin from the nozzle. Through this brief micro-motion, the resin's network structure can be disrupted, restoring its fluidity without causing accidental extrusion.

[0139] Simultaneously, the system begins constructing a stepped back suction negative pressure waveform signal for adhesive cut-off. The first step is to calculate the first-step cut-off negative pressure parameters. The system obtains the residual stress parameters in the pipeline at the end of dispensing by the dispensing valve and the fluid dynamic viscosity parameters calculated in step S5, and performs a weighted calculation. This negative pressure needs to be large enough to overcome the residual pressure in the pipeline and quickly pull the adhesive line back.

[0140]

[0141] The explanations of the symbols in the formula are as follows: The first-step cutoff negative pressure parameter is in megapascals (MPa). The negative sign indicates that this is a negative pressure (vacuum). : Residual stress weighting coefficient, dimensionless. Used to adjust the proportion of residual stress in the calculation, and is set to 1.2 based on experience. : Residual stress parameter in the pipeline, in megapascals (MPa). The residual pressure in the nozzle pipeline after the dispensing process is complete, due to fluid elasticity, can be obtained through experiments or fluid simulation. Set to 0.01 MPa. : Viscous backflow compensation coefficient, in seconds (s⁻¹). Used to convert viscosity parameters into pressure contribution, reflecting the additional negative pressure required to overcome viscous resistance during backflow. Obtained through experimental calibration, set to 0.5 s⁻¹. : Dynamic viscosity parameter of the fluid, in Pascal-seconds (Pa·s). In the formula... This is a unit conversion factor used to uniformly convert the pressure unit (Pa) generated by viscosity into megapascals (MPa).

[0142] Next, the system calculates the second-stage holding negative pressure parameters and the duration of the first-stage negative pressure, i.e., the stress release decay time. The high negative pressure duration should not be too long, otherwise air may be drawn in. After the stress release decay time, it switches to a smaller holding negative pressure, i.e., the second-stage holding negative pressure parameter, to maintain nozzle cleanliness and prevent glue leakage throughout the pause.

[0143]

[0144] The explanations of the symbols in the formula are as follows: Stress release decay time, in seconds (s). : Decay time constant, in megapascals per second (MPa·s). This is an empirical constant that takes into account factors such as nozzle geometry and fluid compressibility. It is set to 0.001 MPa·s. The second-stage pressure holding negative pressure parameter is expressed in megapascals (MPa). : Pressure holding coefficient, dimensionless. Set to 0.3.

[0145] Finally, by sequentially splicing the first-step cut-off negative pressure parameter, the second-step pressure holding negative pressure parameter, and the stress release decay time, a complete stepped back suction negative pressure waveform signal is formed.

[0146] For example, following the previous steps, the system obtains the pause time parameter. For 0.5 seconds, the fluid dynamic viscosity parameter It is 9.9743 Pa·s.

[0147] First, the initial yield stress parameters are generated. The parameters obtained by the system are: The calculation process is as follows: The initial yield stress parameter was obtained as 0.02377 MPa. Next, the critical driving force parameter for glue breaking was generated. The valve core cross-sectional area parameter obtained by the system was also determined. The calculation process is as follows: The critical driving force parameter for breaking the adhesive was obtained as 0.11885 N. Based on this, the system will generate a pre-shear non-adhesive pulse signal with a driving force slightly greater than 0.11885 N and a duration less than the set critical fluid extrusion time (e.g., 5 milliseconds).

[0148] Then, the parameters for the first-step negative pressure cutoff are generated. The parameters obtained by the system are: The calculation process is as follows: The first-step cutoff negative pressure parameter was obtained as -0.012005MPa.

[0149] Subsequently, the stress release decay time and the second-step pressure holding negative pressure parameters are generated. The parameters acquired by the system are: The calculation process is as follows: , The stress release decay time was found to be 0.0833 seconds, and the second-step pressure holding negative pressure parameter was -0.0036015 MPa.

[0150] Finally, the system combines these calculation results into a stepped back suction negative pressure waveform signal: immediately after dispensing, a negative pressure of -0.012005MPa is applied and held for 0.0833 seconds, then the negative pressure is reduced to -0.0036015MPa and maintained until the next dispensing begins.

[0151] S8 combines the opening pulse width compensation parameter, the pre-shear non-dispensing pulse signal and the stepped back suction negative pressure waveform signal to control the dispensing valve actuator and vacuum generator to perform dispensing operations.

[0152] In a specific embodiment of the present invention, the dispensing valve actuator and vacuum generator are controlled to perform dispensing operations by combining the opening pulse width compensation parameter, the pre-shear non-dispensing pulse signal and the stepped back suction negative pressure waveform signal. This includes: acquiring the pre-shear non-dispensing pulse signal and sending it to the dispensing valve actuator for valve core micro-motion control, and generating mesh structure deconstruction state parameters.

[0153] After the state parameters of the mesh structure are generated, the pulse width compensation parameters are converted into duty cycle drive commands and sent to the dispensing valve actuator to generate the fluid continuous extrusion state parameters.

[0154] In a specific embodiment of the present invention, generating fluid continuous extrusion state parameters includes: obtaining network structure deconstruction state parameters and fluid dynamic viscosity parameters for collaborative evaluation, and generating a starting flow resistance compensation coefficient.

[0155] The starting flow resistance compensation coefficient is superimposed on the initial rising edge of the start pulse width compensation parameter to generate the feedforward compensation drive waveform.

[0156] The dispensing valve actuator is opened by controlling the waveform through feedforward compensation, thereby generating a uniform control result for the first drop of glue.

[0157] After the continuous extrusion of the fluid is completed, the stepped back suction negative pressure waveform signal is sent to the vacuum generator for negative pressure back suction control to complete the dispensing operation.

[0158] Specifically, this step is the final execution stage of the entire dispensing control process. It integrates the compensation parameters and control signals calculated in all the previous steps in a timing sequence and sends them to the corresponding hardware actuators, namely the dispensing valve actuator and the vacuum generator, to complete a high-precision, high-consistency dispensing operation. The entire operation process is precisely broken down into three stages: preparation, execution, and completion.

[0159] The first step in the dispensing process is fluid pretreatment. The system acquires the pre-shear non-dispensing pulse signal generated in step S7 and sends it to the dispensing valve actuator. Upon receiving this signal, the actuator drives the valve core to make an extremely brief and minute movement—a micro-motion control. The shear force generated by this micro-motion is sufficient to break the internal network structure formed by the resin during resting, but because its duration is much shorter than the response time of the fluid extruding from the nozzle, it does not cause any adhesive spillage. After this action, the system internally generates a network structure deconstruction state parameter. This parameter serves as a logical indicator that the resin has transitioned from a highly viscous gel state to a readily flowable sol state, preparing it for subsequent smooth extrusion.

[0160] After the network structure deconstruction state parameters are generated, the dispensing operation enters the core extrusion stage. To ensure consistency between the initial dispensing volume and subsequent volumes, a feedforward compensation mechanism is specifically designed for this stage. The system first acquires the network structure deconstruction state parameters and the fluid dynamic viscosity parameters calculated in step S4, and then performs a collaborative evaluation of these two parameters to generate an initial flow resistance compensation coefficient. This coefficient aims to provide an additional driving force at the moment of dispensing initiation to overcome the inertia and residual flow resistance during fluid initiation.

[0161]

[0162] The explanations of the symbols in the formula are as follows: : Starting flow resistance compensation coefficient, dimensionless. It is a dynamically adjusted amplification factor used to enhance the initial drive signal. : Basic initial compensation coefficient, dimensionless. This is a baseline value calibrated experimentally, representing the initial drive enhancement ratio required to achieve first-drop homogenization under calibrated conditions. Set to 1.1. : Viscosity sensitivity adjustment coefficient, dimensionless. This coefficient is used to adjust the sensitivity of the initial compensation to viscosity changes, and is empirically set to 0.5. : Fluid dynamic viscosity parameter, in Pascal-seconds (Pa·s). Calculated from step S5. Initial calibration viscosity parameter, in Pascal-seconds (Pa·s). Defined by step S6.

[0163] Subsequently, the system superimposes this initial flow resistance compensation coefficient onto the initial rising edge of the onset pulse width compensation parameter calculated in step S5, generating a special feedforward compensation drive waveform. Specifically, in the pulse signal that drives the dispensing valve actuator for a total duration equal to the onset pulse width compensation parameter, the drive voltage or current amplitude within the very first extremely short time period (e.g., 1-5 milliseconds) is multiplied by the initial flow resistance compensation coefficient to form a forward spike.

[0164] By controlling the dispensing valve actuator opening using this feedforward compensated drive waveform with a forward spike, a stable flow rate is ensured at the moment of dispensing initiation, thus generating a uniform first drop volume control result. After the initial spike, the drive signal returns to its normal amplitude and continues to act until the total time reaches the duration set by the pulse width compensation parameter. The entire extrusion process is completed, and the system generates fluid continuous extrusion state parameters.

[0165] After the continuous fluid extrusion parameters are completed, the dispensing operation enters its final stage. The system sends the stepped back suction negative pressure waveform signal generated in step S7 to the vacuum generator. Based on the waveform signal, the vacuum generator executes a two-stage negative pressure back suction control. The first stage applies a larger cut-off negative pressure to quickly draw back the adhesive filament outside the nozzle; the second stage switches to a smaller holding negative pressure to prevent leakage during pauses. At this point, a complete dispensing operation is finished.

[0166] For example, following all the previous steps, the system will now perform a complete dispensing operation. The system has the following parameters ready: pulse width compensation enabled. The pre-shear non-glue pulse signal corresponds to the critical driving force for glue breaking. The duration is set to 3 milliseconds. The stepped negative pressure backflow waveform signal includes the parameters for the first step of negative pressure cutoff. Stress release decay time And the second-stage pressure holding negative pressure parameters Fluid dynamic viscosity parameters Initial calibration viscosity parameters .

[0167] First, the controller sends a pre-shear non-dispensing pulse signal to the dispensing valve actuator, driving the valve core to perform micro-motion. After the action is completed, the mesh structure deconstruction state parameters are set to valid. Next, before dispensing, the starting flow resistance compensation coefficient is generated. The parameters acquired by the system are: The calculation process is as follows: The starting flow resistance compensation coefficient is 1.0985865.

[0168] The system then generates a feedforward compensated drive waveform with a total duration of 0.049880 seconds. The initial 3 milliseconds of this waveform have their drive amplitude amplified by a factor of 1.0985865. Subsequently, the controller sends this feedforward compensated drive waveform to the dispensing valve actuator, opening the valve and extruding resin to achieve uniform control of the first drop volume. After 0.049880 seconds, the drive signal stops, and the continuous fluid extrusion state ends.

[0169] Finally, the controller immediately sends a stepped back suction negative pressure waveform signal to the vacuum generator. The vacuum generator applies a negative pressure of -0.012005 MPa for 0.0833 seconds, then adjusts the negative pressure to -0.0036015 MPa and maintains it until the next dispensing command arrives. Thus, the dispensing operation is successfully completed.

[0170] See Figure 4 The second aspect of the present invention provides a dynamic compensation control system for the fluid field of high viscosity resin dispensing, comprising: a consumed resin volume generation module, an equivalent driving pressure parameter calculation module, a dispensing valve parameter acquisition module, a fluid real-time virtual temperature extrapolation module, a fluid dynamic viscosity parameter generation module, an activation pulse width compensation parameter calculation module, a waveform pulse signal matching module, and a dispensing operation execution module.

[0171] The consumed resin volume generation module is connected to the equivalent driving pressure parameter calculation module. The equivalent driving pressure parameter calculation module is connected to the dispensing valve parameter acquisition module. The dispensing valve parameter acquisition module is connected to the fluid real-time virtual temperature extrapolation module. The fluid real-time virtual temperature extrapolation module is connected to the fluid dynamic viscosity parameter generation module. The fluid dynamic viscosity parameter generation module is connected to the pulse width compensation parameter calculation module. The pulse width compensation parameter calculation module is connected to the waveform pulse signal matching module. Both the pulse width compensation parameter calculation module and the waveform pulse signal matching module are connected to the dispensing operation execution module.

[0172] The consumed resin volume generation module is used to obtain the historical cumulative valve opening time parameters of the dispensing valve and the single theoretical extrusion rate parameters, perform integral calculations, and generate the current consumed resin volume parameters.

[0173] The equivalent driving pressure parameter calculation module is used to map the dynamic volume parameter of the air column above the glue cylinder based on the current consumed resin volume parameter, and calculate the equivalent driving pressure parameter under constant work conditions by combining the gas multivariate expansion thermodynamic equation.

[0174] The dispensing valve parameter acquisition module is used to convert the equivalent driving pressure parameters into continuous analog control signals and output them to the electronic proportional pressure regulating valve for air pressure regulation. At the same time, it acquires the dispensing valve's motion frequency parameters, valve core stroke parameters, and fluid back pressure parameters.

[0175] The real-time virtual temperature simulation module for fluids is used to calculate the transient heat accumulation parameters inside the fluid based on the motion frequency parameters, valve core stroke parameters, and fluid back pressure parameters through the fluid shear friction work equation, and to deduce the real-time virtual temperature parameters of the fluid in combination with the valve body heat dissipation model.

[0176] The fluid dynamic viscosity parameter generation module is used to input the real-time virtual temperature parameters of the fluid into the viscosity-temperature curve equation of the high-viscosity resin for calculation, and generate the fluid dynamic viscosity parameters.

[0177] Enable the pulse width compensation parameter calculation module, which is used to calculate the opening pulse width compensation parameter of the dispensing valve using the fluid dynamic viscosity parameter as an adaptive variable, and to obtain the pause time parameter between two dispensing actions.

[0178] The waveform pulse signal matching module is used to input the pause time parameter into the thixotropic recovery time function to calculate the initial yield stress parameter, and generate a pre-shear non-exploding pulse signal and a stepped back suction negative pressure waveform signal that match the initial yield stress parameter.

[0179] The dispensing operation execution module is used to control the dispensing valve actuator and vacuum generator to perform dispensing operations by combining the opening pulse width compensation parameter, the pre-shear non-dispensing pulse signal and the stepped back suction negative pressure waveform signal.

[0180] The above content is merely an example and illustration of the concept of the present invention. Those skilled in the art can make various modifications or additions to the specific embodiments described, or use similar methods to replace them, as long as they do not deviate from the concept of the invention or exceed the scope defined by the present invention, and all such modifications and additions should fall within the protection scope of the present invention.

Claims

1. A method for dynamic compensation and control of the fluid field in high-viscosity resin dispensing, characterized in that, include: S1. Obtain the historical cumulative valve opening time parameter of the dispensing valve and the single theoretical extrusion rate parameter, perform integral calculation, and generate the current consumed resin volume parameter. S2. Map the dynamic volume parameters of the air column above the glue tube according to the current consumed resin volume parameters, and calculate the equivalent driving pressure parameters under constant work conditions by combining the gas multi-directional expansion thermodynamic equation. S3. Convert the equivalent driving pressure parameters into a continuous analog control signal and output it to the electronic proportional pressure regulating valve for air pressure regulation. At the same time, obtain the motion frequency parameters, valve core stroke parameters and fluid back pressure parameters of the dispensing valve. S4. Based on the motion frequency parameters, valve core stroke parameters and fluid back pressure parameters, the transient heat accumulation parameters inside the fluid are calculated through the fluid shear friction work equation, and the real-time virtual temperature parameters of the fluid are deduced by combining the valve body heat dissipation model. S5. Input the real-time virtual temperature parameters of the fluid into the viscosity-temperature curve equation of the high-viscosity resin for calculation to generate the dynamic viscosity parameters of the fluid. S6. Calculate the opening pulse width compensation parameter of the dispensing valve using the fluid dynamic viscosity parameter as an adaptive variable, and obtain the pause time parameter between two dispensing actions. S7. Input the pause time parameter into the thixotropic recovery time function to calculate the initial yield stress parameter, and generate a pre-shear non-exploding pulse signal and a stepped back suction negative pressure waveform signal that match the initial yield stress parameter. S8 combines the opening pulse width compensation parameter, the pre-shear non-dispensing pulse signal and the stepped back suction negative pressure waveform signal to control the dispensing valve actuator and vacuum generator to perform dispensing operations.

2. The method for dynamic compensation and control of the fluid field in high-viscosity resin dispensing according to claim 1, characterized in that, The generation of the currently consumed resin volume parameter includes: Acquire multiple dispensing operation records of the dispensing valve since the last reset or replacement of the resin cartridge, extract the valve opening duration of each dispensing action and sum them up to generate historical cumulative valve opening time parameters. The current driving air pressure parameters, fluid temperature parameters, and resin viscosity parameters of the dispensing valve are obtained. Based on the preset fluid dynamics model, the resin extrusion volume per unit time is calculated as the single theoretical extrusion rate parameter. Using time as the integration variable, the single theoretical extrusion rate parameter is integrated over the interval of the historical cumulative valve opening time parameter to obtain the cumulative extrusion volume; The cumulative extrusion volume is summed with the preset system pipeline loss compensation value to generate the current resin consumption volume parameter.

3. The method for dynamic compensation and control of the dispensing fluid field of high-viscosity resin according to claim 1, characterized in that, The calculation of the equivalent driving pressure parameters under constant work conditions using the gas multivariate expansion thermodynamic equation includes: The difference between the dynamic volume parameters and the initial cavity volume parameters of the rubber tube is calculated to generate real-time gas phase volume parameters. Substitute the real-time gas phase volume parameters and the basic driving gas pressure parameters into the gas multivariate expansion thermodynamic equation to solve for energy conservation, and generate a single pulse as the energy quantity parameter. Based on the single pulse function parameters and real-time gas phase volume parameters, inverse pressure compensation deduction is performed to generate equivalent driving pressure parameters.

4. The method for dynamic compensation and control of the dispensing fluid field of high-viscosity resin according to claim 1, characterized in that, The derivation of real-time virtual temperature parameters of the fluid using the valve body heat dissipation model includes: The motion frequency parameters and valve core stroke parameters are obtained to calculate the valve core motion speed parameters. The valve core motion speed parameters and fluid back pressure parameters are then substituted into the fluid shear friction work equation to generate the shear work parameters per unit time. By integrating the shear work parameter per unit time in the time domain, the transient heat accumulation parameter inside the fluid is generated. The transient heat accumulation parameters inside the fluid are obtained and combined with the heat dissipation model of the valve body to calculate the heat conduction attenuation, thereby generating real-time virtual temperature parameters of the fluid.

5. The method for dynamic compensation and control of the dispensing fluid field of high-viscosity resin according to claim 1, characterized in that, The generated fluid dynamic viscosity parameters include: The activation energy parameters and general gas constant parameters of high viscosity resin are obtained, and exponential calculations are performed in combination with the real-time virtual temperature parameters of the fluid to generate temperature influence factor parameters. Obtain the reference temperature viscosity parameters of the high viscosity resin, and multiply the reference temperature viscosity parameters with the temperature influence factor parameters to generate the theoretical viscosity parameters; The current shear rate parameter of the dispensing valve is obtained, and the theoretical viscosity parameter is corrected for non-Newtonian fluid shear thinning to generate the fluid dynamic viscosity parameter.

6. The method for dynamic compensation and control of the fluid field in high-viscosity resin dispensing according to claim 1, characterized in that, The calculation of the opening pulse width compensation parameters of the dispensing valve using fluid dynamic viscosity parameters as adaptive variables includes: The ratio of the obtained fluid dynamic viscosity parameters to the initial calibrated viscosity parameters is calculated to generate the viscosity drift coefficient parameters. The viscosity drift coefficient parameter is multiplied with the reference valve opening time parameter to generate the initial pulse width adjustment parameter. The current equivalent driving pressure parameters of the electronic proportional pressure regulating valve are obtained, and the initial pulse width adjustment parameters are calibrated by pressure-flow coupling to generate the activation pulse width compensation parameters.

7. The method for dynamic compensation and control of the dispensing fluid field of high-viscosity resin according to claim 1, characterized in that, The generation of the pre-shear non-gluing pulse signal and the stepped back suction negative pressure waveform signal, which match the initial yield stress parameters, includes: The pause time parameter is obtained and substituted into the thixotropic recovery time function for exponential growth fitting to generate the initial yield stress parameter. The critical driving force parameter for glue breaking is generated by multiplying the initial yield stress parameter with the valve core cross-sectional area parameter of the dispensing valve. Based on the critical driving force parameter for breaking the glue, a micro-motion control pulse signal with a duration shorter than the critical time for fluid extrusion is generated to obtain a pre-shear non-glue pulse signal; The residual stress parameters of the pipeline at the end of dispensing valve and the dynamic viscosity parameters of the fluid are weighted and calculated to generate the first-step cut-off negative pressure parameters. The stress release attenuation time is calculated based on the first-step cut-off negative pressure parameters and the pipeline cross-sectional dimensions, and the second-step pressure-holding negative pressure parameters are generated. The first-step cut-off negative pressure parameter, the second-step pressure holding negative pressure parameter, and the stress release decay time are sequentially spliced ​​together to generate a stepped back suction negative pressure waveform signal.

8. The method for dynamic compensation and control of the fluid field in high-viscosity resin dispensing according to claim 1, characterized in that, The method of controlling the dispensing valve actuator and vacuum generator to perform dispensing operations by combining the opening pulse width compensation parameter, the pre-shear non-dispensing pulse signal and the stepped back suction negative pressure waveform signal includes: Acquire the pre-shear non-dispensing pulse signal and send it to the dispensing valve actuator for valve core micro-motion control, and generate mesh structure deconstruction state parameters; After the state parameters of the mesh structure are generated, the pulse width compensation parameters are converted into duty cycle drive commands and sent to the dispensing valve actuator to generate the fluid continuous extrusion state parameters. After the continuous extrusion of the fluid is completed, the stepped back suction negative pressure waveform signal is sent to the vacuum generator for negative pressure back suction control to complete the dispensing operation.

9. The method for dynamic compensation and control of the fluid field in high-viscosity resin dispensing according to claim 8, characterized in that, The continuous extrusion state parameters of the generated fluid include: The deconstruction state parameters of the network structure and the dynamic viscosity parameters of the fluid are obtained and evaluated in a coordinated manner to generate the initial flow resistance compensation coefficient. The starting flow resistance compensation coefficient is superimposed on the initial rising edge of the start pulse width compensation parameter to generate the feedforward compensation drive waveform. The dispensing valve actuator is opened by controlling the waveform through feedforward compensation, thereby generating a uniform control result for the first drop of glue.

10. A dynamic compensation control system for the fluid field of high-viscosity resin dispensing, characterized in that, include: The consumed resin volume generation module is used to obtain the historical cumulative valve opening time parameter and the single theoretical extrusion rate parameter of the dispensing valve, perform integral calculation, and generate the current consumed resin volume parameter. The equivalent driving pressure parameter calculation module is used to map the dynamic volume parameter of the air column above the glue cylinder according to the current consumed resin volume parameter, and calculate the equivalent driving pressure parameter under constant work conditions by combining the gas multi-directional expansion thermodynamic equation. The dispensing valve parameter acquisition module is used to convert the equivalent driving pressure parameters into continuous analog control signals and output them to the electronic proportional pressure regulating valve for air pressure regulation. At the same time, it acquires the dispensing valve's motion frequency parameters, valve core stroke parameters, and fluid back pressure parameters. The real-time virtual temperature deduction module for fluid is used to calculate the transient heat accumulation parameters inside the fluid based on the motion frequency parameters, valve core stroke parameters and fluid back pressure parameters through the fluid shear friction work equation, and to deduce the real-time virtual temperature parameters of the fluid in combination with the valve body heat dissipation model. The fluid dynamic viscosity parameter generation module is used to input the real-time virtual temperature parameters of the fluid into the viscosity-temperature curve equation of the high-viscosity resin for calculation and to generate the fluid dynamic viscosity parameters. Enable the pulse width compensation parameter calculation module, which is used to calculate the opening pulse width compensation parameter of the dispensing valve with the fluid dynamic viscosity parameter as an adaptive variable, and obtain the pause time parameter between two dispensing actions; The waveform pulse signal matching module is used to input the pause time parameter into the thixotropic recovery time function to calculate the initial yield stress parameter, and generate a pre-shear non-gluing pulse signal and a stepped back suction negative pressure waveform signal that match the initial yield stress parameter. The dispensing operation execution module is used to control the dispensing valve actuator and vacuum generator to perform dispensing operations by combining the opening pulse width compensation parameter, the pre-shear non-dispensing pulse signal and the stepped back suction negative pressure waveform signal.

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