Safety discharge control method, device and equipment

Abstract

The embodiments of the present disclosure provide a method, device and equipment for safe discharge control. The method includes: obtaining the current temperature of the real reactor; wherein the real reactor includes a high-energy substance that releases heat greater than a preset heat; if the current temperature reaches the refrigerant injection temperature, a preset amount of refrigerant is injected into the real reactor; based on the temperature change trend of the real reactor and the change trend of the non-condensable gas production rate, it is determined whether the real reactor is a single-phase flow discharge. In this way, an effective discharge protection plan can be adopted early, and it can be automatically and accurately predicted whether the real reactor will have a single-phase flow discharge, and its discharge form can be suppressed from changing to a two-phase flow to ensure safety.

Description

Technical Field

[0001] The present disclosure relates to the field of chemical industry, and in particular to the field of safe discharge technology. Background Art

[0002] In recent years, with the growth of my country's industrial demand and the rapid development of the chemical industry, it is inevitable to come into contact with new synthesis processes and hazardous materials. Many hazardous chemical processes are highly exothermic reactions, and their products are also high-energy substances. When such high-energy substances have runaway reactions, they will cause huge chemical safety risks. However, for the runaway chemical reaction process in which the products in the reactor contain high-energy substances, it is currently impossible to effectively determine whether single-phase flow discharge or two-phase flow discharge will occur, and it is impossible to adopt effective discharge protection plans. Summary of the invention

[0003] The present disclosure provides a safety discharge control method, device, equipment and storage medium.

[0004] According to a first aspect of the present disclosure, a safety discharge control method is provided. The method comprises:

[0005] Acquiring the current temperature of a real reactor; wherein the real reactor contains a high-energy substance that releases heat greater than a preset heat;

[0006] If the current temperature reaches the refrigerant injection temperature, a preset amount of refrigerant is injected into the real reactor; wherein the refrigerant is used to lower the temperature of the real reactor;

[0007] Predicting the temperature change trend and the non-condensable gas production rate change trend of the real reactor after the preset amount of refrigerant is injected; wherein the temperature change trend of the real reactor is the change trend of the temperature in the real reactor over time; the non-condensable gas production rate change trend of the real reactor is the change trend of the non-condensable gas production rate in the real reactor over temperature;

[0008] According to the temperature change trend of the real reactor and the non-condensable gas production rate change trend, it is determined whether the discharge flow type of the real reactor is single-phase flow discharge.

[0009] According to the above aspects and any possible implementation, an implementation is further provided, wherein judging whether the real reactor is a single-phase flow discharge according to the temperature change trend of the real reactor and the change trend of the non-condensable gas production rate comprises:

[0010] Determining the void ratio of the actual reactor after injecting a preset amount of refrigerant;

[0011] Calculating the dimensionless superficial gas velocity of the two-phase flow according to the void fraction;

[0012] Calculate the current dimensionless superficial gas velocity of the real reactor according to the temperature change trend of the real reactor and the change trend of the non-condensable gas production rate, as well as the discharge volume calculation formula;

[0013] If the current dimensionless superficial gas velocity of the real reactor is greater than or equal to the dimensionless superficial gas velocity of the two-phase flow, it is determined that after the preset amount of refrigerant is injected, the discharge flow type of the real reactor is two-phase flow discharge; otherwise, it is determined that the discharge flow type of the real reactor is single-phase flow discharge.

[0014] According to the above aspects and any possible implementation, an implementation is further provided, wherein the current dimensionless superficial gas velocity of the real reactor is calculated according to the temperature change trend of the real reactor and the change trend of the non-condensable gas production rate, and the discharge volume calculation formula, including:

[0015] According to the temperature change trend of the real reactor, the change trend of the non-condensable gas production rate, the mass of the high-energy substance in the real reactor, the density of the non-condensable gas in the real reactor and the discharge amount calculation formula, the gas discharge amount of the real reactor is obtained; wherein the gas discharge amount includes: the discharge amount of the non-condensable gas and steam in the real reactor;

[0016] The dimensionless superficial gas velocity of the real reactor is calculated by using the gas release volume of the real reactor, the cross-sectional area of ​​the real reactor, the gas phase density and the liquid phase density of the real reactor.

[0017] According to the above aspects and any possible implementation manner, an implementation manner is further provided, wherein the method further includes:

[0018] According to the judgment result of whether the real reactor is discharged in single-phase flow under different preset amounts of refrigerant and different masses of high-energy substances, the injection amount of the refrigerant when the discharge flow pattern of the real reactor satisfies the single-phase flow discharge is determined.

[0019] According to the above aspects and any possible implementation, an implementation is further provided, wherein the predicting of the temperature change trend and the non-condensable gas production rate change trend of the real reactor after the preset amount of refrigerant is injected includes:

[0020] Determining the mixed temperature in the actual reactor after injecting the preset amount of coolant;

[0021] Predicting the temperature change trend of the real reactor according to the mixing temperature in the real reactor, the thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor corresponding to the real reactor;

[0022] According to the temperature change trend of the real reactor and the pre-acquired non-condensable gas production rate change trend of the simulated reactor, the non-condensable gas production rate change trend of the real reactor is obtained.

[0023] According to the above aspects and any possible implementation, an implementation is further provided, wherein the variation trend of the non-condensable gas production rate of the simulated reactor is obtained by the following steps:

[0024] Obtaining the temperature change trend and pressure change trend of the simulated reactor when the coolant is not injected into the simulated reactor; wherein the pressure change trend of the simulated reactor is the change trend of the pressure of the non-condensable gas in the simulated reactor over time;

[0025] Determining the gas production rate of the non-condensable gas in the simulated reactor over time according to the pressure change trend of the simulated reactor;

[0026] According to the temperature change trend of the simulated reactor and the gas production rate of the non-condensable gas in the simulated reactor over time, the change trend of the non-condensable gas production rate of the simulated reactor is calculated, wherein the temperature change trend of the simulated reactor is the change trend of the temperature in the simulated reactor over time.

[0027] According to the above aspects and any possible implementation, an implementation is further provided, wherein the thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor are obtained by the following steps:

[0028] Obtaining a temperature change trend of the simulated reactor when the coolant is not injected into the simulated reactor;

[0029] According to the temperature variation trend and the Arrhenius formula, a linear function fitting is performed to obtain the thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor.

[0030] According to the aspects described above and any possible implementation method, an implementation method is further provided, in which the causes of the real reactor reaction being out of control are different, and the corresponding thermodynamic parameters and macroscopic kinetic parameters are different.

[0031] According to a second aspect of the present disclosure, a safety discharge control device is provided. The device comprises:

[0032] An acquisition module, used to acquire the current temperature of a real reactor; wherein the real reactor contains a high-energy substance that releases heat greater than a preset heat;

[0033] An injection module, used for injecting a preset amount of refrigerant into the real reactor if the current temperature reaches the refrigerant injection temperature; wherein the refrigerant is used to reduce the temperature of the real reactor;

[0034] A prediction module is used to predict the temperature change trend and the non-condensable gas production rate change trend of the real reactor after the preset amount of refrigerant is injected; wherein the temperature change trend of the real reactor is the change trend of the temperature in the real reactor over time; the non-condensable gas production rate change trend of the real reactor is the change trend of the non-condensable gas production rate in the real reactor over temperature;

[0035] The judgment module is used to judge whether the real reactor is in single-phase flow discharge according to the temperature change trend and the non-condensable gas production rate change trend of the real reactor.

[0036] According to a third aspect of the present disclosure, an electronic device is provided, which includes a memory and a processor, wherein a computer program is stored in the memory, and when the processor executes the program, the method described above is implemented.

[0037] According to a fourth aspect of the present disclosure, a computer-readable storage medium is provided, on which a computer program is stored. When the program is executed by a processor, the method according to the first aspect and / or the second aspect of the present disclosure is implemented.

[0038] In the present disclosure, by obtaining the current temperature of the real reactor, it can be determined whether the current temperature has reached the refrigerant injection temperature. If reached, a preset amount of refrigerant is injected into the real reactor, and then the temperature change trend of the real reactor and the non-condensable gas production rate change trend are predicted after the preset amount of refrigerant is injected. Therefore, based on the temperature change trend of the real reactor and the non-condensable gas production rate change trend, it is automatically and accurately predicted whether a single-phase flow discharge will occur in the real reactor. If so, it means that after the preset amount of refrigerant is injected, the risk of an out-of-control chemical reaction process in which the product in the real reactor contains high-energy substances is low, and it can be protected by discharge. If not, it means that it is a two-phase flow discharge, and the discharge amount is relatively large, which is not easy to pass the discharge protection. Therefore, an effective discharge protection plan should be adopted as early as possible to ensure safety.

[0039] It should be understood that the contents described in the summary of the invention are not intended to limit the key or important features of the embodiments of the present disclosure, nor are they intended to limit the scope of the present disclosure. Other features of the present disclosure will become easily understood through the following description. BRIEF DESCRIPTION OF THE DRAWINGS

[0040] The above and other features, advantages and aspects of the embodiments of the present disclosure will become more apparent with reference to the following detailed description in conjunction with the accompanying drawings. The accompanying drawings are used to better understand the present solution and do not constitute a limitation of the present disclosure. In the accompanying drawings, the same or similar reference numerals represent the same or similar elements, among which:

[0041] Figure 1A flow chart of a safety discharge control method according to an embodiment of the present disclosure is shown;

[0042] Figure 2 A block diagram of a safety discharge control device according to an embodiment of the present disclosure is shown;

[0043] Figure 3 A schematic diagram showing a change trend of the non-condensable gas production rate according to an embodiment of the present disclosure is shown;

[0044] Figure 4 A schematic diagram showing temperature changes after a refrigerant is injected into a real reactor according to an embodiment of the present disclosure is shown;

[0045] Figure 5 A schematic diagram showing the relationship between the apparent gas velocity on the abscissa and the void fraction on the ordinate according to an embodiment of the present disclosure is shown;

[0046] Figure 6 A block diagram of another safety discharge control device according to an embodiment of the present disclosure is shown;

[0047] Figure 7 A block diagram of an exemplary electronic device capable of implementing embodiments of the present disclosure is shown.

[0048] Below Figure 2 The corresponding relationship between the parts and numbers is explained below:

[0049] 1. Refrigerant storage tank; 2. Oil pump; 3. Flow meter; 4. Flow regulating valve; 5. Agitator; 6. Circulation pump; 7. Distributor; 8. Reactor; 9. Temperature controller; 10. Pressure controller; 11. Safety release device; 12. Heat exchanger; 13. Gas-liquid separation tank; ①-④, refrigerant injection pipeline; ⑤-⑦, release pipeline; ⑧, refrigerant return pipeline. DETAILED DESCRIPTION

[0050] In order to make the purpose, technical solution and advantages of the embodiments of the present disclosure clearer, the technical solution in the embodiments of the present disclosure will be clearly and completely described below in conjunction with the drawings in the embodiments of the present disclosure. Obviously, the described embodiments are part of the embodiments of the present disclosure, not all of the embodiments. Based on the embodiments in the present disclosure, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present disclosure.

[0051] In addition, the term "and / or" in this article is only a description of the association relationship between the associated objects, indicating that there can be three relationships. For example, A and / or B can represent: A exists alone, A and B exist at the same time, and B exists alone. In addition, the character " / " in this article generally indicates that the associated objects before and after are in an "or" relationship.

[0052] Figure 1 A flow chart of a safety discharge control method 100 according to an embodiment of the present disclosure is shown. The method 100 may include:

[0053] Step 110, obtaining the current temperature of the real reactor; wherein the real reactor contains high-energy substances that release heat greater than a preset heat;

[0054] High energy substances include, but are not limited to: peroxides, azides, hydroxylamine salt compounds, oxygen-containing acid compounds, polynitro compounds, etc.

[0055] High-energy substances are substances with relatively large bond energy and contain relatively large energy. Under the induction of high temperature and high pressure, the energy / heat that can be released per unit mass is greater than the preset joules, that is, the energy that can be released by high-energy substances is greater than the first preset joules / gram or the second preset joules / kilogram (thermodynamic parameters).

[0056] High-energy substances can be reactants, products, or a mixture of the two in a real reactor.

[0057] Step 120, if the current temperature reaches the refrigerant injection temperature, inject a preset amount of refrigerant into the real reactor; wherein the refrigerant is used to reduce the temperature of the real reactor;

[0058] The refrigerant includes, but is not limited to, water, an organic solvent, an ionic liquid, or an inert refrigerant with a large latent heat of vaporization.

[0059] Reactors include, but are not limited to, kettle reactors, tubular reactors, and tower reactors.

[0060] The lower limit of the coolant injection temperature is 1.1 times the suitable reaction temperature of the reactor, and the upper limit is the maximum temperature that the reactor can withstand.

[0061] As long as the current temperature is greater than or equal to 1.1 times the suitable reaction temperature of the reactor and less than or equal to the maximum temperature that the reactor can withstand, a preset amount of refrigerant is injected into the real reactor.

[0062] Of course, there is more than one preset amount, and there can be multiple preset amounts, so as to determine the appropriate amount of refrigerant when discharging single-phase flow.

[0063] Step 130, predicting the temperature change trend and the non-condensable gas production rate change trend of the real reactor after the preset amount of refrigerant is injected; wherein the temperature change trend of the real reactor is the change trend of the temperature in the real reactor over time or the change trend of the temperature rise rate in the real reactor over time; the non-condensable gas production rate change trend of the real reactor is the change trend of the non-condensable gas production rate in the real reactor over temperature;

[0064] Non-condensable gas is the gas that cannot be condensed in the actual reactor under normal circumstances. Its composition is different in different devices and systems, and it can be nitrogen, hydrogen, etc.

[0065] Step 140, judging (to be more precise, predicting or evaluating) whether the discharge flow type of the real reactor is single-phase flow discharge according to the temperature change trend and the non-condensable gas production rate change trend of the real reactor. Single-phase flow discharge means that when the discharge pressure is reached, the discharge of the reactor is only gas.

[0066] By obtaining the current temperature of the real reactor, it can be determined whether the current temperature has reached the refrigerant injection temperature. If it has reached it, a preset amount of refrigerant is injected into the real reactor, and then the temperature change trend and the non-condensable gas production rate change trend of the real reactor after the preset amount of refrigerant is injected are predicted. Therefore, according to the temperature change trend and the non-condensable gas production rate change trend of the real reactor, it is automatically and accurately predicted whether the real reactor will have a single-phase flow discharge. If so, it means that after the preset amount of refrigerant is injected, the risk of the runaway chemical reaction process containing high-energy substances in the real reactor is low, and it can be protected by discharge. If not, it means that it is a two-phase flow discharge, and the discharge volume is relatively large. Therefore, an effective discharge protection plan can be taken as soon as possible to ensure safety. If the real reactor is a two-phase flow discharge (that is, when the discharge pressure is reached, the discharge of the reactor is a gas-liquid mixture), the discharge protection plan adopted can be: increase the amount of refrigerant or require a larger discharge safety valve size due to the large discharge volume, so the discharge safety valve size can be increased according to the size of the discharge volume.

[0067] In some embodiments, judging whether the real reactor is a single-phase flow discharge according to the temperature change trend of the real reactor and the non-condensable gas production rate change trend includes:

[0068] Determining the void ratio of the actual reactor after injecting a preset amount of refrigerant;

[0069] The void ratio is used to characterize the ratio of the volume of the unfilled space in the real reactor to the volume of the entire space of the real reactor. Therefore, the larger the preset amount of refrigerant injected into the real reactor, the larger the filled space in the real reactor, and the smaller the void ratio will naturally be.

[0070] According to the void fraction, the dimensionless superficial gas velocity of the two-phase flow is calculated as

[0071] Wherein, α is the porosity of the reactor;

[0072] The superficial gas velocity is used to characterize the rising speed of gas in a real reactor;

[0073] The dimensionless superficial gas velocity of two-phase flow refers to the minimum superficial gas velocity during two-phase discharge.

[0074] Calculate the current dimensionless superficial gas velocity of the real reactor according to the temperature change trend of the real reactor and the change trend of the non-condensable gas production rate, as well as the discharge volume calculation formula;

[0075] The formula for calculating the discharge volume is F, m is the mass of high-energy substances in the real industrial reactor, c p is the specific heat capacity of the high energy content substance in the real reactor, is the temperature rise rate corresponding to the injection of refrigerant under the release pressure, ΔHv is the vaporization heat of the refrigerant or the vaporization heat of the refrigerant and the solvent (solvent of the reactor), Q g is the non-condensable gas production rate after injecting refrigerant under the release pressure, ρ g It is the density of non-condensable gas under the release pressure.

[0076] If the current dimensionless superficial gas velocity of the real reactor is greater than or equal to the dimensionless superficial gas velocity of the two-phase flow, it is determined that after the preset amount of refrigerant is injected, the discharge flow type of the real reactor is two-phase flow discharge; otherwise, it is determined that the discharge flow type of the real reactor is single-phase flow discharge.

[0077] Since the temperature change trend is used to characterize the change trend of the temperature in the real reactor with time, the non-condensable gas production rate change trend is used to characterize the change trend of the non-condensable gas production rate in the real reactor with temperature, and the discharge temperature corresponds to the discharge pressure, therefore, according to the temperature change trend and the non-condensable gas production rate change trend of the real reactor, the temperature rise rate under the discharge pressure and the non-condensable gas production rate under the discharge pressure can be determined, and then combined with the discharge amount calculation formula, the current dimensionless superficial gas velocity of the real reactor can be accurately calculated, and since the dimensionless superficial gas velocity of the two-phase flow is the lowest superficial gas velocity of the two-phase flow discharge calculated based on the void fraction, therefore, if the current dimensionless superficial gas velocity of the real reactor is greater than or equal to the dimensionless superficial gas velocity of the two-phase flow, it is determined that after the preset amount of refrigerant is injected, the discharge flow type of the real reactor is two-phase flow discharge, and the risk of the uncontrolled chemical reaction process is high, otherwise, the discharge flow type of the real reactor is determined to be single-phase flow discharge, and the risk of the uncontrolled chemical reaction process is low.

[0078] In some embodiments, the current dimensionless superficial gas velocity of the real reactor is calculated according to the temperature change trend of the real reactor and the change trend of the non-condensable gas production rate, as well as the discharge volume calculation formula, including:

[0079] According to the temperature change trend of the real reactor, the change trend of the non-condensable gas production rate, the mass of the high-energy substance in the real reactor, the density of the non-condensable gas in the real reactor and the discharge amount calculation formula, the gas discharge amount of the real reactor is obtained; wherein the gas discharge amount includes: the discharge amount of the non-condensable gas and steam in the real reactor;

[0080] The dimensionless superficial gas velocity of the real reactor is calculated by using the gas release volume of the real reactor, the cross-sectional area of ​​the real reactor, the gas phase density and the liquid phase density of the real reactor.

[0081] According to the temperature change trend of the real reactor and the change trend of the non-condensable gas production rate, the temperature rise rate under the relief pressure and the non-condensable gas production rate under the relief pressure can be determined. Then, based on the temperature rise rate under the relief pressure, the non-condensable gas production rate under the relief pressure, the mass of high-energy substances in the real reactor, the density of non-condensable gas in the real reactor, the heat of vaporization of the refrigerant or the heat of vaporization of the refrigerant and the solvent of the reactor, and the discharge amount calculation formula, the gas discharge amount of the reactor under the discharge pressure can be accurately predicted. Then, the gas discharge amount of the real reactor, the cross-sectional area of ​​the real reactor, the gas phase density and the liquid phase density of the real reactor can be used to accurately calculate the dimensionless apparent gas velocity of the real reactor.

[0082] The dimensionless superficial gas velocity is The calculation formula is as follows:

[0083]

[0084]

[0085]

[0086] j g is the apparent gas rising rate, F is the amount of gas (non-condensable gas and steam in the actual reactor) released, ρ g is the density of the gas at the release pressure, A x is the cross-sectional area of ​​the reactor, ρ f is the density of the liquid phase in the real reactor, and σ is the surface tension of the liquid phase in the real reactor.

[0087] In some embodiments, the method further comprises:

[0088] According to the judgment result of whether the real reactor is discharged in single-phase flow under different preset amounts of refrigerant and different masses of high-energy substances, the injection amount of the refrigerant when the discharge flow pattern of the real reactor satisfies the single-phase flow discharge is determined.

[0089] No matter how much the refrigerant and high energy content are, as long as the current dimensionless superficial gas velocity of the real reactor is greater than or equal to the dimensionless superficial gas velocity of the two-phase flow, the real reactor is discharged in a two-phase flow; otherwise, the real reactor is discharged in a single-phase flow. In addition, the discharge type of the real reactor may be different depending on the refrigerant and the high energy content. Therefore, according to the amount of refrigerant in single-phase flow discharge under different masses of high energy content, it can be confirmed that the discharge flow type of the real reactor meets the injection amount of the refrigerant in single-phase flow discharge under different masses of high energy content, so as to ensure safety by controlling the injection amount of the refrigerant to suppress the conversion of its discharge form to two-phase flow.

[0090] In addition, the amount of refrigerant injected when the real reactor meets the single-phase flow discharge under different masses of high-energy substances can be prompted, so that the user of the real reactor can clearly know how much refrigerant to add when the real reactor is used to cause an uncontrolled chemical reaction of high-energy substances, to ensure that the real reactor is discharged in a single-phase flow, and to avoid too little or too much refrigerant added, resulting in a two-phase flow discharge when the real reactor is discharged.

[0091] Finally, the size of the discharge safety valve of the real reactor can be determined by the gas release volume of the real reactor.

[0092] In some embodiments, the prediction of the temperature change trend and the non-condensable gas production rate change trend of the actual reactor after the preset amount of refrigerant is injected includes:

[0093] Determining the mixed temperature in the actual reactor after injecting the preset amount of coolant;

[0094] The mixing temperature is the final temperature of the real reactor after a preset amount of refrigerant is injected into the real reactor.

[0095] Predicting the temperature change trend of the real reactor according to the mixing temperature in the real reactor, the thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor corresponding to the real reactor;

[0096] is the pre-exponential factor, E is the activation energy of the reaction, T is the current temperature (also called the reaction temperature), T f is the maximum temperature that can be reached by the runaway reaction (i.e. the maximum temperature allowed to be reached), ΔT is the adiabatic temperature rise (equal to the maximum temperature T f Subtract the reaction temperature T), C A0 is the initial concentration.

[0097] The macroscopic kinetic parameters are the reaction order n, the reaction activation energy E, and the pre-exponential factor A. The thermodynamic parameter is the specific heat release (i.e., the energy that can be released per unit mass, which can be obtained through the bond energy of high-energy substances). Specific heat release / specific heat capacity = adiabatic temperature rise ΔT, T+ΔT = Tf, i.e. T f It is also a thermodynamic parameter.

[0098] The initial temperature T is the mixing temperature, and then the above formula can be used to get the initial temperature rise rate dT / dt. Then, based on the initial temperature rise rate and the assumed time interval, the next moment T can be obtained. Then, the above formula can be used to get the temperature rise rate at the next moment. In this way, the cycle is repeated continuously to predict the temperature change trend of the real reactor.

[0099] Among them, dT refers to the temperature change, and dT / dt is naturally the temperature rise rate.

[0100] According to the temperature change trend of the real reactor and the pre-acquired non-condensable gas production rate change trend of the simulated reactor, the non-condensable gas production rate change trend of the real reactor is obtained.

[0101] Since the changing trend of the non-condensable gas production rate of the simulated reactor is obtained in advance, and the changing trend of the non-condensable gas production rate of the simulated reactor is used to characterize the changing trend of the non-condensable gas production rate with temperature, and the temperature changing trend of the real reactor is used to characterize the changing trend of the temperature of the real reactor with time, therefore, the changing trend of the non-condensable gas production rate of the real reactor can be accurately obtained according to the temperature changing trend of the real reactor and the changing trend of the non-condensable gas production rate of the simulated reactor.

[0102] In some embodiments, the variation trend of the non-condensable gas production rate of the simulated reactor is obtained by the following steps:

[0103] Obtaining the temperature change trend and pressure change trend of the simulated reactor when the coolant is not injected into the simulated reactor; wherein the pressure change trend of the simulated reactor is the change trend of the pressure of the non-condensable gas in the simulated reactor over time;

[0104] The simulated reactor corresponds to the real reactor, is the same as or similar to the real reactor, and is used to be placed in a laboratory. The simulated reactor can be used to simulate the reaction process of the real reactor.

[0105] Of course, in order to ensure the accuracy of the temperature change trend and the pressure change trend, the simulated reactor temperature sensors can be set at the top, middle and bottom of the reactor, and each temperature measuring point has at least two thermocouples; the final measured temperature can be the middle value or average value of the three temperature sensors.

[0106] The pressure measuring point corresponding to the pressure sensor should measure the gas phase pressure of the reactor, and the reactor should have at least two independent pressure circuits and pressure gauges; the final measured pressure can be taken as the average value.

[0107] Determining the gas production rate of the non-condensable gas in the simulated reactor over time according to the pressure change trend of the simulated reactor;

[0108] According to the temperature change trend of the simulated reactor and the gas production rate of non-condensable gas in the simulated reactor over time, the non-condensable gas production rate change trend of the simulated reactor is calculated, wherein the temperature change trend of the simulated reactor is the temperature change trend in the simulated reactor over time, and the non-condensable gas production rate change trend of the simulated reactor is the non-condensable gas production rate change trend in the simulated reactor over temperature.

[0109] Since pressure is closely related to the production rate of non-condensable gas, and under the same accumulated time, the greater the pressure, the greater the production rate of non-condensable gas, and the smaller the pressure, the smaller the production rate of non-condensable gas. Therefore, according to the pressure change trend with time in the simulated reactor, the production rate of non-condensable gas in the simulated reactor with time can be automatically determined. By combining the temperature change trend with time in the simulated reactor and the production rate of non-condensable gas with time, the change trend of the non-condensable gas production rate with temperature in the simulated reactor can be automatically and accurately calculated.

[0110] In some embodiments, the thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor are obtained by the following steps:

[0111] Obtaining a temperature change trend of the simulated reactor when the coolant is not injected into the simulated reactor;

[0112] According to the temperature change trend and Arrhenius formula, linear function fitting is performed to obtain the thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor. The temperature rise rate expression combined with Arrhenius is:

[0113] A is the pre-exponential factor, E is the activation energy of the reaction, T is the temperature, T f is the maximum temperature that can be reached by the runaway reaction, ΔT is the adiabatic temperature rise, C A0 is the initial concentration.

[0114] The macroscopic kinetic parameters are reaction order, reaction activation energy, and pre-exponential factor, and the thermodynamic parameter is specific heat release.

[0115] After assuming n, the reaction activation energy E and pre-exponential factor A can be obtained by taking the derivative of the temperature rise over time (dT / dt) using the ln logarithm.

[0116] The method of obtaining the reaction level n is as follows: first assume that n = 1.1, then add a preset trend line corresponding to the custom n, and then calculate the variance of the preset trend line and the linear function obtained after the above derivation. When the variance is greater than 0.999, n is reasonable.

[0117] The reaction heat ΔHr can be obtained by subtracting the bond energy between the products and reactants in the real reactor.

[0118] In some embodiments, the reasons for the runaway reaction in the real reactor are different, and the corresponding thermodynamic parameters and macroscopic kinetic parameters are different.

[0119] The reasons for the real reactor reaction to run away with control may include: cooling failure, adding too much material, adding too little material, etc.

[0120] Since the reasons for runaway reactions in real reactors are different, different scenarios need to be simulated in the simulation reactor. For example, if too much material is added to the real reactor, more material needs to be added to the simulation reactor; or if too little material is added to the real reactor, less material needs to be added to the simulation reactor. Therefore, the thermodynamic parameters and macroscopic kinetic parameters in the simulation reactor are different.

[0121] The following will be combined Figures 2 to 7 The disclosed safe discharge control method is specifically described as follows:

[0122] Figure 2 The temperature control loop 9 in the reactor detects that the reactor temperature is abnormal and reaches the interlock injection temperature of the refrigerant injection. The interlock opens the flow regulating valve 4, and the flow meter 3 starts to monitor the injection flow. The refrigerant in the refrigerant storage tank 1 is injected into the reactor 8 through the refrigerant injection pipe ①-④ through the oil pump 2. The refrigerant is evenly distributed and mixed in the reactor 8 through the distributor 7 in the reactor and the internal stirring 8 or pump 6 mixing system (the implementation of the mixing system includes but is not limited to mechanical stirring, external circulation and injection mixing). The flow meter 3 is used to measure the refrigerant injection amount. When the specified injection amount is reached, the refrigerant injection is stopped; when the pressure detection system 10 in the control system detects that the pressure reaches the discharge pressure of the safety relief device, the safety valve 11 is opened, and the gas phase composition in the reactor 8 is discharged through the safety valve 11 and the discharge pipes ⑤ and ⑥, and after condensation by the heat exchanger 12, it flows to the gas-liquid separation tank 13 through ⑦, and the refrigerant returns to the refrigerant storage tank 1 through the refrigerant recovery pipe ⑧ for recycling.

[0123] Specific embodiment: Taking the runaway reaction of a reactor with a design pressure of 4 barg, a design temperature of 150°C, an inner diameter of 7.6 m, a straight section height of 25 m, and standard elliptical heads at the top and bottom as an example, the material filling rate in the reactor is 70%, the material density is 900 kg / m3, the main reaction in the reactor is the oxidation of cumene by air to produce cumene hydroperoxide (CHP), the set pressure of the safety relief device is 3.8 barg, and the material specific heat capacity is 2 kJ / kg / K.

[0124] In step A, the interruption of cumene feed is determined to be the cause of the loss of control of the materials in the reactor. After the interruption of cumene feed, a 24wt% CHP solution containing 91°C is retained in the reactor. Due to the unstable and high bond energy peroxide bonds in CHP, the long-term retention of the material causes a secondary decomposition reaction of CHP. Compared with the main reaction, the decomposition reaction is characterized by a fast reaction rate, a large exothermic power, and a large gas production. Therefore, the reactor is at risk of overpressure and overtemperature.

[0125] In step B, the reaction liquid retained in the reactor is subjected to an ARC (accelerating rate calorimeter) test to simulate the actual industrial runaway reaction trend as much as possible, and obtain a curve of the temperature and pressure of the reaction liquid over time under an adiabatic environment. By performing a Phi value correction, the reaction heat of the reaction liquid is obtained to be 152 kJ / mol CHP. The data is processed to obtain the decomposition kinetic parameters of CHP: the reaction order is 1.1, the reaction activation energy is 150 kJ / mol, and the pre-exponential factor is 5.5E+16 Mol (-0.1) L 0.1 min -1 .

[0126] In step C, the reaction liquid retained in the reactor is subjected to ARC test to obtain the temperature and pressure change curve of the reaction liquid under adiabatic environment over time, and the non-condensable gas production rate is related to the temperature. That is, the model parameter a is 7.57e -6 , see Figure 3 .

[0127] In step D, when the reactor temperature reaches the interlocking refrigerant injection temperature of 100°C, the temperature control module controls the flow regulating valve 4 in the quenching system, the valve 4 is opened, the specific heat capacity of the refrigerant A is 4.18 kJ / kg / K, and the refrigerant A at 25°C is quickly injected into the reaction system. Through the stirring and mixing action in the reaction system, the reaction liquid and the refrigerant A in the reactor are evenly mixed, and then the heat balance t·M is performed. A ·Cp A ·(T R -25)=M R ·Cp R·(100-T R ), that is, the change trend of the reactor temperature with different refrigerant injection amounts is obtained. After the refrigerant is injected, the temperature and pressure changes of the mixed liquid in the reactor can be calculated based on the macroscopic kinetic parameters and thermodynamic parameters obtained in step B. The effect of the injection of refrigerant A on the decomposition reaction of the mixed liquid in the reactor is explained by taking 45t, 90t, 135t, 202t, 225t, 270t and 315t of refrigerant A as examples. Based on the reactor temperature after the refrigerant is injected, the total adiabatic temperature rise is calculated. The fitting formula of temperature rise rate is: The gas production rate fitting formula is: The temperature variation trend of the mixture in the reactor is shown in Figure 5 .

[0128] In step E, to determine whether it is a two-phase flow, first confirm the gas and steam discharge at a discharge temperature of 148°C after the refrigerant is injected. ΔHv is 1062 J / g; the apparent gas rise rate, bubble rise rate, and dimensionless apparent gas velocity are obtained by the following formula: If the discharge is two-phase, it is a two-phase discharge; otherwise, it is a single-phase discharge. The calculation results are shown in Figure 5 .

[0129]

[0130]

[0131]

[0132]

[0133] Where: g is the apparent gas rising rate, F is the gas release amount when 148℃, ρ g is the density of non-condensable gas under the release pressure, U0 is the bubble rising rate, ρ f is the density of the liquid phase, σ is the surface tension of the liquid phase, is the dimensionless superficial gas velocity, is the dimensionless superficial gas velocity of two-phase flow, and α is the void ratio of the reactor. See the table below for specific data.

[0134] 45t 90t 135t 202t 225t 270t 315t F(ib / h) 160938 112436 77162 37479 26455 22046 22046 <![CDATA[ρ g (lb / ft3)]]> 0.3048 0.3048 0.3048 0.3048 0.3048 0.3048 0.3048 <![CDATA[A x (ft2)]]> 488 488 488 488 488 488 488 σ(dynes / cm) 25.4 33.6 35 40 42 45 46 <![CDATA[ρ f (lb / ft3)]]> 49.4 50.3 50.5 50.7 50.8 50.9 51 α 0.264 0.228 0.192 0.138 0.12 0.084 0.048

[0135] In step F, the calculation process is as follows: Figure 5 As shown, Figure 5The horizontal axis is the apparent gas velocity and the vertical axis is the void ratio, and the void ratio corresponds to the apparent gas velocity. Therefore, the apparent gas velocity (the horizontal axis of the light gray line) calculated based on the void ratio (the vertical axis of the light gray line) is less than the two-phase flow apparent gas velocity (the horizontal axis of the black line) calculated based on the void ratio (the vertical axis of the black line), which means that it is a single-phase flow discharge. Therefore, through this method, it can be confirmed that the injection amount of the quenching agent must not be less than 202t, and must not be greater than 280t, otherwise it will be converted into a two-phase flow discharge. Therefore, the injection range of the refrigerant can be confirmed by the method disclosed in the present invention.

[0136] It should be noted that, for the aforementioned method embodiments, for the sake of simplicity, they are all described as a series of action combinations, but those skilled in the art should be aware that the present disclosure is not limited by the order of the actions described, because according to the present disclosure, certain steps can be performed in other orders or simultaneously. Secondly, those skilled in the art should also be aware that the embodiments described in the specification are all optional embodiments, and the actions and modules involved are not necessarily required by the present disclosure.

[0137] The above is an introduction to the method embodiment. The following is a further explanation of the scheme disclosed in the present invention through an apparatus embodiment.

[0138] Figure 6 FIG. 6 shows a block diagram of a safety discharge control device 600 according to an embodiment of the present disclosure. Figure 6 As shown, the device 600 includes:

[0139] The acquisition module 610 is used to acquire the current temperature of the real reactor; wherein the real reactor contains high-energy substances that release heat greater than a preset heat;

[0140] The injection module 620 is used to inject a preset amount of refrigerant into the real reactor if the current temperature reaches the refrigerant injection temperature; wherein the refrigerant is used to reduce the temperature of the real reactor;

[0141] The prediction module 630 is used to predict the temperature change trend and the non-condensable gas production rate change trend of the real reactor after the preset amount of refrigerant is injected; wherein the temperature change trend of the real reactor is the change trend of the temperature in the real reactor over time; the non-condensable gas production rate change trend of the real reactor is the change trend of the non-condensable gas production rate in the real reactor over temperature;

[0142] The judgment module 640 is used to judge whether the discharge flow type of the real reactor is a single-phase flow discharge according to the temperature change trend of the real reactor and the change trend of the non-condensable gas production rate. Those skilled in the art can clearly understand that for the convenience and simplicity of description, the specific working process of the described module can refer to the corresponding process in the aforementioned method embodiment, and will not be repeated here.

[0143] According to an embodiment of the present disclosure, the present disclosure also provides an electronic device and a non-transitory computer-readable storage medium storing computer instructions.

[0144] Figure 7 A schematic block diagram of an electronic device 700 that can be used to implement an embodiment of the present disclosure is shown. The electronic device is intended to represent various forms of digital computers, such as laptop computers, desktop computers, workstations, personal digital assistants, servers, blade servers, mainframe computers, and other suitable computers. The electronic device can also represent various forms of mobile devices, such as personal digital processing, cellular phones, smart phones, wearable devices, and other similar computing devices. The components shown herein, their connections and relationships, and their functions are merely examples and are not intended to limit the implementation of the present disclosure described and / or required herein.

[0145] The device 700 includes a computing unit 701, which can perform various appropriate actions and processes according to a computer program stored in a read-only memory (ROM) 702 or a computer program loaded from a storage unit 708 into a random access memory (RAM) 703. In the RAM 703, various programs and data required for the operation of the device 700 can also be stored. The computing unit 701, the ROM 702, and the RAM 703 are connected to each other via a bus 704. An input / output (I / O) interface 705 is also connected to the bus 704.

[0146] A number of components in the device 700 are connected to the I / O interface 705, including: an input unit 706, such as a keyboard, a mouse, etc.; an output unit 707, such as various types of displays, speakers, etc.; a storage unit 708, such as a disk, an optical disk, etc.; and a communication unit 707, such as a network card, a modem, a wireless communication transceiver, etc. The communication unit 707 allows the device 700 to exchange information / data with other devices through a computer network such as the Internet and / or various telecommunication networks.

[0147] The computing unit 701 may be a variety of general and / or special processing components with processing and computing capabilities. Some examples of the computing unit 701 include, but are not limited to, a central processing unit (CPU), a graphics processing unit (GPU), various dedicated artificial intelligence (AI) computing chips, various computing units running machine learning model algorithms, digital signal processors (DSPs), and any appropriate processors, controllers, microcontrollers, etc. The computing unit 701 performs the various methods and processes described above, such as method 100. For example, in some embodiments, the method 100 may be implemented as a computer software program, which is tangibly contained in a machine-readable medium, such as a storage unit 708. In some embodiments, part or all of the computer program may be loaded and / or installed on the device 700 via the ROM 702 and / or the communication unit 707. When the computer program is loaded into the RAM 703 and executed by the computing unit 701, one or more steps of the method 100 described above may be performed. Alternatively, in other embodiments, the computing unit 701 may be configured to perform the method 100 in any other appropriate manner (e.g., by means of firmware).

[0148] Various implementations of the systems and techniques described above herein can be implemented in digital electronic circuit systems, integrated circuit systems, field programmable gate arrays (FPGAs), application specific integrated circuits (ASICs), application specific standard products (ASSPs), systems on chips (SOCs), load programmable logic devices (CPLDs), computer hardware, firmware, software, and / or combinations thereof. These various implementations can include: being implemented in one or more computer programs that can be executed and / or interpreted on a programmable system including at least one programmable processor, which can be a special purpose or general purpose programmable processor that can receive data and instructions from a storage system, at least one input device, and at least one output device, and transmit data and instructions to the storage system, the at least one input device, and the at least one output device.

[0149] The program code for implementing the method of the present disclosure may be written in any combination of one or more programming languages. These program codes may be provided to a processor or controller of a general-purpose computer, a special-purpose computer, or other programmable data processing device, so that the program code, when executed by the processor or controller, enables the functions / operations specified in the flow chart and / or block diagram to be implemented. The program code may be executed entirely on the machine, partially on the machine, partially on the machine and partially on a remote machine as a stand-alone software package, or entirely on a remote machine or server.

[0150] In the context of the present disclosure, a machine-readable medium may be a tangible medium that may contain or store a program for use by or in conjunction with an instruction execution system, device, or equipment. A machine-readable medium may be a machine-readable signal medium or a machine-readable storage medium. A machine-readable medium may include, but is not limited to, an electronic, magnetic, optical, electromagnetic, infrared, or semiconductor system, device, or equipment, or any suitable combination of the foregoing. A more specific example of a machine-readable storage medium may include an electrical connection based on one or more lines, a portable computer disk, a hard disk, a random access memory (RAM), a read-only memory (ROM), an erasable programmable read-only memory (EPROM or flash memory), an optical fiber, a portable compact disk read-only memory (CD-ROM), an optical storage device, a magnetic storage device, or any suitable combination of the foregoing.

[0151] To provide interaction with a user, the systems and techniques described herein can be implemented on a computer having: a display device (e.g., a CRT (cathode ray tube) or LCD (liquid crystal display) monitor) for displaying information to the user; and a keyboard and pointing device (e.g., a mouse or trackball) through which the user can provide input to the computer. Other types of devices can also be used to provide interaction with the user; for example, the feedback provided to the user can be any form of sensory feedback (e.g., visual feedback, auditory feedback, or tactile feedback); and input from the user can be received in any form (including acoustic input, voice input, or tactile input).

[0152] The systems and techniques described herein may be implemented in a computing system that includes back-end components (e.g., as a data server), or a computing system that includes middleware components (e.g., an application server), or a computing system that includes front-end components (e.g., a user computer with a graphical user interface or a web browser through which a user can interact with implementations of the systems and techniques described herein), or a computing system that includes any combination of such back-end components, middleware components, or front-end components. The components of the system may be interconnected by any form or medium of digital data communication (e.g., a communication network). Examples of communication networks include: a local area network (LAN), a wide area network (WAN), and the Internet.

[0153] A computing system may include a client and a server. The client and the server are generally remote from each other and usually interact through a communication network. The relationship of client and server is generated by computer programs running on respective computers and having a client-server relationship with each other. The server may be a cloud server, a server of a distributed system, or a server combined with a blockchain.

[0154] It should be understood that the various forms of processes shown above can be used to reorder, add or delete steps. For example, the steps recorded in this disclosure can be executed in parallel, sequentially or in different orders, as long as the desired results of the technical solutions disclosed in this disclosure can be achieved, and this document does not limit this.

[0155] The above specific implementations do not constitute a limitation on the protection scope of the present disclosure. It should be understood by those skilled in the art that various modifications, combinations, sub-combinations and substitutions can be made according to design requirements and other factors. Any modification, equivalent substitution and improvement made within the spirit and principle of the present disclosure shall be included in the protection scope of the present disclosure.

Claims

1. A safe discharge control method, characterized in that: include: Acquiring the current temperature of a real reactor; wherein the real reactor contains a high-energy substance that releases heat greater than a preset heat; If the current temperature reaches the refrigerant injection temperature, a preset amount of refrigerant is injected into the real reactor; wherein the refrigerant is used to lower the temperature of the real reactor; Predicting the temperature change trend and the non-condensable gas production rate change trend of the real reactor after the preset amount of refrigerant is injected; wherein the temperature change trend of the real reactor is the change trend of the temperature in the real reactor over time; the non-condensable gas production rate change trend of the real reactor is the change trend of the non-condensable gas production rate in the real reactor over temperature; According to the temperature change trend and the non-condensable gas production rate change trend of the real reactor, judging whether the discharge flow type of the real reactor is single-phase flow discharge; According to the judgment result of whether the real reactor is discharged in a single-phase flow under different preset amounts of refrigerant and different masses of high-energy substances, determining the injection amount of the refrigerant when the discharge flow pattern of the real reactor satisfies the single-phase flow discharge; The predicted temperature change trend and non-condensable gas production rate change trend of the actual reactor after the preset amount of refrigerant is injected include: Determining the mixed temperature in the actual reactor after injecting the preset amount of coolant; Predicting the temperature change trend of the real reactor according to the mixing temperature in the real reactor, the thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor corresponding to the real reactor; Obtaining a non-condensable gas production rate change trend of the real reactor according to the temperature change trend of the real reactor and the pre-acquired non-condensable gas production rate change trend of the simulated reactor; The variation trend of the non-condensable gas production rate of the simulated reactor is obtained by the following steps: Obtaining the temperature change trend and pressure change trend of the simulated reactor when the coolant is not injected into the simulated reactor; wherein the pressure change trend of the simulated reactor is the change trend of the pressure of the non-condensable gas in the simulated reactor over time; Determining the gas production rate of the non-condensable gas in the simulated reactor over time according to the pressure change trend of the simulated reactor; According to the temperature change trend of the simulated reactor and the gas production rate of the non-condensable gas in the simulated reactor over time, the change trend of the non-condensable gas production rate of the simulated reactor is calculated, wherein the temperature change trend of the simulated reactor is the change trend of the temperature in the simulated reactor over time; The thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor are obtained by the following steps: Obtaining a temperature change trend of the simulated reactor when the coolant is not injected into the simulated reactor; According to the temperature variation trend and the Arrhenius formula, a linear function fitting is performed to obtain the thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor.

2. The method according to claim 1, characterized in that The determining whether the real reactor is a single-phase flow discharge according to the temperature change trend of the real reactor and the change trend of the non-condensable gas production rate includes: Determining the void ratio of the actual reactor after injecting a preset amount of refrigerant; Calculating the dimensionless superficial gas velocity of the two-phase flow according to the void fraction; Calculate the current dimensionless superficial gas velocity of the real reactor according to the temperature change trend of the real reactor and the change trend of the non-condensable gas production rate, as well as the discharge volume calculation formula; If the current dimensionless superficial gas velocity of the real reactor is greater than or equal to the dimensionless superficial gas velocity of the two-phase flow, it is determined that after the preset amount of refrigerant is injected, the discharge flow type of the real reactor is two-phase flow discharge; otherwise, it is determined that the discharge flow type of the real reactor is single-phase flow discharge.

3. The method according to claim 1, characterized in that The current dimensionless superficial gas velocity of the real reactor is calculated according to the temperature change trend of the real reactor, the change trend of the non-condensable gas production rate, and the discharge volume calculation formula, including: According to the temperature change trend of the real reactor, the change trend of the non-condensable gas production rate, the mass of the high-energy substance in the real reactor, the density of the non-condensable gas in the real reactor and the discharge amount calculation formula, the gas discharge amount of the real reactor is obtained; wherein the gas discharge amount includes: the discharge amount of the non-condensable gas and steam in the real reactor; The dimensionless superficial gas velocity of the real reactor is calculated by using the gas release volume of the real reactor, the cross-sectional area of ​​the real reactor, the gas phase density and the liquid phase density of the real reactor.

4. The method according to claim 1, characterized in that: The reasons for the runaway reaction in the real reactor are different, and the corresponding thermodynamic parameters and macroscopic kinetic parameters are different.

5. A safety discharge control device, characterized in that: include: An acquisition module, used to acquire the current temperature of a real reactor; wherein the real reactor contains a high-energy substance that releases heat greater than a preset heat; An injection module, used for injecting a preset amount of refrigerant into the real reactor if the current temperature reaches the refrigerant injection temperature; wherein the refrigerant is used to reduce the temperature of the real reactor; A prediction module is used to predict the temperature change trend and the non-condensable gas production rate change trend of the real reactor after the preset amount of refrigerant is injected; wherein the temperature change trend of the real reactor is the change trend of the temperature in the real reactor over time; the non-condensable gas production rate change trend of the real reactor is the change trend of the non-condensable gas production rate in the real reactor over temperature; A judgment module, used for judging whether the discharge flow type of the real reactor is single-phase flow discharge according to the temperature change trend and the non-condensable gas production rate change trend of the real reactor; The device is also used for: According to the judgment result of whether the real reactor is discharged in a single-phase flow under different preset amounts of refrigerant and different masses of high-energy substances, determining the injection amount of the refrigerant when the discharge flow pattern of the real reactor satisfies the single-phase flow discharge; The prediction module is specifically used for: Determining the mixed temperature in the actual reactor after injecting the preset amount of coolant; Predicting the temperature change trend of the real reactor according to the mixing temperature in the real reactor, the thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor corresponding to the real reactor; Obtaining a non-condensable gas production rate change trend of the real reactor according to the temperature change trend of the real reactor and the pre-acquired non-condensable gas production rate change trend of the simulated reactor; The variation trend of the non-condensable gas production rate of the simulated reactor is obtained by the following steps: Obtaining the temperature change trend and pressure change trend of the simulated reactor when the coolant is not injected into the simulated reactor; wherein the pressure change trend of the simulated reactor is the change trend of the pressure of the non-condensable gas in the simulated reactor over time; Determining the gas production rate of the non-condensable gas in the simulated reactor over time according to the pressure change trend of the simulated reactor; According to the temperature change trend of the simulated reactor and the gas production rate of the non-condensable gas in the simulated reactor over time, the change trend of the non-condensable gas production rate of the simulated reactor is calculated, wherein the temperature change trend of the simulated reactor is the change trend of the temperature in the simulated reactor over time; The thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor are obtained by the following steps: Obtaining a temperature change trend of the simulated reactor when the coolant is not injected into the simulated reactor; According to the temperature variation trend and the Arrhenius formula, a linear function fitting is performed to obtain the thermodynamic parameters and macroscopic kinetic parameters of the simulated reactor.

6. An electronic device, characterized in that: include: at least one processor; as well as a memory communicatively connected to the at least one processor; wherein, The memory stores instructions that can be executed by the at least one processor, and the instructions are executed by the at least one processor to enable the at least one processor to perform the method according to any one of claims 1 to 4.

Images