Distillation tower convergence method, device, electronic equipment and medium based on joint module

Abstract

The present invention discloses a distillation tower convergence method, device, electronic device and medium based on a joint module. The method includes obtaining the initial parameter value of the first distillation tower, the initial parameter value of the second distillation tower, the initial parameter value of the first material flow and the initial parameter value of the second material flow; constructing a simplified inner circle iterative objective function based on the first distillation tower and the second distillation tower; solving the simplified inner circle iterative objective function according to the simplified inner circle iterative objective function and the partial derivative of the simplified inner circle iterative objective function to obtain a parameter change value; updating the initial parameter value of the first distillation tower, the initial parameter value of the second distillation tower, the initial parameter value of the first material flow and the initial parameter value of the second material flow according to the parameter change value to obtain the target parameter value of the first distillation tower, the target parameter value of the second distillation tower, the target parameter value of the first material flow and the target parameter value of the second material flow. This technical solution improves the convergence speed of distillation tower calculation.

Description

Technical Field

[0001] The present invention relates to the technical field of distillation tower coupling optimization, and in particular to a distillation tower convergence method, device, electronic equipment and medium based on a joint module. Background Art

[0002] The oil separation process is a complex and sophisticated operation involving multiple steps and technologies, which aims to separate different components in crude oil to meet different industrial needs. The oil separation process mainly includes primary distillation, atmospheric distillation, vacuum distillation, etc. Most of the technical means used are to use the boiling point differences of different components to separate different products such as gasoline, diesel, kerosene, etc. using multi-stage distillation towers. The simulation calculation of the oil separation process has the problem of complex process and difficult calculation convergence caused by the coupling of multiple components and multiple distillation towers in the distillation process.

[0003] The oil simulation process often uses the sequential module method and the simultaneous equation method. The interface between modules in the sequential module method is clear and easy to track errors, but the information transmission between modules requires multiple iterations, which may lead to slow convergence. The simultaneous equation method combines the equations and constraints of the modules to form a large nonlinear equation group for overall solution. The calculation speed is fast, but the simultaneous equation method has high requirements on the initial values ​​and it is difficult to accurately locate the problem after calculation anomalies. Summary of the invention

[0004] The present invention provides a distillation tower convergence method, device, electronic equipment and medium based on simultaneous modules, which effectively solves the convergence difficulty problem of the sequential module method and the problem of being unable to locate errors of the simultaneous equation method, improves the convergence speed of the distillation tower calculation and can improve the accuracy of the calculation.

[0005] According to one aspect of the present invention, a distillation tower convergence method based on a combined module is provided, the method comprising:

[0006] Acquire initial parameter values ​​of the first distillation tower, initial parameter values ​​of the second distillation tower, initial parameter values ​​of the first material flow, and initial parameter values ​​of the second material flow; wherein the coupling of the first distillation tower and the second distillation tower is realized through the first material flow and the second material flow;

[0007] Based on the first distillation tower and the second distillation tower, construct a simplified inner loop iterative objective function;

[0008] Solving the simplified inner loop iterative objective function according to the simplified inner loop iterative objective function and the partial derivative of the simplified inner loop iterative objective function to obtain a parameter change value;

[0009] According to the parameter change value, the initial parameter value of the first distillation tower, the initial parameter value of the second distillation tower, the initial parameter value of the first material flow and the initial parameter value of the second material flow are updated to obtain the target parameter value of the first distillation tower, the target parameter value of the second distillation tower, the target parameter value of the first material flow and the target parameter value of the second material flow.

[0010] According to another aspect of the present invention, a distillation tower convergence device based on a combined module is provided, the device comprising:

[0011] An initial parameter value acquisition module, used to acquire the initial parameter value of the first distillation tower, the initial parameter value of the second distillation tower, the initial parameter value of the first material flow, and the initial parameter value of the second material flow; wherein the coupling of the first distillation tower and the second distillation tower is realized through the first material flow and the second material flow;

[0012] A simplified inner loop iterative objective function construction module, used to construct a simplified inner loop iterative objective function based on the first distillation tower and the second distillation tower;

[0013] A parameter change value obtaining module, used for solving the simplified inner loop iterative objective function according to the simplified inner loop iterative objective function and the partial derivative of the simplified inner loop iterative objective function to obtain the parameter change value;

[0014] The target parameter value obtaining module is used to update the initial parameter value of the first distillation tower, the initial parameter value of the second distillation tower, the initial parameter value of the first material flow and the initial parameter value of the second material flow according to the parameter change value, so as to obtain the target parameter value of the first distillation tower, the target parameter value of the second distillation tower, the target parameter value of the first material flow and the target parameter value of the second material flow.

[0015] According to another aspect of the present invention, an electronic device is provided, the electronic device comprising:

[0016] At least one processor; and a memory in communication with the at least one processor; wherein the memory stores a computer program executable by the at least one processor, and the computer program is executed by the at least one processor so that the at least one processor can execute the distillation tower convergence method based on the joint modules described in any embodiment of the present invention.

[0017] According to another aspect of the present invention, a computer-readable storage medium is provided, wherein the computer-readable storage medium stores computer instructions, and the computer instructions are used to enable a processor to implement the distillation tower convergence method based on joint modules described in any embodiment of the present invention when executed.

[0018] In the technical solution of the embodiment of the present invention, by obtaining the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow; based on the first distillation column and the second distillation column, constructing a simplified inner-loop iteration objective function; according to the simplified inner-loop iteration objective function and the partial derivatives of the simplified inner-loop iteration objective function, solving the simplified inner-loop iteration objective function to obtain parameter change values; according to the parameter change values, updating the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow to obtain the target parameter values of the first distillation column, the target parameter values of the second distillation column, the target parameter values of the first material flow, and the target parameter values of the second material flow. This technical solution preferably solves the problem of difficult convergence of the sequential modular method and the problem of inability to locate errors in the simultaneous equation method, improves the calculation convergence speed of the distillation column, and can improve the calculation accuracy.

[0019] It should be understood that the content described in this part is not intended to identify the key or important features of the embodiments of the present invention, nor is it used to limit the scope of the present invention. Other features of the present invention will become easily understood through the following description. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] In order to more clearly illustrate the technical solutions in the embodiments of the present invention, the following will briefly introduce the drawings required for the description of the embodiments. Obviously, the drawings in the following description are only some embodiments of the present invention. For those of ordinary skill in the art, without creative efforts, other drawings can be obtained based on these drawings.

[0021] Figure 1 is a flowchart of a distillation column convergence method based on simultaneous modules according to Embodiment 1 of the present invention;

[0022] Figure 2 is a schematic diagram of a coupled distillation column provided in Embodiment 1 of the present application;

[0023] Figure 3 is a schematic diagram of a true boiling point curve provided in Embodiment 1 of the present application;

[0024] Figure 4 is a schematic diagram of a distillation column convergence method based on simultaneous modules according to Embodiment 2 of the present invention;

[0025] Figure 5 is a schematic diagram of the structure of a distillation column convergence device based on simultaneous modules according to Embodiment 3 of the present invention;

[0026] Figure 6 is a schematic diagram of the structure of an electronic device for implementing the distillation column convergence method based on simultaneous modules in the embodiments of the present invention. DETAILED DESCRIPTION

[0027] In order to enable those skilled in the art to better understand the scheme of the present invention, the technical scheme in the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings in the embodiments of the present invention. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work should fall within the scope of protection of the present invention.

[0028] It should be noted that the terms "initial", "target", etc. in the specification and claims of the present invention and the above-mentioned drawings are used to distinguish similar objects, and are not necessarily used to describe a specific order or sequence. It should be understood that the data used in this way can be interchanged where appropriate, so that the embodiments of the present invention described herein can be implemented in an order other than those illustrated or described herein. In addition, the terms "including" and "having" and any variations thereof are intended to cover non-exclusive inclusions, for example, a process, method, system, product or device that includes a series of steps or units is not necessarily limited to those steps or units that are clearly listed, but may include other steps or units that are not clearly listed or inherent to these processes, methods, products or devices.

[0029] Embodiment 1

[0030] Figure 1 This is a flow chart of a distillation tower convergence method based on a joint module provided in accordance with the first embodiment of the present invention. This embodiment is applicable to the case of online optimization of distillation tower coupling. The method can be executed by a distillation tower convergence device based on a joint module. The distillation tower convergence device based on a joint module can be implemented in the form of hardware and / or software. The distillation tower convergence device based on a joint module can be configured in a device. For example, the device can be a background server or other device with communication and computing capabilities. Figure 1 As shown, the method includes:

[0031] S110. Obtaining initial parameter values ​​of a first distillation tower, initial parameter values ​​of a second distillation tower, initial parameter values ​​of a first material flow, and initial parameter values ​​of a second material flow; wherein the coupling of the first distillation tower and the second distillation tower is achieved through the first material flow and the second material flow.

[0032] In this scheme, the distillation tower utilizes the difference in volatility of the components in the liquid mixture, and through multiple partial vaporization and partial condensation, the light components in the liquid phase are continuously transferred to the gas phase, and the heavy components in the gas phase are continuously transferred to the liquid phase, thereby achieving separation of the mixture.

[0033] In this embodiment, the coupling of the distillation towers is achieved through material flow, that is, the information of each distillation tower is transmitted through material flow. The multi-distillation tower coupling optimization is mainly used in the fields of petrochemical, environmental protection, metallurgy, etc. Figure 2 A schematic diagram of a coupled distillation tower provided in Example 1 of the present application, such as Figure 2 As shown, the side outlet of the first distillation tower enters the second distillation tower, and the vapor phase outlet of the second distillation tower returns to the first distillation tower. The first distillation tower and the second distillation tower are solved together using a joint module. The inner circle solves the first distillation tower and the second distillation tower together, and the outer circle updates the information of the first material flow and the second material flow, thereby completing the coupled distillation tower solution problem.

[0034] The parameters of the first distillation tower and the second distillation tower include the temperature of each tower plate, the amount of rising steam, the amount of descending liquid, the vapor phase composition, and the liquid phase composition; the parameters of the first material flow and the second material flow include temperature, flow rate, and composition.

[0035] Specifically, initial values ​​are assigned to the temperature of each plate of the first distillation tower and the second distillation tower, the amount of rising steam, the amount of descending liquid, the vapor phase composition, and the liquid phase composition to obtain the initial parameter value of the first distillation tower and the initial parameter value of the second distillation tower; and initial values ​​are assigned to the temperature, flow rate, and component of the first material flow and the second material flow to obtain the initial parameter value of the first material flow and the initial parameter value of the second material flow.

[0036] Optionally, the parameters of the first material flow and the parameters of the second material flow include component contents;

[0037] Accordingly, the process of determining the component content includes:

[0038] Obtain crude oil distillation curve;

[0039] Converting the crude oil distillation curve into a real boiling point curve, and determining component boiling points and component relative molecular weights based on the real boiling point curve;

[0040] The target component is determined according to the boiling point of the component and the relative molecular weight of the component, and the target component is iteratively processed to determine the component content corresponding to the target component.

[0041] In this scheme, the crude oil distillation curve can be extracted from the analytical experiment database.

[0042] In this embodiment, petroleum is a complex mixture containing a large number of hydrocarbon compounds and other non-hydrocarbon substances. When establishing a mathematical model of multi-distillation tower coupling, it is necessary to determine the feed component information, so the oil products need to be converted into a group of mixtures that can represent petroleum. The most common crude oil distillation curve is the Enn distillation curve, so the Enn distillation curve needs to be converted into a real boiling point curve, and the conversion method of the distillation curve adopts the Edmister method.Figure 3 Schematic diagram of the true boiling point curve provided in the first embodiment of the present application, as Figure 3 shown, the form of the true boiling point curve is the volume percentage of the distillate liquid phase and the corresponding temperature. Among them, the volume percentage of the distillate liquid phase includes 0, 10, 30, 50, 70, 90, 100. The temperature values corresponding to different percentages are plotted to form the true boiling point distillation curve. On the true boiling point distillation curve, about every 20 degrees is one component. The boiling point of the component is a trapezoid formed by enclosing the 20-degree interval on the true boiling point distillation curve and the abscissa. The boiling point of the component can be calculated by dividing the area of the trapezoid by the distance of the x-axis.

[0043] Furthermore, the relative molecular weight of the component is calculated based on the boiling point of the component and the preset characterization factor. Specifically, the Hariu-Sage method can be used to estimate the relative molecular weight of the component, and the calculation formula is:

[0044] ;

[0045] Among them, is the relative molecular weight of the component, , , , , , , , , , is the boiling point of the component of the petroleum fraction, the unit is F, and K is the characterization factor.

[0046] In this solution, the boiling point of the component and the relative molecular weight of the component are used to retrieve and match substances such as alkanes, isoparaffins, naphthenes, and aromatics in the pure substance database, and a target component that is closest to the calculated boiling point of the component and the relative molecular weight of the component is matched and calculated to replace the mixture within the boiling range of the oil product.

[0047] Furthermore, after determining the target component, it is also necessary to determine the component content corresponding to the target component. The component content corresponding to the target component can be calculated by using a cyclic iteration method. Specifically, according to the temperature and pressure at different percentages of the true boiling point distillation curve, the distillate percentage is calculated by temperature-pressure flash distillation, and the component content corresponding to the target component is cyclically iterated based on the size of the distillate percentage, so as to determine the component content corresponding to the target component.

[0048] By calculating the target component and the component content corresponding to the target component, a simplified inner-loop iterative objective function can be constructed based on the target component and the component content of the distillation column, so as to realize the optimization of the coupled distillation column.

[0049] Optionally, determining the component content corresponding to the target component includes:

[0050] Obtain the initial component content;

[0051] Calculate the distillate percentage according to the temperature and pressure in the true boiling point curve and the initial component content;

[0052] Determine the error value according to the distillate percentage and the preset distillate percentage;

[0053] When the error value meets the preset error condition, use the initial component content as the component content corresponding to the target component;

[0054] When the error value does not meet the preset error condition, recalculate the distillate percentage, continuously update the initial component content until the error value meets the preset error condition, and use the initial component content as the component content corresponding to the target component.

[0055] In this embodiment, it is assumed that the initial component content is , and N is the number of substances of the target component.

[0056] Furthermore, according to the temperature, pressure and initial component content at different percentages of the true boiling point distillation curve, a set of distillate percentages are calculated by temperature-pressure flash calculation. Then, the distillate percentage is compared with the preset distillate percentage to determine the error . If the error is greater than 0, then to the component mole fraction in the interval decreases, otherwise it increases. represents the error in the interval , represents the calculated distillate percentage corresponding to the th temperature, represents the actual distillate percentage corresponding to the th temperature, that is, the preset distillate percentage. Among them, ; ; is the error value.

[0057] Among them, the preset error condition is used to constrain the error value. That is, when the error value is less than the preset error, the error value meets the preset error condition; when the error value is greater than or equal to the preset error, the error value does not meet the preset error condition.

[0058] In this solution, when is less than the preset error, exit the iteration and use the initial component content as the component content corresponding to the target component.

[0059] Furthermore, when When it is greater than or equal to the preset error, the distillation percentages at different percentages of temperature and pressure are recalculated, and the initial component content is continuously updated until the error value meets the preset error condition, and the initial component content is used as the component content corresponding to the target component.

[0060] In this embodiment, the temperature-pressure flash calculation process is to calculate the gas-liquid phase fraction and the equilibrium concentration of each phase in the equilibrium phase state when the temperature, pressure and content of each component are known. Specifically, the following formula is used for calculation:

[0061] ;

[0062] in, is the content of each component, is the phase equilibrium constant of each component, is the gas phase fraction, is the number of components, the phase equilibrium constant Repeat the iteration until convergence.

[0063] Furthermore, after calculating the gas phase content, the distillation percentage can be obtained. If the boiling point of each component and the relationship between the gas phase content and temperature are known, the relationship between the gas phase content and the distillation percentage can also be indirectly obtained from the distillation curve. For example, according to the distillation temperature at a certain moment, the corresponding distillation percentage is read from the distillation curve, and then the content of each component in the gas phase at this time is calculated according to the phase equilibrium relationship of each component at this temperature.

[0064] By calculating the component content corresponding to the target component, a simplified inner loop iterative objective function can be constructed based on the target component and component content of the distillation tower, thereby realizing the optimization of the coupled distillation tower.

[0065] S120. Construct a simplified inner loop iterative objective function based on the first distillation tower and the second distillation tower.

[0066] In this solution, a simplified inner loop iterative objective function is constructed by combining the first distillation tower and the second distillation tower. Specifically, a simplified inner loop iterative objective function can be constructed based on the parameters of the first distillation tower and the parameters of the second distillation tower.

[0067] Optionally, based on the first distillation tower and the second distillation tower, a simplified inner loop iterative objective function is constructed, including:

[0068] According to the principles of conservation of energy, conservation of mass and phase equilibrium, a simplified inner loop iterative objective function is constructed based on the parameters of the first distillation tower and the parameters of the second distillation tower; wherein the parameters include liquid phase flow rate, vapor phase flow rate, vapor phase molar fraction, liquid phase molar fraction, vapor phase molar enthalpy, liquid phase molar enthalpy, feed enthalpy, liquid phase production, vapor phase production, feed and phase equilibrium constant.

[0069] Among them, the principle of conservation of energy means that energy can neither be created out of nothing nor disappear without a trace. It can only be converted from one form to another, or transferred from one object to other objects, while the total amount of energy remains unchanged.

[0070] In this embodiment, the principle of conservation of mass means that in any isolated system that is isolated from the surrounding environment and contains matter and energy, regardless of what changes or processes occur within the system, its total mass and energy do not change over time.

[0071] In this solution, the principle of phase equilibrium means that under certain conditions, when the properties and quantities of each phase in a multiphase system do not change over time, this system is said to be in phase equilibrium. At phase equilibrium, the chemical potential of each phase is equal.

[0072] In this embodiment, a simplified inner-loop iteration objective function of the distillation column is constructed based on the energy conservation equation, mass conservation equation, and phase equilibrium equation. Specifically, for any tray , the energy conservation equation is:

[0073] ;

[0074] The mass conservation equation is:

[0075] ;

[0076] The phase equilibrium equation is:

[0077] ;

[0078] Among them,

[0079] ;

[0080] ;

[0081] Among them, 、 The 、 Liquid phase flow rates of the 、 th 、 trays; 、 Are the th Vapor and liquid mole fractions of the 、 th tray; Is the The feed enthalpy of the tray is the liquid draw of the tray is the vapor draw of the tray is the feed to the tray is the th phase equilibrium constant of the th is the heat input to the th tray is the th mole fraction of the feed of the th

[0082] In this solution, by means of data interface technologies such as OPC (OLE for Process Control) and Modbus, key data is extracted from the DCS database, the analytical test database, etc.

[0083] By constructing a simplified inner-loop iterative objective function, the solution of each distillation column can be achieved by coupling the first distillation column and the second distillation column.

[0084] Optionally, the determination process of the vapor molar enthalpy includes:

[0085] Calculate the vapor molar enthalpy using the following formula;

[0086] ;

[0087] ;

[0088] Outer-loop iterative update , and the update method is;

[0089] ;

[0090] ;

[0091] ;

[0092] ;

[0093] ;

[0094] ;

[0095] ;

[0096] ;

[0097] ;

[0098] ;

[0099] ;

[0100] ;

[0101] Among them, is the vapor-phase molar enthalpy, is the enthalpy of the ideal gas, is the enthalpy deviation at temperature , is the enthalpy deviation at temperature , is the heat capacity deviation, is the compressibility factor, is the ideal gas constant, is the system temperature, is the system volume, is the th phase equilibrium constant of the th component on the th tray, is the content of component , is the content of component , is the critical temperature of component , is the critical temperature of component , is the critical pressure of component , is the number of components, The reduced temperature of component , is the acentric factor of component , The reduced temperature of component , is the acentric factor of component .

[0102] Specifically, the calculation of enthalpy is divided into two parts. One part is the enthalpy of the ideal gas and the enthalpy deviation, that is, ; Among them, is the enthalpy of the ideal gas, is the enthalpy deviation. The enthalpy of the ideal gas is obtained by weighted average of the enthalpy values of pure substances. Among them, the calculation of the enthalpy deviation is relatively complex. It is necessary to simplify the enthalpy deviation part, and the enthalpy deviation is simplified to: ; Among them, is the heat capacity deviation. In this way, the enthalpy deviation simplifies to a linear equation and is updated by calculation value.

[0103] Specifically, calculate at temperature ;

[0104] ;

[0105] ;

[0106] Calculate at temperature ;

[0107] ;

[0108] ;

[0109] wherein, ;

[0110] ;

[0111] ;

[0112] ;

[0113] ;

[0114] ;

[0115] ;

[0116] ;

[0117] .

[0118] The calculation of the enthalpy deviation is a very complex process. By means of the iteration of the inner and outer circles, the calculation frequency of the enthalpy deviation can be reduced, the calculation amount can be greatly simplified, and the nonlinearity of the objective function can be reduced, so as to achieve the goal of rapid convergence of the distillation column.

[0119] Optionally, the determination process of the correction coefficient of the phase equilibrium constant includes:

[0120] Calculate the outer circle phase equilibrium constant according to the liquid phase fugacity coefficient and the vapor phase fugacity coefficient; wherein, the liquid phase fugacity coefficient is used to characterize the deviation degree of the component fugacity from the fugacity of the component in the ideal solution; the vapor phase fugacity coefficient is used to characterize the deviation degree of the actual gas from the ideal gas;

[0121] Determine the correction coefficient of the phase equilibrium constant based on the outer-phase equilibrium constant and the preset ideal phase equilibrium constant.

[0122] Among them, the liquid-phase fugacity coefficient and the vapor-phase fugacity coefficient are functions of temperature and pressure composition and can be obtained through calculation.

[0123] Furthermore, the liquid-phase fugacity coefficient and the vapor-phase fugacity coefficient can be divided to obtain the outer-phase equilibrium constant. Specifically, ; is the outer-phase equilibrium constant, is the liquid-phase fugacity coefficient, is the vapor-phase fugacity coefficient.

[0124] In this embodiment, the preset ideal phase equilibrium constant can be calculated based on the saturated vapor pressure of the substance at the current temperature, the system pressure, and the correction coefficient of the phase equilibrium constant. Specifically, ; is the preset ideal phase equilibrium constant, is the correction coefficient of the phase equilibrium constant, is the saturated vapor pressure of the substance at the current temperature, is the system pressure.

[0125] In this solution, the correction coefficient of the phase equilibrium constant can be given an initial value to calculate the preset ideal phase equilibrium constant, and then the correction coefficient of the phase equilibrium constant is updated based on the calculated outer-phase equilibrium constant and the preset ideal phase equilibrium constant. Specifically, .

[0126] Among them, the calculation process of the fugacity coefficient includes:

[0127] ;

[0128] ;

[0129] ;

[0130] ;

[0131] ;

[0132] ;

[0133] ;

[0134] ;

[0135] ;

[0136] ;

[0137] ;

[0138] Among them, is the content of component , is the compressibility factor, is the ideal gas constant, is the system temperature, is the content of component , is the content of component , is the system volume, is the critical temperature of component , is the critical pressure of component , The reduced temperature of component , is the acentric factor of component , is the content of component , is the content of component , The reduced temperature of component , is the acentric factor of component .

[0139] The calculation of the phase equilibrium constant is a very complex process. By means of the iteration of the inner and outer loops, the calculation frequency of the phase equilibrium constant can be reduced, the calculation amount can be greatly simplified, and the nonlinearity of the objective function can be reduced, so as to achieve the goal of rapid convergence of the distillation column.

[0140] S130. Solve the simplified inner-loop iteration objective function according to the simplified inner-loop iteration objective function and the partial derivative of the simplified inner-loop iteration objective function to obtain the parameter change value.

[0141] Among them, the partial derivative of the simplified inner-loop iteration objective function is the jacobian matrix, that is .

[0142] In this scheme, the simplified inner loop iterative objective function of the distillation tower adopts the inner and outer loop method to solve the simultaneous equations, and the simplified inner loop iterative objective function of the inner loop is the simplified distillation tower MESH equation. The solution of the inner loop of the distillation tower is the process of solving the nonlinear equation system, and it is necessary to calculate the Jacobian matrix of the equation system. The Jacobian matrix can be solved analytically, which greatly simplifies the calculation amount of the Jacobian matrix and improves the calculation speed. The parameter change value can be obtained through the constructed Jacobian matrix and the MESH equation residual.

[0143] S140. Based on the parameter change value, the initial parameter value of the first distillation tower, the initial parameter value of the second distillation tower, the initial parameter value of the first material flow, and the initial parameter value of the second material flow are updated to obtain the target parameter value of the first distillation tower, the target parameter value of the second distillation tower, the target parameter value of the first material flow, and the target parameter value of the second material flow.

[0144] In this scheme, when the parameter change value is within the allowable error range, the initial parameter value of the first distillation tower is used as the target parameter value of the first distillation tower; and the initial parameter value of the second distillation tower is used as the target parameter value of the second distillation tower; and the initial parameter value of the first material flow is used as the target parameter value of the first material flow; and the initial parameter value of the second material flow is used as the target parameter value of the second material flow.

[0145] In this embodiment, when the parameter change value is not within the allowable error range, the initial parameter value of the first distillation tower, the initial parameter value of the second distillation tower, the initial parameter value of the first material flow, and the initial parameter value of the second material flow are updated according to the parameter change value, and a new simplified inner loop iterative objective function is constructed based on the updated initial parameter value of the first distillation tower, the initial parameter value of the second distillation tower, the initial parameter value of the first material flow, and the initial parameter value of the second material flow; the new simplified inner loop iterative objective function is solved to obtain a new parameter change value until the new parameter change value is within the allowable error range, and the target parameter value of the first distillation tower, the target parameter value of the second distillation tower, the target parameter value of the first material flow, and the target parameter value of the second material flow are determined based on the new parameter change value.

[0146] In the technical solution of the embodiment of the present invention, by obtaining the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow, a simplified inner-loop iteration objective function is constructed based on the first distillation column and the second distillation column. Then, according to the simplified inner-loop iteration objective function and the partial derivatives of the simplified inner-loop iteration objective function, the simplified inner-loop iteration objective function is solved to obtain the parameter change values. And according to the parameter change values, the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow are updated to obtain the target parameter values of the first distillation column, the target parameter values of the second distillation column, the target parameter values of the first material flow, and the target parameter values of the second material flow. By implementing this technical solution, the problem of difficult convergence of the sequential modular method and the problem of inability to locate errors in the simultaneous equation method are better solved, the calculation convergence speed of the distillation column is improved, and the calculation accuracy can be improved.

[0147] Embodiment 2

[0148] Figure 4 FIG. is a schematic diagram of a distillation column convergence method based on a simultaneous module provided by Embodiment 2 of the present invention. The relationship between this embodiment and the above embodiment is a detailed supplement to the operation process of the distillation column. As Figure 4 shown, the method includes:

[0149] S410. Obtain the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow; wherein, the coupling of the first distillation column and the second distillation column is realized through the first material flow and the second material flow.

[0150] S420. Based on the first distillation column and the second distillation column, construct a simplified inner-loop iteration objective function.

[0151] S430. According to the simplified inner-loop iteration objective function and the partial derivatives of the simplified inner-loop iteration objective function, solve the simplified inner-loop iteration objective function to obtain the parameter change values.

[0152] S440. According to the parameter change values, update the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow to obtain the target parameter values of the first distillation column, the target parameter values of the second distillation column, the target parameter values of the first material flow, and the target parameter values of the second material flow.

[0153] S450. Determine the distillation column operating conditions based on the target parameter values of the first distillation column, the target parameter values of the second distillation column, the target parameter values of the first material flow, and the target parameter values of the second material flow; wherein, the distillation column operating conditions are the conditions for controlling the operation of the distillation column.

[0154] In this solution, the distillation column operating conditions are the conditions for controlling the operation of the distillation column. By determining the distillation column operating conditions, the distillation column can be controlled based on the distillation column operating conditions, thereby realizing the petroleum separation process.

[0155] Among them, the distillation column operating conditions include the temperature, pressure, reboiler load, reflux ratio, etc. of the distillation column. The distillation column operating conditions can be obtained by performing combined calculations on the target parameter values of the first distillation column, the target parameter values of the second distillation column, the target parameter values of the first material flow, and the target parameter values of the second material flow.

[0156] Specifically, an optimizer can be superimposed outside the distillation column. Optimization goals such as minimum energy consumption, maximum product purity or yield, etc. can be input, decision variables such as reflux ratio, feed location, reboil ratio, etc. can be determined, and the operating conditions of the distillation column, such as the temperature, pressure, reboiler load, reflux ratio, etc. of the distillation column, can be output through an optimization algorithm.

[0157] The technical solution of the embodiment of the present invention obtains the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow. Based on the first distillation column and the second distillation column, a simplified inner-loop iterative objective function is constructed. Then, according to the simplified inner-loop iterative objective function and the partial derivatives of the simplified inner-loop iterative objective function, the simplified inner-loop iterative objective function is solved to obtain the parameter change values, and based on the parameter change values, the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow are updated to obtain the target parameter values of the first distillation column, the target parameter values of the second distillation column, the target parameter values of the first material flow, and the target parameter values of the second material flow. Then, the distillation column operating conditions are calculated based on the target parameter values of the first distillation column, the target parameter values of the second distillation column, the target parameter values of the first material flow, and the target parameter values of the second material flow. By implementing this technical solution, the problem of difficult convergence of the sequential modular method and the problem of inability to locate errors in the simultaneous equation method are better solved, the calculation convergence speed of the distillation column is improved, the calculation accuracy can be improved, and petroleum separation is realized.

[0158] Embodiment III

[0159] Figure 5 It is a schematic structural diagram of a distillation column convergence device based on simultaneous modules provided by Embodiment III of the present invention. As Figure 5 shown, the device includes:

[0160] An initial parameter value acquisition module 510 is configured to acquire the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow; wherein, the coupling of the first distillation column and the second distillation column is achieved through the first material flow and the second material flow.

[0161] A simplified inner-loop iteration objective function construction module 520 is configured to construct a simplified inner-loop iteration objective function based on the first distillation column and the second distillation column.

[0162] A parameter change value obtaining module 530 is configured to solve the simplified inner-loop iteration objective function according to the simplified inner-loop iteration objective function and the partial derivative of the simplified inner-loop iteration objective function to obtain a parameter change value.

[0163] A target parameter value obtaining module 540 is configured to update the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow according to the parameter change value to obtain the target parameter values of the first distillation column, the target parameter values of the second distillation column, the target parameter values of the first material flow, and the target parameter values of the second material flow.

[0164] Optionally, the simplified inner-loop iteration objective function construction module 520 includes:

[0165] A simplified inner-loop iteration objective function construction unit is configured to construct a simplified inner-loop iteration objective function based on the parameters of the first distillation column and the parameters of the second distillation column according to the principle of energy conservation, the principle of mass conservation, and the principle of phase equilibrium; wherein, the parameters include liquid phase flow rate, vapor phase flow rate, vapor phase mole fraction, liquid phase mole fraction, vapor phase molar enthalpy, liquid phase molar enthalpy, feed enthalpy, liquid phase draw, vapor phase draw, feed, and phase equilibrium constant.

[0166] Optionally, the simplified inner-loop iteration objective function construction unit is specifically configured to:

[0167] Calculate the vapor phase molar enthalpy using the following formula;

[0168] ;

[0169] ;

[0170] Outer-loop iteration update , and the update method is;

[0171] ;

[0172] ;

[0173] ;

[0174] ;

[0175] ;

[0176] ;

[0177] ;

[0178] ;

[0179] ;

[0180] ;

[0181] ;

[0182] ;

[0183] wherein, is the vapor-phase molar enthalpy, is the enthalpy of the ideal gas, is the deviation enthalpy at temperature , is the deviation enthalpy at temperature , is the deviation heat capacity, is the compressibility factor, is the ideal gas constant, is the system temperature, is the system volume, is the th phase equilibrium constant of the th component on the th tray, is the content of component is the content of component , is the critical temperature of component ; is the critical temperature of component ; is the critical pressure of component ; is the critical pressure of component ; is the number of components, Component 's reduced temperature, is the acentric factor of component ; Component The reduced temperature of is the component acentric factor of

[0184] Optionally, the simplified inner-loop iteration objective function construction unit is further configured to:

[0185] Calculate the outer-loop phase equilibrium constant according to the liquid-phase fugacity coefficient and the vapor-phase fugacity coefficient; wherein, the liquid-phase fugacity coefficient is used to characterize the deviation degree of the component fugacity from the fugacity of the component in the ideal solution; the vapor-phase fugacity coefficient is used to characterize the deviation degree of the real gas from the ideal gas;

[0186] Determine the correction coefficient of the phase equilibrium constant according to the outer-loop phase equilibrium constant and the preset ideal phase equilibrium constant.

[0187] Optionally, the parameters of the first material flow and the parameters of the second material flow include component contents;

[0188] Correspondingly, the device further includes:

[0189] A crude oil distillation curve acquisition module, configured to acquire a crude oil distillation curve;

[0190] A component boiling point and component relative molecular weight determination module, configured to convert the crude oil distillation curve into a true boiling point curve, and determine the component boiling point and the component relative molecular weight according to the true boiling point curve;

[0191] A component content determination module, configured to determine a target component according to the component boiling point and the component relative molecular weight, and perform cyclic iteration processing on the target component to determine the component content corresponding to the target component.

[0192] Optionally, the component content determination module is specifically configured to:

[0193] Obtain an initial component content;

[0194] Calculate the distillate percentage according to the initial component content, the temperature and the pressure in the true boiling point curve;

[0195] Determine an error value according to the distillate percentage and a preset distillate percentage;

[0196] When the error value meets a preset error condition, use the initial component content as the component content corresponding to the target component;

[0197] When the error value does not meet the preset error condition, recalculate the distillate percentage, continuously update the initial component content until the error value meets the preset error condition, and use the initial component content as the component content corresponding to the target component.

[0198] Optionally, the device further comprises:

[0199] The distillation tower operating condition determination module is used to determine the distillation tower operating conditions according to the target parameter value of the first distillation tower, the target parameter value of the second distillation tower, the target parameter value of the first material flow and the target parameter value of the second material flow; wherein the distillation tower operating conditions are the conditions for controlling the operation of the distillation tower.

[0200] The distillation tower convergence device based on the joint module provided in the embodiment of the present invention can execute the distillation tower convergence method based on the joint module provided in any embodiment of the present invention, and has the functional modules and beneficial effects corresponding to the execution method.

[0201] Embodiment 4

[0202] Figure 6 A schematic diagram of the structure of an electronic device 10 that can be used to implement an embodiment of the present invention 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 (such as helmets, glasses, watches, etc.) 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 invention described and / or required herein.

[0203] like Figure 6 As shown, the electronic device 10 includes at least one processor 11, and a memory connected to the at least one processor 11, such as a read-only memory (ROM) 12, a random access memory (RAM) 13, etc., wherein the memory stores a computer program that can be executed by at least one processor, and the processor 11 can perform various appropriate actions and processes according to the computer program stored in the read-only memory (ROM) 12 or the computer program loaded from the storage unit 18 to the random access memory (RAM) 13. In the RAM 13, various programs and data required for the operation of the electronic device 10 can also be stored. The processor 11, the ROM 12, and the RAM 13 are connected to each other through a bus 14. The input / output (I / O) interface 15 is also connected to the bus 14.

[0204] Multiple components in the electronic device 10 are connected to the I / O interface 15, including: an input unit 16, such as a keyboard, a mouse, etc.; an output unit 17, such as various types of displays, speakers, etc.; a storage unit 18, such as a disk, an optical disc, etc.; and a communication unit 19, such as a network card, a modem, a wireless communication transceiver, etc. The communication unit 19 allows the electronic device 10 to exchange information / data with other devices via a computer network such as the Internet and / or various telecommunication networks.

[0205] The processor 11 can be various general-purpose and / or special-purpose processing components with processing and computing capabilities. Some examples of the processor 11 include but are not limited to a central processing unit (CPU), a graphics processing unit (GPU), various dedicated artificial intelligence (AI) computing chips, various processors running machine learning model algorithms, a digital signal processor (DSP), and any suitable processor, controller, microcontroller, etc. The processor 11 executes the various methods and processes described above, such as the distillation column convergence method based on simultaneous modules.

[0206] In some embodiments, the distillation column convergence method based on simultaneous modules can be implemented as a computer program, which is tangibly contained in a computer-readable storage medium, such as the storage unit 18. In some embodiments, part or all of the computer program can be loaded and / or installed onto the electronic device 10 via the ROM 12 and / or the communication unit 19. When the computer program is loaded into the RAM 13 and executed by the processor 11, one or more steps of the distillation column convergence method described above can be executed. Alternatively, in other embodiments, the processor 11 can be configured to execute the distillation column convergence method based on simultaneous modules in any other suitable manner (e.g., by means of firmware).

[0207] The various embodiments 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 a chip (SOCs), complex programmable logic devices (CPLDs), computer hardware, firmware, software, and / or combinations thereof. These various embodiments can include: being implemented in one or more computer programs, which can be executed and / or interpreted on a programmable system including at least one programmable processor, which can be a special or general programmable processor, and can receive data and instructions from a storage system, at least one input device, and at least one output device, and transmit the data and instructions to the storage system, the at least one input device, and the at least one output device.

[0208] A computer program for implementing the method of the present invention may be written in any combination of one or more programming languages. These computer programs may be provided to a processor of a general purpose computer, a special purpose computer, or other programmable data processing apparatus, such that the computer programs, when executed by the processor, cause the functions / operations specified in the flowchart and / or block diagram to be implemented. The computer program may be executed entirely on the machine, partly on the machine, as a stand-alone software package partly on the machine and partly on a remote machine, or entirely on the remote machine or server.

[0209] In the context of the present invention, a computer-readable storage medium may be a tangible medium that can contain or store a computer program for use by or in connection with an instruction execution system, apparatus, or device. The computer-readable storage medium may include, but is not limited to, electronic, magnetic, optical, electromagnetic, infrared, or semiconductor systems, apparatus, or devices, or any suitable combination of the foregoing. Alternatively, the computer-readable storage medium may be a machine-readable signal medium. More specific examples of the machine-readable storage medium would include an electrical connection based on one or more wires, a portable computer diskette, 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 disc read-only memory (CD-ROM), an optical storage device, a magnetic storage device, or any suitable combination of the foregoing.

[0210] In order to provide interaction with a user, the systems and techniques described herein may be implemented on an electronic device 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 a pointing device (e.g., a mouse or a trackball) by which the user can provide input to the electronic device. Other kinds of devices may also be used to provide interaction with the user; for example, the feedback provided to the user may be any form of sensory feedback (e.g., visual feedback, auditory feedback, or tactile feedback); and input from the user may be received in any form (including acoustic input, voice input, or tactile input).

[0211] The systems and techniques described herein can be implemented in a computing system including backend components (e.g., as a data server), or a computing system including middleware components (e.g., an application server), or a computing system including frontend components (e.g., a user computer having a graphical user interface or a web browser through which a user can interact with an implementation of the systems and techniques described herein), or a computing system including any combination of such backend components, middleware components, or frontend components. The components of the system can be interconnected with each other by digital data communication in any form or medium (e.g., a communication network). Examples of communication networks include: local area network (LAN), wide area network (WAN), blockchain network, and the Internet.

[0212] A computing system can include a client and a server. The client and the server are generally far from each other and typically interact through a communication network. The client-server relationship is created by computer programs running on respective computers and having a client-server relationship with each other. The server can be a cloud server, also known as a cloud computing server or a cloud host, which is a host product in the cloud computing service system, solving the defects of difficult management and weak business scalability existing in traditional physical hosts and VPS services.

[0213] It should be understood that the various forms of processes shown above can be used, with steps reordered, added, or deleted. For example, the steps recited in the present invention can be executed in parallel, sequentially, or in a different order, as long as the desired results of the technical solution of the present invention can be achieved, and no limitations are imposed herein.

[0214] The above specific embodiments do not constitute a limitation on the protection scope of the present invention. Those skilled in the art should understand that various modifications, combinations, sub-combinations, and substitutions can be made according to design requirements and other factors. Any modifications, equivalent substitutions, and improvements made within the spirit and principles of the present invention shall be included within the protection scope of the present invention.

Claims

1. A distillation tower convergence method based on a combined module, characterized in that: Including: Obtain the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow; wherein, the coupling of the first distillation column and the second distillation column is realized through the first material flow and the second material flow; the parameters of the first distillation column and the second distillation column include the temperature of each tray, the rising steam flow rate, the descending liquid flow rate, the vapor phase composition, and the liquid phase composition; the parameters of the first material flow and the second material flow include temperature, flow rate, and components. Based on the first distillation column and the second distillation column, construct a simplified inner-loop iterative objective function. According to the simplified inner-loop iterative objective function and the partial derivatives of the simplified inner-loop iterative objective function, solve the simplified inner-loop iterative objective function to obtain the parameter change values. According to the parameter change values, update the initial parameter values of the first distillation column, the initial parameter values of the second distillation column, the initial parameter values of the first material flow, and the initial parameter values of the second material flow to obtain the target parameter values of the first distillation column, the target parameter values of the second distillation column, the target parameter values of the first material flow, and the target parameter values of the second material flow. Among them, constructing a simplified inner-loop iterative objective function based on the first distillation column and the second distillation column includes: Based on the principle of energy conservation, the principle of mass conservation, and the principle of phase equilibrium, construct a simplified inner-loop iterative objective function based on the parameters of the first distillation column and the parameters of the second distillation column; wherein, the parameters include liquid phase flow rate, vapor phase flow rate, vapor phase mole fraction, liquid phase mole fraction, vapor phase molar enthalpy, liquid phase molar enthalpy, feed enthalpy, liquid phase draw, vapor phase draw, feed, and phase equilibrium constant.

2. The method according to claim 1, characterized in that, The determination process of the vapor phase molar enthalpy includes: Calculate the vapor phase molar enthalpy using the following formula. ； ； Outer ring iterative update , and the update method is; ； ； ； ； ； ； ； ； ； ； ； ； Among them, is the vapor molar enthalpy, is the ideal gas enthalpy value, is the deviation enthalpy at temperature , is the deviation enthalpy at temperature , is the deviation heat capacity, is the compressibility factor, is the ideal gas constant, is the system temperature, is the system volume, is the th phase equilibrium constant of the th component on the th tray, is the content of component , is the content of component , is the critical temperature of component , is the critical temperature of component , is the critical pressure of component , is the number of components, The reduced temperature of component , is the acentric factor of component , The reduced temperature of component , is the acentric factor of component .

3. The method according to claim 1, characterized in that, The determination process of the correction coefficient of the phase equilibrium constant includes: Calculate the outer-loop phase equilibrium constant according to the liquid phase fugacity coefficient and the vapor phase fugacity coefficient; wherein, the liquid phase fugacity coefficient is used to characterize the deviation degree of the component fugacity from the fugacity of the component in the ideal solution; the vapor phase fugacity coefficient is used to characterize the deviation degree of the real gas from the ideal gas. Determine the correction coefficient of the phase equilibrium constant according to the outer-loop phase equilibrium constant and the preset ideal phase equilibrium constant.

4. The method according to claim 1, characterized in that, The parameters of the first material flow and the second material flow include component content. Correspondingly, the determination process of the component content includes: Obtain the crude oil distillation curve. Convert the crude oil distillation curve into a true boiling point curve, and determine the component boiling point and the component relative molecular weight according to the true boiling point curve. According to the component boiling point and the component relative molecular weight, determine the target component, and perform cyclic iterative processing on the target component to determine the component content corresponding to the target component.

5. The method according to claim 4, characterized in that, Determining the component content corresponding to the target component includes: Obtain the initial component content. Calculate the distillate percentage according to the initial component content and the temperature and pressure in the true boiling point curve. Determine the error value according to the distillate percentage and the preset distillate percentage. When the error value meets the preset error condition, use the initial component content as the component content corresponding to the target component. In the case where the error value does not satisfy the preset error condition, the distillation percentage is recalculated, and the initial component content is continuously updated until the error value satisfies the preset error condition, and the initial component content is used as the component content corresponding to the target component.

6. The method according to claim 1, wherein The method further comprises: The operating conditions of the distillation tower are determined according to the target parameter value of the first distillation tower, the target parameter value of the second distillation tower, the target parameter value of the first material flow and the target parameter value of the second material flow; wherein the operating conditions of the distillation tower are the conditions for controlling the operation of the distillation tower.

7. A distillation tower convergence device based on a combined module, characterized in that: include: An initial parameter value acquisition module is used to acquire the initial parameter values ​​of the first distillation tower, the initial parameter values ​​of the second distillation tower, the initial parameter values ​​of the first material flow, and the initial parameter values ​​of the second material flow; wherein the coupling of the first distillation tower and the second distillation tower is realized through the first material flow and the second material flow; the parameters of the first distillation tower and the second distillation tower include the temperature of each tray, the amount of rising steam, the amount of descending liquid, the vapor phase composition, and the liquid phase composition; the parameters of the first material flow and the second material flow include temperature, flow rate, and composition; A simplified inner loop iterative objective function construction module, used to construct a simplified inner loop iterative objective function based on the first distillation tower and the second distillation tower; A parameter change value obtaining module, used for solving the simplified inner loop iterative objective function according to the simplified inner loop iterative objective function and the partial derivative of the simplified inner loop iterative objective function to obtain the parameter change value; a target parameter value obtaining module, for updating the initial parameter value of the first distillation tower, the initial parameter value of the second distillation tower, the initial parameter value of the first material flow, and the initial parameter value of the second material flow according to the parameter change value, and obtaining the target parameter value of the first distillation tower, the target parameter value of the second distillation tower, the target parameter value of the first material flow, and the target parameter value of the second material flow; Among them, the simplified inner loop iterative objective function building module includes: A simplified inner loop iterative objective function construction unit is used to construct a simplified inner loop iterative objective function based on the parameters of the first distillation tower and the parameters of the second distillation tower according to the principle of conservation of energy, the principle of conservation of mass and the principle of phase equilibrium; wherein the parameters include liquid phase flow rate, vapor phase flow rate, vapor phase molar fraction, liquid phase molar fraction, vapor phase molar enthalpy, liquid phase molar enthalpy, feed enthalpy, liquid phase production, vapor phase production, feed and phase equilibrium constant.

8. An electronic device, characterized in that, The electronic device comprises: At least one processor; and a memory communicatively connected to the at least one processor; wherein the memory stores a computer program executable by the at least one processor, and the computer program is executed by the at least one processor so that the at least one processor can execute the distillation tower convergence method based on the joint modules as described in any one of claims 1-6.

9. A computer-readable storage medium, characterized in that, The computer-readable storage medium stores computer instructions, and the computer instructions are used to enable a processor to implement the distillation tower convergence method based on simultaneous modules according to any one of claims 1 to 6 when executed.

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