Rectifying tower convergence method and device based on simultaneous module, electronic equipment and medium

Abstract

The invention discloses a rectifying tower convergence method and device based on a simultaneous module, electronic equipment and a medium. The method comprises the following steps: acquiring an initial parameter value of a first rectifying tower, an initial parameter value of a second rectifying tower, an initial parameter value of a first substance flow and an initial parameter value of a second substance flow; based on the first rectifying tower and the second rectifying tower, constructing a simplified inner ring iteration objective function; according to the simplified inner ring iteration objective function and the partial derivative of the simplified inner ring iteration objective function, solving the simplified inner ring iteration objective function to obtain a parameter change value; updating the initial parameter value of the first rectifying tower, the initial parameter value of the second rectifying 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 a target parameter value of the first rectifying tower, a target parameter value of the second rectifying tower, a target parameter value of the first material flow and a target parameter value of the second material flow. According to the technical scheme, the calculation convergence speed of the rectifying tower is improved.

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] The technical solution of the embodiment of the present invention obtains 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; based on the first distillation tower and the second distillation tower, a simplified inner circle iterative objective function is constructed; according to the simplified inner circle iterative objective function and the partial derivative of the simplified inner circle iterative objective function, the simplified inner circle iterative objective function is solved to obtain the parameter change value; 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. This technical solution better solves the convergence difficulty problem of the sequential module method and the problem of the inability 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.

[0019] It should be understood that the contents described in this section are not intended to identify the key or important features of the embodiments of the present invention, nor are they intended 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 briefly introduces the drawings required for use in the description of the embodiments. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without creative work.

[0021] Figure 1 is a flow chart of a distillation tower convergence method based on a joint module according to Embodiment 1 of the present invention;

[0022] Figure 2 A schematic diagram of a coupled distillation tower provided in Example 1 of the present application;

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

[0024] Figure 4 A schematic diagram of a distillation tower convergence method based on a joint module provided in Example 2 of the present invention;

[0025] Figure 5 A schematic diagram of the structure of a distillation tower convergence device based on a combined module provided in Example 3 of the present invention;

[0026] Figure 6 It is a structural schematic diagram of an electronic device for implementing a distillation tower convergence method based on a joint module according to an embodiment 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 This is a schematic diagram of the actual boiling point curve provided in Example 1 of the present application, as shown in FIG. Figure 3 As shown, the actual boiling point curve is expressed as the volume percentage of the distillate phase and the corresponding temperature. Among them, the volume percentage of the distillate phase includes 0, 10, 30, 50, 70, 90, and 100. The corresponding temperature values ​​under different percentages are plotted at the same time. On the actual boiling point distillation curve, there is one component every 20 degrees or so, and the boiling point of the component is the interval of 20 degrees on the actual boiling point distillation curve and the horizontal axis to form a trapezoid. The boiling point of the component can be calculated by dividing the area of ​​the trapezoid by the distance of the x-axis.

[0043] Further, the relative molecular weight of the component is calculated based on the boiling point of the component and the preset characteristic factor. Specifically, the relative molecular weight of the component can be estimated using the Hariu-Sage method, and the calculation formula is:

[0044] ;

[0045] in, is the relative molecular weight of the component, , , , , , , , , , It is the boiling point of the components of the petroleum fraction, the unit is F, and K is the characteristic factor.

[0046] In this scheme, the component boiling point and the relative molecular weight of the component are used to search and match the alkanes, isoalkanes, cycloalkanes, aromatics and other substances in the pure substance database, and a target component with the closest component boiling point and relative molecular weight is matched 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, and the component content corresponding to the target component can be calculated by a cyclic iteration method. Specifically, according to the temperature and pressure at different percentages of the actual boiling point distillation curve, the distillation percentage is calculated by temperature and pressure flash distillation, and the component content corresponding to the target component is cyclically iterated based on the distillation percentage, thereby determining 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 component content of the distillation tower, thereby realizing the optimization of the coupled distillation tower.

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

[0050] Obtaining initial component content;

[0051] Calculating the distillation percentage according to the initial component content and the temperature and pressure in the actual boiling point curve;

[0052] Determining an error value according to the distillation percentage and a preset distillation percentage;

[0053] When the error value satisfies a preset error condition, the initial component content is used as the component content corresponding to the target component;

[0054] 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.

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

[0056] Furthermore, according to the temperature, pressure and initial component content at different percentages of the actual boiling point distillation curve, a set of distillation percentages are calculated using temperature and pressure flash calculation. The distillation percentage is then compared with the preset distillation percentage to determine the error. If the error Greater than 0, then arrive The mole fraction of the component in the interval decreases, otherwise it increases. Representation interval The error, Indicates The calculated distillation percentage corresponding to the temperature, Indicates The actual distillation percentage corresponding to the temperature is the preset distillation percentage. ; ; is the error value.

[0057] 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 satisfies the preset error condition; when the error value is greater than or equal to the preset error, the error value does not satisfy the preset error condition.

[0058] In this scheme, when When it is less than the preset error, the iteration is exited and the initial component content is used 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 nor disappear out of thin air. It can only be transformed from one form to another, or transferred from one object to another, 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, the total mass and energy of the system do not change over time regardless of any changes or processes that occur in the system.

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

[0072] In this embodiment, a simplified inner loop iteration objective function of the distillation tower 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] in,

[0079] ;

[0080] ;

[0081] in, , No. , Liquid flow rate per tray; , For the , The vapor phase flow rate of each tray; , For the The first plate The vapor and liquid phase mole fractions of each component; , For the The vapor phase molar enthalpy and liquid phase molar enthalpy of each plate; For the The feed enthalpy of each tray; For the Liquid phase extraction from the tower plates; For the The vapor phase is extracted through the tower plates; For the Feed to the trays; For the The first plate The phase equilibrium constant of each component, To the The heat input of each tray, For the Plate No. The feed mole fraction of each component.

[0082] In this solution, with the help of data interface technologies such as OPC (OLE for Process Control) and Modbus, key data can be extracted from DCS databases, analytical and testing experiment databases, etc.

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

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

[0085] The vapor phase molar enthalpy was calculated using the following formula;

[0086] ;

[0087] ;

[0088] Outer ring iteration update , the update method is;

[0089] ;

[0090] ;

[0091] ;

[0092] ;

[0093] ;

[0094] ;

[0095] ;

[0096] ;

[0097] ;

[0098] ;

[0099] ;

[0100] ;

[0101] in, is the vapor phase molar enthalpy, is the ideal gas enthalpy, The temperature is The deviation enthalpy at The temperature is The deviation enthalpy at is the deviation heat capacity, is the compression factor, is the ideal gas constant, is the system temperature, is the system volume, It is The first plate The phase equilibrium constant of each component, It is a component The content of It is a component The content of It is a component The critical temperature, It is a component The critical temperature, It is a component The critical pressure, It is a component The critical pressure, is the number of components, Components The contrast temperature, It is a component The eccentricity factor, Components The contrast temperature, It is a component The eccentricity factor.

[0102] Specifically, the calculation of enthalpy is divided into two parts, one part is the ideal gas enthalpy and the other part is the deviation enthalpy, that is, ;in, is the ideal gas enthalpy, is the deviation enthalpy. The ideal gas enthalpy is calculated by weighted average of the ideal gas enthalpy of pure substances. The calculation of the deviation enthalpy is more complicated, and the deviation enthalpy part needs to be simplified. The deviation enthalpy is simplified to: ;in, is the deviation heat capacity. The deviation enthalpy is thus simplified to a linear equation, which is updated by calculating value.

[0103] Specifically, the calculated temperature is of ;

[0104] ;

[0105] ;

[0106] The calculated temperature is of ;

[0107] ;

[0108] ;

[0109] in, ;

[0110] ;

[0111] ;

[0112] ;

[0113] ;

[0114] ;

[0115] ;

[0116] ;

[0117] .

[0118] The calculation of deviation enthalpy is a very complicated process. The iterative method of inner and outer circles can reduce the calculation frequency of deviation enthalpy, greatly simplify the amount of calculation, and reduce the nonlinearity of the objective function, thereby achieving the goal of rapid convergence of the distillation tower.

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

[0120] The outer ring phase equilibrium constant is calculated according to the liquid phase fugacity coefficient and the vapor phase fugacity coefficient; wherein the liquid phase fugacity coefficient is used to characterize the degree of deviation between the fugacity of the component and the fugacity of the component in the ideal solution; and the vapor phase fugacity coefficient is used to characterize the degree of deviation between the actual gas and the ideal gas;

[0121] A correction coefficient of the phase equilibrium constant is determined according to the outer ring phase equilibrium constant and a 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 and can be obtained by calculation.

[0123] Furthermore, the liquid phase fugacity coefficient and the vapor phase fugacity coefficient can be divided to obtain the outer ring phase equilibrium constant. Specifically, ; is the phase equilibrium constant to the outer ring, 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 scheme, the correction factor of the phase equilibrium constant can be given by Assign initial values, calculate the preset ideal phase equilibrium constant, and then update the correction coefficient of the phase equilibrium constant based on the calculated outer ring phase equilibrium constant and the preset ideal phase equilibrium constant. Specifically, .

[0126] The calculation process of the fugacity coefficient includes:

[0127] ;

[0128] ;

[0129] ;

[0130] ;

[0131] ;

[0132] ;

[0133] ;

[0134] ;

[0135] ;

[0136] ;

[0137] ;

[0138] in, It is a component The content of is the compression factor, is the ideal gas constant, is the system temperature, It is a component The content of It is a component The content of is the system volume, It is a component The critical temperature, It is a component The critical pressure, Components The contrast temperature, It is a component The eccentricity factor, It is a component The critical temperature, It is a component The critical pressure, Components The contrast temperature, It is a component The eccentricity factor.

[0139] The calculation of the phase equilibrium constant is a very complex process. The iterative method of inner and outer circles can reduce the calculation frequency of the phase equilibrium constant, greatly simplify the amount of calculation, and reduce the nonlinearity of the objective function, thereby achieving the goal of rapid convergence of the distillation tower.

[0140] S130. Solve 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.

[0141] Among them, the partial derivative of the simplified inner loop iterative 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] The technical solution of the embodiment of the present invention obtains 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, and constructs a simplified inner circle iterative objective function based on the first distillation tower and the second distillation tower, and then solves 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 the parameter change value, and updates 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. By implementing this technical solution, the convergence difficulty of the sequential module method and the problem of the inability to locate errors of the simultaneous equation method are better solved, and the convergence speed of the distillation tower calculation is improved, and the accuracy of the calculation can be improved.

[0147] Embodiment 2

[0148] Figure 4 This is a schematic diagram of a distillation tower convergence method based on a combined module provided in Example 2 of the present invention. The relationship between this embodiment and the above embodiment is a detailed supplement to the distillation tower operation process. Figure 4 As shown, the method includes:

[0149] S410. 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.

[0150] S420: construct a simplified inner loop iterative objective function based on the first distillation tower and the second distillation tower.

[0151] S430. Solve 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.

[0152] S440. 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.

[0153] S450. Determine operating conditions of the distillation tower 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 conditions for controlling the operation of the distillation tower.

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

[0155] The operating conditions of the distillation tower include the temperature, pressure, reboiler load, reflux ratio, etc. of the distillation tower. The operating conditions of the distillation tower can be obtained by combining and calculating 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.

[0156] Specifically, an optimizer is superimposed on the outside of the distillation tower, and optimization objectives such as minimum energy consumption, maximum product purity or output can be input to determine decision variables such as reflux ratio, feed position, reboiler ratio, etc. The operating conditions of the distillation tower are output through the optimization algorithm, such as the temperature, pressure, reboiler load, reflux ratio, etc. of the distillation tower.

[0157] The technical solution of the embodiment of the present invention is to obtain 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, and then construct a simplified inner circle iterative objective function based on the first distillation tower and the second distillation tower, and then solve 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 the parameter change value, and 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 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, and then calculate the distillation tower operating conditions based on 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. By implementing this technical solution, the convergence difficulty problem of the sequential module method and the inability to locate errors of the simultaneous equation method are better solved, the convergence speed of the distillation tower calculation is improved, the accuracy of the calculation can be improved, and oil separation is achieved.

[0158] Embodiment 3

[0159] Figure 5 This is a schematic diagram of the structure of a distillation tower convergence device based on a combined module provided in Example 3 of the present invention. Figure 5 As shown, the device comprises:

[0160] An initial parameter value acquisition module 510 is used to acquire an initial parameter value of a first distillation tower, an initial parameter value of a second distillation tower, an initial parameter value of a first material flow, and an initial parameter value of a 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;

[0161] A simplified inner loop iterative objective function construction module 520, configured to construct a simplified inner loop iterative objective function based on the first distillation tower and the second distillation tower;

[0162] A parameter change value obtaining module 530 is used to solve 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;

[0163] The target parameter value obtaining module 540 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.

[0164] Optionally, a simplified inner loop iterative objective function building module 520 includes:

[0165] 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.

[0166] Optional, simplified inner loop iterative objective function building block, specifically used for:

[0167] The vapor phase molar enthalpy was calculated using the following formula;

[0168] ;

[0169] ;

[0170] Outer ring iteration update , the update method is;

[0171] ;

[0172] ;

[0173] ;

[0174] ;

[0175] ;

[0176] ;

[0177] ;

[0178] ;

[0179] ;

[0180] ;

[0181] ;

[0182] ;

[0183] in, is the vapor phase molar enthalpy, is the ideal gas enthalpy, The temperature is The deviation enthalpy at The temperature is The deviation enthalpy at is the deviation heat capacity, is the compression factor, is the ideal gas constant, is the system temperature, is the system volume, It is The first plate The phase equilibrium constant of each component, It is a component The content of It is a component The content of It is a component The critical temperature, It is a component The critical temperature, It is a component The critical pressure, It is a component The critical pressure, is the number of components, Components The contrast temperature, It is a component The eccentricity factor, Components The contrast temperature, It is a component The eccentricity factor.

[0184] An optional, simplified inner loop iterative objective function building block is also used to:

[0185] The outer ring phase equilibrium constant is calculated according to the liquid phase fugacity coefficient and the vapor phase fugacity coefficient; wherein the liquid phase fugacity coefficient is used to characterize the degree of deviation between the fugacity of the component and the fugacity of the component in the ideal solution; and the vapor phase fugacity coefficient is used to characterize the degree of deviation between the actual gas and the ideal gas;

[0186] A correction coefficient of the phase equilibrium constant is determined according to the outer ring phase equilibrium constant and a 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] Accordingly, the device further comprises:

[0189] A crude oil distillation curve acquisition module is used to acquire a crude oil distillation curve;

[0190] A component boiling point and component relative molecular weight determination module, used for converting the crude oil distillation curve into a real boiling point curve, and determining the component boiling point and the component relative molecular weight according to the real boiling point curve;

[0191] The component content determination module is used to determine the target component according to the component boiling point and the relative molecular weight of the component, and to perform cyclic iterative processing on the target component to determine the component content corresponding to the target component.

[0192] Optionally, a component content determination module is specifically used to:

[0193] Obtaining initial component content;

[0194] Calculating the distillation percentage according to the initial component content and the temperature and pressure in the actual boiling point curve;

[0195] Determining an error value according to the distillation percentage and a preset distillation percentage;

[0196] When the error value satisfies a preset error condition, the initial component content is used as the component content corresponding to the target component;

[0197] 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.

[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] A number of 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 disk, 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 through a computer network such as the Internet and / or various telecommunication networks.

[0205] The processor 11 may be a variety of general and / or dedicated processing components with processing and computing power. 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 appropriate processor, controller, microcontroller, etc. The processor 11 executes the various methods and processes described above, such as a distillation column convergence method based on a joint module.

[0206] In some embodiments, the distillation column convergence method based on the joint module can be implemented as a computer program, which is tangibly contained in a computer-readable storage medium, such as a storage unit 18. In some embodiments, part or all of the computer program can be loaded and / or installed on 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 based on the joint module described above can be performed. Alternatively, in other embodiments, the processor 11 can be configured to execute the distillation column convergence method based on the joint module in any other appropriate manner (for example, by means of firmware).

[0207] 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.

[0208] Computer programs for implementing the methods 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 device, so that when the computer program is executed by the processor, the functions / operations specified in the flow chart and / or block diagram are implemented. The computer program 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.

[0209] In the context of the present invention, a computer-readable storage medium may be a tangible medium that may contain or store a computer program for use by or in conjunction with an instruction execution system, device, or equipment. A computer-readable storage medium may include, but is not limited to, electronic, magnetic, optical, electromagnetic, infrared, or semiconductor systems, devices, or equipment, or any suitable combination of the foregoing. Alternatively, a computer-readable storage medium may be a machine-readable signal medium. 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.

[0210] 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 trackball) through which the user can provide input to the electronic device. Other types 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 may be implemented in a computing system that includes backend 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 frontend 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 backend components, middleware components, or frontend 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), a blockchain network, and the Internet.

[0212] 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 client and server relationship is generated by computer programs running on the corresponding computers and having a client-server relationship with each other. The server may be a cloud server, also known as a cloud computing server or cloud host, which is a host product in the cloud computing service system to solve the defects of difficult management and weak business scalability in traditional physical hosts and VPS services.

[0213] 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 described in the present invention can be executed in parallel, sequentially or in different orders, as long as the desired results of the technical solution of the present invention can be achieved, and this document does not limit this.

[0214] The above specific implementations do not constitute a limitation on the protection scope of the present invention. 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 invention should be included in the protection scope of the present invention.

Claims

1. A distillation tower convergence method based on a combined module, characterized in that: include: 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; Based on the first distillation tower and the second distillation tower, construct a simplified inner loop iterative objective function; 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; 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.

2. The method according to claim 1, characterized in that Based on the first distillation tower and the second distillation tower, a simplified inner loop iterative objective function is constructed, including: 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.

3. The method according to claim 2, characterized in that The process of determining the vapor phase molar enthalpy comprises: The vapor phase molar enthalpy was calculated using the following formula; ； ； Outer ring iteration update , the update method is; ； ； ； ； ； ； ； ； ； ； ； ； in, is the vapor phase molar enthalpy, is the ideal gas enthalpy, The temperature is The deviation enthalpy at The temperature is The deviation enthalpy at is the deviation heat capacity, is the compression factor, is the ideal gas constant, is the system temperature, is the system volume, It is The first plate The phase equilibrium constant of each component, It is a component The content of It is a component The content of It is a component The critical temperature, It is a component The critical temperature, It is a component The critical pressure, It is a component The critical pressure, is the number of components, Components The contrast temperature, It is a component The eccentricity factor, Components The contrast temperature, It is a component The eccentricity factor.

4. The method according to claim 2, characterized in that: The process of determining the correction coefficient of the phase equilibrium constant includes: The outer ring phase equilibrium constant is calculated according to the liquid phase fugacity coefficient and the vapor phase fugacity coefficient; wherein the liquid phase fugacity coefficient is used to characterize the degree of deviation between the fugacity of the component and the fugacity of the component in the ideal solution; and the vapor phase fugacity coefficient is used to characterize the degree of deviation between the actual gas and the ideal gas; A correction coefficient of the phase equilibrium constant is determined according to the outer ring phase equilibrium constant and a preset ideal phase equilibrium constant.

5. The method according to claim 1, characterized in that The parameters of the first material flow and the parameters of the second material flow include component contents; Accordingly, the process of determining the component content includes: Obtain crude oil distillation curve; 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; 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.

6. The method according to claim 5, characterized in that Determine the component content corresponding to the target component, including: Obtaining initial component content; Calculating the distillation percentage according to the initial component content and the temperature and pressure in the actual boiling point curve; Determining an error value according to the distillation percentage and a preset distillation percentage; When the error value satisfies a preset error condition, the initial component content is used 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.

7. The method according to claim 1, characterized in that 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.

8. A distillation tower convergence device based on a combined module, characterized in that: include: 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; 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; 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.

9. 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 1-7.

10. 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 7 when executed.

Images