A method and device for optimizing parameters of a positive pressure heating crude oil stabilization system

Abstract

A positive pressure heating crude oil stabilization system parameter optimization method and device, the method comprises the following steps: constructing a crude oil stabilization simulation model of a positive pressure heating crude oil stabilization system, at least including a stabilization tower module and a pre-tower heating furnace module; inputting crude oil component parameters into the crude oil stabilization simulation model, and setting the heating furnace outlet temperature as different temperature values T n sequentially; n Carrying out positive pressure heating crude oil stabilization process simulation to obtain the stabilization tower overhead pressure P n and fuel consumption F n corresponding to the highest light hydrocarbon yield Q n at each temperature value T n ; calculating the corresponding profit value A n according to each set of yield and energy consumption data, each set of yield and energy consumption data comprising Q n and F n ; obtaining the maximum profit value from N profit values A n , and taking the T n and P n corresponding to the maximum profit value as the optimal heating furnace outlet temperature and the optimal stabilization tower overhead pressure respectively; and based on the crude oil stabilization simulation model, analyzing the light hydrocarbon yield and fuel energy consumption to ensure the maximum economic benefit while saving energy and reducing costs.

Description

Technical Field

[0001] This article relates to the field of oil and gas gathering and transportation, and in particular to a method and apparatus for optimizing parameters of a positive pressure heating crude oil stabilization system. Background Technology

[0002] There are many methods for crude oil stabilization, among which positive pressure heating flash stabilization is a commonly used method. This method involves heating the crude oil after oil-gas separation and dehydration, and then flash-separating it under slight positive pressure to achieve flash stabilization. From the current operation of crude oil stabilization systems, it is clear that operating parameters can only be adjusted based on experience or planned light hydrocarbon production. Crude oil stabilization systems often cannot operate under optimal conditions, resulting in high energy consumption, increased production costs, and low economic efficiency. Under the current dual-carbon background, there are severe challenges to energy conservation, carbon reduction, and green transformation. In order to achieve high-quality development of oil fields and improve economic efficiency, it is urgent to conduct research on the optimization of the process and operating parameters of crude oil stabilization systems to maximize the production benefits of crude oil stabilization while ensuring energy conservation and environmental protection. Summary of the Invention

[0003] This application provides a method and apparatus for optimizing parameters of a positive pressure heated crude oil stabilization system. Based on a crude oil stabilization simulation model, it analyzes light hydrocarbon production and fuel energy consumption, ensuring maximum economic benefits while saving energy, protecting the environment, and reducing production costs. It provides a scientific and feasible parameter optimization scheme for the actual production and operation of the positive pressure heated crude oil stabilization system.

[0004] On the one hand, embodiments of this application provide a method for predicting energy consumption and adjusting parameters of an oil and gas gathering and transportation system, including:

[0005] A crude oil stabilization simulation model of a positive pressure heating crude oil stabilization system is constructed, wherein the crude oil stabilization simulation model includes at least a stabilization tower module and a tower front heater module;

[0006] The crude oil composition parameters are input into the crude oil stability simulation model, and the furnace outlet temperature is sequentially set to different temperature values ​​T. n A positive pressure heating crude oil stabilization process simulation was conducted to obtain the results at various temperature values ​​T. n Achieving maximum light hydrocarbon production Q under these conditions n The corresponding stabilizer tower top pressure P n and fuel consumption F n , where n = 1, 2, ..., N;

[0007] Calculate the corresponding revenue value A based on each set of production and energy consumption data. n Each set of production and energy consumption data includes the highest light hydrocarbon production Q. n and the fuel consumption F n ;

[0008] In N of the aforementioned revenue values ​​A n Obtain the maximum profit value, and set the T corresponding to the maximum profit value. n and P n These are respectively used as the optimal furnace outlet temperature and the optimal stabilizer tower top pressure.

[0009] On the other hand, this application also provides a parameter optimization device for a positive pressure heating crude oil stabilization system, including a memory and a processor;

[0010] The memory is used to store the parameter optimization program for the positive pressure heating crude oil stabilization system;

[0011] The processor is used to read the parameter optimization program of the positive pressure heating crude oil stabilization system and perform the parameter optimization method of the positive pressure heating crude oil stabilization system as described in the above embodiments.

[0012] Compared with related technologies, the parameter optimization method and apparatus for a positive pressure heating crude oil stabilization system according to the embodiments of this application simulates the positive pressure heating crude oil stabilization process under different heating furnace outlet temperatures and different stabilization tower top pressures using a crude oil stabilization simulation model. This enables parameter optimization of the heating furnace outlet temperature and stabilization tower top pressure. Combined with analysis of light hydrocarbon production and fuel consumption, it ensures maximum economic benefits while saving energy, protecting the environment, and reducing production costs. This provides a scientific and feasible parameter optimization scheme for the actual production and operation of the positive pressure heating crude oil stabilization system.

[0013] Other features and advantages of this application will be set forth in the following description, and will be apparent in part from the description, or may be learned by practicing the application. Other advantages of this application can be realized and obtained by means of the embodiments described in the description and the accompanying drawings. Attached Figure Description

[0014] The accompanying drawings are used to provide an understanding of the technical solutions of this application and constitute a part of the specification. They are used together with the embodiments of this application to explain the technical solutions of this application and do not constitute a limitation on the technical solutions of this application.

[0015] Figure 1 This is a flowchart illustrating a parameter optimization method for a positive pressure heating crude oil stabilization system according to an embodiment of this application.

[0016] Figure 2 A graph showing the relationship between light hydrocarbon production and tower top pressure when the furnace outlet temperature is 180°C, as a specific example of this application.

[0017] Figure 3 A graph showing the relationship between light hydrocarbon production and tower top pressure when the furnace outlet temperature is 190°C, as a specific example of this application.

[0018] Figure 4 A graph showing the relationship between light hydrocarbon production and tower top pressure when the furnace outlet temperature is 200°C, as a specific example of this application.

[0019] Figure 5 A graph showing the relationship between light hydrocarbon production and tower top pressure when the furnace outlet temperature is 210°C, as a specific example of this application.

[0020] Figure 6 This is a schematic diagram of a parameter optimization device for a positive pressure heating crude oil stabilization system according to an embodiment of this application. Detailed Implementation

[0021] This application describes several embodiments, but these descriptions are exemplary and not limiting, and it will be apparent to those skilled in the art that many more embodiments and implementations are possible within the scope of the embodiments described herein. Although many possible combinations of features are shown in the drawings and discussed in the detailed description, many other combinations of the disclosed features are also possible. Unless specifically limited, any feature or element of any embodiment may be used in combination with, or may replace, any feature or element of any other embodiment.

[0022] This application includes and contemplates combinations of features and elements known to those skilled in the art. The embodiments, features, and elements disclosed in this application can also be combined with any conventional features or elements to form unique inventive solutions. Any feature or element of any embodiment can also be combined with features or elements from other inventive solutions to form another unique inventive solution. Therefore, it should be understood that any feature shown and / or discussed in this application can be implemented individually or in any suitable combination. Therefore, the embodiments are not limited except by the limitations imposed by the appended claims and their equivalents. Furthermore, various modifications and changes can be made within the scope of the appended claims.

[0023] Furthermore, in describing representative embodiments, the specification may have presented methods and / or processes as a specific sequence of steps. However, the method or process should not be limited to the specific order of steps described herein, to the extent that it does not depend on such a specific order. As will be understood by those skilled in the art, other sequences of steps are also possible. Therefore, the specific order of steps set forth in the specification should not be construed as a limitation of the claims. Moreover, the claims concerning the method and / or process should not be limited to the steps performed in the written order, and those skilled in the art will readily understand that these orders can be varied and still remain within the spirit and scope of the embodiments of this application.

[0024] Crude oil stabilization systems are crucial production systems in oilfield surface operations. Crude oil stabilization involves processing the crude oil gathered and transported in a closed system to separate and recover light hydrocarbons such as methane, ethane, propane, and butane, yielding high-value-added products like light oil. This process also reduces the evaporation loss of remaining products after stabilization. However, current positive-pressure heating stabilization systems suffer from high energy consumption and poor economic efficiency. To achieve high-quality oilfield development and improve economic efficiency, it is urgent to conduct optimization research on the existing stabilization system's processes and operating parameters.

[0025] This application provides a method for optimizing parameters of a positive pressure heated crude oil stabilization system, including steps S100-S400, such as... Figure 1 As shown:

[0026] S100: Construct a crude oil stability simulation model for a positive pressure heating crude oil stabilization system, wherein the crude oil stability simulation model includes at least a stabilization tower module and a tower front heater module;

[0027] S200: Input the crude oil component parameters into the crude oil stability simulation model, and sequentially set the furnace outlet temperature to different temperature values ​​T. n A positive pressure heating crude oil stabilization process simulation was conducted to obtain the results at various temperature values ​​T. n Achieving maximum light hydrocarbon production Q under these conditions n The corresponding stabilizer tower top pressure P n and fuel consumption F n , where n = 1, 2, ..., N;

[0028] S300: Calculate the corresponding revenue value A based on each set of production and energy consumption data. n Each set of production and energy consumption data includes the highest light hydrocarbon production Q. n and the fuel consumption F n ;

[0029] S400: In N said revenue values ​​A n Obtain the maximum profit value, and set the T corresponding to the maximum profit value. n and P n These are respectively used as the optimal furnace outlet temperature and the optimal stabilizer tower top pressure.

[0030] In this embodiment, the crude oil stabilization simulation model is a computer simulation model established based on the positive pressure heating crude oil stabilization system. It can reflect the process flow, various production equipment and their parameters of the positive pressure heating crude oil stabilization system. The crude oil stabilization simulation model includes at least a stabilization tower module and a tower preheater module. The stabilization tower module is a simulation model of the stabilization tower in the positive pressure heating crude oil stabilization system, and the tower preheater module is a simulation model of the tower preheater in the positive pressure heating crude oil stabilization system. The parameters of the stabilization tower module include at least the stabilization tower top pressure, and the parameters of the tower preheater module include at least the heater outlet temperature. By optimizing the stabilization tower top pressure and the heater outlet temperature, the positive pressure heating crude oil stabilization system can obtain the maximum economic benefits when carrying out the crude oil stabilization process according to the optimal heater outlet temperature and the optimal stabilization tower top pressure.

[0031] In this embodiment, in the crude oil stabilization simulation model, the crude oil to be stabilized can first be pre-treated in the crude oil buffer tank, such as desalting, dehydration and pressure stabilization, so that the stable flowing medium enters the tower front heater module. The medium heated by the tower front heater module enters the stabilization tower module for flash evaporation, so that the light components and heavy components can be separated. The removed light hydrocarbons flow out from the top of the stabilization tower module, and the remaining stabilized crude oil flows out from the bottom of the stabilization tower module.

[0032] In this embodiment, when performing step S200, the furnace outlet temperature of the tower front heating furnace module can be set to N temperature values ​​T. n The furnace outlet temperature was gradually adjusted from low to high. After fixing the furnace outlet temperature at a certain value, the tower top pressure was adjusted sequentially from low to high. Positive pressure heating crude oil stabilization process simulation was conducted to obtain the correspondence between light hydrocarbon production and tower top pressure. The tower top pressure corresponding to the highest light hydrocarbon production was taken as the stabilization tower top pressure P. n .

[0033] In this embodiment, after obtaining N sets of production process data (T) n P n After that, in each set of production process data (T) n P n Under the condition of ), run the crude oil stability simulation model respectively and calculate the corresponding fuel consumption F. n And combined with the highest light hydrocarbon production Q n Obtain N sets of data (T) n P n Q n F n ), where (Q n F n () represents production and energy consumption data.

[0034] In this embodiment, by executing steps S300 and S400, the revenue value A corresponding to each set of production energy consumption data is calculated. n The set of production process data (T) corresponding to the maximum profit value n P n () serves as the optimal furnace outlet temperature and the optimal stabilizer tower top pressure.

[0035] The parameter optimization method for the positive pressure heating crude oil stabilization system in this embodiment simulates the positive pressure heating crude oil stabilization process under different heater outlet temperatures and different stabilizer tower top pressures using a crude oil stabilization simulation model. This method can optimize the parameters of the heater outlet temperature and stabilizer tower top pressure. Combined with the analysis of light hydrocarbon production and fuel consumption, it ensures maximum economic benefits while saving energy, protecting the environment, and reducing production costs. This provides a scientific and feasible parameter optimization scheme for the actual production and operation of the positive pressure heating crude oil stabilization system.

[0036] In one exemplary embodiment, P min ≤P n ≤P max ;T min ≤T1<T2<……<T N ≤T max ;

[0037] [P min P max ] and [T min T max These refer to the design pressure range and design temperature range of the positive pressure heating crude oil stabilization system, respectively.

[0038] In this embodiment, [P] min P max ] and [T min T max To implement the constraints in steps S100-S400, the optimization of the stabilizing tower top pressure and the heater outlet temperature is achieved under these constraints. The obtained optimization parameters (T) are... n P n This approach not only aligns with actual production practices and satisfies the stable production conditions of crude oil under positive pressure heating, but also maximizes economic benefits.

[0039] In one exemplary embodiment, step S200 involves "sequentially setting the furnace outlet temperature to different temperature values ​​T". n A positive pressure heating crude oil stabilization process simulation was conducted to obtain the results at various temperature values ​​T. n Achieving maximum light hydrocarbon production Q under these conditions n The corresponding stabilizer tower top pressure P n This may include steps S210-S230:

[0040] S210: Input the initial temperature value T1, temperature step t, initial pressure value P0, and pressure step p into the crude oil stability simulation model;

[0041] S220: The initial temperature value T1 is used as the furnace outlet temperature, and the furnace outlet temperature is gradually increased with the temperature step size t. At each temperature value T... n Perform step S230 under the following conditions:

[0042] S230: The initial pressure value P0 is used as the top pressure of the stabilizer module, and the top pressure is gradually increased with the pressure step size p to obtain the pressure at the temperature value T. n Under the conditions described, the highest light hydrocarbon production Q is achieved. n The corresponding pressure P at the top of the stabilizer tower n Where, P0 = P min .

[0043] In this embodiment, the furnace outlet temperature can be increased sequentially, and the temperature step t = (T max -T min ) / (N-1), set N T respectively n T1 = T min , T2=T1+t, T3=T1+2t, T4=T1+3t,……,T N =T1+(N-1)t=T max .

[0044] In one exemplary embodiment, step S230 may include steps S231-S232:

[0045] S231: Set the outlet temperature of the heating furnace to the temperature value T. n Keeping the pressure constant and setting the initial pressure value P0 at the top of the column, the pressure is gradually increased in increments p. At each pressure level, a simulation of the positive pressure heating crude oil stabilization process is performed to obtain the temperature value T. n The relationship between light hydrocarbon production and tower top pressure;

[0046] S232: Obtain the temperature value T from the relationship between the light hydrocarbon production and the top pressure of the tower. n The highest light hydrocarbon production Q is described below. n And the highest light hydrocarbon production Q n The corresponding pressure P at the top of the stabilizer tower n .

[0047] In this embodiment, the outlet temperature of the heating furnace is fixed at one of the T values. n Then, the pressure step size p can be set to (Pmax -P min ) / (M-1), set M tower top pressures respectively, and set the tower top pressures sequentially as P0 = P min ,P0+p,P0+2p,P0+3p,…,P0+(M-1)p=P max That is, at a temperature value T n Next, run the crude oil stability simulation model M times; complete steps S220-S230, a total of N*M times of crude oil stability simulation model running is required; for each temperature value T n The corresponding stabilizer tower top pressure P n For M pressure values ​​P min ,P0+p,P0+2p,P0+3p,…,P0+(M-1)p=P max One of the values.

[0048] In this embodiment, with a fixed furnace outlet temperature, the light hydrocarbon production will vary with changes in the tower top pressure, with the maximum light hydrocarbon production Q. n The corresponding pressure at the top of the tower is the pressure P at the top of the steady-state tower. n .

[0049] In one exemplary embodiment, step S200 involves obtaining the "fuel consumption F". n "This may include step S240:

[0050] S240: For each group T n and P n As production process data, the pressure at the top of the stabilizer module is set to P. n The outlet temperature of the heating furnace of the tower front heating furnace module is set to T. n The positive pressure heating crude oil stabilization process is simulated to obtain the fuel consumption F corresponding to the production process data. n .

[0051] In this embodiment, each group (T) n P n As production process data, production process conditions are set, namely, the heater outlet temperature and tower top pressure are set respectively. The crude oil stability simulation model is run to simulate the positive pressure heating crude oil stability process and obtain the fuel consumption F under these production process conditions. n Among them, fuel consumption F n At a minimum, this includes the fuel consumption required for heating by the pre-tower heater. When the crude oil stability simulation model also includes other modules that require fuel, the fuel consumption of these modules can also be included as F. n Part of it.

[0052] In one exemplary embodiment, step S300 may include step S310:

[0053] S310: According to formula A n =∑R j Q j -R g F n Calculate the revenue value A corresponding to each set of production and energy consumption data. n ;

[0054] In this embodiment, R j Q represents the unit price of the j-th type of light hydrocarbon, in yuan / ton; j Let Q be the yield of the j-th type of light hydrocarbon, in tons per day; j =Q n ;R g This is the unit price of fuel, expressed in yuan / m³. 3 ;F n The fuel consumption is expressed in m³. 3 / sky.

[0055] In this embodiment, the light hydrocarbons flowing out from the top of the stabilizing tower can be of various types, such as methane, ethane, propane, butane, etc. The yield and unit price of each light hydrocarbon are obtained, and then calculated according to the formula ∑R j Q j Calculate the light hydrocarbon gain, R g F n The fuel cost required for producing light hydrocarbons, according to formula A n =∑R j Q j -R g F n Production energy consumption data (Q) were obtained n F n The corresponding profit value A) n .

[0056] In this embodiment, after step S310 is executed, step S400 is executed, and max(A) is set to the maximum value. n ) is taken as the maximum profit value, and max(A) is used as the maximum profit value. n The corresponding set of T) n and P n As the optimal process data, max(A) n The corresponding T n As the optimal outlet temperature of the heating furnace, max(A) n P corresponding to ) n The optimal stabilizing pressure is the pressure at the top of the tower.

[0057] In one exemplary embodiment, the fuel consumption F n Calculated based on the following formula:

[0058]

[0059] In this embodiment, Q r This represents the calorific value of the fuel, expressed in MJ / m³. 3 c o This represents the specific heat capacity of oil, expressed in kJ / (kg·K); c w f represents the specific heat capacity of water, expressed in kJ / (kg·K); w The water content of the crude oil medium entering the preheating furnace module represents the water content of the crude oil medium, 0 < f. w <1; G represents the flow rate of crude oil medium entering the tower front heating furnace module, in tons / day; ΔT represents the temperature difference between the outlet and inlet of the tower front heating furnace module, in K (Kelvin); η represents the heating efficiency of the tower front heating furnace module, 0 < η < 1.

[0060] In one exemplary embodiment, step S110 may be included before step S200:

[0061] S110: Obtain the content data of each component of the crude oil to be stabilized, and generate the crude oil component parameters based on the content data.

[0062] In this implementation, the design pressure range and design temperature range of the positive pressure heating crude oil stabilization system can be different depending on the different components of the crude oil to be stabilized. Therefore, before simulating the positive pressure heating crude oil stabilization process, the components of the crude oil to be stabilized can be analyzed to obtain the content of each component in the crude oil to be stabilized. This provides a data basis for the design of the temperature constraint conditions and pressure constraint conditions of the crude oil stabilization simulation model, and also provides a data basis for the entire positive pressure heating crude oil stabilization process simulation.

[0063] In this embodiment, the components of the crude oil to be stabilized may include nitrogen, carbon dioxide, methane, ethane, propane, n-butane, isobutane, n-pentane, isopentane, hexane, heptane, etc.

[0064] In one exemplary embodiment, the crude oil stabilization simulation model is used to simulate the production process of the positive pressure heating crude oil stabilization system performing positive pressure heating flash evaporation on the crude oil to be stabilized to remove light hydrocarbons and generate stable crude oil.

[0065] To illustrate the parameter optimization method for the positive pressure heated crude oil stabilization system according to the embodiments of this application, a specific example is described in detail below, which includes steps S1-S7:

[0066] S1: Construct a crude oil stability simulation model for a positive pressure heating crude oil stabilization system;

[0067] S2: Obtain the content data of each component of the crude oil to be stabilized and generate crude oil component parameters;

[0068] S3: Input the crude oil component parameters into the crude oil stability simulation model, and set the furnace outlet temperature of the crude oil stability simulation model to 180℃, 190℃, 200℃, and 210℃ respectively:

[0069] S3-1: Set the furnace outlet temperature to T1 = 180℃, and set the tower top pressure to 70KPa, 80KPa, 90KPa, 100KPa, 110KPa, 120KPa, 130KPa, 140KPa, and 150KPa respectively to simulate the positive pressure heating crude oil stabilization process. Figure 2 The graph showing the relationship between light hydrocarbon production and tower top pressure indicates that the highest light hydrocarbon production Q1 is 272.5 tons / day, and the corresponding tower top pressure P1 is 100 kPa.

[0070] S3-2: Set the furnace outlet temperature to T2 = 190℃, and set the tower top pressure to 70KPa, 80KPa, 90KPa, 100KPa, 110KPa, 120KPa, 130KPa, 140KPa, and 150KPa respectively to simulate the positive pressure heating crude oil stabilization process. Figure 3 The graph showing the relationship between light hydrocarbon production and tower top pressure indicates that the highest light hydrocarbon production Q2 is 293.8 tons / day, and the corresponding tower top pressure P2 is 100 kPa.

[0071] S3-3: Set the furnace outlet temperature to T3 = 200℃, and set the tower top pressure to 70KPa, 80KPa, 90KPa, 100KPa, 110KPa, 120KPa, 130KPa, 140KPa, and 150KPa respectively to simulate the positive pressure heating crude oil stabilization process. Figure 4 The graph showing the relationship between light hydrocarbon production and tower top pressure indicates that the highest light hydrocarbon production Q3 is 322 tons / day, and the corresponding stabilizer tower top pressure P3 is 100 kPa.

[0072] S3-4: Set the furnace outlet temperature to T4 = 210℃, and set the tower top pressure to 70KPa, 80KPa, 90KPa, 100KPa, 110KPa, 120KPa, 130KPa, 140KPa, and 150KPa respectively to simulate the positive pressure heating crude oil stabilization process. Figure 5 The graph showing the relationship between light hydrocarbon production and tower top pressure indicates that the highest light hydrocarbon production Q4 is 347.3 tons / day, and the corresponding stabilizer tower top pressure P4 is 100 kPa.

[0073] S4: Calculate fuel consumption F1, F2, F3, F4:

[0074] S4-1: Using (T1, P1) = (180℃, 100KPa) as the production process data, setting the tower top pressure to 100KPa and the heater outlet temperature to 180℃, the positive pressure heating crude oil stabilization process is simulated to obtain the fuel consumption F1.

[0075] S4-2: Using (T2, P2) = (190℃, 100KPa) as the production process data, setting the tower top pressure to 100KPa and the heater outlet temperature to 190℃, the positive pressure heating crude oil stabilization process is simulated to obtain the fuel consumption F2.

[0076] S4-3: Using (T3, P3) = (200℃, 100KPa) as the production process data, setting the tower top pressure to 100KPa and the heater outlet temperature to 200℃, the positive pressure heating crude oil stabilization process is simulated to obtain the fuel consumption F3.

[0077] S4-4: Using (T4, P4) = (210℃, 100KPa) as the production process data, setting the tower top pressure to 100KPa and the heater outlet temperature to 210℃, the positive pressure heating crude oil stabilization process is simulated to obtain the fuel consumption F4.

[0078] S5: Calculate the profit values ​​A1, A2, A3, and A4:

[0079] A1=∑R j Q j -R g F1, ∑Q j =Q1; A2 = ∑R j Q j -R g F2, ∑Q j =Q2;

[0080] A3=∑R j Q j -R g F3, ∑Q j =Q3; A4 =∑R j Q j -R g F4, ∑Q j =Q4;

[0081] S6: Find the T value corresponding to the maximum value among A1, A2, A3, and A4. n and P n These are respectively used as the optimal furnace outlet temperature and the optimal stabilizer tower top pressure.

[0082] This application also provides a parameter optimization device for a positive pressure heated crude oil stabilization system, including a memory and a processor, such as... Figure 6 As shown:

[0083] The memory is used to store the parameter optimization program for the positive pressure heating crude oil stabilization system;

[0084] The processor is used to read the parameter optimization program of the positive pressure heating crude oil stabilization system and perform the parameter optimization method of the positive pressure heating crude oil stabilization system as described in the above embodiments.

[0085] It will be understood by those skilled in the art that all or some of the steps, systems, or apparatuses disclosed above, and their functional modules / units, can be implemented as software, firmware, hardware, or suitable combinations thereof. In hardware implementations, the division between functional modules / units mentioned above does not necessarily correspond to the division of physical components; for example, a physical component may have multiple functions, or a function or step may be performed collaboratively by several physical components. Some or all components may be implemented as software executed by a processor, such as a digital signal processor or microprocessor, or as hardware, or as an integrated circuit, such as an application-specific integrated circuit (ASIC). Such software may be distributed on a computer-readable medium, which may include computer storage media (or non-transitory media) and communication media (or transient media). As is known to those skilled in the art, the term "computer storage medium" includes volatile and non-volatile, removable and non-removable media implemented in any method or technology for storing information (such as computer-readable instructions, data structures, program modules, or other data). Computer storage media include, but are not limited to, RAM, ROM, EEPROM, flash memory or other memory technologies, CD-ROM, digital versatile disc (DVD) or other optical disc storage, magnetic cartridges, magnetic tape, disk storage or other magnetic storage devices, or any other medium that can be used to store desired information and can be accessed by a computer. Furthermore, it is well known to those skilled in the art that communication media typically contain computer-readable instructions, data structures, program modules, or other data in modulated data signals such as carrier waves or other transmission mechanisms, and may include any information delivery medium.

Claims

1. A method for optimizing parameters of a positive pressure heated crude oil stabilization system, characterized in that, include: A crude oil stabilization simulation model of a positive pressure heating crude oil stabilization system is constructed, wherein the crude oil stabilization simulation model includes at least a stabilization tower module and a tower front heater module; The crude oil composition parameters are input into the crude oil stability simulation model, and the furnace outlet temperature is sequentially set to different temperature values ​​T. n A positive pressure heating crude oil stabilization process simulation was conducted to obtain the results at various temperature values ​​T. n Achieving maximum light hydrocarbon production Q under these conditions n The corresponding stabilizer tower top pressure P n and fuel consumption F n , where n = 1, 2, ..., N; Calculate the corresponding revenue value A based on each set of production and energy consumption data. n Each set of production and energy consumption data includes the highest light hydrocarbon production Q. n and the fuel consumption F n ; In N of the aforementioned revenue values ​​A n Obtain the maximum profit value, and set the T corresponding to the maximum profit value. n and P n These are respectively used as the optimal furnace outlet temperature and the optimal stabilizer tower top pressure.

2. The method for optimizing parameters of a positive pressure heated crude oil stabilization system as described in claim 1, characterized in that: P min ≤P n ≤P max ;T min ≤T1﹤T2﹤……﹤T N ≤T max ; [P min P max ] and [T min T max These refer to the design pressure range and design temperature range of the positive pressure heating crude oil stabilization system, respectively.

3. The parameter optimization method for a positive pressure heating crude oil stabilization system as described in claim 2, characterized in that, The heating furnace outlet temperature is sequentially set to different temperature values ​​T. n A positive pressure heating crude oil stabilization process simulation was conducted to obtain the results at various temperature values ​​T. n Achieving maximum light hydrocarbon production Q under these conditions n The corresponding stabilizer tower top pressure P n ,include: Input the initial temperature value T1, temperature step t, initial pressure value P0, and pressure step p into the crude oil stability simulation model; The initial temperature value T1 is taken as the outlet temperature of the heating furnace, and the outlet temperature of the heating furnace is gradually increased with the temperature step t. At each temperature value T... n Perform the following operations under the following conditions: The initial pressure value P0 is used as the top pressure of the stabilizer module, and the top pressure is gradually increased with the pressure step size p to obtain the pressure at the temperature value T. n Under the conditions described, the highest light hydrocarbon production Q is achieved. n The corresponding pressure P at the top of the stabilizer tower n Where, P0 = P min .

4. The parameter optimization method for a positive pressure heating crude oil stabilization system as described in claim 3, characterized in that, The initial pressure value P0 is used as the top pressure of the stabilizer module, and the top pressure is gradually increased with the pressure step size p to obtain the pressure at the temperature value T. n Under the conditions described, the highest light hydrocarbon production Q is achieved. n The corresponding pressure P at the top of the stabilizer tower n ,include: The outlet temperature of the heating furnace is set to this temperature value T. n Keeping the pressure constant and setting the initial pressure value P0 at the top of the column, the pressure is gradually increased in increments p. At each pressure level, a simulation of the positive pressure heating crude oil stabilization process is performed to obtain the temperature value T. n The relationship between light hydrocarbon production and tower top pressure; The temperature value T is obtained from the relationship between the light hydrocarbon production and the top pressure of the column. n The highest light hydrocarbon production Q is described below. n And the highest light hydrocarbon production Q n The corresponding pressure P at the top of the stabilizer tower n .

5. The parameter optimization method for a positive pressure heating crude oil stabilization system as described in claim 1, characterized in that, Obtain the fuel consumption F n ,include: Each group of T n and P n As production process data, the pressure at the top of the stabilizer module is set to P. n The outlet temperature of the heating furnace of the tower front heating furnace module is set to T. n The positive pressure heating crude oil stabilization process is simulated to obtain the fuel consumption F corresponding to the production process data. n .

6. The parameter optimization method for a positive pressure heating crude oil stabilization system as described in claim 1, characterized in that, The corresponding revenue value A is calculated based on each set of production and energy consumption data. n ,include: According to formula A n =∑R j Q j -R g F n Calculate the revenue value A corresponding to each set of production and energy consumption data. n ; Among them, R j Let Q be the unit price of the j-th light hydrocarbon; j Let Q be the yield of the j-th light hydrocarbon; j =Q n ;R g F is the unit price of fuel; n This refers to the fuel consumption.

7. The method for optimizing parameters of a positive pressure heating crude oil stabilization system as described in claim 1, characterized in that: The fuel consumption F n Calculated based on the following formula: Among them, Q r Represents the calorific value of the fuel; c o Represents the specific heat capacity of oil; c w f represents the specific heat capacity of water; w ΔT represents the water content of the crude oil medium entering the tower preheater module; G represents the flow rate of the crude oil medium entering the tower preheater module; ΔT represents the temperature difference between the outlet and inlet of the tower preheater module; and η represents the heating efficiency of the tower preheater module.

8. The method for optimizing parameters of a positive pressure heating crude oil stabilization system as described in claim 1, characterized in that, Before inputting the crude oil component parameters into the crude oil stability simulation model, the following steps are included: Obtain the content data of each component of the crude oil to be stabilized, and generate the crude oil component parameters based on the content data.

9. The parameter optimization method for a positive pressure heating crude oil stabilization system as described in claim 9, characterized in that: The crude oil stabilization simulation model is used to simulate the production process of the positive pressure heating crude oil stabilization system performing positive pressure heating flash evaporation on the crude oil to be stabilized to remove light hydrocarbons and generate stable crude oil.

10. A parameter optimization device for a positive pressure heated crude oil stabilization system, comprising a memory and a processor, characterized in that: The memory is used to store the parameter optimization program for the positive pressure heating crude oil stabilization system; The processor is used to read the parameter optimization program of the positive pressure heating crude oil stabilization system and perform the parameter optimization method of the positive pressure heating crude oil stabilization system as described in any one of claims 1-9.

Images