Gas enrichment pretreatment method, device, equipment and medium based on membrane separation device

Abstract

This application discloses a method, apparatus, equipment, and medium for rich gas pretreatment based on a membrane separation device, belonging to the field of component separation technology. The method comprises: obtaining first operating parameters after simulating the operation of the rich gas treatment device; obtaining initial membrane separation parameters of the membrane separation device; inputting the initial membrane separation parameters into a preset membrane separation model for iterative optimization; during each iteration, decomposing the mass transfer differential domain into multiple micro-units; solving each micro-unit successively to obtain the first gas phase composition output by the membrane separation device; obtaining second operating parameters after simulating the operation of the rich gas treatment device based on the first gas phase composition; adjusting the initial membrane separation parameters based on the difference between the first and second operating parameters to obtain the final membrane separation parameters; and performing component separation of the rich gas through a stable absorption system based on the final membrane separation parameters. This application can improve the accuracy of rich gas component separation, thereby improving the stable absorption and utilization rate of rich gas.

Description

Technical Field

[0001] This application relates to the field of component separation technology, and in particular to a rich gas pretreatment method, apparatus, equipment and medium based on a membrane separation device. Background Technology

[0002] In oil refining and chemical production processes, rich gas, as a by-product resource containing various valuable components such as hydrogen and light hydrocarbons, is crucial to the economic benefits of enterprises through efficient recovery and comprehensive utilization. However, with the expansion of processing scale and the increasing requirements for energy conservation and consumption reduction, directly feeding rich gas with complex components into traditional absorption stabilization systems can lead to excessively high operating loads and a surge in energy consumption in downstream towers. Therefore, it is necessary to pre-separate the components in the rich gas using membrane separation devices.

[0003] Existing pretreatment process design and simulation methods often fail to achieve deep coupling optimization between membrane separation parameters and downstream process performance. Traditional simulation methods typically treat the membrane separation process as a simple macroscopic distribution ratio, or isolate the membrane unit from the downstream absorption stabilization process during design. This approach struggles to accurately characterize the component variation patterns within the microscopic mass transfer differential domain of membrane separation, and cannot capture in real-time the dynamic impact of component fluctuations on the operating parameters of subsequent series towers. This results in a lack of accurate simulation basis for feedback regulation, thereby reducing the overall rich gas recovery efficiency. Summary of the Invention

[0004] This application provides a rich gas pretreatment method, apparatus, equipment and medium based on a membrane separation device, which can solve the problem of low rich gas recovery and utilization efficiency caused by low accuracy of rich gas component separation in the prior art.

[0005] This application provides a gas enrichment pretreatment method based on a membrane separation device, applied to a stable absorption system. The stable absorption system includes a membrane separation device and a gas enrichment treatment device. The gas enrichment pretreatment method based on the membrane separation device includes: Obtain the first operating parameters after simulating the operation of the rich gas treatment device; The initial membrane separation parameters of the membrane separation device are obtained, and the initial membrane separation parameters are input into a preset membrane separation model. In each iteration optimization process, based on the initial membrane separation parameters, the mass transfer differential domain corresponding to the membrane separation model is decomposed into multiple micro-units, and each micro-unit is solved successively to obtain the first gas phase composition output by the membrane separation device. In each iteration of optimization, based on the first gas phase composition, the second operating parameters after simulating the operation of the rich gas treatment device are obtained, and the initial membrane separation parameters are adjusted according to the difference between the first operating parameters and the second operating parameters until the initial membrane separation parameters meet the preset process performance requirements, and the final membrane separation parameters of the membrane separation device are determined. The membrane separation device is initialized according to the final membrane separation parameters, and the rich gas acquired in real time is separated into components by the stable absorption system.

[0006] Compared with existing technologies, the above embodiments have the following beneficial effects: This application first simulates the operation of a rich gas treatment unit without introducing a membrane separation device to obtain baseline operating parameters and establish a comparable process reference system. Subsequently, in the process of optimizing membrane separation parameters, instead of simplifying the membrane separation process to a fixed distribution ratio, it performs microscopic discretization and unit-by-unit solution of the mass transfer differential domain based on the membrane separation model, thereby accurately obtaining the gas phase composition on the membrane permeate side. This gas phase composition is further used to drive the re-simulation of the downstream absorption stable process, so that the impact of the microscopic mass transfer behavior inside the membrane separation on the tower load, energy consumption, and operating status can be truly reflected. On this basis, by comparing the differences in operating parameters before and after the membrane separation is introduced, a feedback adjustment path for the membrane separation parameters is formed, enabling the design of the membrane separation unit and the downstream process performance objectives to achieve linked optimization, rather than isolated optimization. As a result, not only is the adaptability of the rich gas pretreatment stage to complex component changes improved, but the operating load of the downstream tower and system energy consumption can also be reduced at the source, significantly improving the overall recovery and utilization efficiency of rich gas.

[0007] Further, the membrane separation model includes: a component balance equation, a mass transfer equation, and a normalization equation; based on the initial membrane separation parameters, the mass transfer differential domain corresponding to the membrane separation model is decomposed into multiple micro-units, and each micro-unit is solved successively to obtain the first gas phase composition output by the membrane separation device, including: Along the gas-rich mass transfer direction within the membrane separation device, the mass transfer differential domain corresponding to the mass transfer equation is discretized into multiple interconnected micro-units. The micro-units are recursively calculated sequentially. For the current micro-unit, based on the second gas phase composition output by the previous micro-unit, the third gas phase composition output by the current micro-unit is calculated using the component balance equation and the normalization equation. The first gas phase composition is then obtained based on all the third gas phase groups.

[0008] Compared to existing technologies, the above embodiments have the following advantages: By simultaneously introducing component balance equations, mass transfer equations, and normalization equations into the membrane separation model, and discretizing the mass transfer differential domain corresponding to the membrane separation process into multiple continuously connected micro-units along the gas-rich mass transfer direction and solving them recursively, a refined characterization of the internal component evolution law of the membrane separation process is achieved. Compared to the existing technology that simplifies the membrane separation process to an overall segmentation ratio or single-point calculation, this application can truly reflect the segmented cumulative effect of each component due to transmembrane mass transfer during the axial position change of the gas-rich membrane module, thereby obtaining a more realistic gas phase composition of the membrane separation device output. Therefore, this provides a reliable, continuous, and physically consistent composition input basis for subsequent coupling simulation of the membrane separation results with the downstream absorption stabilization process, significantly improving the accuracy and reliability of the overall process simulation.

[0009] Furthermore, the third gas phase composition output by the current micro-unit is calculated based on the second gas phase composition output by the previous micro-unit, using the component balance equation and the normalization equation, including: Based on the initial membrane separation parameters and the second gas phase composition, the permeation flux of each gas-rich component within the current micro-unit is calculated using the mass transfer equation. Using the component balance equation, the corresponding permeation flux is subtracted from the first flow rate of each component received by the current micro-unit to obtain the second flow rate of each component output by the current micro-unit; Using the normalization equation, the second flow rates of each component are normalized to obtain the third gas phase composition.

[0010] Compared to existing technologies, the above embodiments offer the following advantages: permeate flux is calculated using the mass transfer equation, transmembrane loss is deducted using the component balance equation, and a new gas phase composition is obtained through a normalization equation. This stepwise calculation mechanism ensures that the material conservation relationships and mole fraction constraints of each component are simultaneously satisfied during membrane separation, avoiding compositional distortion caused by estimations based solely on experience or proportions. Consequently, the gas phase composition output by each micro-unit has clear physical meaning and traceability, giving the membrane separation model good numerical stability and scalability, and providing a stable and reliable basic calculation unit for subsequent membrane separation parameter optimization.

[0011] Further, the initial membrane separation parameters include: membrane module pressure; the calculation of the permeate flux of each gas-rich component in the current micro-unit using the mass transfer equation based on the initial membrane separation parameters and the second gas phase composition includes: Based on the membrane module pressure, determine the pressure gradient across the inner membrane of the current micro-unit; Based on the pressure gradient and the mole fraction of each component in the second gas phase composition, calculate the transmembrane partial pressure difference of each component within the current micro-unit; Obtain the component permeability coefficient of each component, and obtain the permeation flux of the corresponding component based on the transmembrane partial pressure difference and the component permeability coefficient.

[0012] Compared to existing technologies, the above embodiments offer the following advantages: By explicitly incorporating membrane module pressure as a membrane separation parameter into the permeate flux calculation process, the driving force for transmembrane mass transfer of each component can be quantitatively characterized. Compared to simplified models that do not distinguish pressure factors or only use average pressure difference, this approach can accurately reflect the differentiated impact of operating pressure changes on the permeate behavior of different components, thereby improving the adaptability of the membrane separation model to actual operating conditions. This not only enhances the adjustability of membrane separation parameters (especially operating pressure) in the model but also provides a clear physical adjustment path for subsequent synergistic optimization of energy efficiency and separation performance at the system level.

[0013] Further, adjusting the initial membrane separation parameters based on the difference between the first operating parameter and the second operating parameter includes: Based on the first operating parameters and the second operating parameters, the difference in system energy efficiency before and after the membrane separation device is connected is calculated, and the objective function value characterizing the process performance is obtained by combining the preset membrane module cost parameters. If the objective function value does not reach the preset optimal value range, the initial membrane separation parameters are readjusted, and the adjusted initial membrane separation parameters are returned to the membrane separation model for the next iteration.

[0014] Compared with existing technologies, the above embodiments have the following beneficial effects: By introducing an objective function with system energy efficiency differences, equipment load changes, and membrane module costs as comprehensive constraints, a quantitative feedback adjustment mechanism for membrane separation parameters is constructed. This application overcomes the limitations of existing technologies that adjust membrane parameters only for a single separation index or empirical rules, transforming the optimization objective of membrane separation parameters from local separation optimization to overall process performance optimization. By quantitatively evaluating the differences in operating parameters before and after membrane separation and participating in iterative optimization, this method can avoid over-design of membrane separation devices or energy transfer problems while ensuring the stable operation of the downstream absorption system, thereby improving the economy and feasibility of the rich gas pretreatment process at the system level.

[0015] Further, the step of obtaining the second operating parameters based on the first gas phase composition after simulating the operation of the rich gas treatment device includes: Obtain the design parameters for a stable absorption process; wherein, the design parameters include: equipment operating conditions and first rich gas feed data; The first rich gas feed data is updated based on the first gas phase composition to obtain the second rich gas feed data; A series simulation process for component separation is established based on the second rich gas feed data and the equipment operating conditions; The series simulation process is converged and solved using a preset chemical simulation engine to obtain the second operating parameters when the dry gas output from the rich gas treatment device reaches the preset dry gas purity.

[0016] Compared to existing technologies, the above embodiments offer the following advantages: By directly using the first gas phase composition output from the membrane separation unit as the updated feed condition for the downstream absorption stabilization process, and utilizing a chemical engineering simulation engine to convergently solve the series process including the absorption tower, reabsorption tower, stripping tower, and stabilization tower, a true mapping of the membrane separation pretreatment effect to the downstream process operating parameters is achieved. This approach overcomes the problem in existing technologies that cannot accurately reflect the impact of changes in feed composition caused by membrane separation on tower load, separation efficiency, and energy consumption, enabling the second operating parameter to truly reflect the overall operating conditions after membrane separation intervention. Therefore, it provides a highly reliable simulation basis for feedback optimization based on differences in operating parameters, significantly enhancing the accuracy of membrane separation parameter optimization.

[0017] Another embodiment of this application provides a gas enrichment pretreatment device based on a membrane separation device, applied to a stable absorption system. The stable absorption system includes a membrane separation device and a gas enrichment treatment device. The gas enrichment pretreatment device based on the membrane separation device includes a simulation module, a first iteration module, a second iteration module, and a pretreatment module. The simulation module is used to acquire the first operating parameters after simulating the operation of the rich gas treatment device; The first iteration module is used to obtain the initial membrane separation parameters of the membrane separation device, input the initial membrane separation parameters into a preset membrane separation model, and in each iteration optimization process, based on the initial membrane separation parameters, decompose the mass transfer differential domain corresponding to the membrane separation model into multiple micro-units, solve each micro-unit successively, and obtain the first gas phase composition output by the membrane separation device. The second iteration module is used to obtain the second operating parameters after simulating the operation of the rich gas treatment device based on the first gas phase composition during each iteration optimization process, and adjust the initial membrane separation parameters according to the difference between the first operating parameters and the second operating parameters until the initial membrane separation parameters meet the preset process performance requirements, and determine the final membrane separation parameters of the membrane separation device. The pretreatment module is used to initialize the membrane separation device according to the final membrane separation parameters, and to perform component separation on the real-time acquired rich gas through the stable absorption system.

[0018] Further, the membrane separation model includes: a component balance equation, a mass transfer equation, and a normalization equation; the first iteration module includes: a partitioning unit and a recursive unit; the first iteration module is used to decompose the mass transfer differential domain corresponding to the membrane separation model into multiple micro-units based on the initial membrane separation parameters, and to solve each of the micro-units successively to obtain the first gas phase composition output by the membrane separation device, including: The partitioning unit is used to discretize the mass transfer differential domain corresponding to the mass transfer equation into multiple interconnected micro-units along the gas-rich mass transfer direction in the membrane separation device. The recursive unit is used to perform recursive calculations on each of the micro-units in sequence. For the current micro-unit, based on the second gas phase composition output by the previous micro-unit, the third gas phase composition output by the current micro-unit is calculated using the component balance equation and the normalization equation, and the first gas phase composition is obtained based on all the third gas phase groups.

[0019] Another embodiment of this application also provides a terminal device, including: a processor, a memory, and a computer program stored in the memory and configured to be executed by the processor. When the processor executes the computer program, it implements the steps of the gas-rich pretreatment method based on the membrane separation device of this application.

[0020] Another embodiment of this application also provides a computer-readable storage medium item, including: a stored computer program, which, when the computer program is running, controls the device where the computer-readable storage medium is located to perform the steps of the gas-rich pretreatment method based on the membrane separation device of this application. Attached Figure Description

[0021] To more clearly illustrate the technical solution of this application, the drawings used in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of this application. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0022] Figure 1 This is a schematic flowchart of a gas-rich pretreatment method based on a membrane separation device provided in some embodiments of this application; Figure 2 This is another schematic diagram of a gas-rich pretreatment method based on a membrane separation device provided in some embodiments of this application; Figure 3 This is a schematic diagram of a gas-rich pretreatment principle provided in some embodiments of this application; Figure 4 This is a schematic diagram of the permeate side results of a multi-component membrane separation model provided in some embodiments of this application; Figure 5 This is a schematic diagram of the permeate side results of a multi-component membrane separation model provided in some embodiments of this application; Figure 6 This is a schematic diagram illustrating a comparison of yield results in one example provided in some embodiments of this application; Figure 7 This is a schematic diagram illustrating the comparison of annual total costs in one example provided in some embodiments of this application; Figure 8 This is a schematic diagram illustrating the comparison of annual investment costs in one example provided in some embodiments of this application; Figure 9 This is a schematic diagram showing the comparison of total operating costs for one example provided in some embodiments of this application; Figure 10 This is a schematic diagram of the structure of a gas-rich pretreatment device based on a membrane separation device provided in some embodiments of this application. Detailed Implementation

[0023] To make the objectives, technical solutions, and advantages of this application clearer, the technical solutions of this application will be clearly and completely described below with reference to the accompanying drawings of the embodiments. Obviously, the described embodiments are only some embodiments of this application, not all embodiments. Based on the embodiments of this application, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of this application.

[0024] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application pertains; the terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the application; the terms “comprising” and “having”, and any variations thereof, in the specification, claims, and foregoing description of the drawings are intended to cover non-exclusive inclusion.

[0025] In the description of the embodiments of this application, technical terms such as "first" and "second" are used only to distinguish different objects and should not be construed as indicating or implying relative importance or implicitly specifying the number, specific order, or primary and secondary relationship of the indicated technical features. In the description of the embodiments of this application, "multiple" means two or more, unless otherwise explicitly defined.

[0026] In this document, the term "embodiment" means that a particular feature, structure, or characteristic described in connection with an embodiment may be included in at least one embodiment of this application. The appearance of this phrase in various places throughout the specification does not necessarily refer to the same embodiment, nor is it a separate or alternative embodiment mutually exclusive with other embodiments. It will be explicitly and implicitly understood by those skilled in the art that the embodiments described herein can be combined with other embodiments.

[0027] In the description of the embodiments in this application, the term "and / or" is merely a description of the relationship between related objects, indicating that three relationships can exist. For example, A and / or B can represent: A existing alone, A and B existing simultaneously, and B existing alone. Additionally, the character " / " in this document generally indicates that the preceding and following related objects have an "or" relationship.

[0028] In the description of the embodiments of this application, the term "multiple" refers to two or more (including two), similarly, "multiple sets" refers to two or more (including two sets), and "multiple pieces" refers to two or more (including two pieces).

[0029] In the description of the embodiments of this application, unless otherwise expressly specified and limited, technical terms such as "installation," "connection," "joining," and "fixing" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components. For those skilled in the art, the specific meaning of the above terms in the embodiments of this application can be understood according to the specific circumstances.

[0030] Existing pretreatment process design and simulation methods often fail to achieve deep coupling optimization between membrane separation parameters and downstream process performance. Traditional simulation methods typically treat the membrane separation process as a simple macroscopic distribution ratio, or isolate the membrane unit from the downstream absorption stabilization process during design. This approach struggles to accurately characterize the component variation patterns within the microscopic mass transfer differential domain of membrane separation, and cannot capture in real-time the dynamic impact of component fluctuations on the operating parameters of subsequent series towers. This results in a lack of accurate simulation basis for feedback regulation, thereby reducing the overall rich gas recovery efficiency.

[0031] Please refer to Figure 1 To address the problem of low rich gas recovery efficiency due to low accuracy of rich gas component separation in existing technologies, this application provides a rich gas pretreatment method based on a membrane separation device, applied to a stable absorption system. The stable absorption system includes a membrane separation device and a rich gas treatment device. The rich gas pretreatment method based on the membrane separation device includes the following steps S101 to S104: S101: Obtain the first operating parameters after simulating the operation of the rich gas treatment device.

[0032] Preferably, in some embodiments of this application, reference is made to Figure 1 The process of obtaining the first operating parameters after simulating the operation of the rich gas treatment device includes the following steps S1011 to S1012: S1011: Feed collected from the refinery , , , and and the towers (Right now , , as well as )and (Right now , , as well as Design parameters such as ) are included. Represents the amount of material fed in, in units. ; Representative components ; Subscript Represents material input; Components in the feed material Molar composition, unit ; The permeability coefficients of each component are given in units of... ; For feed temperature, in units ; For feed pressure, unit ; , , as well as These are the number of trays in the absorption tower, reabsorption tower, stripping tower, and stabilizer tower, respectively. , , as well as The pressure of the absorption tower, reabsorption tower, stripping tower, and stabilizer tower, per unit. .

[0033] S1012: Based on the design parameters in step S1011, the traditional gasoline absorption stabilization process is simulated in the calculation software, and the following first operating parameters are calculated according to the design specifications and product purity requirements: , , (Right now and ), , and .in , as well as These are the flow rates of dry gas, liquefied petroleum gas (LPG), and stabilized gasoline, respectively, in units of... ; and These are the absorbent dosages for the absorption tower and the reabsorption tower, in units. ; For the load of the stripping tower reboiler, unit ; and To stabilize the condenser and reboiler loads of the tower, unit .

[0034] S102: Obtain the initial membrane separation parameters of the membrane separation device, input the initial membrane separation parameters into a preset membrane separation model, so that in each iteration optimization process, based on the initial membrane separation parameters, the mass transfer differential domain corresponding to the membrane separation model is decomposed into multiple micro-units, and each micro-unit is solved successively to obtain the first gas phase composition output by the membrane separation device.

[0035] Furthermore, in some embodiments of this application, the membrane separation model includes: a component balance equation, a mass transfer equation, and a normalization equation.

[0036] Preferably, in some embodiments of this application, the component balance equation includes: ; in, Indicates components Initial flow rate entering the membrane separation unit ; and Each represents a component Flow rates on the permeate and residual sides, per unit .

[0037] Preferably, in some embodiments of this application, the mass transfer equation includes: ; ; ; ; ; in, Represents membrane area, unit ; for right Find the partial derivative; For residual pressure, in units ; For osmotic pressure, unit ; Indicates the components on the osmotic side Molar composition, in % Indicates permeable side components Molar composition, in % for differential; It is a set of combinations.

[0038] Preferably, in some embodiments of this application, the normalization equation includes: ; .

[0039] Furthermore, in some embodiments of this application, the step of decomposing the mass transfer differential domain corresponding to the membrane separation model into multiple micro-units based on the initial membrane separation parameters, and solving each of the micro-units successively to obtain the first gas phase composition output by the membrane separation device includes: Along the gas-rich mass transfer direction within the membrane separation device, the mass transfer differential domain corresponding to the mass transfer equation is discretized into multiple interconnected micro-units. The micro-units are recursively calculated sequentially. For the current micro-unit, based on the second gas phase composition output by the previous micro-unit, the third gas phase composition output by the current micro-unit is calculated using the component balance equation and the normalization equation. The first gas phase composition is then obtained based on all the third gas phase groups.

[0040] It is important to note that the membrane separation model described above has excessively high solution complexity when solving the mass transfer equation, which is described by partial differential equations. Furthermore, when the research object is extended to multi-component systems, the solution complexity of this equation increases significantly, with the complexity of the solution process growing exponentially. Therefore, referring to... Figure 3 This application utilizes the finite element method to decompose the entire membrane separation module into... n Mass transfer occurs within each of the small micro-units. The entire differential domain is subdivided into numerous smaller intervals, transforming the differential problem into an iterative solution. Solving the mass transfer equation for each individual unit sequentially is relatively straightforward. The finer the differential domain is divided, the more closely the iterative solution matches the actual results. Summarizing the results from all units effectively reflects the entire membrane separation process.

[0041] This application achieves a refined characterization of the internal component evolution law of the membrane separation process by simultaneously introducing component balance equations, mass transfer equations, and normalization equations into the membrane separation model, and discretizing the mass transfer differential domain corresponding to the membrane separation process into multiple continuously connected micro-units along the gas-rich mass transfer direction and solving them recursively. Compared with the existing technology that simplifies the membrane separation process to a whole-scale segmentation or single-point calculation, this application can realistically reflect the segmented cumulative effect of each component due to transmembrane mass transfer during the axial position change of the gas-rich gas in the membrane module, thereby obtaining a more realistic gas phase composition of the membrane separation device output. This provides a reliable, continuous, and physically consistent composition input basis for subsequent coupling simulation of membrane separation results with downstream absorption stabilization processes, significantly improving the accuracy and reliability of the overall process simulation.

[0042] Furthermore, in some embodiments of this application, the calculation of the third gas phase composition output by the current micro-unit based on the second gas phase composition output by the previous micro-unit, using the component balance equation and the normalization equation, includes: Based on the initial membrane separation parameters and the second gas phase composition, the permeation flux of each gas-rich component within the current micro-unit is calculated using the mass transfer equation. Using the component balance equation, the corresponding permeation flux is subtracted from the first flow rate of each component received by the current micro-unit to obtain the second flow rate of each component output by the current micro-unit; Using the normalization equation, the second flow rates of each component are normalized to obtain the third gas phase composition.

[0043] Preferably, in some embodiments of this application, the calculation step of the second flow rate of each component output by the current micro-unit includes: ; ; in, and They represent the first n Unit components Flow rates on the permeate and residual sides, per unit ; and They represent the first Unit components Flow rates on the permeate and residual sides, per unit ; Indicates the first Components of a micro-unit The permeation flux.

[0044] This application calculates the permeate flux using the mass transfer equation, subtracts the transmembrane loss flow rate using the component balance equation, and obtains the new gas phase composition using a normalization equation. This stepwise calculation mechanism ensures that the material conservation relationships and mole fraction constraints of each component are simultaneously satisfied during membrane separation, avoiding composition distortion problems caused by estimations based solely on experience or proportions. Therefore, the gas phase composition output by each micro-unit has clear physical meaning and traceability, giving the membrane separation model good numerical stability and scalability, and providing a stable and reliable basic calculation unit for subsequent membrane separation parameter optimization.

[0045] Further, in some embodiments of this application, the initial membrane separation parameters include: membrane module pressure; the calculation of the permeate flux of each gas-rich component in the current micro-unit using the mass transfer equation based on the initial membrane separation parameters and the second gas phase composition includes: Based on the membrane module pressure, determine the pressure gradient across the inner membrane of the current micro-unit; Based on the pressure gradient and the mole fraction of each component in the second gas phase composition, calculate the transmembrane partial pressure difference of each component within the current micro-unit; Obtain the component permeability coefficient of each component, and obtain the permeation flux of the corresponding component based on the transmembrane partial pressure difference and the component permeability coefficient.

[0046] Preferably, in some embodiments of this application, the formula for calculating the permeation flux includes: ; ; ; in, Indicates the first n Components of a micro-unit The permeation flux, per unit ; and They represent the first and the Unit diastolic side components Molar composition, in % They represent the first and the Unit permeable side components Molar composition, in % This represents the membrane area of ​​each tiny unit, in units of... .

[0047] This application introduces membrane module pressure as a membrane separation parameter into the permeate flux calculation process, enabling a quantitative characterization of the driving force for transmembrane mass transfer of each component. Compared to simplified models that do not distinguish pressure factors or only use average pressure difference, this approach accurately reflects the differentiated impact of operating pressure changes on the permeate behavior of different components, thereby improving the adaptability of the membrane separation model to actual operating conditions. This not only enhances the adjustability of membrane separation parameters (especially operating pressure) in the model but also provides a clear physical adjustment path for subsequent synergistic optimization of energy efficiency and separation performance at the system level.

[0048] S103: In each iteration of optimization, based on the first gas phase composition, the second operating parameters after simulating the operation of the rich gas treatment device are obtained, and the initial membrane separation parameters are adjusted according to the difference between the first operating parameters and the second operating parameters until the initial membrane separation parameters meet the preset process performance requirements, and the final membrane separation parameters of the membrane separation device are determined.

[0049] Furthermore, in some embodiments of this application, obtaining the second operating parameters based on the first gas phase composition after simulating the operation of the rich gas treatment device includes: Obtain the design parameters for a stable absorption process; wherein, the design parameters include: equipment operating conditions and first rich gas feed data; The first rich gas feed data is updated based on the first gas phase composition to obtain the second rich gas feed data; A series simulation process for component separation is established based on the second rich gas feed data and the equipment operating conditions; The series simulation process is converged and solved using a preset chemical simulation engine to obtain the second operating parameters when the dry gas output from the rich gas treatment device reaches the preset dry gas purity.

[0050] Preferably, in some embodiments of this application, when obtaining the second operating parameters after simulating the operation of the rich gas treatment device based on the first gas phase composition, the data is still obtained by simulating the first operating parameters. However, unlike the first operating parameter acquisition process, the second operating parameter acquisition process uses the gas phase on the permeate side obtained by finally solving the membrane separation model as the initial feed to the rich gas treatment device, while the first operating parameter acquisition process uses the untreated rich gas directly as the initial feed to the rich gas treatment device.

[0051] Preferably, in some embodiments of this application, the step of using a preset chemical simulation engine to converge and solve the series simulation process to obtain the second operating parameters when the output dry gas of the rich gas treatment device reaches the preset dry gas purity includes: simulating the gasoline absorption stabilization process of the rich gas treatment device in the calculation software Aspen Plus, and similarly calculating the above process according to the design parameters. , , , , and .in, Indicates hydrogen flow rate, in units .

[0052] This application directly uses the first gas phase composition output from the membrane separation unit as the updated feed condition for the downstream absorption stabilization process. It then utilizes a chemical engineering simulation engine to convergently solve the series process involving the absorption tower, reabsorption tower, stripping tower, and stabilization tower, achieving a true mapping of the membrane separation pretreatment effect to the downstream process operating parameters. This approach overcomes the problem in existing technologies that cannot accurately reflect the impact of feed composition changes caused by membrane separation on tower load, separation efficiency, and energy consumption, enabling the second operating parameter to accurately reflect the overall operating conditions after membrane separation intervention. Therefore, it provides a highly reliable simulation basis for feedback optimization based on differences in operating parameters, significantly enhancing the accuracy of membrane separation parameter optimization.

[0053] Furthermore, in some embodiments of this application, adjusting the initial membrane separation parameters based on the difference between the first operating parameter and the second operating parameter includes: Based on the first operating parameters and the second operating parameters, the difference in system energy efficiency before and after the membrane separation device is connected is calculated, and the objective function value characterizing the process performance is obtained by combining the preset membrane module cost parameters. If the objective function value does not reach the preset optimal value range, the initial membrane separation parameters are readjusted, and the adjusted initial membrane separation parameters are returned to the membrane separation model for the next iteration.

[0054] Product flow based on two processes , and The production value of each process can be calculated. Since the membrane separation unit only affects the dry gas output, while the output of liquefied petroleum gas (LPG) and stabilized gasoline remains unchanged, the difference in production value between the two processes can be obtained by subtracting the value of dry gas from the value of dry gas from the uncoupled membrane separation unit's stable absorption process from the total value of dry gas and hydrogen produced in the stable absorption process. Furthermore, the introduction of membrane separation technology inevitably leads to an increase in the cost of the traditional process. Based on Aspen Plus simulation results, the operating and investment costs of each device in the process can be calculated and summarized into the total annual cost; the difference in the total annual cost between the two processes is used as the additional cost for modification. Combining these two cost factors, an objective function value can be obtained to determine the feasibility and potential of modifying the new hybrid process, and to quantify the process performance of the coupled membrane separation-absorption-stabilization process.

[0055] Preferably, in some embodiments of this application, the formula for calculating the objective function value is: ; in, The objective function value; The value corresponding to the amount of dry gas separated in the second operating parameter is the value corresponding to the total amount of dry gas obtained after coupling the membrane separation device. This represents the value corresponding to the amount of hydrogen separated in the second operating parameter; The value corresponding to the amount of dry gas separated in the first operating parameter is the value corresponding to the total amount of dry gas obtained without the membrane separation device. and This represents the total annual cost of a stable absorption process, both with and without a membrane separation unit.

[0056] Preferably, in some embodiments of this application, the step of readjusting the initial membrane separation parameters if the objective function value does not reach a preset optimal value range, and returning the adjusted initial membrane separation parameters to the membrane separation model for the next iteration, includes: calculating... ,like If the value is less than the preset threshold, it means that the membrane separation parameters set by the current membrane separation device are insufficient to improve the original absorption stabilization process. Then, return to step S102 to adjust the pressure and area of ​​the membrane module, and repeat steps S102 to S103 until the requirements are met.

[0057] This application constructs a quantitative feedback adjustment mechanism for membrane separation parameters by introducing an objective function that comprehensively constrains system energy efficiency differences, equipment load variations, and membrane module costs. This application overcomes the limitations of existing technologies that adjust membrane parameters only for a single separation index or empirical rules, shifting the optimization objective of membrane separation parameters from local separation optimization to overall process performance optimization. By quantitatively evaluating the differences in operating parameters before and after membrane separation integration and participating in iterative optimization, this method can avoid over-design of the membrane separation unit or energy transfer issues while ensuring the stable operation of the downstream absorption system, thereby improving the economy and feasibility of the rich gas pretreatment process at the system level.

[0058] S104: Initialize the membrane separation device according to the final membrane separation parameters, and perform component separation on the real-time acquired rich gas through the stable absorption system.

[0059] As can be seen from the above embodiments, the rich gas pretreatment method based on a membrane separation device provided in this application has the following advantages: This application targets rich gases (such as dry gas from oil refineries, coal chemical emission gas, associated gas from natural gas treatment, etc., which typically contain H2, CH4, and C2). + To address the pretreatment needs of multi-component gases (such as hydrocarbons and CO2), an innovative solution centered on membrane separation is proposed. Traditional rich gas treatment often employs a "full-volume delivery + downstream centralized separation" model, which not only ignores the early recovery value of hydrogen in the rich gas but also forces downstream units to bear the separation load of all components. This application utilizes a highly selective membrane to preferentially extract a stream of high-purity hydrogen, the value of which has the potential to offset the cost of process modification, forming a virtuous cycle of "technology investment - value output - cost compensation." Furthermore, after membrane separation pretreatment, the downstream processing volume is reduced from the "source," bringing multi-dimensional optimizations to downstream units (such as absorption towers, reabsorption towers, stripping towers, stabilization towers, compressors, heat exchangers, and flash tanks): reduced energy consumption, extended equipment life, and optimized separation efficiency. The efficient operation of the membrane separation unit relies on accurate prediction of the mass transfer behavior of multi-component gases within the membrane and optimized design of the component structure. This application breaks through the limitations of traditional "single-component mass transfer modeling" and proposes a multi-component membrane separation modeling method. It combines the finite element method to calculate the mass transfer equation, which can accurately predict the composition of the separated materials. This modeling method has strong universality.

[0060] To more clearly demonstrate the effect of the gas-rich pretreatment method based on a membrane separation device provided in the application embodiments, the following will provide further explanation of the effect with specific examples.

[0061] In this embodiment, the feed sample is a stream of superheated steam from a fluid catalytic cracking unit, which, after flash evaporation, yields rich gas and crude gasoline. To ensure precise separation, it is desirable to pre-treat the rich gas using a membrane separation unit to reduce the separation pressure on downstream units, while simultaneously extracting hydrogen to improve process performance. The feed information and design specifications for each tower are shown in the table below.

[0062] Table 1 below shows the material feeding information. Table 1 Feeding Information The membrane material selected in this application is the Matrimid 5218® fluorinated composite hollow fiber membrane. The permeability of each component in the enriched gas on the membrane is shown in Table 2. Since larger molecular pore sizes result in lower permeability, C3-C... 12 The permeability of the component can be replaced by the permeability of C2H6. Table 2. Permeability of each component Table 3 below shows the design parameters for the four-tower tower. Four-Tower Design Parameters The membrane separation model in this application is written in Python. To demonstrate the model's effectiveness, it has been validated in another multi-component membrane separation case (separation of H2, CO2, CH4, and C2H6), and the results are as follows. Figure 4 and Figure 5 As shown. By Figure 4 and Figure 5 As can be seen, the experimental data and the model's predictions are in good agreement, proving the effectiveness of the membrane separation modeling method in this application.

[0063] The gasoline absorption stabilization process of the coupled membrane separation unit was simulated and calculated using chemical process simulation software. Combined with the membrane separation pretreatment enrichment method proposed in this application, after several iterations, a membrane area of ​​22000 was selected. The transmembrane pressure is 25.5. At this point, the economic benefits of the hybrid process are maximized. To facilitate the explanation and presentation of the differences in results, the gasoline absorption stabilization process without membrane separation is referred to as Case 1, and the gasoline absorption stabilization process with membrane separation is referred to as Case 2. The four-tower simulation results for the two processes are shown in Table 4 below. Table 4 Comparison of Four-Tower Simulation Results for Case 1 and Case 2 Figures 6 to 9 The comparison results of product output, total annual cost (TAC), annual investment cost (TCC), and annual operating cost (TOC) for the two options are shown.

[0064] Depend on Figures 6 to 9 It can be seen that the yields of liquefied petroleum gas and stabilized gasoline obtained from both processes are highly consistent. Compared to Case 1, the yields of dry gas and rich absorbent oil are reduced in Case 2. This is because, by introducing a membrane separation unit to pretreat the rich gas, some hydrogen can be selectively extracted, thereby reducing the amount of gas to be processed in subsequent separation equipment. As shown in Table 4, the absorbent usage in the absorption tower and reabsorption tower in Case 2 is reduced by 48.7% and 65.9%, respectively, which significantly reduces the yield of rich absorbent oil and saves on the recovery cost of rich absorbent oil to some extent.

[0065] Meanwhile, according to the data in Table 4, the reboiler heat load of the stripping tower decreased by 16%; the condenser load of the stabilizer tower decreased by 6.4%, the reboiler load decreased by 26.7%, and the reflux ratio decreased from 1.52 to 1.4. These results are consistent with... Figure 8 and Figure 9 The data in Case 2 is consistent with that in Case 2, the total investment cost (TCC) and total operating cost (TOC) of the four separation towers are lower than those in Case 1.

[0066] However, Figure 9 The data shows that the total operating cost (TOC) in Case 2 was higher than that in Case 1, resulting in a 41.2% increase in the system's total annual cost (TAC). Combined with... Figure 8 and Figure 9 Analysis reveals that the compressor and membrane module are the main factors contributing to the differences in TAC (Total Hydrogen Acrylamide) levels. To ensure that the hydrogen separated by the membrane module achieves a purity of 97%, both the osmotic pressure and membrane area must meet specific design requirements. The osmotic pressure is achieved through a two-stage compression process, leading to an increase in the compressor's TCC (Total Cycle Control) and TOC (Total Hydrogen Consumption), which in turn affects the investment in cooling equipment. The increased membrane area requirement directly translates to higher investment costs for the membrane module.

[0067] Although the introduction of membrane separation technology in Case 2 increased the system's total annual cost, the process achieved the additional separation of high-purity hydrogen (≥97% purity, flow rate 3.48 t / h). This high-purity hydrogen has significant economic value and can offset part of the process modification costs. Comparative analysis shows that the net profit from dry gas in Case 2 is expected to increase by 7.9%. In conclusion, while combining traditional absorption stabilization processes with membrane separation technology leads to an increase in the system's total annual cost, it effectively reduces various costs associated with the separation tower and improves overall production profitability.

[0068] In summary, the rich gas pretreatment method based on a membrane separation device provided in this application has the following advantages compared to the prior art: Firstly, this application simulates the operation of a rich gas treatment device without introducing a membrane separation device to obtain baseline operating parameters and establish a comparable process reference system. Subsequently, in the process of optimizing membrane separation parameters, instead of simplifying the membrane separation process to a fixed distribution ratio, it performs microscopic discretization and unit-by-unit solution of the mass transfer differential domain based on the membrane separation model, thereby accurately obtaining the gas phase composition on the membrane permeate side. This gas phase composition is further used to drive the re-simulation of the downstream absorption stable process, enabling the impact of the microscopic mass transfer behavior inside the membrane separation on the tower load, energy consumption, and operating status to be truly reflected. Based on this, by comparing the differences in operating parameters before and after the membrane separation is introduced, a feedback adjustment path for the membrane separation parameters is formed, enabling the design of the membrane separation device and the downstream process performance objectives to achieve linked optimization, rather than isolated optimization. Therefore, it not only improves the adaptability of the rich gas pretreatment stage to complex component changes but also reduces the downstream tower operating load and system energy consumption at the source, significantly improving the overall recovery and utilization efficiency of rich gas.

[0069] like Figure 10 As shown, based on the above method embodiments, an embodiment of this application provides a gas enrichment pretreatment device based on a membrane separation device, applied to a stable absorption system. The stable absorption system includes a membrane separation device and a gas enrichment treatment device. The gas enrichment pretreatment device based on the membrane separation device includes a simulation module 201, a first iteration module 202, a second iteration module 203, and a pretreatment module 204. The simulation module 201 is used to acquire the first operating parameters after simulating the operation of the rich gas treatment device; The first iteration module 202 is used to obtain the initial membrane separation parameters of the membrane separation device, input the initial membrane separation parameters into a preset membrane separation model, and in each iteration optimization process, based on the initial membrane separation parameters, decompose the mass transfer differential domain corresponding to the membrane separation model into multiple micro-units, solve each micro-unit successively, and obtain the first gas phase composition output by the membrane separation device. The second iteration module 203 is used to obtain the second operating parameters after simulating the operation of the rich gas treatment device based on the first gas phase composition during each iteration optimization process, and adjust the initial membrane separation parameters according to the difference between the first operating parameters and the second operating parameters until the initial membrane separation parameters meet the preset process performance requirements, and determine the final membrane separation parameters of the membrane separation device. The pretreatment module 204 is used to initialize the membrane separation device according to the final membrane separation parameters, and to perform component separation on the real-time acquired rich gas through the stable absorption system.

[0070] In summary, the rich gas pretreatment device based on a membrane separation unit provided in this application has the following advantages compared to the prior art: Firstly, this application simulates the operation of the rich gas treatment device without introducing a membrane separation unit to obtain baseline operating parameters and establish a comparable process reference system. Subsequently, in the process of optimizing membrane separation parameters, instead of simplifying the membrane separation process to a fixed distribution ratio, it performs microscopic discretization and unit-by-unit solution of the mass transfer differential domain based on the membrane separation model, thereby accurately obtaining the gas phase composition on the membrane permeate side. This gas phase composition is further used to drive the re-simulation of the downstream absorption stable process, enabling the impact of the microscopic mass transfer behavior inside the membrane separation on the tower load, energy consumption, and operating status to be truly reflected. Based on this, by comparing the differences in operating parameters before and after the membrane separation is introduced, a feedback adjustment path for the membrane separation parameters is formed, enabling the design of the membrane separation unit and the downstream process performance objectives to achieve linked optimization, rather than isolated optimization. Therefore, it not only improves the adaptability of the rich gas pretreatment stage to complex component changes but also reduces the downstream tower operating load and system energy consumption at the source, significantly improving the overall recovery and utilization efficiency of rich gas.

[0071] Further, in some embodiments of this application, the membrane separation model includes: a component balance equation, a mass transfer equation, and a normalization equation; the first iteration module 202 includes: a partitioning unit and a recursive unit; the first iteration module 202 is used to decompose the mass transfer differential domain corresponding to the membrane separation model into multiple micro-units based on the initial membrane separation parameters, and to solve each of the micro-units successively to obtain the first gas phase composition output by the membrane separation device, including: The partitioning unit is used to discretize the mass transfer differential domain corresponding to the mass transfer equation into multiple interconnected micro-units along the gas-rich mass transfer direction in the membrane separation device. The recursive unit is used to perform recursive calculations on each of the micro-units in sequence. For the current micro-unit, based on the second gas phase composition output by the previous micro-unit, the third gas phase composition output by the current micro-unit is calculated using the component balance equation and the normalization equation, and the first gas phase composition is obtained based on all the third gas phase groups.

[0072] Furthermore, in some embodiments of this application, the recursive unit is used to calculate the third gas phase composition output by the current micro-unit based on the second gas phase composition output by the previous micro-unit, using the component balance equation and the normalization equation, including: Based on the initial membrane separation parameters and the second gas phase composition, the permeation flux of each gas-rich component within the current micro-unit is calculated using the mass transfer equation. Using the component balance equation, the corresponding permeation flux is subtracted from the first flow rate of each component received by the current micro-unit to obtain the second flow rate of each component output by the current micro-unit; Using the normalization equation, the second flow rates of each component are normalized to obtain the third gas phase composition.

[0073] Further, in some embodiments of this application, the initial membrane separation parameters include: membrane module pressure; the calculation of the permeate flux of each gas-rich component in the current micro-unit using the mass transfer equation based on the initial membrane separation parameters and the second gas phase composition includes: Based on the membrane module pressure, determine the pressure gradient across the inner membrane of the current micro-unit; Based on the pressure gradient and the mole fraction of each component in the second gas phase composition, calculate the transmembrane partial pressure difference of each component within the current micro-unit; Obtain the component permeability coefficient of each component, and obtain the permeation flux of the corresponding component based on the transmembrane partial pressure difference and the component permeability coefficient.

[0074] Further, in some embodiments of this application, the second iteration module 203 includes: a calculation unit and a parameter adjustment unit; the second iteration module 203 is used to adjust the initial membrane separation parameters based on the difference between the first operating parameters and the second operating parameters, including: The calculation unit is used to calculate the difference in system energy efficiency before and after the membrane separation device is connected based on the first operating parameters and the second operating parameters, and to obtain the objective function value characterizing the process performance by combining the preset membrane module cost parameters. The parameter adjustment unit is used to readjust the initial membrane separation parameters if the objective function value does not reach the preset optimal value range, and then return the adjusted initial membrane separation parameters to the membrane separation model for the next iteration solution.

[0075] Further, in some embodiments of this application, the second iteration module 203 includes: a parameter acquisition unit, a data update unit, a process simulation unit, and a solution unit; the second iteration module 203 is used to acquire second operating parameters after simulating the operation of the rich gas treatment device based on the first gas phase composition, including: The parameter acquisition unit is used to acquire the design parameters of the stable absorption process; wherein, the design parameters include: equipment operating conditions and first rich gas feed data; The data update unit is used to update the first rich gas feed data according to the first gas phase composition to obtain the second rich gas feed data. The process simulation unit is used to establish a series simulation process for component separation based on the second rich gas feed data and the equipment operating conditions. The solution unit is used to perform convergent solution on the series simulation process using a preset chemical simulation engine to obtain the second operating parameters when the dry gas output by the rich gas treatment device reaches the preset dry gas purity.

[0076] It is understood that the above-described device embodiments correspond to the method embodiments of this application, and can implement the gas-rich pretreatment method based on a membrane separation device provided by any of the above-described method embodiments of this application.

[0077] It should be noted that the device embodiments described above are merely illustrative, and some or all of the modules can be selected to achieve the purpose of this embodiment according to actual needs. Furthermore, in the accompanying drawings of the device embodiments provided in this application, the connection relationships between modules indicate that they have communication connections, which can specifically be implemented as one or more communication buses or signal lines. Those skilled in the art can understand and implement this without any creative effort.

[0078] Based on the above embodiments of the gas-rich pretreatment method based on a membrane separation device, another embodiment of this application provides a terminal device, which includes a processor, a memory, and a computer program stored in the memory and configured to be executed by the processor. When the processor executes the computer program, it implements the gas-rich pretreatment method based on a membrane separation device according to any embodiment of this application.

[0079] For example, in this embodiment, the computer program can be divided into one or more modules, which are stored in the memory and executed by the processor to complete this application. The one or more module units may be a series of computer program instruction segments capable of performing a specific function, which describe the execution process of the computer program in the terminal device.

[0080] The terminal device may be a desktop computer, laptop, handheld computer, or cloud server, etc. The terminal device may include, but is not limited to, a processor and a memory.

[0081] The processor can be a Central Processing Unit (CPU), or other general-purpose processors, digital signal processors (DSPs), application-specific integrated circuits (ASICs), field-programmable gate arrays (FPGAs), or other programmable logic devices, discrete gate or transistor logic devices, discrete hardware components, etc. A general-purpose processor can be a microprocessor or any conventional processor. The processor is the control center of the terminal device, connecting all parts of the terminal device via various interfaces and lines.

[0082] Based on the above-described method embodiments, another embodiment of this application provides a computer-readable storage medium including a stored computer program, wherein, when the computer program is executed, it controls the device where the computer-readable storage medium is located to perform the gas-rich pretreatment method based on a membrane separation device as described in any of the above-described method embodiments of this application.

[0083] The modules / units integrated in the device / terminal equipment, if implemented as software functional units and sold or used as independent products, can be stored in a computer-readable storage medium. Based on this understanding, all or part of the processes in the methods of the above embodiments can also be implemented by a computer program instructing related hardware. The computer program can be stored in a computer-readable storage medium, and when executed by a processor, it can implement the steps of the various method embodiments described above. The computer program includes computer program code, which can be in the form of source code, object code, executable files, or certain intermediate forms. The computer-readable medium can include: any entity or device capable of carrying the computer program code, recording media, USB flash drives, portable hard drives, magnetic disks, optical disks, computer memory, read-only memory (ROM), random access memory (RAM), electrical carrier signals, telecommunication signals, and software distribution media, etc.

Claims

1. A gas-rich pretreatment method based on a membrane separation device, characterized in that, Applied to a stable absorption system, the stable absorption system includes: a membrane separation unit and a gas enrichment unit, wherein the gas enrichment pretreatment method based on the membrane separation unit includes: Obtain the first operating parameters after simulating the operation of the rich gas treatment device; The initial membrane separation parameters of the membrane separation device are obtained, and the initial membrane separation parameters are input into a preset membrane separation model. In each iteration optimization process, based on the initial membrane separation parameters, the mass transfer differential domain corresponding to the membrane separation model is decomposed into multiple micro-units, and each micro-unit is solved successively to obtain the first gas phase composition output by the membrane separation device. In each iteration of optimization, based on the first gas phase composition, the second operating parameters after simulating the operation of the rich gas treatment device are obtained, and the initial membrane separation parameters are adjusted according to the difference between the first operating parameters and the second operating parameters until the initial membrane separation parameters meet the preset process performance requirements, and the final membrane separation parameters of the membrane separation device are determined. The membrane separation device is initialized according to the final membrane separation parameters, and the rich gas acquired in real time is separated into components by the stable absorption system.

2. The gas-rich pretreatment method based on a membrane separation device as described in claim 1, characterized in that, The membrane separation model includes: a component balance equation, a mass transfer equation, and a normalization equation; based on the initial membrane separation parameters, the mass transfer differential domain corresponding to the membrane separation model is decomposed into multiple micro-units, and each micro-unit is solved successively to obtain the first gas phase composition output by the membrane separation device, including: Along the gas-rich mass transfer direction within the membrane separation device, the mass transfer differential domain corresponding to the mass transfer equation is discretized into multiple interconnected micro-units. The micro-units are recursively calculated sequentially. For the current micro-unit, based on the second gas phase composition output by the previous micro-unit, the third gas phase composition output by the current micro-unit is calculated using the component balance equation and the normalization equation. The first gas phase composition is then obtained based on all the third gas phase groups.

3. The gas-rich pretreatment method based on a membrane separation device as described in claim 2, characterized in that, The third gas phase composition output by the current micro-unit is calculated based on the second gas phase composition output by the previous micro-unit using the component balance equation and the normalization equation, including: Based on the initial membrane separation parameters and the second gas phase composition, the permeation flux of each gas-rich component within the current micro-unit is calculated using the mass transfer equation. Using the component balance equation, the corresponding permeation flux is subtracted from the first flow rate of each component received by the current micro-unit to obtain the second flow rate of each component output by the current micro-unit; Using the normalization equation, the second flow rates of each component are normalized to obtain the third gas phase composition.

4. The gas-rich pretreatment method based on a membrane separation device as described in claim 3, characterized in that, The initial membrane separation parameters include: membrane module pressure; the calculation of the permeate flux of each gas-rich component in the current micro-unit using the mass transfer equation based on the initial membrane separation parameters and the second gas phase composition includes: Based on the membrane module pressure, determine the pressure gradient across the inner membrane of the current micro-unit; Based on the pressure gradient and the mole fraction of each component in the second gas phase composition, calculate the transmembrane partial pressure difference of each component within the current micro-unit; Obtain the component permeability coefficient of each component, and obtain the permeation flux of the corresponding component based on the transmembrane partial pressure difference and the component permeability coefficient.

5. The gas-rich pretreatment method based on a membrane separation device as described in claim 1, characterized in that, The step of adjusting the initial membrane separation parameters based on the difference between the first operating parameter and the second operating parameter includes: Based on the first operating parameters and the second operating parameters, the difference in system energy efficiency before and after the membrane separation device is connected is calculated, and combined with the preset membrane module cost parameters, the objective function value characterizing the process performance is obtained. If the objective function value does not reach the preset optimal value range, the initial membrane separation parameters are readjusted, and the adjusted initial membrane separation parameters are returned to the membrane separation model for the next iteration.

6. The gas-rich pretreatment method based on a membrane separation device as described in claim 1, characterized in that, The step of obtaining second operating parameters based on the first gas phase composition after simulating the operation of the rich gas treatment device includes: Obtain the design parameters for a stable absorption process; wherein, the design parameters include: equipment operating conditions and first rich gas feed data; The first rich gas feed data is updated based on the first gas phase composition to obtain the second rich gas feed data; A series simulation process for component separation is established based on the second rich gas feed data and the equipment operating conditions; The series simulation process is converged and solved using a preset chemical simulation engine to obtain the second operating parameters when the dry gas output from the rich gas treatment device reaches the preset dry gas purity.

7. A gas-rich pretreatment device based on a membrane separation unit, characterized in that, The method is applied to a stable absorption system, which includes a membrane separation device and a gas enrichment device. The gas enrichment pretreatment device based on the membrane separation device includes a simulation module, a first iteration module, a second iteration module, and a pretreatment module. The simulation module is used to acquire the first operating parameters after simulating the operation of the rich gas treatment device; The first iteration module is used to obtain the initial membrane separation parameters of the membrane separation device, input the initial membrane separation parameters into a preset membrane separation model, and in each iteration optimization process, based on the initial membrane separation parameters, decompose the mass transfer differential domain corresponding to the membrane separation model into multiple micro-units, solve each micro-unit successively, and obtain the first gas phase composition output by the membrane separation device. The second iteration module is used to obtain the second operating parameters after simulating the operation of the rich gas treatment device based on the first gas phase composition during each iteration optimization process, and adjust the initial membrane separation parameters according to the difference between the first operating parameters and the second operating parameters until the initial membrane separation parameters meet the preset process performance requirements, and determine the final membrane separation parameters of the membrane separation device. The pretreatment module is used to initialize the membrane separation device according to the final membrane separation parameters, and to perform component separation on the real-time acquired rich gas through the stable absorption system.

8. The gas-rich pretreatment device based on a membrane separation unit as described in claim 7, characterized in that, The membrane separation model includes: a component balance equation, a mass transfer equation, and a normalization equation; the first iteration module includes: a partitioning unit and a recursive unit; the first iteration module is used to decompose the mass transfer differential domain corresponding to the membrane separation model into multiple micro-units based on the initial membrane separation parameters, and to solve each of the micro-units successively to obtain the first gas phase composition output by the membrane separation device, including: The partitioning unit is used to discretize the mass transfer differential domain corresponding to the mass transfer equation into multiple interconnected micro-units along the gas-rich mass transfer direction in the membrane separation device. The recursive unit is used to perform recursive calculations on each of the micro-units in sequence. For the current micro-unit, based on the second gas phase composition output by the previous micro-unit, the third gas phase composition output by the current micro-unit is calculated using the component balance equation and the normalization equation, and the first gas phase composition is obtained based on all the third gas phase groups.

9. A terminal device, characterized in that, The device includes a processor, a memory, and a computer program stored in the memory and configured to be executed by the processor, wherein the processor, when executing the computer program, implements a gas-rich pretreatment method based on a membrane separation device as described in any one of claims 1 to 6.

10. A computer-readable storage medium, characterized in that, The computer-readable storage medium includes a stored computer program, wherein, when the computer program is executed, it controls the device containing the computer-readable storage medium to perform a gas-rich pretreatment method based on a membrane separation device as described in any one of claims 1 to 6.

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