Chemical industry park operation optimization method and system considering multi-production-line sequential coupling

Abstract

The invention belongs to the technical field of operation optimization control, and provides a chemical industry park operation optimization method and system considering multi-production-line sequential coupling. Acquiring equipment parameters of different equipment in the wind-light-hydrogen-ammonia-alcohol integrated comprehensive energy chemical industrial park, load requirements of the comprehensive energy chemical industrial park, and initial energy storage states and output power prediction information of the multi-element energy storage equipment; the method comprises the following steps: constructing models of an electrolytic cell, synthesis ammonia equipment and methanol synthesis equipment, and modeling a wind and light distributed power supply and multi-element energy storage equipment; a material flow sequential coupling relation among multiple chemical production lines is considered, an optimized operation model oriented to the wind-solar-hydrogen-ammonia-alcohol integrated comprehensive energy chemical industry park is constructed, and the lowest comprehensive operation cost is used as a target function; and solving the optimization operation model to obtain a scheduling scheme. According to the invention, the optimal day-ahead scheduling of the integrated energy chemical industry park can be realized.

Description

Technical Field

[0001] This invention belongs to the field of operation optimization and control technology, specifically relating to a method and system for operation optimization of chemical industrial parks that takes into account the sequential coupling of multiple production lines. Background Technology

[0002] The statements in this section are merely background information related to the present invention and do not necessarily constitute prior art.

[0003] Replacing fossil fuels with green electricity and green hydrogen to power heavy chemical systems, constructing integrated energy and chemical industrial parks combining wind, solar, hydrogen, ammonia, and methanol, integrating controllable units such as distributed power generation, energy storage, and complete sets of chemical production equipment, coordinating the flexible adjustment capabilities of each link, and realizing the transformation of the energy supply model for heavy chemical production are of great significance for promoting the green and efficient development of the industry, exploring new flexible resources, and improving the absorption capacity of new power systems with high penetration rates of wind and solar energy.

[0004] However, due to the significant volatility and randomness of wind and solar renewable energy, the long-term steady-state operation mode of traditional chemical processes will be disrupted. The autonomous operation of integrated energy and chemical industrial parks faces a severe power balance problem, and the safety of chemical production cannot be effectively guaranteed, posing a huge threat to personal and property losses.

[0005] Meanwhile, heavy chemical production typically consists of multiple inseparable production stages, accompanied by continuous material-energy conversion processes. The heterogeneous flow of electrical / thermal energy and the multi-material flow of hydrogen / ammonia / alcohol / ester have complex spatiotemporal cross-coupling relationships, which will further increase the difficulty for heavy chemical systems to participate in power balance scheduling.

[0006] Currently, the operation optimization methods for integrated energy and chemical industrial parks with sequentially coupled multi-chemical production lines, including wind, solar, hydrogen, ammonia, and alcohol, have the following problems: On the one hand, the existing modeling methods for power systems and chemical systems are very different. If only the power system perspective is used to build a scheduling optimization model, usually only a binary function relationship between the input of raw materials or the output of products in the heavy chemical system and its power consumption is constructed, thereby achieving a simple coupling between the power system and the chemical system. However, this ignores the strong coupling relationship between the chemical reaction principle and the heterogeneous energy flow of electricity / heat and the multi-material flow of hydrogen / ammonia / alcohol in the chemical production process.

[0007] On the other hand, most existing scheduling methods only use products such as hydrogen as energy storage carriers to realize energy transfer between different time periods in integrated energy and chemical industrial parks, ignoring their role as raw materials or products in realizing the time-series coupling and connection of heterogeneous energy flow and multi-material flow across processes and sections of various types of chemical production lines. In other words, the energy-material supply and demand situation will directly affect the capacity of heavy chemical system and will seriously affect the enthusiasm of chemical system to participate in the power balance scheduling of power system. Summary of the Invention

[0008] To address the aforementioned problems, this invention proposes a method and system for optimizing the operation of chemical industrial parks that considers the sequential coupling of multiple production lines. This invention can achieve optimal day-ahead scheduling for integrated energy and chemical industrial parks.

[0009] According to some embodiments, the present invention adopts the following technical solution: A method for optimizing the operation of a chemical industrial park that takes into account the sequential coupling of multiple production lines includes the following steps: Obtain the equipment parameters of different equipment in the integrated energy and chemical industrial park combining wind, solar, hydrogen, ammonia, and methanol; Obtain the load demand of the integrated energy and chemical industrial park, including electricity load, heat load, and demand for ammonia and methanol; obtain the initial energy storage status of multi-energy storage equipment including electric energy storage, thermal energy storage, and hydrogen energy storage; obtain the power output forecast information of photovoltaic and wind turbine units in the integrated energy and chemical industrial park within the total scheduling cycle; The production processes of different green energy chemical production lines are analyzed, the constraints corresponding to the production processes are determined, and models of electrolyzers, ammonia synthesis equipment and methanol synthesis equipment are constructed by combining the obtained equipment parameters and prediction information. Models of wind and solar distributed power sources and multi-element energy storage equipment are also constructed. Based on the models of different equipment, and taking into account the sequential coupling relationship of material flow between multiple chemical production lines, an optimized operation model for the integrated energy and chemical industrial park of wind, solar, hydrogen, ammonia and methanol is constructed. The optimized operation model takes the lowest comprehensive operating cost as the objective function. Based on the optimized operation model of the integrated energy and chemical industrial park, and under the constraints corresponding to the production process and the scheduling constraints of the integrated energy and chemical industrial park, the optimized operation model is solved to obtain the scheduling scheme.

[0010] As an alternative implementation method, the process of obtaining equipment parameters for different equipment in an integrated energy and chemical industrial park combining wind, solar, hydrogen, ammonia, and methanol includes: For electrolyzers, obtain the electrolyzer hydrogen production efficiency, electrolyzer water consumption efficiency, electrolyzer power upper and lower limits, and hydrogen low-grade heat energy. For ammonia synthesis equipment, the molar mass of air is obtained. 、 Gas constant, air inlet temperature of air separator, air inlet pressure of air separator compressor, air outlet pressure of air separator compressor, mechanical efficiency of air separator compressor, fixed power of ammonia synthesis reactor, power consumed per unit molar flow rate of ammonia produced, upper and lower limits of power of ammonia synthesis equipment, heat release rate of ammonia synthesis equipment and heat release per unit mass of ammonia produced. For methanol synthesis equipment, obtain the methanol synthesis efficiency, the heat of reaction released per unit mass of methanol synthesized, and the upper and lower limits of the electrical power of the methanol synthesis equipment. For energy storage, obtain the energy storage capacity, energy storage self-discharge rate, energy storage maximum charging power, energy storage maximum discharging power, energy storage charging efficiency, energy storage discharging efficiency, and energy storage charging state upper and lower limits. For hydrogen storage tanks, obtain the tank capacity, filling and discharging efficiency, inlet temperature, and inlet pressure of the compressor. 、 The outlet gas pressure of the hydrogen storage tank compressor, the mechanical efficiency of the hydrogen storage tank, the maximum mass flow rate of the hydrogen storage tank inlet and outlet, the upper and lower limits of the hydrogen storage tank filling state, and the molar mass of hydrogen. For thermal energy storage, obtain the thermal energy storage capacity, self-heating rate, maximum thermal storage power, maximum heat release power, thermal storage efficiency, heat release efficiency, and upper and lower limits of thermal storage state. ； For wind and solar new energy power generation equipment, obtain the installed capacity of photovoltaic and wind turbine units. ； For electric heating equipment, obtain the heat generation efficiency and upper and lower limits of the power consumption of the electric heating equipment.

[0011] As an alternative implementation method, the process of constructing models of electrolyzers, ammonia synthesis equipment, and methanol synthesis equipment includes: setting electrolyzer operation constraints based on the chemical reaction equation for hydrogen production from water electrolysis, including constraints on electrolyzer power consumption-gas production, electrolyzer water consumption, electrolyzer input power, and electrolyzer input power ramp-up, thereby realizing the construction of the electrolyzer model; A model was created for the green electricity ammonia synthesis equipment. Based on the chemical reaction equation for ammonia synthesis, operational constraints were set for the ammonia synthesis equipment, including power constraints for the air separation unit, material balance constraints for the methanol synthesis equipment, power constraints for the ammonia synthesis reactor, input power ramp-up constraints for the ammonia synthesis equipment, and constraints on the input power and heating power of the ammonia synthesis equipment. Based on the chemical reaction equation for ammonia synthesis, operational constraints for the methanol synthesis equipment are set, including constraints on gas consumption, material balance, heat generation, input power, and input power ramp-up. This completes the construction of the methanol synthesis equipment model.

[0012] As an optional implementation method, the process of modeling multi-element energy storage equipment includes: modeling the energy storage, setting operational constraints for the energy storage, including energy balance constraints, state of charge (SOC) constraints, periodic state regression constraints, upper and lower limits of SOC constraints, charging and discharging power constraints, and mutual exclusion constraints between charging and discharging states. Under the periodic state regression constraint, the energy storage state of charge is determined every [period]. T Go back once to complete the construction of the energy storage model; Model the hydrogen storage tank and set the operating constraints of the hydrogen storage tank, including the energy balance constraint of the hydrogen storage tank, the power consumption constraint of the hydrogen storage tank compressor, the periodic state regression constraint, the upper and lower limits constraint of the hydrogen storage tank filling state, and the constraint of the gas volume of the hydrogen storage tank entering and leaving the hydrogen storage tank, and complete the construction of the hydrogen storage tank model. A model for thermal energy storage is constructed, and operational constraints are set, including energy balance constraints, state constraints, periodic state regression constraints, upper and lower limits of the state of charge (SOC) of thermal energy storage, and constraints on the charge and discharge heat power and mutual exclusion constraints of the charge and discharge states of thermal energy storage.

[0013] As an alternative implementation method, the process of modeling wind and solar distributed power sources includes setting output constraints and curtailment constraints for wind and solar distributed power sources, and setting operational constraints for electric heating equipment, including heat generation power constraints, output power constraints, and maximum number of start-stop cycles within the scheduling period.

[0014] As an alternative implementation method, the process that takes into account the sequential coupling relationship of material flow between multiple chemical production lines includes: setting the actual production / energy consumption power of electrolyzers, ammonia synthesis equipment, methanol synthesis equipment, wind and solar distributed power sources, and multi-energy storage equipment as decision variables; setting the operating costs of each piece of equipment; setting the penalty costs for curtailing wind, solar, and load; setting the cost of purchasing electricity from the external grid and the cost of purchasing raw materials for chemical production; and setting the carbon emission costs caused by purchasing electricity from the external grid. Considering the sequential coupling of products and raw materials among multiple production lines in the integrated energy and chemical industrial park, a material flow balance constraint is set between the upstream and downstream hydrogen ammonia production lines and hydrogen storage tanks, and a hydrogen ammonia production constraint is also set.

[0015] As an alternative implementation method, the constraints corresponding to the production process include: power balance constraints, heat balance constraints, material flow balance constraints between sequential multi-chemical production lines, and output constraints.

[0016] A chemical industrial park operation optimization system considering the sequential coupling of multiple production lines includes: The integrated energy and chemical industrial park parameter acquisition module is used to acquire equipment parameters of different equipment in the integrated wind, solar, hydrogen, ammonia, and methanol integrated energy and chemical industrial park. The demand and forecast parameter acquisition module is used to acquire the load demand of the integrated energy and chemical industrial park, including the power load, heat load, and the demand for ammonia and methanol; acquire the initial energy storage status of multi-energy storage equipment including electric energy storage, thermal energy storage and hydrogen energy storage; and acquire the output power forecast information of photovoltaic and wind turbine units in the integrated energy and chemical industrial park within the total scheduling cycle. The integrated energy and chemical industrial park modeling module is used to analyze the production processes of different green energy chemical production lines, determine the constraints corresponding to the production processes, and, in combination with the acquired equipment parameters and prediction information, construct models of electrolyzers, synthetic ammonia equipment, and methanol synthesis equipment, and model wind and solar distributed power sources and multi-element energy storage equipment. An optimized operation model construction module is used to construct an optimized operation model for an integrated energy and chemical industrial park that combines wind, solar, hydrogen, ammonia, and methanol production, based on the models of different equipment and taking into account the sequential coupling relationship of material flow between multiple chemical production lines. The optimized operation model takes the lowest overall operating cost as its objective function. The operation optimization module is used to solve the optimized operation model based on the modeled integrated energy and chemical industrial park, under the constraints corresponding to the production process and the scheduling constraints of the integrated energy and chemical industrial park, to obtain the scheduling scheme.

[0017] A computer-readable storage medium for storing computer instructions, which, when executed by a processor, perform the steps in the above method.

[0018] An electronic device includes a memory and a processor, as well as computer instructions stored in the memory and running on the processor, wherein the computer instructions, when executed by the processor, perform the steps in the method described above.

[0019] Compared with the prior art, the beneficial effects of the present invention are as follows: This invention takes into account the strong coupling relationship between the heterogeneous electrical / thermal energy flow and the multi-material flow of hydrogen / ammonia / alcohol in the chemical production process, and considers the material flow coupling constraints between multiple sequential chemical production lines. It optimizes the operation of integrated energy and chemical industrial parks, and fully leverages the flexible adjustment capabilities of chemical systems and multi-energy storage while ensuring the output and safety of chemical products. This ensures the power balance of integrated energy and chemical industrial parks under the high penetration rate of wind and solar new energy, reduces overall operating costs, improves the new energy consumption rate, and promotes carbon reduction and emission reduction in heavy chemical production.

[0020] To make the above-mentioned objects, features and advantages of the present invention more apparent and understandable, preferred embodiments are described below in detail with reference to the accompanying drawings. Attached Figure Description

[0021] The accompanying drawings, which form part of this invention, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an improper limitation of the invention.

[0022] Figure 1 Flowchart of the design scheme provided in the embodiments of the present invention; Figure 2A schematic diagram of an integrated energy and chemical industrial park combining wind, solar, hydrogen, ammonia, and methanol is provided in this embodiment of the invention. Figure 3 The day-ahead power dispatching results diagram of the integrated wind-solar-hydrogen-ammonia-ethanol comprehensive energy and chemical industrial park provided in this embodiment of the invention; Figure 4 The day-ahead thermal power dispatching results of the integrated wind-solar-hydrogen-ammonia-ethanol comprehensive energy and chemical industrial park provided in this embodiment of the invention; Figure 5 The present invention provides a diagram showing the day-to-day hydrogen dispatch results for an integrated energy and chemical industrial park combining wind, solar, hydrogen, ammonia, and methanol. Detailed Implementation

[0023] The present invention will be further described below with reference to the accompanying drawings and embodiments.

[0024] It should be noted that the following detailed description is illustrative and intended to provide further explanation of the invention. Unless otherwise specified, 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 invention pertains.

[0025] It should be noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to limit the scope of exemplary embodiments according to the invention. As used herein, the singular form is intended to include the plural form as well, unless the context clearly indicates otherwise. Furthermore, it should be understood that when the terms "comprising" and / or "including" are used in this specification, they indicate the presence of features, steps, operations, devices, components, and / or combinations thereof.

[0026] Where there is no conflict, the embodiments and features described in this application may be combined with each other.

[0027] Example 1 according to Figure 1 This embodiment provides a method for operating a comprehensive energy and chemical industrial park that takes into account the sequential coupling of multiple production lines, specifically including the following steps: Step 1: Obtain the equipment parameters of various types of equipment in the integrated energy and chemical industrial park for wind, solar, hydrogen, ammonia, and methanol. The park's equipment includes chemical equipment such as electrolyzers, synthetic ammonia equipment, and methanol synthesis equipment, as well as multi-energy storage equipment such as electric energy storage, hydrogen energy storage, and thermal energy storage, and distributed power sources and electric heating equipment for wind and solar power.

[0028] Specifically, including: (1) For the electrolyzer, obtain the hydrogen production efficiency of the electrolyzer. η EL Water consumption efficiency of electrolyzer α 0. Upper and lower limits of electrolytic cell power P P2H min and P P2H max and lower heat energy of hydrogenq H2 Parameters such as these.

[0029] (2) For ammonia synthesis equipment, obtain the molar mass of air. M air Gas constant R Air separation unit inlet temperature T AS The intake air pressure of the air separator compressor p AS in, outlet air pressure of the air separator compressor p AS out, mechanical efficiency of air separator compressor η C Fixed power of the ammonia synthesis reactor P P2A N, Electrical power consumed per unit molar flow rate of ammonia produced l Upper and lower limits of electrical power for ammonia synthesis equipment P P2A max and P P2A min, heat release rate of ammonia synthesis equipment η h,P2A The heat released per unit mass of ammonia produced q NH3 .

[0030] (3) For methanol synthesis equipment, obtain the methanol synthesis efficiency. η P2M The heat of reaction released Δt per unit mass of methanol synthesized H P2M Upper and lower limits of electrical power for methanol synthesis equipment P P2M max and P Parameters such as P2M min.

[0031] (4) For energy storage, obtain the energy storage capacity. E BESS Energy storage self-discharge rate α BESS Maximum charging power of energy storage P ch max, maximum discharge power of electrical energy storage P dismax, energy storage charging efficiency η BESS, energy storage discharge efficiency η disBESS, upper and lower limits of energy storage charging status SOC BESS Max and SOC Parameters such as BESS min.

[0032] (5) For hydrogen storage tanks, obtain the capacity of the hydrogen storage tanks. V HSS Hydrogen storage tank filling and discharging efficiency η ch HSS and η dis HSS, hydrogen storage tank inlet temperature T HSS Inlet gas pressure of hydrogen storage tank compressor p HSS in 、 outlet gas pressure of hydrogen storage tank compressor p HSS out, mechanical efficiency of hydrogen storage tank η HC Maximum mass flow rate of gas entering and exiting the hydrogen storage tank Q Hmax, upper and lower limits of hydrogen storage tank filling status S HSSmax and S HSS min, molar mass of hydrogen M H2 Parameters such as these.

[0033] (6) For thermal energy storage, obtain the thermal energy storage capacity. E HST Thermal energy storage self-heating rate α HST Maximum thermal energy storage capacity H ch max, maximum heat release power of thermal energy storage H dismax, thermal energy storage efficiency η ch HST, thermal energy storage heat release efficiency η disHST, thermal energy storage thermal state limits SOC HST max and SOC Parameters such as HST min.

[0034] (7) For wind and solar new energy power generation equipment, obtain the installed capacity of photovoltaic and wind turbine units. P PV,max and P WT,max Parameters such as these.

[0035] (8) For electric heating equipment, obtain the heat generation efficiency of the electric heating equipment. η EH Upper and lower limits of power consumption of electric heating equipment P EH max and P Parameters such as EH min.

[0036] Step 2: Obtain the diverse load demands of the integrated energy and chemical industrial park, including electricity load, heat load, and the demand for ammonia and methanol; obtain the initial energy storage status of the electricity, heat, and hydrogen multi-energy storage; obtain the total scheduling duration. T Power output prediction information of photovoltaic and wind turbine units in the integrated energy and chemical industrial park, generating T ×1D photovoltaic output prediction matrix P Pred PV and T×1D wind turbine output prediction matrix P Pred WT.

[0037] Step 3: Model chemical equipment such as electrolytic cells, ammonia synthesis equipment, and methanol synthesis equipment, as well as multi-energy storage equipment such as electric energy storage, hydrogen energy storage, and thermal energy storage, and distributed power sources and electric heating equipment such as wind and solar power.

[0038] Step 3.1: Model the electrolyzer. Specifically, based on the chemical reaction equation for producing hydrogen through water electrolysis, i.e. The electrolyzer's operational constraints are set, including constraints on power consumption-gas production, water consumption, input power, and input power ramp-up. Through these methods, the electrolyzer model is constructed.

[0039] In this embodiment, the above-mentioned electrolytic cell model can be represented as: ; in, for t Molar flow rate of hydrogen produced in the electrolyzer at any given time; for t The electrical power consumed by the electrolytic cell at any given time; for t Water consumption for hydrogen production in the electrolyzer during a given time period; Ramp P2H This represents the upper limit of the ramp rate (both upward and downward) of the input power to the electrolytic cell. Δ t The scheduling time interval is 1 hour in this embodiment.

[0040] Step 3.2: Model the green electricity ammonia synthesis equipment, which mainly includes an air separation unit for producing syngas (main nitrogen) and an ammonia synthesis reactor. Specifically, based on the chemical reaction equation for ammonia synthesis, i.e. Operating constraints for the ammonia synthesis equipment were set, including power constraints for the air separator, material balance constraints for the methanol synthesis equipment, power constraints for the ammonia synthesis reactor, input power ramp-up constraints for the ammonia synthesis equipment, input power constraints for the ammonia synthesis equipment, and heat generation power constraints for the ammonia synthesis equipment. Through these methods, the ammonia synthesis equipment model was completed.

[0041] In this embodiment, the above-mentioned ammonia synthesis equipment model can be represented as: ; in, for t The electrical power consumed by the air separation device at any given time; , , and They are respectively tThe molar flow rates of air, nitrogen, hydrogen, and ammonia produced by the ammonia synthesis equipment at all times; yes t The total electrical power consumed by the ammonia synthesis reactor at any given time; for t The heat release power of the ammonia synthesis equipment at all times; for t Ammonia production at any given time.

[0042] Step 3.3: Model the methanol synthesis equipment. Specifically, based on the chemical reaction equation for ammonia synthesis, i.e. Operating constraints for the methanol synthesis equipment were set, including constraints on gas consumption, material balance, heat generation, input power, and input power ramp-up. Through these methods, the methanol synthesis equipment model was successfully built.

[0043] In this embodiment, the methanol synthesis equipment model described above can be represented as follows: ; in, for t The electrical power consumed by the methanol synthesis equipment at any given time; , and They are respectively t The amount of carbon dioxide and hydrogen consumed by the methanol synthesis equipment at any given time, and the molar flow rate of the synthesized methanol. for t The exothermic power of the methanol synthesis equipment at all times.

[0044] Step 3.4: Model the energy storage system. Specifically, set the operational constraints for the energy storage system, including energy balance constraints, State of Charge (SOC) constraints, periodic state regression constraints, upper and lower limits of SOC constraints, charging and discharging power constraints, and mutual exclusion constraints between charging and discharging states. Under the periodic state regression constraint, the SOC of the energy storage system is set at each... T Let's go back to the previous steps. Using the methods described above, we can complete the construction of the energy storage model.

[0045] In this embodiment, the above-mentioned energy storage model can be expressed as: ; in, for t The amount of energy stored in a time-sensitive energy storage device; and for t The charging and discharging power of the electrical energy storage at any given time; for t The energy storage status of the electrical energy storage at any given time.

[0046] Step 3.5: Model the hydrogen storage tank. This tank serves as a buffer between the upstream electrolyzer hydrogen production line and the downstream ammonia and methanol production lines, ensuring a stable hydrogen supply to the downstream lines. Its main power-consuming equipment is the hydrogen storage tank compressor. Specifically, set operational constraints for the hydrogen storage tank, including energy balance constraints, compressor power consumption constraints, periodic state regression constraints, upper and lower limits for hydrogen storage tank filling status, and inlet and outlet gas volume constraints. Through the above methods, the hydrogen storage tank model is completed.

[0047] In this embodiment, the above-mentioned hydrogen storage tank model can be represented as: ; in, for t Monitor the constant gas level of the hydrogen storage tank; and for t Real-time inlet and outlet mass flow rates of hydrogen storage tank; for t The electrical power consumed by the compressor of the hydrogen storage tank at all times.

[0048] Step 3.6: Model the thermal energy storage. Specifically, set the operational constraints for the thermal energy storage, including energy balance constraints, state constraints, periodic state regression constraints, upper and lower limits of the State of Charge (SOC) of the thermal energy storage, and constraints on the thermal power of charge and discharge, as well as mutual exclusion constraints on the charge and discharge states. Through the above methods, the thermal energy storage model is completed.

[0049] In this embodiment, the above thermal energy storage model can be expressed as: ; in, for t The amount of heat stored in thermal energy at all times; and for t The constant charge and discharge heat power of thermal energy storage; for t The energy storage status of thermal energy storage at all times.

[0050] Step 3.7: Model the wind and solar renewable energy sources. Specifically, set output constraints for distributed wind and solar power generation and constraints on wind and solar curtailment. Through the above methods, complete the construction of the wind and solar renewable energy model.

[0051] In this embodiment, the above-mentioned wind and solar new energy model can be represented as: ; in, and They are respectively tThe actual output of photovoltaic and wind turbines at any given time; P Pred PV, t and P Pred WT, t for t Predicted power output of photovoltaic and wind turbine units at any given time; and They are respectively t Real-time curtailment of solar and wind power from photovoltaic and wind turbine units.

[0052] Step 3.8: Model the electric heating equipment. Specifically, set the operational constraints for the electric heating equipment, including constraints on the heat generation power, output power, and maximum number of start-stop cycles within a scheduling period. Through the above methods, the model of the electric heating equipment is completed.

[0053] In this embodiment, the above-mentioned electric heating equipment model can be represented as: ; in, for t The electrical power consumed by the electric heating equipment at all times; for t The heat output of the electric heating equipment at all times; Let t be the on / off state of the electric heating equipment. This indicates that the electric heating equipment is in working condition, while the opposite indicates that it is in a stopped condition. N EH For electric heating equipment during the scheduling cycle T Maximum number of start-stop cycles.

[0054] Step 4: Based on the different equipment models, and considering the sequential coupling relationship of material flow between multiple chemical production lines, construct a day-ahead scheduling model for an integrated energy and chemical industrial park combining wind, solar, hydrogen, ammonia, and methanol. Specifically, set the actual production / consumption power of electrolyzers, ammonia synthesis equipment, methanol synthesis equipment, wind and solar distributed power sources, and various energy storage equipment such as electric energy storage, hydrogen energy storage, and thermal energy storage as decision variables; set the operating costs of the above equipment; set the penalty costs for wind curtailment, solar curtailment, and load curtailment; set the cost of purchasing electricity from the external grid and the cost of purchasing raw materials for chemical production; and set the carbon emission costs caused by purchasing electricity from the external grid.

[0055] Following the model established in step 3, constraints are set for power consumption, electricity purchase, wind and solar power output, chemical equipment operation, and diversified energy storage operation. Constraints for power and heat consumption balance are also set for the integrated energy and chemical industrial park. Furthermore, considering the sequential coupling of products and raw materials among multiple production lines in the integrated energy and chemical industrial park, material flow balance constraints are set between the upstream and downstream hydrogen ammonia and methanol production lines and hydrogen storage tanks. To ensure the interests of chemical enterprises and thus guarantee their participation in the flexible regulation of the power system, hydrogen ammonia and methanol production constraints are set. The optimization objective for low-carbon economic operation is set as comprehensive operating cost. f The lowest can be expressed as: ; in, f purc Cost of purchasing electricity from external networks; f material Cost of raw materials for chemical production; f ope The operating costs of the comprehensive energy and chemical industrial park include the operating costs of electrolyzers, synthetic ammonia equipment, methanol synthesis equipment, wind and solar distributed power sources, and various energy storage equipment such as electric energy storage, hydrogen energy storage, and thermal energy storage. f env The environmental costs of operating a comprehensive energy and chemical industrial park include the costs of penalties for curtailing wind and solar power and the costs of carbon emissions.

[0056] In this embodiment, the optimization objective for low-carbon economic operation can be further refined as follows: ; ; ; ; in, Let t be the power purchased from the external power grid. C TOU The time-of-use electricity price for electricity purchased from the external power grid by the integrated energy and chemical industrial park; for t The carbon dioxide consumption of the methanol synthesis equipment at any given time; C H2O and C CO2 The unit price of water and carbon dioxide, the raw materials consumed in the production of electrolyzers and methanol synthesis equipment; C i , i ({PV, WT, P2H, P2A, P2M, EH, BESS, HSS, HST} are the unit operating costs of different equipment; C cut PV and C WT represents the unit cost of curtailment of solar and wind power for photovoltaic and wind turbine generators.C Em The penalty cost per unit of carbon dioxide emissions.

[0057] In this embodiment, in addition to the constraints listed in step 3, the constraints on electricity balance, heat balance, material flow balance between sequential multi-chemical production lines, and output for optimizing the low-carbon economic operation of the integrated energy and chemical industrial park can be further refined as follows: ; ; ; ; in, and The methanol and ammonia production of the methanol synthesis equipment and the ammonia synthesis equipment during time period t; M Total CH3OH and M Total NH3 represents the daily target production of methanol and ammonia.

[0058] Step 5: Under the condition that the operation constraints of the integrated energy and chemical industrial park are met, call the IPOPT solver to obtain the scheduling scheme of the integrated energy and chemical industrial park that satisfies the objective function. This will realize the operation optimization of multiple sequential chemical production lines in the integrated energy and chemical industrial park. Under the premise of ensuring the output and safety of chemical products, give full play to the flexible adjustment capabilities of the chemical system and diversified energy storage, ensure the power balance of the integrated energy and chemical industrial park under the high penetration rate of wind and solar new energy, reduce the overall operating cost, improve the new energy consumption rate, and promote carbon reduction and emission reduction in heavy chemical production.

[0059] The invention will now be illustrated with some specific examples.

[0060] This invention employs, as follows Figure 2 A case study is conducted on a small-scale integrated energy and chemical industrial park combining wind, solar, hydrogen, ammonia, and methanol. This park is equipped with a 1.5MW photovoltaic power generation unit and a 1.5MW wind power generation unit, along with a 700kW electrolytic cell, a 200kW ammonia synthesis unit, a 500kW methanol synthesis unit, a 500kW / 1MWh energy storage system, a 500kW / 1MWh thermal storage system, and a 500m³ / h thermal storage system. 3 Hydrogen storage tanks and a 400kW electric heating system are provided, assuming a daily production target of 1 ton / day for both ammonia and methanol. The day-ahead scheduling problem based on mixed-integer nonlinear programming is solved using the IPOPT solver. The results are compared with those obtained using traditional fixed-capacity production methods, and the overall operating cost comparison is shown in Table 1. The scheduling schemes for electricity, heat, and hydrogen at different power / mass flows in the integrated energy and chemical industrial park using the low-carbon optimization scheduling strategy of this invention are as follows: Figures 3-5 As shown.

[0061] Table 1. Operating Costs of Integrated Energy and Chemical Industrial Parks under Different Production Methods

[0062] The results above demonstrate that, compared to the traditional fixed-capacity production methods in the heavy chemical industry, the low-carbon economic operation strategy proposed in this invention can fully leverage the flexibility of electricity consumption in various chemical production processes such as electro-hydrogen production, ammonia synthesis, and methanol synthesis. By shifting some chemical product production tasks to the peak periods of wind and solar power generation, the power balance of the integrated energy and chemical industrial park can be ensured, fully absorbing wind and solar renewable energy generation and reducing wind and solar curtailment. Furthermore, it can reduce the amount of electricity purchased from the external grid, thereby reducing carbon emissions. Consequently, the comprehensive operating cost per unit output of green ammonia and green methanol in the integrated energy and chemical industrial park decreased from 1082.08 yuan to 746.10 yuan, effectively reducing operating costs by 31.05%. This demonstrates the significant cost-reduction, efficiency-enhancing, and carbon emission-reduction benefits of implementing renewable energy substitution in the heavy chemical industry.

[0063] Example 2 This embodiment provides a chemical industrial park operation optimization system that takes into account the sequential coupling of multiple production lines, including: The integrated energy and chemical industrial park parameter acquisition module is used to acquire equipment parameters of different equipment in the integrated wind, solar, hydrogen, ammonia, and methanol integrated energy and chemical industrial park. The demand and forecast parameter acquisition module is used to acquire the load demand of the integrated energy and chemical industrial park, including the power load, heat load, and the demand for ammonia and methanol; acquire the initial energy storage status of multi-energy storage equipment including electric energy storage, thermal energy storage and hydrogen energy storage; and acquire the output power forecast information of photovoltaic and wind turbine units in the integrated energy and chemical industrial park within the total scheduling cycle. The integrated energy and chemical industrial park modeling module is used to analyze the production processes of different green energy chemical production lines, determine the constraints corresponding to the production processes, and, in combination with the acquired equipment parameters and prediction information, construct models of electrolyzers, synthetic ammonia equipment, and methanol synthesis equipment, and model wind and solar distributed power sources and multi-element energy storage equipment. An optimized operation model construction module is used to construct an optimized operation model for an integrated energy and chemical industrial park that combines wind, solar, hydrogen, ammonia, and methanol production, based on the models of different equipment and taking into account the sequential coupling relationship of material flow between multiple chemical production lines. The optimized operation model takes the lowest overall operating cost as its objective function. The operation optimization module is used to solve the optimized operation model based on the modeled integrated energy and chemical industrial park, under the constraints corresponding to the production process and the scheduling constraints of the integrated energy and chemical industrial park, to obtain the scheduling scheme.

[0064] Example 3 This embodiment provides an electronic device, including: a memory for storing executable instructions; and a processor for executing the executable instructions stored in the memory to implement the method described in Embodiment 1.

[0065] Example 4 This embodiment also provides a computer-readable storage medium storing executable instructions, which, when executed by a processor, will cause the processor to execute the method described in Embodiment 1.

[0066] Those skilled in the art will understand that embodiments of the present invention can be provided as methods, systems, or computer program products. Therefore, the present invention can take the form of a completely hardware embodiment, a completely software embodiment, or an embodiment combining software and hardware aspects. Furthermore, the present invention can take the form of one or more computer-usable storage media (including, but not limited to, disk storage, etc.) containing computer-usable program code. CD - ROM It takes the form of a computer program product implemented on (such as optical memory, etc.).

[0067] This invention is described with reference to flowchart illustrations and / or block diagrams of methods, apparatus (systems), and computer program products according to embodiments of the invention. It will be understood that each block of the flowchart illustrations and / or block diagrams, and combinations of blocks in the flowchart illustrations and / or block diagrams, can be implemented by computer program instructions. These computer program instructions can be provided to a processor of a general-purpose computer, special-purpose computer, embedded processor, or other programmable data processing apparatus to produce a machine, such that the instructions, which execute via the processor of the computer or other programmable data processing apparatus, generate instructions for implementing the flowchart illustrations and / or block diagrams. Figure 1 One or more processes and / or boxes Figure 1 A device that provides the functions specified in one or more boxes.

[0068] These computer program instructions may also be stored in a computer-readable storage medium that can direct a computer or other programmable data processing device to function in a particular manner, such that the instructions stored in the computer-readable storage medium produce an article of manufacture including instruction means, which are implemented in a process Figure 1 One or more processes and / or boxes Figure 1 The function specified in one or more boxes.

[0069] These computer program instructions may also be loaded onto a computer or other programmable data processing equipment to cause a series of operational steps to be performed on the computer or other programmable equipment to produce a computer-implemented process, thereby providing instructions that execute on the computer or other programmable equipment for implementing the process. Figure 1One or more processes and / or boxes Figure 1 The steps of the function specified in one or more boxes.

[0070] The above description is merely a preferred embodiment of the present invention and is not intended to limit the invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made by those skilled in the art without creative effort within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A method for optimizing the operation of a chemical industrial park considering the sequential coupling of multiple production lines, characterized in that, Includes the following steps: Obtain the equipment parameters of different equipment in the integrated energy and chemical industrial park combining wind, solar, hydrogen, ammonia, and methanol; Obtain the load demand of the integrated energy and chemical industrial park, including electricity load, heat load, and demand for ammonia and methanol; obtain the initial energy storage status of multi-energy storage equipment including electric energy storage, thermal energy storage, and hydrogen energy storage; obtain the power output forecast information of photovoltaic and wind turbine units in the integrated energy and chemical industrial park within the total scheduling cycle; The production processes of different green energy chemical production lines are analyzed, the constraints corresponding to the production processes are determined, and models of electrolyzers, ammonia synthesis equipment and methanol synthesis equipment are constructed by combining the obtained equipment parameters and prediction information. Models of wind and solar distributed power sources and multi-element energy storage equipment are also constructed. Based on the models of different equipment, and taking into account the sequential coupling relationship of material flow between multiple chemical production lines, an optimized operation model for the integrated energy and chemical industrial park of wind, solar, hydrogen, ammonia and methanol is constructed. The optimized operation model takes the lowest comprehensive operating cost as the objective function. Based on the optimized operation model of the integrated energy and chemical industrial park, and under the constraints corresponding to the production process and the scheduling constraints of the integrated energy and chemical industrial park, the optimized operation model is solved to obtain the scheduling scheme.

2. The method for optimizing the operation of a chemical industrial park considering the sequential coupling of multiple production lines as described in claim 1, characterized in that, The process of obtaining equipment parameters for different equipment in an integrated energy and chemical industrial park combining wind, solar, hydrogen, ammonia, and methanol includes: For electrolyzers, obtain the electrolyzer hydrogen production efficiency, electrolyzer water consumption efficiency, electrolyzer power upper and lower limits, and hydrogen low-grade heat energy. For ammonia synthesis equipment, the molar mass of air is obtained. 、 Gas constant, air inlet temperature of air separator, air inlet pressure of air separator compressor, air outlet pressure of air separator compressor, mechanical efficiency of air separator compressor, fixed power of ammonia synthesis reactor, power consumed per unit molar flow rate of ammonia produced, upper and lower limits of power of ammonia synthesis equipment, heat release rate of ammonia synthesis equipment and heat release per unit mass of ammonia produced. For methanol synthesis equipment, obtain the methanol synthesis efficiency, the heat of reaction released per unit mass of methanol synthesized, and the upper and lower limits of the electrical power of the methanol synthesis equipment. For energy storage, obtain the energy storage capacity, energy storage self-discharge rate, energy storage maximum charging power, energy storage maximum discharging power, energy storage charging efficiency, energy storage discharging efficiency, and energy storage charging state upper and lower limits. For hydrogen storage tanks, obtain the tank capacity, filling and discharging efficiency, inlet temperature, and inlet pressure of the compressor. 、 The outlet gas pressure of the hydrogen storage tank compressor, the mechanical efficiency of the hydrogen storage tank, the maximum mass flow rate of the hydrogen storage tank inlet and outlet, the upper and lower limits of the hydrogen storage tank filling state, and the molar mass of hydrogen. For thermal energy storage, obtain the thermal energy storage capacity, self-heating rate, maximum thermal storage power, maximum heat release power, thermal storage efficiency, heat release efficiency, and upper and lower limits of thermal storage state. ； For wind and solar new energy power generation equipment, obtain the installed capacity of photovoltaic and wind turbine units. ； For electric heating equipment, obtain the heat generation efficiency and upper and lower limits of the power consumption of the electric heating equipment.

3. The method for optimizing the operation of a chemical industrial park considering the sequential coupling of multiple production lines as described in claim 1, characterized in that, The process of constructing models of electrolyzers, ammonia synthesis equipment, and methanol synthesis equipment includes: setting operating constraints for electrolyzers based on the chemical reaction equations for hydrogen production from water electrolysis, including constraints on electrolyzer power consumption-gas production, electrolyzer water consumption, electrolyzer input power, and electrolyzer input power ramp-up, thereby realizing the construction of the electrolyzer model; A model was created for the green electricity ammonia synthesis equipment. Based on the chemical reaction equation for ammonia synthesis, operational constraints were set for the ammonia synthesis equipment, including power constraints for the air separation unit, material balance constraints for the methanol synthesis equipment, power constraints for the ammonia synthesis reactor, input power ramp-up constraints for the ammonia synthesis equipment, and constraints on the input power and heating power of the ammonia synthesis equipment. Based on the chemical reaction equation for ammonia synthesis, operational constraints for the methanol synthesis equipment are set, including constraints on gas consumption, material balance, heat generation, input power, and input power ramp-up. This completes the construction of the methanol synthesis equipment model.

4. The method for optimizing the operation of a chemical industrial park considering the sequential coupling of multiple production lines as described in claim 1, characterized in that, The process of modeling multi-element energy storage equipment includes: modeling the energy storage, setting operational constraints for the energy storage, including energy balance constraints, state of charge (SOC) constraints, periodic state regression constraints, upper and lower limits of SOC constraints, charging and discharging power constraints, and mutual exclusion constraints between charging and discharging states. Under the periodic state regression constraint, the energy storage state is set at each... T Go back once to complete the construction of the energy storage model; Model the hydrogen storage tank and set the operating constraints of the hydrogen storage tank, including the energy balance constraint of the hydrogen storage tank, the power consumption constraint of the hydrogen storage tank compressor, the periodic state regression constraint, the upper and lower limits constraint of the hydrogen storage tank filling state, and the constraint of the gas volume of the hydrogen storage tank entering and leaving the hydrogen storage tank, and complete the construction of the hydrogen storage tank model. A model for thermal energy storage is constructed, and operational constraints are set, including energy balance constraints, state constraints, periodic state regression constraints, upper and lower limits of the state of charge (SOC) of thermal energy storage, and constraints on the charge and discharge heat power and mutual exclusion constraints of the charge and discharge states of thermal energy storage.

5. The method for optimizing the operation of a chemical industrial park considering the sequential coupling of multiple production lines as described in claim 1, characterized in that, The process of modeling wind and solar distributed power sources includes setting output constraints and curtailment constraints for wind and solar distributed power sources, as well as setting operational constraints for electric heating equipment, including heat generation power constraints, output power constraints, and maximum number of start-stop cycles within the scheduling period.

6. The method for optimizing the operation of a chemical industrial park considering the sequential coupling of multiple production lines as described in claim 1, characterized in that, The process of considering the sequential coupling relationship of material flow between multiple chemical production lines includes: setting the actual production / energy consumption power of electrolyzers, ammonia synthesis equipment, methanol synthesis equipment, wind and solar distributed power sources, and multi-energy storage equipment as decision variables; setting the operating costs of each piece of equipment; setting the penalty costs for curtailment of wind, solar, and loads; setting the cost of purchasing electricity from the external grid and the cost of purchasing raw materials for chemical production; and setting the carbon emission costs caused by purchasing electricity from the external grid. Considering the sequential coupling of products and raw materials among multiple production lines in the integrated energy and chemical industrial park, a material flow balance constraint is set between the upstream and downstream hydrogen ammonia production lines and hydrogen storage tanks, and a hydrogen ammonia production constraint is also set.

7. The method for optimizing the operation of a chemical industrial park considering the sequential coupling of multiple production lines as described in claim 1, characterized in that, The constraints corresponding to the production process include: power balance constraints, heat balance constraints, material flow balance constraints between sequential multi-chemical production lines, and output constraints.

8. A chemical industrial park operation optimization system considering the sequential coupling of multiple production lines, characterized in that, include: The integrated energy and chemical industrial park parameter acquisition module is used to acquire equipment parameters of different equipment in the integrated wind, solar, hydrogen, ammonia, and methanol integrated energy and chemical industrial park. The demand and forecast parameter acquisition module is used to acquire the load demand of the integrated energy and chemical industrial park, including the power load, heat load, and the demand for ammonia and methanol; acquire the initial energy storage status of multi-energy storage equipment including electric energy storage, thermal energy storage and hydrogen energy storage; and acquire the output power forecast information of photovoltaic and wind turbine units in the integrated energy and chemical industrial park within the total scheduling cycle. The integrated energy and chemical industrial park modeling module is used to analyze the production processes of different green energy chemical production lines, determine the constraints corresponding to the production processes, and, in combination with the acquired equipment parameters and prediction information, construct models of electrolyzers, synthetic ammonia equipment, and methanol synthesis equipment, and model wind and solar distributed power sources and multi-element energy storage equipment. An optimized operation model construction module is used to construct an optimized operation model for an integrated energy and chemical industrial park that combines wind, solar, hydrogen, ammonia, and methanol production, based on the models of different equipment and taking into account the sequential coupling relationship of material flow between multiple chemical production lines. The optimized operation model takes the lowest overall operating cost as its objective function. The operation optimization module is used to solve the optimized operation model based on the modeled integrated energy and chemical industrial park, under the constraints corresponding to the production process and the scheduling constraints of the integrated energy and chemical industrial park, to obtain the scheduling scheme.

9. A computer-readable storage medium, characterized in that, Used to store computer instructions, which, when executed by a processor, complete the steps of the method according to any one of claims 1-7.

10. An electronic device, characterized in that, It includes a memory and a processor, as well as computer instructions stored in the memory and running on the processor, which, when executed by the processor, perform the steps of the method according to any one of claims 1-7.

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