A Design and Evaluation Method and System for Carbon Dioxide Electrochemical Reduction Systems Based on Techno-Economic Analysis

Abstract

This invention discloses a design and evaluation method and system for a carbon dioxide electrochemical reduction system based on techno-economic analysis. The method includes: determining the system flow diagram and energy and material flow information; constructing a techno-economic analysis model for the carbon dioxide electrochemical reduction system, including: an electrolyzer operating status model, a capital and operating cost composition model, and a financial summary analysis model; determining the operating parameters, market parameters, and technical parameters of the carbon dioxide electrochemical reduction system, and using them as model inputs; and optimizing or comparatively evaluating the preliminary design of the carbon dioxide electrochemical reduction system based on the techno-economic analysis results output by the model. This method can incorporate carbon emission costs into economic considerations while taking into account anode substitution reactions, and can reasonably and scientifically assess the impact of various factors on the economics of the carbon dioxide electrochemical reduction system; it provides suggestions and guidance for system optimization design and can demonstrate the feasibility of the system for commercial application.

Description

Technical Field

[0001] This invention belongs to the field of chemical system design technology, and relates to a design method and system for a carbon dioxide electrochemical reduction system based on techno-economic analysis. In particular, it relates to a design and evaluation method and system for a carbon dioxide electrochemical reduction system based on techno-economic analysis that considers anode substitution reactions and incorporates carbon emission costs into economic considerations. Background Technology

[0002] The advancement of the national dual-carbon strategy is beneficial to the development of the carbon capture and utilization industry. Electrochemical methods for capturing and purifying carbon dioxide from the atmosphere and converting it into economically valuable single-carbon products such as formic acid, methanol, and methane, as well as multi-carbon products such as ethanol, ethylene, and propanol, have become a hot topic in the industry in recent years. Compared to the relatively mature and commercially available water electrolysis hydrogen production technology, carbon dioxide electroreduction technology systems still face many obstacles and challenges before commercial operation, with economic barriers being a significant factor. The techno-economic viability of carbon dioxide electroreduction technology systems is affected by various factors, including electricity pricing frameworks, the selection of anode substitution reactions, equipment technical parameters, market prices of relevant consumables and components, and carbon trading policies related to achieving a zero-carbon transition. This necessitates the establishment of accurate and reasonable mathematical models to assess the degree of influence of each factor and provide guidance for further system optimization and adjustment. Summary of the Invention

[0003] The purpose of this invention is to address the shortcomings of existing technologies by providing a design and evaluation method and system for carbon dioxide electrochemical reduction systems based on techno-economic analysis. The core of this method is a techno-economic analysis approach for carbon dioxide electrochemical reduction systems that considers anode substitution reactions and incorporates carbon emission costs into economic considerations. Based on the technical design of the carbon dioxide electrochemical reduction system, its economics can be calculated, and guidance can be provided for further optimization and improvement of the electrochemical reduction system, supporting the development of carbon dioxide electrochemical reduction technology systems and facilitating their commercial application.

[0004] To achieve the above objectives, the present invention adopts the following technical solution.

[0005] A design and evaluation method for a carbon dioxide electrochemical reduction system based on techno-economic analysis includes:

[0006] 1) Draw a flowchart of the preliminary design of the carbon dioxide electrochemical reduction system, clarify the design products, clarify the composition and operating principle of each component of the system, and determine the path and direction of energy flow and material flow in the system;

[0007] 2) Combining the system flow diagram and energy and material flow information determined in step 1), construct a technical and economic analysis model for the carbon dioxide electrochemical reduction system, including: an electrolyzer operating status model, a capital and operating cost composition model, and a financial summary analysis model;

[0008] 3) Determine the operating parameters, market parameters, and technical parameters of the carbon dioxide electrochemical reduction system, and use them as model inputs. Based on the technical and economic analysis results of the system output by the model, optimize or evaluate the preliminary design of the carbon dioxide electrochemical reduction system. Further, in the above technical solution, the flowchart includes: carbon dioxide capture and purification process, carbon dioxide electrochemical reduction process, gas-liquid product separation process, electrolyte solution regeneration process, carbon dioxide / carbonate separation and recovery process, gas product compression, storage and utilization process, and liquid product storage, processing and utilization process. The composition and operating principle of each component of the system include: gas pressure swing adsorption equipment and pressure swing adsorption process for gas product separation and recovery, distillation equipment and distillation process for liquid product separation and recovery, as well as key electrolytic cell membrane electrode components, electrolyte composition, and electrode reactions, etc.

[0009] Furthermore, the operational parameters include: designed output, annual operating time, facility lifespan, and auxiliary equipment cost ratio, etc.; the market parameters include: electricity prices and carbon emission factors of different power grids, renewable electricity prices and carbon emission factors, carbon emission prices of various carbon emission markets, carbon dioxide procurement prices, procurement prices of selected anode alternative reaction raw materials, and system component installation and operation related cost parameters, etc., based on official data; wherein the electricity prices and carbon emission factors of different power grids, renewable electricity prices and carbon emission factors refer to representative industrial (commercial) electricity prices of different national power grids in recent years and carbon emission factors determined by the national power energy structure, and the carbon emission prices of various carbon emission markets refer to local carbon emission trading prices in countries (regions) that have established carbon emission trading market mechanisms; the technical parameters include: current density, electrolysis voltage, anode and cathode selectivity, and raw material single-pass conversion rate, etc.

[0010] This invention also provides an evaluation system for a carbon dioxide electrochemical reduction system based on techno-economic analysis, comprising:

[0011] The model determination module is used to determine the mathematical model for the economic analysis of the carbon dioxide electrochemical reduction system based on the input system flowchart and energy and material flow information. This model includes the electrolyzer operating status model, the capital and operating cost composition model, and the financial summary analysis model.

[0012] The results analysis module is used to output the techno-economic analysis results of the system based on the input operating parameters, market parameters, and technical parameters of the carbon dioxide electrochemical reduction system. After completing the techno-economic analysis based on the determined parameter set, it can draw data analysis results such as bar charts of capital cost and operating cost composition, and contour plots of average production cost, to help quantitatively analyze the impact of various factors on the system's economy.

[0013] The beneficial effects of this invention are:

[0014] This invention, based on consideration of different anode substitution reactions and the inclusion of carbon emission costs in economic considerations, assesses the contribution of the capital costs and operating costs of each component of the designed carbon dioxide electrochemical reduction technology system to the overall economic efficiency, further evaluates the impact of various influencing parameters on the overall economic efficiency, and thus demonstrates the feasibility of the system for commercial application, and provides suggestions and guidance for system optimization design. Attached Figure Description

[0015] Figure 1 Overall flowchart of the method;

[0016] Figure 2 Energy and mass flow diagram of a traditional AEM-CO2R / OER electrolyzer system;

[0017] Figure 3 Energy and mass flow diagram of a membrane-free compact CO2 / GOR electrolyzer system;

[0018] Figure 4 Bar chart comparing the economic efficiency of four electrolytic cell systems;

[0019] Figure 5 Schematic diagram illustrating the economic changes of the membrane-free compact CO2R / GOR electrolyzer system under different grid electricity prices and high and low carbon emission price combinations;

[0020] Figure 6 Sensitivity analysis of certain important parameters. Detailed Implementation

[0021] The present invention will now be described in detail with reference to specific embodiments. These embodiments will help those skilled in the art to further understand the present invention, but do not limit the invention in any way.

[0022] According to one embodiment of the present invention, a design and evaluation system for a carbon dioxide electrochemical reduction system based on techno-economic analysis includes:

[0023] The model determination module is used to determine the mathematical model for the economic analysis of the carbon dioxide electrochemical reduction system based on the input system flowchart and energy and material flow information. This model includes the electrolyzer operating status model, the capital and operating cost composition model, and the financial summary model.

[0024] The results analysis module is used to output the technical and economic analysis results of the system based on the input operating parameters, market parameters, and technical parameters of the carbon dioxide electrochemical reduction system. After the determined parameter set is input and the system economic analysis is completed, data analysis results such as bar charts of capital cost and operating cost composition, and contour plots of average production cost can be drawn to help quantitatively analyze the impact of various factors on the system's economy.

[0025] According to a specific embodiment of the present invention, such as Figure 1 As shown, a design and evaluation method for a carbon dioxide electrochemical reduction system based on techno-economic analysis is presented. This method incorporates carbon emission costs into economic considerations, taking into account anode substitution reactions, and rationally and scientifically assesses the impact of various factors on the economics of the carbon dioxide electrochemical reduction system. Based on the analytical results, the method optimizes or comparatively evaluates the design of the carbon dioxide electrochemical reduction system. The method includes:

[0026] Step S1: Summarize and draw a flowchart of the initial design of the carbon dioxide electrochemical reduction system, clarify the design products, clarify the composition and operating principle of each component of the system, and determine the path and direction of the overall energy flow and material flow.

[0027] Step S2: Based on the flowchart drawn in Step S1, determine the mathematical model for the techno-economic analysis of the carbon dioxide electrochemical reduction system, including the electrolyzer operating status model, the capital and operating cost composition model, and the financial summary analysis model.

[0028] Step S3: Based on the mathematical model determined in Step S2, the parameters involved in the model are divided into three groups for determination: First, operational parameters are determined based on the potential market demand and development prospects of the designed product, as well as industry practices and experience in the chemical production field. These include designed output, annual operating time, facility lifespan, and auxiliary equipment cost ratios. Second, market parameters are determined, including: electricity prices and carbon emission factors for different power grids, renewable electricity prices and carbon emission factors, carbon emission prices in various carbon emission markets, carbon dioxide procurement prices, procurement prices of selected anode replacement reaction feedstocks, and system component installation and operation-related cost parameters, based on official data. Finally, technical parameters are determined based on laboratory experimental data, including current density, electrolysis voltage, anode and cathode selectivity, and single-pass conversion rate of raw materials.

[0029] Step S4 involves using the three sets of parameters determined as model inputs and outputting the economic analysis results of the system. This provides suggestions and guidance for the optimized design of the carbon dioxide electrochemical reduction system and can also be used to demonstrate the feasibility of putting the system into commercial use.

[0030] The flow chart of the carbon dioxide electrochemical reduction system in step S1 may include the following or other processes with similar functions: carbon dioxide capture and purification process, carbon dioxide electrochemical reduction process, gas-liquid product separation process, electrolyte (solution) regeneration process, carbon dioxide (carbonate) separation and recovery process, gaseous product compression, storage and utilization process, liquid product storage, processing and utilization process, etc. To accurately describe the system's techno-economic efficiency, it is necessary to determine the overall energy flow and the path and direction of the material flow.

[0031] In step S2, the electrolyzer operating state model is a mathematical model that clarifies the energy and material flow through the electrolyzer under specified operating parameter sets and technical parameter sets. It includes the following parameters and their calculation methods:

[0032] The formula for calculating the total current of an electrolytic cell is as follows:

[0033]

[0034] In the formula Y d The design yield is given by: F is the Faraday constant; M is the molar mass of the substance corresponding to the subscript; FE is the electrode selectivity corresponding to the subscript; Z is the number of electrons transferred to generate 1 mol of product molecules corresponding to the subscript when the reactant undergoes oxidation / reduction to produce the product.

[0035] Accordingly, the formulas for calculating the total electrode area and total power of the electrolytic cell are as follows:

[0036]

[0037] P total =VI total

[0038] In the formula, V is the electrolysis voltage;

[0039] The formulas for calculating the mass flow rates of CO2 and anolyte reactants required to achieve the designed output are as follows:

[0040]

[0041] In the formula, M is the molar mass of the substance molecule corresponding to the subscript; n is the number of product molecules generated by consuming 1 substance molecule corresponding to the subscript.

[0042] The formulas for calculating the mass flow rates of CO2 at the inlet and outlet of the electrolytic cell and the anode reactants are as follows:

[0043]

[0044] In the formula, SPC is the single-pass conversion rate; r is the proportion of the corresponding reactants that do not directly participate in the electrode reaction and flow directly out of the reactor from the outlet after being introduced into the electrode inlet;

[0045] The formulas for calculating the volumetric flow rate of the product (pure) and the volumetric flow rate of the electrolyte (assuming the product is liquid) are as follows:

[0046]

[0047]

[0048] In the formula ρ p The product density at a given temperature and pressure; x p This represents the volume fraction of the products in the electrolyte.

[0049] These parameters are mainly used to calculate the relevant parameters of the subsequent separation section, such as the gas / liquid volume flow rate that needs to be separated. In other words, the output parameters of the electrolyzer operating status model are used as inputs into the capital and operating cost model for calculation.

[0050] In step S2, the capital and operating cost composition model is a specific representation of the system's economics derived from the parameters of the electrolyzer operating state model and the market parameter set. It includes the following parameters and their calculation methods:

[0051] The formulas for calculating the capital cost of the electrolyzer, the capital cost of auxiliary equipment, and the capital cost of each separation device are as follows:

[0052] CAPEX electrolyzer =c stack A total

[0053]

[0054] In the formula, c stack For stack cost; r BOP The proportion of auxiliary equipment costs; CAPEX separation,i,r The rated capital cost of the equipment corresponding to separation process i; The volumetric flow rate of the gas / liquid substance that needs to undergo separation process i; f is the rated gas / liquid volumetric flow rate of the equipment corresponding to separation process i; capex,i This refers to the capital cost load factor corresponding to separation process i.

[0055] The formulas for calculating the electricity cost of the electrolytic cell, the carbon emission cost of the electrolytic cell, the equipment maintenance and replacement cost, the raw material procurement cost, and the operating cost of each separation unit are as follows:

[0056] OPEXelectricity =P total p e

[0057] OPEX emission =P total f emission p emission

[0058] OPEX maintenance,i =CAPEX i ·r maintenance,i

[0059]

[0060] OPEX reactant =N reactant p reactant

[0061]

[0062] In the formula p e For electricity price; f emission p is the power grid emission factor. emission For carbon emission prices; CAPEX i The capital cost corresponding to equipment i that requires maintenance and replacement; r maintenance,i For equipment i requiring maintenance and replacement, the maintenance and replacement cost is the percentage of the equipment's capital cost per maintenance and replacement cycle; p is the market price of the corresponding raw material; OPEX separation,i,r f is the rated operating cost of the equipment corresponding to separation process i; opex,i This is the operating cost load scaling factor corresponding to separation process i;

[0063] In step S2, the financial summary analysis model uses target parameters to evaluate the overall economic performance of the system and analyzes the impact of a certain parameter on the target parameter using univariate sensitivity analysis. This includes the following parameters and their calculation methods:

[0064] The average production cost of a product is defined as the ratio of the total cost over the facility's life to the designed total output over the facility's life, and its calculation formula is as follows:

[0065]

[0066] In the formula, CAPEX i OPEX is the cost of capital defined in the capital and operating cost composition model. j The various operating costs defined in the capital and operating cost composition model; L plant Total facility lifespan (years); T operating The annual operating time is [number].

[0067] Univariate sensitivity analysis typically ensures that changing specific parameters results in an arithmetic or geometrical relationship between the pessimistic, baseline, and optimistic parameters, i.e., according to the following formula:

[0068] a i,pessimistic =a i,basic f i ,a i,optimistic =a i,basic f i -1

[0069] a i,pessimistic =a i,basic +f i ,a i,optimistic =a i,basic -f i

[0070] In the formula a i It can represent any parameter from the operations, marketing, or technical parameter groups; a i The subscripts represent the pessimistic, baseline, and optimistic parameters, respectively; f i For sensitivity analysis factors;

[0071] Change a alone i After performing the above model calculations on the baseline, optimistic, and pessimistic values, a can be quantitatively analyzed. i For target parameters The degree of influence is given by the following formula:

[0072]

[0073] In this method, the average production cost of the product is selected. The target parameter is R.

[0074] Taking the glycerol oxidation anode substitution reaction carbon dioxide electrochemical reduction for formic acid production system based on a compact membrane-free reactor developed and designed in a certain laboratory as an example, the effects of the present invention are illustrated:

[0075] Step 1: Summarize and draw the system flowchart, mainly including schematic diagrams of the traditional and improved electrolytic cell structures and energy and material flow, and reasonably assume supporting equipment and process technology. (See...) Figure 2 , Figure 3 )

[0076] Step 2: Determine appropriate operating parameters, market parameters, and suitable technical parameters based on laboratory test data. (See Tables 1, 2, and 3)

[0077] Step 3: Using the method of this invention, establish a suitable mathematical model for the economic analysis of the carbon dioxide electrochemical reduction system, and solve it to obtain the composition of the system's capital and operating costs and the target parameters for evaluating the overall economic efficiency.

[0078] Under the same operating parameter group and market parameter group, the economics of four electrolyzer systems—AEM-CO2R / OER, AEM-CO2R / GOR, membrane-free CO2R / GOR, and membrane-free compact CO2R / GOR—were calculated and compared (see [link to relevant documentation]). Figure 4 );

[0079] The impact of grid electricity price and carbon emission price on the economics of the membraneless compact CO2R / GOR electrolyzer system under different combinations of grid electricity price and high and low carbon emission price was studied (see [link]). Figure 5 );

[0080] Univariate sensitivity analysis (parameter set shown in Table 4) was used to quantitatively analyze the impact of certain market and technical parameters on the system's economics (see Table 4). Figure 6 ).

[0081] Table 1. Basic Parameters

[0082]

[0083]

[0084] *MEA refers to membranes and catalysts.

[0085] Table 2. Experimental electrolysis voltages of four CO2 electrolyzers at a current density of 0.1 A cm⁻²

[0086]

[0087]

[0088] Table 3. Electricity Prices and Carbon Emission Factors in Major Regions

[0089] power grid Electricity price ($kWh - 1) <![CDATA[Carbon emission factor (kgCO2 kWh -1 )]]> Region 1 0.089 0.602 Region 2 0.151 0.365 Region 3 0.152 0.226 Regional renewable electricity 0.071 0.037

[0090] *As of the end of 2023, the carbon emission price in a regional trading market was US$11.05. CO2 -1 The carbon emission price in the third regional trading market is US$104.62. CO2 -1 ).

[0091] Table 4. Baseline, optimistic, and pessimistic parameters used for univariate sensitivity analysis

[0092] parameter unit pessimism value Baseline value Optimism Electricity price <![CDATA[US$kWh -1 ]]> 0.2 0.15 0.1 Glycerin purchase price <![CDATA[US$ton -1 ]]> 900 600 300 Battery voltage V 3.308 2.308 1.308 CO2 purchase price <![CDATA[US$ton -1 ]]> 60 40 20 Stack cost <![CDATA[US$m -2 ]]> 6450 4300 2150 Cathode selectivity ％ 80 90 100 Anode selectivity ％ 60 80 100

[0093] It will be understood by those skilled in the art that embodiments of the present invention may be provided as methods, systems, or computer program products. Thus, the present invention may take the form of an entirely hardware embodiment, an entirely software embodiment, or an embodiment combining software and hardware. Furthermore, the present invention may take the form of a computer program product implemented on one or more computer-usable storage media (including but not limited to magnetic disk storage, CD-ROM, optical storage, etc.) containing computer-usable program code.

[0094] 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 a process or multiple processes and / or boxes Figure 1 A device that provides the functions specified in one or more boxes.

[0095] These computer program instructions may also be stored in a computer readable memory that can direct a computer or other programmable data processing device to work in a specific manner, so that the instructions stored in the computer readable memory produce an article of manufacture comprising an instruction device, which implements the process Figure 1 a process or multiple processes and / or boxes Figure 1 The function specified in one or more boxes.

[0096] These computer program instructions can also be loaded onto a computer or other programmable data processing device so that a series of operational steps are executed on the computer or other programmable device to produce a computer-implemented process, thereby providing the instructions executed on the computer or other programmable device for implementing the process. Figure 1 a process or multiple processes and / or boxes Figure 1 A step that specifies a function in one or more boxes.

[0097] Specific embodiments of the present invention have been described above. It should be understood that the present invention is not limited to the specific embodiments described above, and those skilled in the art can make various changes or modifications within the scope of the claims, which do not affect the essence of the present invention.

[0098] All modifications and equivalent substitutions made within the spirit and principles of the invention should be included within the scope of protection of the invention.

Claims

1. A design and evaluation method for carbon dioxide electrochemical reduction systems based on techno-economic analysis, characterized in that, include: 1) Draw a flowchart of the preliminary design of the carbon dioxide electrochemical reduction system, clarify the design products, clarify the composition and operating principle of each component of the system, and determine the path and direction of energy flow and material flow in the system; The flowchart includes: carbon dioxide capture and purification process, carbon dioxide electrochemical reduction process, gas-liquid product separation process, electrolyte solution regeneration process, carbon dioxide / carbonate separation and recovery process, gas product compression, storage and utilization process, and liquid product storage, processing and utilization process; the composition and operating principle of each component of the system include: gas pressure swing adsorption equipment and pressure swing adsorption process for gas product separation and recovery, distillation equipment and distillation process for liquid product separation and recovery, as well as electrolytic cell membrane electrode components, electrolyte composition and electrode reactions; 2) Combining the system flow diagram and energy and material flow information determined in step 1), construct a technical and economic analysis model for the carbon dioxide electrochemical reduction system, including: an electrolyzer operating status model, a capital and operating cost composition model, and a financial summary analysis model; 3) Determine the operating parameters, market parameters, and technical parameters of the carbon dioxide electrochemical reduction system, and use them as model inputs. Based on the technical and economic analysis results of the system output by the model, optimize or evaluate the design of the initially designed carbon dioxide electrochemical reduction system.

2. The design and evaluation method for carbon dioxide electrochemical reduction systems based on techno-economic analysis according to claim 1, characterized in that, The electrolyzer operating state model is used to describe the energy and material flow through the electrolyzer under operating and technical parameters, including the total current I of the electrolyzer. total The mass flow rate of carbon dioxide required to participate in the electrode reaction to achieve the designed yield. and the mass flow rate of the anolyte reactant N reactant CO2 mass flow rate at the inlet of the electrolytic cell mass flow rate of anolyte reactant and CO2 mass flow rate at the electrolyzer outlet mass flow rate of anolyte reactant 3. The design and evaluation method for carbon dioxide electrochemical reduction systems based on techno-economic analysis according to claim 2, characterized in that, The electrolytic cell operating state model is as follows: In the formula, Y d The design yield is given by: F, Faraday constant; M, molar mass of the substance molecule corresponding to the subscript; FE, electrode selectivity of the corresponding subscript; Z, number of electrons transferred to generate 1 mol of product molecules corresponding to the subscript when reactants undergo oxidation / reduction to produce products; V, electrolysis voltage; n, number of product molecules generated by consuming 1 molecule of the substance corresponding to the subscript; SPC, single-pass conversion rate; r, proportion of the substance corresponding to the subscript that does not directly participate in the electrode reaction and flows directly out of the reactor after entering the electrode inlet; ρ p The product density at a given temperature and pressure; x p This represents the volume fraction of the product in the electrolyte.

4. The design and evaluation method for a carbon dioxide electrochemical reduction system based on techno-economic analysis according to claim 1, characterized in that, The aforementioned capital and operating cost composition model is based on the electrolyzer operating status model, utilizing its model parameters and market parameters to obtain various economic indicators of the system, including capital costs and operating costs. The capital costs include the electrolyzer capital cost (CAPEX). electrolyzer Auxiliary equipment capital cost (CAPEX) BOP The capital cost (CAPEX) of the equipment corresponding to separation process i separation,i Operating costs include the electricity cost of the electrolyzer (OPEX). electricity OPEX (Oil Carbon Emission Cost) of Electrolyzer emission The maintenance and replacement cost (OPEX) corresponding to equipment j maintenance,j Raw material procurement cost OPEX reactant The equipment operating cost (OPEX) corresponding to separation process i separation,i .

5. The design and evaluation method for carbon dioxide electrochemical reduction systems based on techno-economic analysis according to claim 4, characterized in that, The aforementioned capital and operating cost composition model is as follows: CAPEX electrolyzer =c stack A total OPEX electricity =P total p e OPEX emission =P total f emission p emission OPEX maintenance,j =CAPEX j ·r maintenance,j OPEX reactant =N reactant p reactant In the formula c stack For stack cost; A total r is the total area of ​​the electrodes in the electrolytic cell. BOP The proportion of auxiliary equipment costs; CAPEX separation,i,r The rated capital cost of the equipment corresponding to separation process i; The volumetric flow rate of the gas / liquid substance that needs to undergo separation process i; The rated gas / liquid volumetric flow rate of the equipment corresponding to separation process i; f capex,i P represents the capital cost load factor corresponding to separation process i; total p represents the total power of the electrolytic cell. e For electricity price; f emission p is the power grid emission factor. emission For carbon emission prices; CAPEX j The capital cost corresponding to equipment j that requires maintenance and replacement; r maintenance,j For equipment j requiring maintenance and replacement, the maintenance and replacement cost is the percentage of the equipment's capital cost within each maintenance and replacement cycle; p is the market price of the corresponding raw material; OPEX separation,i,r f is the rated operating cost of the equipment corresponding to separation process i; opex,i This is the operating cost load ratio factor corresponding to separation process i.

6. The design and evaluation method for a carbon dioxide electrochemical reduction system based on techno-economic analysis according to claim 1, characterized in that, The financial summary analysis model includes evaluating the overall economic efficiency of the system using the average production cost of the target parameter product, which is the ratio of the total cost over the facility's life to the total designed output over the facility's life. The calculation formula is as follows: In the formula, CAPEX i OPEX represents the various capital costs in the capital and operating cost composition model. j The various operating costs in the capital and operating cost composition model; L plant For the total lifespan of the facility; T operating The annual operating time is [number].

7. A design and evaluation system for a carbon dioxide electrochemical reduction system based on techno-economic analysis, characterized in that, For implementing the techno-economic analysis-based design and evaluation method for a carbon dioxide electrochemical reduction system as described in any one of claims 1-6, the system comprises: The model determination module is used to determine the techno-economic analysis model of the carbon dioxide electrochemical reduction system based on the input system flow diagram and energy flow and material flow information, including the electrolyzer operating status model, the capital and operating cost composition model, and the financial summary model. The results analysis module is used to output the techno-economic analysis results of the system based on the input operating parameters, market parameters, and technical parameters of the carbon dioxide electrochemical reduction system.

8. A computer-readable storage medium having a computer program stored thereon, characterized in that, When executed by a processor, the program implements the design and evaluation method for a carbon dioxide electrochemical reduction system based on techno-economic analysis as described in any one of claims 1-6.

9. An electronic device, characterized in that, The device includes: One or more processors; Memory, used to store one or more programs; When the one or more programs are executed by the one or more processors, the one or more processors implement the design and evaluation method for carbon dioxide electrochemical reduction systems based on techno-economic analysis as described in any one of claims 1-6.

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