A method for calculating the thermodynamic performance of temperature swing adsorption carbon capture with multi-node desorption

Abstract

The present invention discloses a method for calculating the thermodynamic performance of temperature-swing adsorption carbon capture with multi-node desorption, comprising: defining adsorption bed parameters, dividing the adsorption bed to obtain a number of discrete nodes, solving the heat and mass transfer equations for the discrete units to obtain the final adsorption state parameters; constructing the thermodynamic cycle corresponding to each discrete point based on the final adsorption state parameters, and calculating the cycle parameters of each thermodynamic cycle process; and obtaining the overall thermodynamic performance parameters of the adsorption bed cycle process based on the final adsorption state parameters and the cycle parameters. The present invention fully considers the non-uniform CO2 adsorption capacity distribution inside the adsorption bed during the actual adsorption process, overcomes the lumped model deviation problem caused by the nonlinear solution of parameters such as the minimum separation work recovery rate, and helps to obtain more accurate energy consumption and consumption results for the carbon capture process. At the same time, it reveals the distribution law of the non-uniform temperature field, heat field and quantity field inside the adsorption bed, and promotes the optimal matching design of the desorption temperature field.

Description

Technical Field

[0001] The present invention belongs to the field of carbon capture thermodynamic performance, and in particular relates to a method for calculating the thermodynamic performance of temperature-swing adsorption carbon capture with multi-node desorption. Background Art

[0002] Carbon capture technology is an important way to alleviate and control carbon dioxide emissions. Among them, the adsorption method uses solid adsorbents, which greatly reduces the impact on the environment compared to the absorbent chemical absorption method. It also has the advantages of low regeneration heat consumption and less equipment required. It has become one of the most mature demonstration technologies at present.

[0003] During the entire adsorption capture process, the heat and work required for the desorption process are the main factors affecting the thermal performance of the entire capture device. In terms of theoretical analysis, the energy consumption evaluation of the capture process is usually based on the solution of the adsorption model and the solid-gas heat and mass transfer equations in the adsorption-desorption process. Efficiency evaluation, the carbon pump cycle model based on the minimum separation work can be used to characterize the energy efficiency of the capture process from the perspective of the efficiency of the second law of thermodynamics. It is worth noting that in order to prevent CO2 overflow, the adsorption process usually ends before the breakthrough point, and there is usually a non-uniform decreasing distribution of CO2 adsorption capacity in the axial direction inside the adsorption bed, that is, the CO2 adsorption capacity near the inlet is higher than that at the outlet. Based on this, there is a non-uniform CO2 adsorption capacity field in the adsorption bed at the end of adsorption. When the high-temperature desorption process is completed, the recovery rates of different adsorption capacity areas of the adsorption bed will be different. The power consumption of the capture and separation process, especially the minimum separation work and the recovery rate, are not simply linearly related. This makes it so that if the minimum separation work of the separation process is calculated according to the average recovery rate of the capture process, it will cause a certain deviation.

[0004] On the other hand, since the adsorption of adsorbent materials at different positions occurs at different times, after the adsorption operation is completed, the temperature of the adsorbent material near the cavity outlet is significantly different from that near the inlet, and the adsorption bed as a whole will present a non-uniform temperature field. The desorption heat consumption of the entire adsorption-desorption process and Energy consumption cannot be evaluated according to the adsorption temperature and partial pressure under completely ideal adsorption conditions. Therefore, how to establish a thermodynamic model of the real capture process for non-uniform CO2 adsorption capacity and temperature distribution to more accurately evaluate its energy consumption and Consumption needs further exploration.

[0005] There is a thermodynamic carbon pump cycle construction method for indirect heat exchange and temperature swing adsorption carbon capture technology in the existing technology. The thermodynamic research method is applied to the field of carbon capture technology. Based on the physical properties of the adsorbent material, adsorption phase and flue gas in the circulation system, a thermodynamic carbon pump cycle process is constructed. The process is presented in the relationship between CO2 adsorption amount-CO2 partial pressure-temperature. The basic construction method of the carbon pump cycle is proposed, which provides a thermodynamic energy efficiency evaluation scheme for the design of the indirect heat exchange and temperature swing adsorption carbon capture system. However, the model still has certain deficiencies. After the adsorption is completed, the adsorption amount of the material is stripped off during the actual adsorption process, and the adsorption amount is calculated by the ideal adsorption temperature and partial pressure value, resulting in the non-uniform adsorption capacity distribution in the adsorption bed being ignored, further making the minimum separation work and The calculation of efficiency is biased, which affects energy consumption and Impact on consumption assessment.

[0006] Another evaluation method for the thermal energy utilization efficiency of temperature swing adsorption carbon capture technology has completed a complete benchmarking through the steps of benchmarking process - clarifying the evaluation object - setting boundaries - collecting and analyzing data - performance evaluation, thus forming an empirical analysis system for the thermal energy utilization efficiency of temperature swing adsorption carbon capture technology. The evaluation framework and standard experimental methods of temperature swing adsorption carbon capture under different boundaries were benchmarked, providing a reasonable benchmark for the integration of the overall framework of carbon capture energy efficiency analysis. However, the calculation of capture energy consumption in this method is still not detailed enough, and the unit capture energy consumption and The efficiency is obtained by the lumped model, and the experimental benchmarking method can only obtain the temperature and concentration values ​​of a limited number of measurement points. The evaluation of the energy consumption changes and the distribution of non-uniform field quantities in the actual capture process is still not comprehensive enough. Summary of the Invention

[0007] In order to solve the above technical problems, the present invention proposes a method for calculating the thermodynamic performance of temperature swing adsorption carbon capture with multi-node desorption to solve the problems existing in the above-mentioned prior art.

[0008] To achieve the above objectives, the present invention provides a method for calculating the thermodynamic performance of temperature swing adsorption carbon capture with multi-node desorption, comprising:

[0009] Define the adsorption bed parameters, divide the adsorption bed into nodes, obtain several discrete nodes, solve the heat and mass transfer differential equations for several discrete units based on the adsorption bed parameters, and obtain the final adsorption state parameters;

[0010] Constructing adsorption-desorption cycle processes corresponding to a plurality of discrete points based on the final adsorption state parameters, and calculating the thermodynamic cycle parameters of each adsorption-desorption cycle process;

[0011] The overall thermodynamic performance parameters of all node unit cycle processes are calculated based on the final adsorption state parameters and the thermodynamic cycle parameters.

[0012] Optionally, the process of obtaining the final adsorption state parameters includes:

[0013] Based on the adsorption bed parameters, the heat and mass transfer differential equations are solved for several discrete units respectively to obtain the final adsorption state parameters, wherein the heat and mass transfer differential equations include the adsorption equation, the mass balance equation, the energy balance equation, and the momentum balance equation; the final adsorption state parameters include but are not limited to the non-uniform adsorption CO2 capacity inside the adsorption bed and the adsorption material temperature; the energy balance equation includes the gas phase energy balance equation, the solid phase adsorption material energy balance equation, the cooling tube wall energy balance equation, and the cooling fluid energy balance equation.

[0014] Optionally, the CO2 adsorption amount distribution of each node unit at different temperatures and partial pressures is calculated using the adsorption isotherm equation.

[0015] Optionally, the thermodynamic cycle parameters include the CO2 desorption amount, recovery rate, minimum separation work, desorption heat consumption, desorption heat consumption.

[0016] Optionally, the desorption heat consumption of a single node is calculated based on the final desorption temperature of the node, the material temperature at the final moment of the adsorption stage, the container volume, the adsorption material volume, the desorption latent heat of each gas component, the container density and specific heat capacity, and the adsorption material density and specific heat capacity using the following formula:

[0017]

[0018] Where Q des.j , T des.j , T s.j , V wall.j , V s.j , Δq i.j , ΔH i are the desorption heat consumed by desorption node j, the final desorption temperature, the material temperature in the final adsorption stage, the container wall volume, the adsorption material volume, the desorption capacity of different node unit components i, and the desorption latent heat, ρ w ,ρ s are the container density and adsorption material density, C pw , C pg , C ps They are the specific heat capacity of the container wall, the specific heat capacity of the gas component and the specific heat capacity of the adsorption material.

[0019] Optionally, the desorption heat is calculated based on the desorption heat consumed by the node, the ambient temperature and the desorption temperature. consumption.

[0020] Optionally, the overall thermodynamic performance parameters include total recovery rate, specific heat consumption, minimum separation work, specific Consumption, efficiency.

[0021] Optionally, the process of obtaining the overall thermodynamic performance parameters includes: taking the ratio of the sum of the CO2 desorption capacity of each node to the sum of the adsorption capacity as the total recovery rate; calculating the specific heat consumption based on the sum of the heat consumed by each node and the sum of the CO2 desorption capacity of each node; calculating the minimum separation work of the node based on the initial carbon dioxide concentration, recovery rate, and separation temperature, and calculating the minimum separation work in the carbon capture process from the sum of the minimum separation work of each node; calculating the desorption heat of each node based on the calorific value, desorption temperature value and ambient temperature value. Amount, based on the CO2 desorption amount and desorption heat of each node The calculation of the energy consumption, the energy consumption of filling and the energy consumption of vacuuming is used to obtain the ratio Consumption; Based on minimum separation work and ratio The consumption ratio is calculated efficiency.

[0022] Alternatively, the minimum separation work for CO2 desorption within a single node unit is obtained based on the initial carbon dioxide concentration, the node recovery rate, and the separation temperature, as follows:

[0023]

[0024] Compared with the prior art, the present invention has the following advantages and technical effects:

[0025] The present invention defines adsorption bed parameters, divides the adsorption bed into nodes, obtains a plurality of discrete nodes, solves heat and mass transfer differential equations for the plurality of discrete nodes respectively, and obtains final adsorption state parameters; constructs adsorption-desorption cycle processes corresponding to the plurality of discrete points based on the final adsorption state parameters, and calculates and obtains thermodynamic cycle parameters of each adsorption-desorption cycle process; and calculates and obtains overall thermodynamic performance parameters of all cycle processes based on the final adsorption state parameters and the thermodynamic cycle parameters.

[0026] The multi-node desorption carbon capture process thermodynamic performance calculation method proposed in this invention fully considers the non-uniform capacity distribution inside the adsorption bed during the actual adsorption process. Compared with the traditional lumped model, the multi-node desorption model overcomes the lumped model deviation problem caused by the nonlinear solution of parameters such as the minimum separation work and recovery rate, which helps to obtain more accurate energy consumption and At the same time, the multi-node thermodynamic model can effectively reveal the temperature field, heat field and The distribution law of the quantity field is analyzed, thereby promoting the optimal matching design of the desorption temperature field and reducing the desorption energy consumption. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] The accompanying drawings, which constitute part of this application, are intended to provide a further understanding of this application. The exemplary embodiments and descriptions of this application are intended to explain this application and do not constitute an improper limitation on this application. In the accompanying drawings:

[0028] Figure 1 Schematic diagram of a method flow in an embodiment of the present invention;

[0029] Figure 2 This is a schematic diagram of the axial node division of the adsorption bed according to an embodiment of the present invention;

[0030] Figure 3 Schematic diagram of a multi-node desorption thermodynamic cycle model according to an embodiment of the present invention; Description of the drawings:

[0032] 1. Adsorption bed inlet, 2. Adsorption bed outlet, 3. Adsorption bed node unit, 4. Container wall, 5. Fluid pipeline. DETAILED DESCRIPTION

[0033] It should be noted that, in the absence of conflict, the embodiments and features of the embodiments in this application can be combined with each other. The present application will be described in detail below with reference to the accompanying drawings and in combination with the embodiments.

[0034] It should be noted that the steps shown in the flowcharts of the accompanying drawings can be executed in a computer system such as a set of computer-executable instructions, and that, although a logical order is shown in the flowcharts, in some cases, the steps shown or described can be executed in an order different from that shown here.

[0035] Example 1

[0036] like Figure 1 As shown, this embodiment provides a method for calculating the thermodynamic performance of temperature swing adsorption carbon capture with multi-node desorption, including:

[0037] The adsorption and desorption processes are separated independently. First, the adsorption bed parameters are defined. By solving the adsorption equation and the mass, energy, and momentum balance equations, the overall state parameters of the adsorption bed at the end of adsorption are obtained, including CO2 adsorption capacity, adsorption material temperature, gas phase concentration, temperature and other parameters.

[0038] Specifically,

[0039] The adsorption capacity of the components can be obtained by fitting the extended Langmuir equation, as shown in formula (1):

[0040]

[0041] In formula (1), is the CO2 equilibrium adsorption amount corresponding to the CO2 partial pressure value during the adsorption process, T is the adsorption temperature value, P i is the gas partial pressure of component i, IP 1i ~IP 4i is the adsorption fitting parameter of component i.

[0042] The mass balance equation of component i during the adsorption process is:

[0043]

[0044] In formula (2), ε b and ε p are the porosity of the adsorption bed and particles, respectively, c i is the molar density of component i, ρ b is the bulk density of the adsorption material, u is the superficial velocity of the gas, and t is the adsorption time.

[0045] The mass transfer process of the components in the adsorption process can be obtained by the linear driving force equation as shown below:

[0046]

[0047] In formula (3), k LDF.i is the linear driving force coefficient of component i in the mixed gas, q i is the adsorption phase concentration of component i.

[0048] During the adsorption process, the gas phase energy balance equation is:

[0049]

[0050] The energy balance equation of solid adsorption material is:

[0051]

[0052] In formula (4) and formula (5), k g , k s are the thermal conductivities of gas and adsorbent material, C pg and C ps are the specific heat capacities of gas and adsorbent material, T g , T s and T w are the temperatures of gas, adsorption material and tube wall respectively, h f , h w is the heat transfer coefficient between gas, adsorption material and cooling tube wall, α p is the specific surface area of ​​the adsorption material, D b is the inner diameter of the cooling tube, ΔHi is the adsorption heat of component i.

[0053] During the adsorption process, the cooling fluid flows in the cooling tube and continuously takes away the adsorption heat released by the adsorption bed. The energy balance equation of the cooling tube wall is:

[0054]

[0055] Furthermore, the cooling fluid energy balance equation is:

[0056]

[0057] In formulas (6) and (7), k w and k m is the thermal conductivity of the tube wall and cooling fluid, C pw and C pm are the specific heat capacities of the cooling tube wall and the cooling fluid, T m is the temperature of the cooling fluid, ρ w and ρ m is the density of the cooling tube wall and the cooling fluid, h m is the heat transfer coefficient between the cooling fluid and the cooling tube wall, α HX is the specific area of ​​the cooling tube, W l is the thickness of the cooling tube wall.

[0058] The momentum transfer equation during the adsorption process is:

[0059]

[0060] In formula (7), P is the gas pressure in the adsorption bed, M is the molar mass of the gas, μ is the viscosity of the gas, and r p is the particle radius of the adsorption material.

[0061] The energy, mass, and momentum balance equations (1) to (8) in the adsorption process can be obtained by directly solving partial differential equations or by process simulation software such as Aspen Adsorption. To prevent CO2 overflow, the adsorption end time t should not be later than the breakthrough time.

[0062] Equations (1) to (8) in this embodiment are only used to solve the adsorption process. By dividing the axial adsorption bed into m units, parameters such as the non-uniform adsorption capacity of CO2 in the adsorption bed and the temperature of the adsorption material at the end of adsorption are obtained.

[0063] Furthermore, based on the final state parameters of adsorption, m cyclic processes are constructed, corresponding to the adsorption-desorption process of each node from the inlet to the outlet of the adsorption bed. For variable temperature vacuum adsorption, since heating and vacuuming operations are usually carried out simultaneously during the actual desorption process, each cyclic process can be simplified into a triangular cycle. The initial point of each independent cycle is recorded as point 1, point 2, point 3...point m. Therefore, the cyclic process for any point j can be recorded as j—j'(heating and vacuuming desorption)—j" (cooling and pressurizing)—j (adsorption), where j is the final adsorption state point of the node after the adsorption step, j' is the state point of the adsorption bed unit corresponding to the end of the heating and desorption process, and j" is the state point before the adsorption process after the adsorption bed is cooled and pressurized.

[0064] If the final adsorption capacity of adsorption bed node j is q r.j After the heating and desorption is completed, the remaining CO2 adsorption capacity of node j is q min.j , then the CO2 desorption amount at node j is as follows:

[0065] Δq j =q r.j -q min.j (9)

[0066] Since the adsorption operation ends before the breakthrough time point, it can be assumed that the CO2 in the mixed gas is completely absorbed. The recovery rate formula for each node is as follows:

[0067]

[0068] The desorption heat of adsorption bed unit j mainly includes the sensible heat of the adsorbent, the latent heat of the adsorption phase and the sensible heat of the reaction vessel wall. The calculation formula is as follows:

[0069]

[0070] In formula (11), Q des.j , T des.j , T s.j , V wall.j , V s.j , Δq i.j , ΔH i are the desorption heat consumed by desorption node j, the final desorption temperature, the material temperature in the final adsorption stage, the container volume, the adsorption material volume, the desorption capacity of different node unit components i, and the desorption latent heat. w , ρ s are the container density and adsorption material density, respectively.

[0071] V wall.j , V s.j It can be obtained from the total volume of the container, the total volume of the adsorption material and the total number of divided units m:

[0072] V wall.j =V wall / m (12)

[0073] V s.j =V s / m (13)

[0074] The total recovery rate of the capture process can be calculated by the ratio of the sum of CO2 desorption and adsorption at each node:

[0075]

[0076] The specific heat consumption of the desorption process can be obtained by the ratio of the total heat consumed by each unit node to the total CO2 desorption amount of each node:

[0077]

[0078] The minimum separation work for desorption of CO2 in adsorption bed unit j can be obtained from the initial concentration of carbon dioxide, the recovery rate of the node and the separation temperature, as shown in formula (16):

[0079]

[0080] Similar to the specific heat consumption, the minimum separation work of the capture process can be calculated by the ratio of the sum of the minimum separation work of each node to the total CO2 desorption amount:

[0081]

[0082] The adsorption bed unit j is brought by the desorption heat The amount consumed can be determined by the desorption heat Q des.j , desorption temperature value and ambient temperature value are obtained:

[0083] Qx des.j =Q des.j (1-T0 / T des.j ) (18)

[0084] Heat removal In addition to the energy consumption, for variable temperature vacuum adsorption, the energy consumption during the inflation and vacuuming stages is:

[0085]

[0086] In formulas (19) and (20), W comp , W vac are compression power consumption and vacuum pump power consumption respectively; η comp , η vac is the operating efficiency of the compressor and vacuum pump; k gas is the polyvariability index, the value is 1.4; P feed , Pvac , P atm are respectively inflation pressure, vacuum pressure and atmospheric pressure; y CO2 is the gas concentration of CO2 in the initial mixed gas.

[0087] Therefore, the ratio of the cyclic process The consumption can be obtained from formula (21):

[0088]

[0089] Furthermore, the capture process The efficiency is:

[0090] η ex.total =W min.total / Ex total 100% (22)

[0091] Specifically, based on the final adsorption state parameter distribution of the adsorption bed, the adsorption bed is divided into m nodes along the axial direction, and m temperature-swing vacuum adsorption cycles with different initial adsorption capacities are constructed respectively. By solving the parameters such as desorption capacity, recovery rate and minimum separation work of each cycle, the overall thermodynamic performance parameters of the entire cycle process are finally obtained. The effect of dividing the adsorption bed along the axial direction is as follows: Figure 2 As shown, in this embodiment, m is 100.

[0092] like Figure 3 As shown in the figure, the multi-node desorption thermodynamic model uses the adsorption bed node unit parameters in the final adsorption state as the initial point to construct the thermodynamic cycle. The number of nodes divided axially in the adsorption bed is marked as 1, 2, 3...100, 1-1' is the heating and vacuum desorption process, 1'-1" is the cooling and pressurization process, and 1"-1 is the adsorption process. Similarly, 2-2', 2'-2"... until 100-100', 100'-100" correspond to the cycle processes of different nodes.

[0093] The above 1', 2'...100' are the final states of each node after the desorption step is completed. Assuming that each adsorption bed unit has completely reached the desorption temperature value after the desorption is completed, the remaining CO2 adsorption capacity in this state can be considered equal. The CO2 adsorption capacity q min It can be calculated by equation (1), namely

[0094]

[0095] Where, T des is the desorption temperature, P i is the gas partial pressure of component i, IP 1i ~IP 4iis the adsorption fitting parameter of component i. In this embodiment, taking solid adsorption material zeolite-13X as an example, its adsorption of CO2 fitting IP 1i ~IP 4i The values ​​are 2.88e-7, 3574, 6.18e-5, and 3603, respectively, and the adsorption N2 fitting IP 1i ~IP 4i The values ​​are 7.18e-7, 1670, 6.21e-4, and 1359 respectively. Partial pressure P i The value is determined by the gas concentration in the adsorption bed and the vacuum pressure value P after the adsorption is completed. vac Sure.

[0096] When the vacuum pressure P vac When the pressure is 1 bar, the cycle process can represent the traditional temperature swing adsorption process, and the heating and desorption heat can come from solar energy, waste heat or electric heat conversion devices.

[0097] Taking the capture of CO2 (15% CO2, 85% nitrogen) from flue gas as an example, the specific calculation method of the multi-node desorption thermodynamic cycle is further explained:

[0098] Adsorption process: Figure 2 As shown in the figure, air containing 15% CO2 concentration, with a total air pressure of 1.5 bar and a temperature of 298K, is introduced from the adsorption bed inlet 1, and the unadsorbed nitrogen flows out from the adsorption bed outlet 2 on the other side. The adsorption time is 1000s. The heat released during the CO2 adsorption process is taken away by the cooling fluid in the pipeline 5. At the end of adsorption, the CO2 adsorption capacity q1~q 100 Reduced from 2.95 to 1.47 mol / kg.

[0099] Heating and desorption (vacuuming) process: The adsorption bed obtains heat through hot fluid or electric heating, and the temperature of each adsorption bed node 3 and the container wall 4 gradually increases. When the temperature of the adsorption bed rises to the desorption temperature of 353K and the vacuum pressure drops to 0.1 bar, the actual adsorption amount of each node unit is higher than the saturated adsorption amount at the temperature and pressure. Therefore, the CO2 in each adsorption unit will be gradually released. The CO2 capacity desorbed by node units 1 to 100 is in the range of 1.43 to 2.92 mol / kg, the heat required for nodes 1 to 100 is in the range of 6.66 to 10.27 kJ, the recovery rate is in the range of 97.51 to 98.71%, and the minimum separation work is in the range of 6.754 to 6.844 kJ / mol.

[0100] Cooling and pressurization process: When the adsorption bed temperature reaches the desorption temperature of 353K, the cooling fluid flows through the cooling pipe again, and the adsorption bed temperature gradually drops to the ambient temperature. Each node unit returns from the 1'~100' state to the 1"~100" state, thus continuing the next cycle.

[0101] According to formulas (14), (15), (17), (21), and (22), the total recovery rate in this embodiment is 98.26%, the specific heat consumption is 111.9 kJ / mol, the minimum separation work is 6.810 kJ / mol, and the specific heat consumption is 111.9 kJ / mol. The consumption is 29.1kJ / mol, The efficiency is 23.4%.

[0102] The above are merely preferred embodiments of the present application, but the scope of protection of the present application is not limited thereto. Any changes or substitutions that can be easily conceived by a person skilled in the art within the technical scope disclosed in this application should be included in the scope of protection of the present application. Therefore, the scope of protection of the present application should be based on the scope of protection of the claims.

Claims

1. A method for calculating thermodynamic performance of temperature swing adsorption carbon capture with multi-node desorption, characterized in that: The following steps are involved: Define the adsorption bed parameters, divide the adsorption bed into nodes, obtain several discrete nodes, solve the heat and mass transfer differential equations for several discrete units based on the adsorption bed parameters, and obtain the final adsorption state parameters; Constructing adsorption-desorption cycle processes corresponding to a plurality of discrete points based on the final adsorption state parameters, and calculating the thermodynamic cycle parameters of each adsorption-desorption cycle process; The overall thermodynamic performance parameters of all node unit cycle processes are calculated based on the final adsorption state parameters and the thermodynamic cycle parameters; The thermodynamic cycle parameters include the CO2 desorption amount, recovery rate, minimum separation work, desorption heat consumption, desorption heat consumption, and desorption heat consumption corresponding to each node unit. consumption; The desorption heat consumption of a single node is calculated based on the final desorption temperature of the node, the material temperature at the end of the adsorption phase, the container volume, the adsorption material volume, the desorption latent heat of each gas component, the container density and specific heat capacity, and the adsorption material density and specific heat capacity using the following formula: Where Q des.j , T des.j , T s.j , V wall.j , V s.j , Δq i.j , ΔH i are the desorption heat consumed by desorption node j, the final desorption temperature, the material temperature in the final adsorption stage, the container wall volume, the adsorption material volume, the desorption capacity of different node unit components i, and the desorption latent heat, ρ w ,ρ s are the container density and adsorption material density, C pw , C pg , C ps are the specific heat capacity of the container wall, the specific heat capacity of the gas component and the specific heat capacity of the adsorption material, respectively, and M is the molar mass of the gas.

2. The method for calculating thermodynamic performance of temperature swing adsorption carbon capture with multi-node desorption according to claim 1, characterized in that: The process of obtaining the final adsorption state parameters includes: Based on the adsorption bed parameters, the heat and mass transfer differential equations are solved for several discrete units respectively to obtain the final adsorption state parameters, wherein the heat and mass transfer differential equations include the adsorption equation, the mass balance equation, the energy balance equation, and the momentum balance equation; the final adsorption state parameters include but are not limited to the non-uniform adsorption CO2 capacity inside the adsorption bed and the adsorption material temperature; the energy balance equation includes the gas phase energy balance equation, the solid phase adsorption material energy balance equation, the cooling tube wall energy balance equation, and the cooling fluid energy balance equation.

3. The method for calculating thermodynamic performance of temperature swing adsorption carbon capture with multi-node desorption according to claim 2, characterized in that: The CO2 adsorption distribution of each node unit at different temperatures and partial pressures is calculated using the adsorption isotherm equation.

4. The method for calculating thermodynamic performance of temperature swing adsorption carbon capture with multi-node desorption according to claim 1, characterized in that: The desorption heat is calculated based on the desorption heat consumed by the node, the ambient temperature and the desorption temperature. consumption.

5. The method for calculating thermodynamic performance of temperature swing adsorption carbon capture with multi-node desorption according to claim 1, characterized in that: The overall thermodynamic performance parameters include total recovery rate, specific heat consumption, minimum separation work, specific Consumption, efficiency.

6. The method for calculating thermodynamic performance of temperature swing adsorption carbon capture with multi-node desorption according to claim 5, characterized in that: The process of obtaining the overall thermodynamic performance parameters includes: taking the ratio of the sum of the CO2 desorption capacity of each node to the sum of the adsorption capacity as the total recovery rate; calculating the specific heat consumption based on the sum of the heat consumed by each node and the sum of the CO2 desorption capacity of each node; calculating the minimum separation work of the node based on the initial concentration of carbon dioxide, recovery rate, and separation temperature, and calculating the minimum separation work in the carbon capture process from the sum of the minimum separation work of each node; calculating the desorption heat of each node based on the calorific value, desorption temperature value and ambient temperature value. Amount, based on the CO2 desorption amount and desorption heat of each node The calculation of the energy consumption, the energy consumption of filling and the energy consumption of vacuuming is used to obtain the ratio Consumption; Based on minimum separation work and ratio The consumption ratio is calculated efficiency.

7. The method for calculating thermodynamic performance of temperature swing adsorption carbon capture with multi-node desorption according to claim 6, characterized in that: The minimum separation work for CO2 desorption within a single node unit is obtained based on the initial carbon dioxide concentration, the node recovery rate, and the separation temperature. The formula is as follows: in, is the gas concentration of CO2 in the initial mixed gas, ρ s is the density of adsorption material, V s.j is the volume of adsorption material, Δq j is the desorption capacity of different node units, η Rec.j is the node recovery rate.

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