Methanol steam reforming hydrogen production parameter optimization method and system

Abstract

The invention relates to a methanol steam reforming hydrogen production parameter optimization method and a methanol steam reforming hydrogen production system.The method comprises the steps that a target partition drag force model is obtained, and a first methanol steam reforming hydrogen production fluidized bed model is established based on the target partition drag force model; performing model verification on the first methanol steam reforming hydrogen production fluidized bed model; after the first methanol steam reforming hydrogen production fluidized bed model passes verification, setting particles of the first methanol steam reforming hydrogen production fluidized bed model as catalyst particles and carbon dioxide adsorbent particles so as to form a second methanol steam reforming hydrogen production fluidized bed model; and carrying out numerical simulation on the second methanol steam reforming hydrogen production fluidized bed model to determine a target parameter according to a numerical simulation result of the second methanol steam reforming hydrogen production fluidized bed model, thereby improving a parameter optimization effect during methanol reforming hydrogen production. Reliable basis and theoretical support are provided for actual methanol steam reforming hydrogen production fluidized bed hydrogen production.

Description

Technical Field

[0001] The present application relates to the field of methanol reforming hydrogen production, and in particular to a method and device for optimizing parameters of methanol steam reforming hydrogen production. Background Art

[0002] As the global demand for clean energy continues to grow, hydrogen has become an important choice for addressing climate change and achieving energy transformation due to its high energy density and zero carbon emission characteristics during use. Among hydrogen production technologies, methanol steam reforming is a mature and potential technology. Its reaction produces carbon dioxide as a byproduct while generating hydrogen. Therefore, how to effectively capture carbon dioxide to reduce environmental impact has become one of the research focuses.

[0003] Fluidized bed reactors have been widely used in gas-solid phase reactions due to their excellent mass transfer and heat transfer characteristics. In recent years, many studies have developed different drag models to improve the simulation accuracy and further improve the parameter optimization effect of methanol steam reforming hydrogen production model based on the gas-solid flow behavior and reaction characteristics in the fluidized bed. However, the parameter optimization effect of methanol reforming hydrogen production using the drag model is not good. Summary of the invention

[0004] Based on this, the present application provides a method and system for optimizing parameters of methanol steam reforming hydrogen production to improve the parameter optimization effect during methanol reforming hydrogen production, and provides a reliable basis and theoretical support for actual methanol steam reforming hydrogen production in a fluidized bed.

[0005] On the one hand, a method for optimizing parameters of hydrogen production by methanol steam reforming is provided, the method comprising:

[0006] Acquire a target partition drag model, establish a first methanol steam reforming hydrogen production fluidized bed model based on the target partition drag model, and perform model verification on the first methanol steam reforming hydrogen production fluidized bed model;

[0007] After the first methanol steam reforming hydrogen production fluidized bed model is verified, the particles of the first methanol steam reforming hydrogen production fluidized bed model are set to catalyst particles and carbon dioxide adsorbent particles to form a second methanol steam reforming hydrogen production fluidized bed model;

[0008] A numerical simulation is performed on the second methanol steam reforming hydrogen production fluidized bed model to determine target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model, wherein the target parameters are parameters related to hydrogen production efficiency.

[0009] In one embodiment, before obtaining the target partition drag model, the method further includes:

[0010] Predetermining a plurality of particle volume fraction intervals according to the particle volume fraction, and dividing the fluidized bed model according to the particle volume fraction intervals to form a partitioned drag model;

[0011] Establishing a first fluidized bed simulation model based on the partition drag model, setting the fluidizing medium of the first fluidized bed simulation model to air, and setting the particles of the first fluidized bed simulation model to glass bead particles;

[0012] Performing model verification on the first fluidized bed simulation model, and after the first fluidized bed simulation model passes the verification, determining a particle volume fraction interval corresponding to the verified first fluidized bed simulation model;

[0013] The particle volume fraction interval corresponding to the verified first fluidized bed simulation model is used as the target particle volume fraction interval, so as to determine the target partition drag model according to the target particle volume fraction interval.

[0014] In one embodiment, the step of establishing a first fluidized bed simulation model based on the partition drag model, setting the fluidizing medium of the first fluidized bed simulation model to air, and setting the particles of the first fluidized bed simulation model to glass bead particles comprises:

[0015] Establishing a first fluidized bed physical model, and meshing the first fluidized bed physical model to form a first mesh model;

[0016] A first fluidized bed simulation model is established based on the partition drag model and the first grid model, and the fluidizing medium of the first fluidized bed simulation model is set to air, and the particles of the first fluidized bed simulation model are set to glass bead particles.

[0017] In one embodiment, the model verification of the first fluidized bed simulation model includes:

[0018] Obtaining a first preset parameter table, and configuring a first boundary condition of the first fluidized bed simulation model according to the first model preset parameter table;

[0019] Performing numerical simulation on the first fluidized bed simulation model under the first boundary condition to obtain numerical simulation results of the first fluidized bed simulation model;

[0020] performing a model test on the first fluidized bed simulation model under the first boundary condition to obtain a model test result of the first fluidized bed simulation model;

[0021] The first fluidized bed simulation model is verified according to the numerical simulation results and model test results of the first fluidized bed simulation model.

[0022] In one embodiment, the target partition drag model includes a dense phase region, a transition phase region and a dilute phase region. The drag calculation model of the dense phase region is an Ergun model, the drag calculation model of the transition phase region is a Koch-Hill model, and the drag calculation model of the dilute phase region is a Wen-Yu model. Corresponding conversion functions are set between the dense phase region and the transition phase region and between the transition phase region and the dilute phase region.

[0023] In one embodiment, the establishing of a first methanol steam reforming hydrogen production fluidized bed model based on the target partition drag model includes:

[0024] Establishing a second fluidized bed physical model, and meshing the second fluidized bed physical model to form a second mesh model;

[0025] The first methanol steam reforming hydrogen production fluidized bed model is established based on the target partition drag model and the second grid model, and the fluidizing medium of the first methanol steam reforming hydrogen production fluidized bed model is set to methanol steam, and the particles of the first methanol steam reforming hydrogen production fluidized bed model are set to catalyst particles.

[0026] In one embodiment, the model verification of the first methanol steam reforming hydrogen production fluidized bed model includes:

[0027] Obtaining a second preset parameter table, and configuring a second boundary condition of the first methanol steam reforming hydrogen production fluidized bed model according to the second preset parameter table;

[0028] Numerical simulation and model experiment are carried out on the first fluidized bed model of methanol steam reforming hydrogen production under the second boundary condition to verify the first fluidized bed model of methanol steam reforming hydrogen production.

[0029] In one embodiment, the numerical simulation and model experiment of the first methanol steam reforming hydrogen production fluidized bed model under the second boundary condition to verify the first methanol steam reforming hydrogen production fluidized bed model includes:

[0030] Performing numerical simulation on the first methanol steam reforming hydrogen production fluidized bed model under the second boundary condition to obtain numerical simulation results of the first methanol steam reforming hydrogen production fluidized bed model;

[0031] Conducting a model experiment on the first methanol steam reforming hydrogen production fluidized bed model under the second boundary condition to obtain a model test result of the first methanol steam reforming hydrogen production fluidized bed model;

[0032] Model verification of the first methanol steam reforming hydrogen production fluidized bed model is performed based on the numerical simulation results of the first methanol steam reforming hydrogen production fluidized bed model and the model test results of the model test.

[0033] In one embodiment, the numerical simulation of the second methanol steam reforming hydrogen production fluidized bed model is performed to determine the target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model, including:

[0034] Obtaining a third preset parameter table, and configuring a third boundary condition of the second methanol steam reforming hydrogen production fluidized bed model according to the third preset parameter table;

[0035] Performing numerical simulation on the second methanol steam reforming hydrogen production fluidized bed model under the third boundary condition, and obtaining numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model;

[0036] A preset index is obtained, and target parameters of the second methanol steam reforming hydrogen production fluidized bed model are determined according to the preset index and the numerical simulation result of the second methanol steam reforming hydrogen production fluidized bed model.

[0037] On the other hand, a methanol steam reforming hydrogen production system is provided for realizing the methanol steam reforming hydrogen production parameter optimization method, the system comprising:

[0038] A first model module is used to obtain a target partition drag model, establish a first methanol steam reforming hydrogen production fluidized bed model based on the target partition drag model, and perform model verification on the first methanol steam reforming hydrogen production fluidized bed model;

[0039] A second model module is used for setting the particles of the first methanol steam reforming hydrogen production fluidized bed model as catalyst particles and carbon dioxide adsorbent particles to form a second methanol steam reforming hydrogen production fluidized bed model after the first methanol steam reforming hydrogen production fluidized bed model is verified;

[0040] The target parameter module is used to perform numerical simulation on the second methanol steam reforming hydrogen production fluidized bed model to determine the target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model.

[0041] The above technical solution of the present application has the following advantages compared with the prior art:

[0042] The method for optimizing parameters of methanol steam reforming hydrogen production in the present application first establishes a first methanol steam reforming hydrogen production fluidized bed model based on the target partition drag model to improve the drag prediction accuracy of the first methanol steam reforming hydrogen production fluidized bed model and further accurately reflect the distribution state of particles; then, on the premise of accurately predicting the distribution state of particles, the verified first methanol steam reforming hydrogen production fluidized bed model is added with carbon dioxide adsorbent particles for numerical simulation, so as to determine the target parameters according to the numerical simulation results, under which the parameter optimization effect of methanol reforming hydrogen production can be improved to maximize the hydrogen production efficiency, provide reliable theoretical guidance for the actual hydrogen production process, and improve the actual hydrogen production yield. In addition, the carbon dioxide capture rate and hydrogen purity of the methanol steam reforming model based on the target partition drag model and carbon dioxide adsorbent particles have been effectively improved, which can provide theoretical support for actual production. BRIEF DESCRIPTION OF THE DRAWINGS

[0043] In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings required for use in the description of the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present application. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0044] Figure 1 This is a first method flow chart of the method for optimizing parameters of methanol steam reforming hydrogen production provided in an embodiment of the present application;

[0045] Figure 2 This is a second method flow chart of the method for optimizing parameters of methanol steam reforming hydrogen production provided in an embodiment of the present application;

[0046] Figure 3 It is a structural schematic diagram of a test bench provided in an embodiment of the present application;

[0047] Figure 4 It is a particle volume fraction cloud diagram of the model test and numerical simulation at different inlet superficial gas velocities of the first fluidized bed simulation model provided in the embodiment of the present application;

[0048] Figure 5 The curves of the change of the bed expansion rate with the inlet superficial gas velocity in the numerical simulation of different drag models and the model test of the first fluidized bed simulation model provided in the embodiment of the present application;

[0049] Figure 6 It is a curve of the change of the time-averaged total pressure drop of the bed layer of different drag model numerical simulation and model test at different inlet superficial gas velocities of the first fluidized bed simulation model provided in the embodiment of the present application;

[0050] Figure 7It is a curve of the change of the average local pressure drop of the bed layer under different drag model numerical simulation and model test at different inlet superficial gas velocities of the first fluidized bed simulation model provided in the embodiment of the present application;

[0051] Figure 8 It is a distribution curve diagram of the time-averaged particle axial velocity of the first fluidized bed simulation model provided in the embodiment of the present application under the set inlet superficial gas velocity and different drag model numerical simulations at the set height and the model test;

[0052] Fig. 9 It is a change curve of methanol conversion rate, outlet carbon monoxide content and carbon dioxide selectivity of the numerical simulation and model test of the first methanol steam reforming hydrogen production fluidized bed model at different reaction temperatures provided in the embodiment of the present application;

[0053] Fig.10 It is a dry basis mole fraction diagram of the outlet components of the first methanol steam reforming hydrogen production fluidized bed model (catalyst particles) and the second methanol steam reforming hydrogen production fluidized bed model (catalyst particles and carbon dioxide adsorbent particles);

[0054] Fig.11 is a curve showing changes in methanol conversion rate and hydrogen yield at different reaction temperatures of the second methanol steam reforming hydrogen production fluidized bed model provided in an embodiment of the present application;

[0055] Fig.12 is a curve showing the change of outlet carbon dioxide content and carbon dioxide capture rate at different reaction temperatures of the second methanol steam reforming hydrogen production fluidized bed model provided in the embodiment of the present application;

[0056] Fig.13 is a curve showing the change of methanol conversion rate and hydrogen yield at different inlet superficial gas velocities of the second methanol steam reforming hydrogen production fluidized bed model provided in an embodiment of the present application;

[0057] Fig.14 is a curve showing the change of the outlet carbon dioxide content and the carbon dioxide capture rate at different inlet superficial gas velocities of the second methanol steam reforming hydrogen production fluidized bed model provided in the embodiment of the present application;

[0058] Fig.15 is a curve showing the change of outlet carbon dioxide content and carbon dioxide capture rate under different carbon dioxide adsorbent particle sizes of the second methanol steam reforming hydrogen production fluidized bed model provided in the embodiment of the present application;

[0059] Fig.16 is a curve showing the change of methanol conversion rate and hydrogen yield under different carbon dioxide adsorbent particle sizes in the second methanol steam reforming hydrogen production fluidized bed model provided in the embodiment of the present application;

[0060] Fig.17 It is a system structure diagram of the methanol steam reforming hydrogen production parameter optimization system provided in the embodiment of the present application.

[0061] Description of the Figures in the Specification:

[0062] 1. Blower; 2. Control valve; 3. Flow meter; 4. Gas-solid fluidized bed; 5. Lighting lamp; 6. Pressure sensor; 7. Data acquisition system; 8. Camera equipment; 9. Speed ​​meter; 10. Computer. DETAILED DESCRIPTION

[0063] In order to make the purpose, technical solution and advantages of the present application more clearly understood, the present application is further described in detail below in conjunction with the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present application and are not used to limit the present application.

[0064] Embodiment 1

[0065] Reference Figure 1 As shown, Figure 1 This is a flow chart of the first method of the method for optimizing parameters of methanol steam reforming hydrogen production provided in an embodiment of the present application.

[0066] The method comprises the following steps:

[0067] Acquire a target partition drag model, establish a first methanol steam reforming hydrogen production fluidized bed model based on the target partition drag model, and perform model verification on the first methanol steam reforming hydrogen production fluidized bed model;

[0068] Specifically, the methanol steam reforming hydrogen production fluidized bed model in the methanol steam reforming hydrogen production parameter optimization method of the present application adopts a partition drag model. Therefore, it is necessary to first obtain the target partition drag model, and then establish the first methanol steam reforming hydrogen production fluidized bed model based on the target partition drag model. The drag prediction of the target partition drag model is relatively accurate and can accurately predict the distribution of particles. Therefore, the drag prediction accuracy of the first methanol steam reforming hydrogen production fluidized bed model established based on the target partition drag model is relatively high, and it can provide effective theoretical guidance for actual hydrogen production. Of course, when using the first methanol steam reforming hydrogen production fluidized bed model for particle distribution prediction, the accuracy of the first methanol steam reforming hydrogen production fluidized bed model must first be verified.

[0069] After the first methanol steam reforming hydrogen production fluidized bed model is verified, the particles of the first methanol steam reforming hydrogen production fluidized bed model are set to catalyst particles and carbon dioxide adsorbent particles to form a second methanol steam reforming hydrogen production fluidized bed model;

[0070] Specifically, after the first methanol steam reforming hydrogen production fluidized bed model is verified, the particles (solid phase) of the first methanol steam reforming hydrogen production fluidized bed model can be set to catalyst particles and carbon dioxide adsorbent particles, and the fluidizing medium (gas phase) of the first methanol steam reforming hydrogen production fluidized bed model can be set to methanol vapor to form a second methanol steam reforming hydrogen production fluidized bed model.

[0071] A numerical simulation is performed on the second methanol steam reforming hydrogen production fluidized bed model to determine target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model, wherein the target parameters are parameters related to hydrogen production efficiency and carbon dioxide capture rate.

[0072] Specifically, after obtaining the second methanol steam reforming hydrogen production fluidized bed model, the second methanol steam reforming hydrogen production fluidized bed model can be numerically simulated, and then the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model can be obtained, so as to determine the target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model, and the target parameters are parameters that optimize the hydrogen production and carbon dioxide capture rate of the second methanol steam reforming hydrogen production fluidized bed model.

[0073] The method for optimizing parameters of methanol steam reforming hydrogen production in the present application first establishes a first methanol steam reforming hydrogen production fluidized bed model based on a target partition drag model to improve the drag prediction accuracy of the first methanol steam reforming hydrogen production fluidized bed model and further accurately reflect the distribution state of particles; then, on the premise of accurately predicting the distribution state of particles, a numerical simulation is performed by adding carbon dioxide adsorbent particles to the verified first methanol steam reforming hydrogen production fluidized bed model to facilitate determining target parameters based on the numerical simulation results. Under the target parameters, the parameter optimization effect of methanol reforming hydrogen production can be improved to maximize the hydrogen production efficiency and carbon dioxide capture rate, thereby providing reliable theoretical guidance for the actual hydrogen production process and improving the actual hydrogen production yield.

[0074] In one embodiment, before obtaining the target partition drag model, the method further includes:

[0075] Predetermining a plurality of particle volume fraction intervals according to the particle volume fraction, and dividing the fluidized bed model according to the particle volume fraction intervals to form a partitioned drag model;

[0076] Specifically, the partition drag model needs to be divided according to the interval of particle volume fraction. Therefore, a reasonable particle volume fraction interval must be determined first. First, a number of particle volume fractions are determined in advance, and then the fluidized bed model is divided according to the predetermined particle volume fraction interval, which can be divided into dense phase area, transition phase area and dilute phase area. That is, the dense phase area is where the particle volume fraction is higher, the dilute phase area is where the particle volume fraction is lower, and the transition phase area is where the particle volume fraction is in between, thereby establishing a partition drag model. In addition, not only three intervals can be set, but multiple phase areas can also be divided according to multiple intervals.

[0077] Establishing a first fluidized bed simulation model based on the partition drag model, setting the fluidizing medium of the first fluidized bed simulation model to air, and setting the particles of the first fluidized bed simulation model to glass bead particles;

[0078] Specifically, after the partitioned drag model is built, the first fluidized bed simulation model is established based on the partitioned drag model, and the fluidizing medium of the first fluidized bed simulation model is set to air, and the particles of the first fluidized bed simulation model are set to glass bead particles, so as to verify the effectiveness of the partitioned drag model through the gas-solid two-phase reaction kinetic model of air and glass bead particles.

[0079] Performing model verification on the first fluidized bed simulation model, and after the first fluidized bed simulation model passes the verification, determining a particle volume fraction interval corresponding to the verified first fluidized bed simulation model;

[0080] Specifically, the first fluidized bed simulation model is subjected to model verification, mainly verifying the validity of the first fluidized bed simulation model based on the model test results of the first fluidized bed simulation model. If the first fluidized bed simulation model passes the verification, it means that the partition drag model used by the first fluidized bed simulation model is valid, then the particle volume fraction interval corresponding to the verified first fluidized bed simulation model is obtained.

[0081] The particle volume fraction interval corresponding to the verified first fluidized bed simulation model is used as the target particle volume fraction interval, so as to determine the target partition drag model according to the target particle volume fraction interval.

[0082] Specifically, after the particle volume fraction interval corresponding to the verified first fluidized bed simulation model is obtained, the particle volume fraction interval is used as the target particle volume fraction interval. When the relevant gas-solid two-phase reaction kinetics simulation is subsequently performed, the target partition drag model can be directly determined according to the target particle volume fraction interval.

[0083] In one embodiment, the step of establishing a first fluidized bed simulation model based on the partition drag model, setting the fluidizing medium of the first fluidized bed simulation model to air, and setting the particles of the first fluidized bed simulation model to glass bead particles comprises:

[0084] Establishing a first fluidized bed physical model, and meshing the first fluidized bed physical model to form a first mesh model;

[0085] Specifically, a first fluidized bed physical model is established to simulate the reaction chamber of the reactor. The first fluidized bed physical model is a two-dimensional fluidized bed model. Then, the first fluidized bed physical model is meshed to form a first fluidized bed physical model with mesh data, that is, a first mesh model.

[0086] A first fluidized bed simulation model is established based on the partition drag model and the first grid model, and the fluidizing medium of the first fluidized bed simulation model is set to air, and the particles of the first fluidized bed simulation model are set to glass bead particles.

[0087] Specifically, after the first grid model and the partitioned drag model are determined, the first fluidized bed simulation model can be established based on the partitioned drag model and the first grid model, and the fluidizing medium of the first fluidized bed simulation model can be set to air, and the particles of the first fluidized bed simulation model can be set to glass bead particles, so as to verify the effectiveness of the partitioned drag model through the gas-solid two-phase reaction kinetic model of air and glass bead particles.

[0088] In one embodiment, the model verification of the first fluidized bed simulation model includes:

[0089] Obtaining a first preset parameter table, and configuring a first boundary condition of the first fluidized bed simulation model according to the first model preset parameter table;

[0090] Specifically, a first preset parameter table is obtained, in which parameters for configuring the first boundary condition are stored, such as reaction temperature, inlet superficial gas velocity and other parameters. After obtaining the first preset parameter table, the first boundary condition of the first fluidized bed simulation model is configured by the parameters in the first preset parameter table, so as to perform numerical simulation and model test under the first boundary condition. The first boundary condition is shown in Table 1.

[0091] Table 1 Parameters of the first boundary condition

[0092]

[0093] Performing numerical simulation on the first fluidized bed simulation model under the first boundary condition to obtain numerical simulation results of the first fluidized bed simulation model;

[0094] Specifically, after the first boundary condition of the first fluidized bed simulation model is configured, the first fluidized bed simulation model can be numerically simulated by using FLUENT software to obtain the numerical simulation results of the first fluidized bed simulation model, and the numerical simulation results can be directly output by using FLUENT software. Among them, the Eulerian-Eulerian multiphase flow model is adopted.

[0095] performing a model test on the first fluidized bed simulation model under the first boundary condition to obtain a model test result of the first fluidized bed simulation model;

[0096] Specifically, after the first boundary condition of the first fluidized bed simulation model is configured, a model test is required for the first fluidized bed simulation model. The test is carried out on a test bench to obtain the model test results of the first fluidized bed simulation model. The model test results are collected through equipment related to the test bench. Figure 3 As shown, the test bench consists of a gas-solid fluidized bed 4 with a thickness of 30 mm, a width of 100 mm, and a height of 660 mm. A gas distribution plate (not shown in the figure) is provided at the bottom of the gas-solid fluidized bed 4 to evenly distribute the incoming air flow. The gas-solid fluidized bed 4 is filled with glass beads with a diameter of 250 microns (corresponding to the methanol steam reforming hydrogen production model, it is carbon dioxide adsorbent particles), and the initial height of the particles is 300 mm. Air is used as the fluidizing medium (corresponding to the methanol steam reforming hydrogen production model, it is methanol steam), and the fluidizing medium is provided by a blower 1 (Roots blower is selected), and the flow rate of the fluidizing medium is adjusted by a control valve 2, and the flow rate is displayed by a flow meter 3. In order to obtain fine data on the movement of glass bead particles, the experimental system is equipped with a camera 8 (a high-speed camera is selected) and a velocimeter 9 (a laser Doppler velocimeter, LDV, Laser Doppler Velocimetry) to capture and analyze the dynamic behavior of glass bead particles. In addition, sufficient lighting is provided by the lighting lamp 5 (LED spotlight is selected) to improve the dynamic capture effect of the camera and the velocimeter. Pressure sensors 6 are set at different heights of the gas-solid fluidized bed 4 to measure the pressure changes in the gas-solid fluidized bed 4, and the data acquisition system 7 (high-speed data acquisition system is selected) transmits all experimental data to the computer 10 for processing. Further, the two-dimensional fluidized bed of the methanol steam reforming hydrogen production fluidized bed model has no internal components, is 0.66m high and 0.10m wide.

[0097] The first fluidized bed simulation model is verified according to the numerical simulation results and model test results of the first fluidized bed simulation model.

[0098] Specifically, after the numerical simulation results are output by FLUENT software and the model test results are collected by relevant equipment, the first fluidized bed simulation model can be verified according to the numerical simulation results and model test results of the first fluidized bed simulation model. Among them, the numerical simulation results and model test results mainly include bubble shape, bed expansion rate, time-averaged total pressure drop, time-averaged local pressure drop and time-averaged particle axial velocity under different inlet superficial gas velocities.

[0099] Further, such as Figure 4 As shown, Figure 4 The instantaneous particle volume fraction cloud diagram of the model test and numerical simulation at different inlet superficial gas velocities of the first fluidized bed simulation model. The left side of each figure is the simulation test result, and the right side is the numerical simulation result. The bubble shape size predicted by the numerical simulation of the partition drag model is similar to the bubble shape size observed in the model test, indicating that the numerical simulation of the partition drag model predicts the shape and size of the bubble well. In addition, Figure 4 With the increase of the superficial gas velocity at the inlet, the height of the bed expansion also increases. The higher the velocity, the higher the height of the bed expansion. Figure 3 The calculated bed expansion ratio is consistent. Figure 5 As shown, Figure 5 The bed expansion rate change curves of different drag models under different inlet superficial gas velocities of the first fluidized bed simulation model and the bed expansion rate change curve of the model test with the inlet superficial gas velocity are shown in Figure 2. The bed expansion rates predicted by the traditional drag model (Gidaspow model, Wen-Yu model, Syamlal-O′Brien model, Hulin-Gidaspow model) and the partitioned drag model numerical simulation all increase with the increase of the inlet superficial gas velocity, and are consistent with the bed expansion rate change trend obtained by the model test, which shows the prediction effectiveness of the partitioned drag model. Figure 5 It can be seen that with the increase of the inlet superficial gas velocity, the prediction accuracy of the partition drag model for the bed expansion rate is improved. It can be seen that the partition drag model of the present application has a high prediction accuracy for the bed expansion rate, which can further improve the prediction accuracy of the methanol steam reforming hydrogen production fluidized bed model for the bed expansion rate, so as to provide theoretical support for actual production.

[0100] like Figure 6 As shown, Figure 6 The curves of the change of the bed layer time-averaged total pressure drop under different drag model numerical simulation and model test under different inlet superficial gas velocities of the first fluidized bed simulation model are shown in Figure 2. Figure 6 It can be seen that with the increase of the inlet superficial gas velocity, the time-averaged total pressure drop of the model test and the time-averaged total pressure drop of the drag model numerical simulation are both in a relatively stable range, and the time-averaged total pressure drop is less affected by the inlet superficial gas velocity.

[0101] like Figure 7 As shown, Figure 7 The curves of the change of the average local pressure drop of the bed layer under different drag model numerical simulation and model test at different inlet superficial gas velocities of the first fluidized bed simulation model are shown in Figure 2. Figure 7 It can be seen that with the increase of the inlet superficial gas velocity, the time-averaged local pressure drop of the model test shows a trend of gradually decreasing. The time-averaged local pressure drop of the drag model numerical simulation conforms to this law, and the prediction accuracy of the partition drag model is higher, which is better than the Gidaspow and Hulin-Gidaspow drag models, and the error is within 3%. Therefore, with the increase of the inlet superficial gas velocity, the time-averaged local pressure drop simulated by the partition drag model is closer to the experimental value. It can be seen that the partition drag model of the present application has a high prediction accuracy for the time-averaged local pressure drop, which can further improve the prediction accuracy of the methanol steam reforming hydrogen production fluidized bed model for the time-averaged local pressure drop, so as to provide theoretical support for actual production.

[0102] like Figure 8 As shown, Figure 8 The distribution curves of the time-averaged particle axial velocity at the radial position of 0.38 m / s and a height of 0.25 m for the numerical simulation of different drag models of the first fluidized bed simulation model and the model test are shown. Figure 8 It can be seen that the time-averaged axial velocity of the partition drag model numerical simulation and the time-averaged axial velocity measured by the model test show the same trend, and the prediction result of the partition drag model is more accurate. It can be seen that the partition drag model of the present application has a high prediction accuracy for the time-averaged axial velocity, which can further improve the prediction accuracy of the methanol steam reforming hydrogen production fluidized bed model for the time-averaged axial velocity, so as to provide theoretical support for actual production.

[0103] By comparing the model test results with the numerical simulation results at four different inlet superficial gas velocities (0.10m / s, 0.21m / s, 0.38m / s, and 0.46m / s), it is found that the partitioned drag model can more accurately predict the change trends of bubble morphology, bed expansion rate, time-averaged local pressure drop, and time-averaged total pressure drop, showing a better prediction ability than the traditional drag model. The results show that the partitioned drag model has significant advantages in improving the accuracy and reliability of fluidized bed simulation, especially under high inlet superficial gas velocity conditions. Therefore, the prediction accuracy of the methanol steam reforming hydrogen production fluidized bed model based on the partitioned drag model is high, which can provide a reliable basis and theoretical guidance for the actual methanol steam reforming hydrogen production fluidized bed hydrogen production.

[0104] In one embodiment, the target partition drag model includes a dense phase region, a transition phase region and a dilute phase region. The drag calculation model of the dense phase region is an Ergun model, the drag calculation model of the transition phase region is a Koch-Hill model, and the drag calculation model of the dilute phase region is a Wen-Yu model. Corresponding conversion functions are set between the dense phase region and the transition phase region and between the transition phase region and the dilute phase region.

[0105] The Wen-Yu drag model formula is:

[0106]

[0107] Among them, C D is the drag coefficient; α is the volume fraction; ρ is the density, kg / m 3 ; is the velocity, m / s; subscripts g and s represent the gas phase (fluidizing medium) and solid phase (i.e. particles), respectively; d s is the particle diameter, m; k gs-Wen-Yu is the drag force of the Wen-Yu model, kg / (m 3 ·s).

[0108]

[0109] Among them, Re s is the Reynolds number,

[0110]

[0111] Where, μ is the shear viscosity, Pa / s;

[0112] The Ergun drag model formula is:

[0113]

[0114] k gs-Ergun is the drag force of the Ergun model.

[0115] The Koch-Hill drag model formula is:

[0116]

[0117] k gs-Koch-Hill is the drag force of the Koch-Hill model.

[0118] in,

[0119]

[0120] Among them, the conversion function between the dilute phase region and the transition phase region is:

[0121]

[0122] The conversion function between the dense phase region and the transition phase region is:

[0123]

[0124] Specifically, the drag force is calculated between the dense phase region and the transition phase region, and between the transition phase region and the dilute phase region through corresponding conversion functions to achieve a smooth transition of the drag force models in different regions. Preferably, the particle volume fraction in the dense phase region is greater than 0.4, the particle volume fraction in the dilute phase region is less than 0.1; and the particle volume fraction in the transition phase region is between 0.1 and 0.4.

[0125] In one embodiment, the first methanol steam reforming hydrogen production fluidized bed model is established based on the target partition drag model, including:

[0126] Establishing a second fluidized bed physical model, and meshing the second fluidized bed physical model to form a second mesh model;

[0127] Specifically, a second fluidized bed physical model is established to simulate the reaction chamber of the reactor. The second fluidized bed physical model is a two-dimensional fluidized bed model. Then, the second fluidized bed physical model is meshed to form a second fluidized bed physical model with mesh data, that is, the first mesh model.

[0128] The first methanol steam reforming hydrogen production fluidized bed model is established based on the target partition drag model and the second grid model, and the fluidizing medium of the first methanol steam reforming hydrogen production fluidized bed model is set to methanol steam, and the particles of the first methanol steam reforming hydrogen production fluidized bed model are set to catalyst particles.

[0129] Specifically, after the second grid model and the target partition drag model are determined, a second fluidized bed simulation model can be established based on the target partition drag model and the second grid model, and the fluidizing medium of the second fluidized bed simulation model can be set to methanol vapor, and the particles of the second fluidized bed simulation model can be set to catalyst particles, so as to simulate the methanol vapor reforming to produce hydrogen through the gas-solid two-phase reaction kinetic model of the methanol vapor catalyst particles.

[0130] Furthermore, the fluidized bed model of methanol steam reforming hydrogen production mainly involves three chemical reactions, namely methanol steam reforming reaction, methanol decomposition reaction and water-gas replacement reaction.

[0131] Among them, the chemical equation of methanol steam reforming (SR, Steam Reforming) reaction is:

[0132]

[0133] The chemical equation for the methanol decomposition reaction is:

[0134]

[0135] The chemical equation for the water-gas shift (WGS) reaction is:

[0136]

[0137] Furthermore, the reaction rate r1 of the methanol steam reforming reaction in the methanol steam reforming hydrogen production model is:

[0138]

[0139] The reaction rate r2 of methanol decomposition reaction in the methanol steam reforming hydrogen production model is:

[0140]

[0141] The reaction rate r3 of methanol steam reforming reaction in the methanol steam reforming hydrogen production model is:

[0142]

[0143] Among them, P i is the partial pressure of component i, where i is CH3OH, H2O, H2, CO2 and CO respectively;

[0144] K j is the adsorption constant of surface component j, j is CH3O (1) , HCOO (1) , OH (1) , H (1a) , CH3O (2) , OH (2) and H (2a) ;

[0145] C Sm is the total catalyst surface concentration of active sites m, where m is 1, 2, 1a, and 2a respectively;

[0146] K r is the chemical reaction equilibrium constant of reaction r (r is R, W, D respectively);

[0147] k r is the rate constant of reaction r (r is R, W, D respectively).

[0148] ρ b is the catalyst density;

[0149] Further, the model of carbon dioxide capture by hydrotalcite adsorbent is as follows:

[0150]

[0151] in,

[0152] is the adsorption coefficient,

[0153]

[0154] D p is the pore diffusion coefficient, ρ p is the density of adsorbent particles, r P is the particle radius, R is the gas universal constant, and T is the thermodynamic temperature of the gas;

[0155] is the concentration of carbon dioxide on the carbon dioxide adsorbent particles when carbon dioxide adsorption is in equilibrium,

[0156]

[0157] is the real-time concentration of carbon dioxide on the carbon dioxide adsorbent particles;

[0158] is the maximum saturation capacity of the carbon dioxide adsorbent particles,

[0159]

[0160] is the adsorption isotherm constant related to the reaction temperature,

[0161]

[0162] Where ΔH ads is the heat of adsorption under standard conditions;

[0163] In one embodiment, the model verification of the first methanol steam reforming hydrogen production fluidized bed model includes:

[0164] Obtaining a second preset parameter table, and configuring a second boundary condition of the first methanol steam reforming hydrogen production fluidized bed model according to the second preset parameter table;

[0165] Specifically, a second preset parameter table is obtained, in which parameters for configuring the second boundary condition are stored, such as reaction temperature, inlet superficial gas velocity and other parameters. After obtaining the second preset parameter table, the second boundary condition of the second fluidized bed simulation model is configured by the parameters in the second preset parameter table, so as to facilitate numerical simulation and model test of hydrogen production by methanol steam reforming under the second boundary condition. The second boundary condition is shown in Table 2.

[0166] Table 2 Parameters of the second boundary condition

[0167] Parameter name Parameter Value unit Reactor height 0.66 m Reactor width 0.10 m Reaction temperature 473-613 K Inlet superficial velocity 0.15-0.90 m / s Water-alcohol ratio 1.3:1 - Outlet pressure 101325 Pa

[0168] Numerical simulation and model experiment are carried out on the first fluidized bed model of methanol steam reforming hydrogen production under the second boundary condition to verify the first fluidized bed model of methanol steam reforming hydrogen production.

[0169] Specifically, after the second boundary condition of the first methanol steam reforming hydrogen production fluidized bed model is configured, numerical simulation and model test can be carried out on the first methanol steam reforming hydrogen production fluidized bed model, so as to verify the model of the first methanol steam reforming hydrogen production fluidized bed model according to the numerical simulation results and model test results of the first methanol steam reforming hydrogen production fluidized bed model.

[0170] In one embodiment, the numerical simulation and model experiment of the first methanol steam reforming hydrogen production fluidized bed model under the second boundary condition to verify the first methanol steam reforming hydrogen production fluidized bed model includes:

[0171] Performing numerical simulation on the first methanol steam reforming hydrogen production fluidized bed model under the second boundary condition to obtain numerical simulation results of the first methanol steam reforming hydrogen production fluidized bed model;

[0172] Specifically, after the second boundary condition of the first methanol steam reforming hydrogen production fluidized bed model is configured, the first methanol steam reforming hydrogen production fluidized bed model can be numerically simulated. The simulation is performed through FLUENT software to obtain the numerical simulation results of the first methanol steam reforming hydrogen production fluidized bed model. The numerical simulation results can be directly output through the FLUENT software.

[0173] Conducting a model experiment on the first methanol steam reforming hydrogen production fluidized bed model under the second boundary condition to obtain a model test result of the first methanol steam reforming hydrogen production fluidized bed model;

[0174] Specifically, after the second boundary condition of the first methanol steam reforming hydrogen production fluidized bed model is configured, it is also necessary to carry out a model test on the first methanol steam reforming hydrogen production fluidized bed model. The test is carried out on a constructed test bench to obtain the model test results of the first methanol steam reforming hydrogen production fluidized bed model. The model test results are collected through equipment related to the test bench.

[0175] Model verification of the first methanol steam reforming hydrogen production fluidized bed model is performed based on the numerical simulation results of the first methanol steam reforming hydrogen production fluidized bed model and the model test results of the model test.

[0176] Specifically, after the numerical simulation results are output by FLUENT software and the model test results are collected by relevant equipment, the first methanol steam reforming hydrogen production fluidized bed model can be model verified according to the numerical simulation results and model test results of the first methanol steam reforming hydrogen production fluidized bed model. Among them, the numerical simulation results and model test results mainly include the methanol conversion rate, outlet carbon monoxide content and carbon dioxide selectivity at different reaction temperatures under the target inlet superficial gas velocity (setting the inlet superficial gas velocity and keeping the inlet superficial gas velocity unchanged).

[0177] like Fig. 9 As shown, Fig. 9 The numerical simulation of the first methanol steam reforming hydrogen production fluidized bed model at different reaction temperatures of the first methanol steam reforming hydrogen production fluidized bed model and the methanol conversion rate, outlet carbon monoxide content and carbon dioxide selectivity of the model test are compared with the numerical simulation results and the model test results. Keeping the target inlet superficial gas velocity unchanged and changing the reaction temperature, the average relative error between the numerical simulation results of methanol conversion rate and the model test results is 3.09%, which is within the standard 4%; the relative error of carbon dioxide selectivity is 2.37%, which is within the standard 3%; the outlet carbon monoxide content of the numerical simulation and the outlet carbon monoxide content of the model test are both below 0.6%, and the content is extremely low, within the standard 2%. Therefore, the error of the first methanol steam reforming hydrogen production fluidized bed model is within the allowable range, indicating that the reaction kinetics model is feasible. It can be seen that the first methanol steam reforming hydrogen production fluidized bed model of the present application has a high prediction accuracy for methanol conversion rate, outlet carbon monoxide content and carbon dioxide selectivity, which can provide theoretical support for actual production.

[0178] The calculation formula of methanol conversion rate is:

[0179]

[0180] The dry basis mole fraction of the outlet component is calculated as:

[0181]

[0182] The calculation formula for hydrogen yield is:

[0183]

[0184] The formula for calculating the carbon dioxide selectivity is:

[0185]

[0186] The carbon dioxide capture rate is calculated as:

[0187]

[0188] and represent the mole fraction of methanol at the inlet and the mole fraction of methanol at the outlet, respectively; n CO,out and They are the mole fraction of hydrogen, mole fraction of carbon monoxide and mole fraction of carbon dioxide at the outlet respectively; the dry basis mole fraction of the outlet component is defined as the ratio of the mole fraction of the outlet component to the sum of the mole fractions of other outlet components except water vapor.

[0189] In one embodiment, the numerical simulation of the second methanol steam reforming hydrogen production fluidized bed model is performed to determine the target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model, including:

[0190] Obtaining a third preset parameter table, and configuring a third boundary condition of the second methanol steam reforming hydrogen production fluidized bed model according to the third preset parameter table;

[0191] Specifically, a third preset parameter table is obtained, in which parameters for configuring the third boundary condition are stored, such as reaction temperature, inlet superficial gas velocity and other parameters. After obtaining the third preset parameter table, the third boundary condition of the second methanol steam reforming hydrogen production fluidized bed model is configured by the parameters in the third preset parameter table, so as to facilitate the numerical simulation of the second methanol steam reforming hydrogen production fluidized bed model under the third boundary condition. The third boundary condition is shown in Table 3. The second boundary condition of the present application is consistent with the third boundary condition.

[0192] Table 3 Parameters of the third boundary condition

[0193] Parameter name Parameter Value unit Reactor height 0.66 m Reactor width 0.10 m Reaction temperature 473-613 K Inlet superficial velocity 0.15-0.90 m / s Water-alcohol ratio 1.3:1 - Outlet pressure 101325 Pa

[0194] Performing numerical simulation on the second methanol steam reforming hydrogen production fluidized bed model under the third boundary condition, and obtaining numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model;

[0195] Specifically, after the second methanol steam reforming hydrogen production fluidized bed model is configured according to the third boundary condition, the second methanol steam reforming hydrogen production fluidized bed model is numerically simulated, and the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model are obtained, so as to determine the target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model, that is, to optimize the parameters and obtain the optimal parameters.

[0196] A preset index is obtained, and target parameters of the second methanol steam reforming hydrogen production fluidized bed model are determined according to the preset index and the numerical simulation result of the second methanol steam reforming hydrogen production fluidized bed model.

[0197] Specifically, the parameters of the second methanol steam reforming hydrogen production fluidized bed model need to be optimized through corresponding indicators. The indicators adopted are preset indicators, which can be selected according to experiments or experience. The preset indicators select methanol conversion rate, outlet carbon monoxide content and carbon dioxide selectivity. According to the preset indicators and the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model, the target parameters of the second methanol steam reforming hydrogen production fluidized bed model are determined. The target parameters include reaction temperature, inlet superficial gas velocity and carbon dioxide adsorbent particle size. The simulation results of the second methanol steam reforming hydrogen production fluidized bed model are ensured to reach the preset indicators by adjusting the parameter values ​​of the reaction temperature, inlet superficial gas velocity and carbon dioxide adsorbent particle size. It can be seen from the model test results that the reaction temperature, inlet superficial gas velocity and carbon dioxide adsorbent particle size affect the methanol conversion rate, hydrogen yield, carbon dioxide content and carbon dioxide capture rate. Therefore, the methanol conversion rate, hydrogen yield, carbon dioxide content and carbon dioxide capture rate under different reaction temperatures, different inlet superficial gas velocities and different carbon dioxide adsorbent particle sizes are different. Therefore, it is necessary to study the effects of the combined conditions of reaction temperature, inlet superficial gas velocity and carbon dioxide adsorbent particle size on methanol conversion, hydrogen yield, carbon dioxide content and carbon dioxide capture rate, so as to obtain the optimal parameter combination of reaction temperature, inlet superficial gas velocity and carbon dioxide adsorbent particle size to achieve the optimal methanol conversion, hydrogen yield, carbon dioxide content or carbon dioxide capture rate. Furthermore, the optimal parameter combination of reaction temperature, inlet superficial gas velocity and carbon dioxide adsorbent particle size can be determined by orthogonal design experiments.

[0198] like Fig.10 As shown, Fig.10 The figure shows the dry mole fraction of the outlet components of the first methanol steam reforming hydrogen production fluidized bed model (catalyst particles) and the second methanol steam reforming hydrogen production fluidized bed model (catalyst particles and carbon dioxide adsorbent particles). Under the conditions of reaction temperature of 593K, water-to-methanol ratio of 1.3, and inlet superficial gas velocity of 0.22m / s, the gas components at the outlet of the fluidized bed with and without hydrotalcite adsorbent particles are compared. Fig.10 It can be seen that the addition of hydrotalcite adsorbent particles effectively captures carbon dioxide, and the dry molar fraction of carbon dioxide is reduced from 19.93% to 2.62%; and the addition of hydrotalcite adsorbent particles plays a positive role in the output of hydrogen, and the concentration of hydrogen increases from 75.38% to 94.22%, and the purity of hydrogen is effectively improved; and both methanol and carbon monoxide are in a lower concentration range. The capture of carbon dioxide breaks the balance of the methanol steam reforming reaction, and the reaction moves toward the direction of hydrogen generation. More methanol is consumed through the methanol steam reforming reaction, and the concentration of methanol decreases (that is, the conversion rate of methanol increases), and the concentration of hydrogen increases. It can be seen that the hydrogen purity of the methanol steam reforming model based on the target partition drag model and carbon dioxide adsorbent particles has been effectively improved, which can provide theoretical support for actual production.

[0199] like Fig.11 As shown, Fig.11 The curves of methanol conversion rate and hydrogen yield at different reaction temperatures for the second methanol steam reforming hydrogen production fluidized bed model are shown in Figure 2. Fig.11 It can be seen that the methanol conversion rate increases with the increase of reaction temperature, and the hydrogen yield also increases with the increase of reaction temperature. The increase of reaction temperature is conducive to the conversion of methanol and the output of hydrogen, and has a positive effect on the methanol conversion rate and hydrogen yield. The reaction temperature is from 493K to 593K, and the methanol conversion rate increases from 11.89% to 85.81%, and the conversion rate is greatly improved. Steam reforming reaction and methanol decomposition reaction are both endothermic reactions. The increase of reaction temperature promotes the reaction rate of the two reactions to increase, resulting in an increase in the consumption of methanol, which further increases the methanol conversion rate. With the continuous increase of methanol conversion rate, the output of hydrogen continues to increase, and the hydrogen yield increases from 0.86 to 2.38. It can be seen that the methanol steam reforming hydrogen production fluidized bed model of the present application can significantly improve the methanol conversion rate and hydrogen output after adding carbon dioxide adsorbent particles.

[0200] like Fig.12 As shown, Fig.12 The curves of the outlet carbon dioxide content and carbon dioxide capture rate at different reaction temperatures of the second methanol steam reforming hydrogen production fluidized bed model are shown in Figure 2. Fig.12It can be seen that the outlet carbon dioxide content and carbon dioxide capture rate both increase with the increase of reaction temperature. When the reaction temperature increases from 493K to 593K, the outlet carbon dioxide content increases from 1.29% to 3.59%, and the dioxygen capture rate increases from 7.69% to 74.73%. The outlet carbon dioxide content is maintained below 4%. The increase in reaction temperature promotes the forward progress of methanol steam reforming reaction, and the generation of carbon dioxide continues to increase. The addition of carbon dioxide adsorbent particles effectively captures the generated carbon dioxide. As the reaction temperature increases, the capture capacity continues to increase. More carbon dioxide is captured in the fluidized bed reactor, and the final outlet carbon dioxide content remains at a low level without a significant increase. Carbon dioxide is effectively captured, the product carbon dioxide of the methanol steam reforming reaction is reduced, the forward progress of the reaction is promoted, and the hydrogen output and methanol conversion are improved to a certain extent. The increase in reaction temperature not only promotes the conversion of methanol, but also, because carbon dioxide is effectively captured, the reaction proceeds in the direction of generating more hydrogen. This synergistic effect leads to a high level of methanol conversion and hydrogen yield at high temperatures. It can be seen that after adding carbon dioxide adsorbent particles, the methanol steam reforming hydrogen production fluidized bed model of the present application can not only improve the methanol conversion rate and hydrogen production, but also improve the carbon dioxide capture rate.

[0201] like Fig.13 As shown, Fig.13 The curves of methanol conversion rate and hydrogen yield at different inlet superficial gas velocities of the second methanol steam reforming hydrogen production fluidized bed model are shown in Figure 2. Fig.13 It can be seen that Fig.13 With the continuous increase of the inlet superficial gas velocity, the methanol conversion rate and hydrogen yield continued to decrease. When the gas velocity increased from 0.15m / s to 0.90m / s, the methanol conversion rate decreased from 95.05% to 62.02%, a decrease of 33%; the hydrogen yield decreased from 2.57 to 1.93. The higher gas velocity shortens the residence time of methanol and water vapor in the reactor, reduces the contact time with the catalyst, and cannot fully react. Methanol is taken out of the reactor before it is completely reacted, which leads to a decrease in methanol conversion. With the continuous increase of gas velocity, hydrogen yield and methanol conversion rate show similar trends, which shows that the output of hydrogen depends on the methanol conversion rate, and the lower methanol conversion rate directly affects the hydrogen production.

[0202] like Fig.14 As shown, Fig.14 The curves of the outlet carbon dioxide content and carbon dioxide capture rate at different inlet superficial gas velocities of the second methanol steam reforming hydrogen production fluidized bed model are shown in Figure 2. Fig.14It can be seen that with the continuous increase of gas velocity, the carbon dioxide content at the outlet increases continuously. When the gas velocity is 0.15m / s, the carbon dioxide content is 3.60%, and when the gas velocity reaches 0.90m / s, the carbon dioxide content is 6.30%. The carbon dioxide capture rate decreases significantly with the increase of gas velocity. When the gas velocity is 0.15m / s, the capture rate is 83.61%, and when the gas velocity is 0.90m / s, the capture rate is 44.69%, which decreases by 38.92%. At a lower gas velocity, the generated carbon dioxide stays in the reactor for a longer time, which is conducive to the full contact between carbon dioxide and carbon dioxide adsorbent particles, so that the capture rate of carbon dioxide is higher, the uncaptured carbon dioxide is less, and the carbon dioxide content at the outlet is at a lower level. With the increase of gas velocity, the residence time of the generated carbon dioxide in the reactor is shortened, resulting in a decrease in the capture efficiency of carbon dioxide, and then the carbon dioxide content gradually increases. Especially at high gas velocity, the capture rate is significantly reduced, and the unabsorbed carbon dioxide increases significantly, resulting in a significant increase in the carbon dioxide content in the reactor outlet gas.

[0203] like Fig.15 As shown, Fig.15 The curves of the outlet carbon dioxide content and carbon dioxide capture rate under different carbon dioxide adsorbent particle sizes of the second methanol steam reforming hydrogen production fluidized bed model are shown in Figure 2. Fig.15 It can be seen that the increase in particle size leads to an increase in the outlet carbon dioxide content and a decrease in the carbon dioxide capture rate. When the particle size is 0.20 mm, the outlet carbon dioxide content is 2.33% and the capture rate is 83.47%; when the particle size is 1.40 mm, the outlet carbon dioxide content is 8.68% and the capture rate is 51.62%. Under the condition that other conditions remain unchanged, as the particle size increases, the specific surface area decreases, and the effective contact between carbon dioxide and carbon dioxide adsorbent particles decreases, which in turn reduces the carbon dioxide capture capacity of the carbon dioxide adsorbent particles, the carbon dioxide capture rate shows a downward trend, and the outlet carbon dioxide content increases. Smaller particle sizes have larger specific surface areas. The smaller the particle size of the carbon dioxide adsorbent particles, the stronger the carbon dioxide capture capacity, the higher the carbon dioxide capture rate, and the lower the outlet carbon dioxide content.

[0204] like Fig.16 As shown, Fig.16 The curves of methanol conversion rate and hydrogen yield under different carbon dioxide adsorbent particle sizes in the second methanol steam reforming hydrogen production fluidized bed model are shown in Figure 2. Fig.16It can be seen that with the increase of the particle size of the carbon dioxide adsorbent particles, the methanol conversion rate and hydrogen yield show a downward trend. When the particle size is 0.20mm, the methanol conversion rate is 91.03%, and the hydrogen yield is 2.48. When the particle size is 1.40mm, the methanol conversion rate is 76.43%, and the hydrogen yield is 2.22. The methanol conversion rate has decreased by 14.6%, and the hydrogen yield has decreased by 0.26. With the increase of the particle size of the carbon dioxide adsorbent particles, the carbon dioxide capture capacity decreases, and the carbon dioxide in the fluidized bed reactor increases, which is not conducive to the forward reaction, inhibiting the methanol conversion, and then reducing the hydrogen produced, the methanol conversion rate decreases, and the hydrogen yield decreases.

[0205] Embodiment 2

[0206] Reference Figure 2 As shown, Figure 2 This is a second method flow chart of the method for optimizing parameters of methanol steam reforming hydrogen production provided in the embodiment of the present application. Figure 2 In the method shown, Figure 1 For the same or similar contents in the method shown, please refer to Figure 1 The description in the method will not be repeated here.

[0207] S201, predetermining a plurality of particle volume fraction intervals according to the particle volume fraction, and dividing the fluidized bed model according to the particle volume fraction intervals to form a partitioned drag model;

[0208] The partition drag model needs to be divided according to the interval of particle volume fraction. Therefore, a reasonable particle volume fraction interval must be determined first. First, a number of particle volume fractions are determined in advance, and then the fluidized bed model is divided according to the predetermined particle volume fraction interval, which can be divided into dense phase area, transition phase area and dilute phase area, that is, the area with higher particle volume fraction is dense phase area, the area with lower particle volume fraction is dilute phase area, and the area with particle volume fraction in between is transition phase area, so as to establish the partition drag model.

[0209] S202, establishing a first fluidized bed physical model, and meshing the first fluidized bed physical model to form a first mesh model;

[0210] A first fluidized bed physical model is established to simulate the reaction chamber of the reactor. The first fluidized bed physical model is a two-dimensional fluidized bed model. The first fluidized bed physical model is then meshed to form a first fluidized bed physical model with mesh data, that is, a first mesh model.

[0211] S203, establishing a first fluidized bed simulation model based on the partition drag model and the first grid model, and setting the fluidizing medium of the first fluidized bed simulation model to air, and setting the particles of the first fluidized bed simulation model to glass bead particles;

[0212] A first fluidized bed simulation model is established based on the partition drag model and the first grid model, and the fluidizing medium of the first fluidized bed simulation model is set to air, and the particles of the first fluidized bed simulation model are set to glass bead particles.

[0213] S204, obtaining a first preset parameter table, and configuring a first boundary condition of the first fluidized bed simulation model according to the first model preset parameter table;

[0214] Obtain a first preset parameter table, which stores parameters for configuring the first boundary condition, such as reaction temperature, inlet superficial gas velocity and other parameters. After obtaining the first preset parameter table, configure the first boundary condition of the first fluidized bed simulation model through the parameters in the first preset parameter table to facilitate numerical simulation and model testing under the first boundary condition.

[0215] S205, performing numerical simulation on the first fluidized bed simulation model under the first boundary condition to obtain a numerical simulation result of the first fluidized bed simulation model;

[0216] After the first boundary condition of the first fluidized bed simulation model is configured, the first fluidized bed simulation model can be numerically simulated by using FLUENT software to obtain the numerical simulation results of the first fluidized bed simulation model, and the numerical simulation results can be directly output by FLUENT software. Among them, the Eulerian-Eulerian multiphase flow model is used.

[0217] S206, performing a model test on the first fluidized bed simulation model under the first boundary condition to obtain a model test result of the first fluidized bed simulation model;

[0218] After the first boundary condition of the first fluidized bed simulation model is configured, a model test is also required for the first fluidized bed simulation model. The test is carried out through the constructed test bench to obtain the model test results of the first fluidized bed simulation model. The model test results are collected through equipment related to the test bench.

[0219] S207, performing model verification on the first fluidized bed simulation model according to the numerical simulation results and model test results of the first fluidized bed simulation model;

[0220] After the numerical simulation results are output through FLUENT software and the model test results are collected through relevant equipment, the first fluidized bed simulation model can be verified according to the numerical simulation results and model test results of the first fluidized bed simulation model.

[0221] S208, after the first fluidized bed simulation model is verified, determining a particle volume fraction interval corresponding to the verified first fluidized bed simulation model;

[0222] The model verification of the first fluidized bed simulation model is mainly to verify the validity of the first fluidized bed simulation model based on the model test results of the first fluidized bed simulation model. If the first fluidized bed simulation model passes the verification, it means that the partition drag model used by the first fluidized bed simulation model is valid, then the particle volume fraction interval corresponding to the verified first fluidized bed simulation model is obtained.

[0223] S209, taking the particle volume fraction interval corresponding to the verified first fluidized bed simulation model as a target particle volume fraction interval, and determining a target partition drag model according to the target particle volume fraction interval;

[0224] After obtaining the particle volume fraction interval corresponding to the first fluidized bed simulation model that has passed verification, the particle volume fraction interval is used as the target particle volume fraction interval. When performing subsequent related gas-solid two-phase reaction kinetics simulations, the target partition drag model can be directly determined according to the target particle volume fraction interval.

[0225] S210, establishing a second fluidized bed physical model, and meshing the second fluidized bed physical model to form a second mesh model;

[0226] A second fluidized bed physical model is established to simulate the reaction chamber of the reactor. The second fluidized bed physical model is a two-dimensional fluidized bed model. The second fluidized bed physical model is then meshed to form a second fluidized bed physical model with mesh data, which is the first mesh model.

[0227] S211, obtaining a target partition drag model, establishing the first methanol steam reforming hydrogen production fluidized bed model based on the target partition drag model and the second grid model, setting the fluidized medium of the first methanol steam reforming hydrogen production fluidized bed model to methanol steam, and setting the particles of the first methanol steam reforming hydrogen production fluidized bed model to catalyst particles;

[0228] After the second grid model and the target partition drag model are determined, the second fluidized bed simulation model can be established based on the target partition drag model and the second grid model, and the fluidizing medium of the second fluidized bed simulation model can be set to methanol vapor, and the particles of the second fluidized bed simulation model can be set to catalyst particles, so as to simulate the methanol vapor reforming to produce hydrogen through the gas-solid two-phase reaction kinetic model of the methanol vapor catalyst particles.

[0229] S212, obtaining a second preset parameter table, and configuring a second boundary condition of the first methanol steam reforming hydrogen production fluidized bed model according to the second preset parameter table;

[0230] Obtain a second preset parameter table, which stores parameters for configuring the second boundary conditions, such as reaction temperature, inlet superficial gas velocity and other parameters. After obtaining the second preset parameter table, configure the second boundary conditions of the second fluidized bed simulation model through the parameters in the second preset parameter table, so as to facilitate numerical simulation and model testing of methanol steam reforming to produce hydrogen under the second boundary conditions.

[0231] S213, performing numerical simulation on the first fluidized bed model for producing hydrogen through steam reforming of methanol under the second boundary condition to obtain numerical simulation results of the first fluidized bed model for producing hydrogen through steam reforming of methanol;

[0232] After the second boundary condition of the first methanol steam reforming hydrogen production fluidized bed model is configured, the first methanol steam reforming hydrogen production fluidized bed model can be numerically simulated. The simulation is performed through FLUENT software to obtain the numerical simulation results of the first methanol steam reforming hydrogen production fluidized bed model. The numerical simulation results can be directly output through FLUENT software.

[0233] S214, performing a model experiment on the first methanol steam reforming hydrogen production fluidized bed model under the second boundary condition to obtain a model test result of the first methanol steam reforming hydrogen production fluidized bed model;

[0234] After the second boundary condition of the first methanol steam reforming hydrogen production fluidized bed model is configured, it is also necessary to carry out a model test on the first methanol steam reforming hydrogen production fluidized bed model. The test is carried out on a constructed test bench to obtain the model test results of the first methanol steam reforming hydrogen production fluidized bed model. The model test results are collected through equipment related to the test bench.

[0235] S215, performing model verification on the first fluidized bed model for producing hydrogen through steam reforming of methanol according to the numerical simulation result of the first fluidized bed model for producing hydrogen through steam reforming of methanol and the model test result of the model test;

[0236] After outputting the numerical simulation results through FLUENT software and collecting the model test results through relevant equipment, the first methanol steam reforming hydrogen production fluidized bed model can be verified according to the numerical simulation results and model test results of the first methanol steam reforming hydrogen production fluidized bed model.

[0237] S216, after the first methanol steam reforming hydrogen production fluidized bed model is verified, the particles of the first methanol steam reforming hydrogen production fluidized bed model are set to catalyst particles and carbon dioxide adsorbent particles to form a second methanol steam reforming hydrogen production fluidized bed model;

[0238] After the first methanol steam reforming hydrogen production fluidized bed model is verified, the particles (solid phase) of the first methanol steam reforming hydrogen production fluidized bed model can be set to catalyst particles and carbon dioxide adsorbent particles, and the fluidizing medium (gas phase) of the first methanol steam reforming hydrogen production fluidized bed model can be set to methanol vapor to form a second methanol steam reforming hydrogen production fluidized bed model.

[0239] S217, obtaining a third preset parameter table, and configuring a third boundary condition of the second methanol steam reforming hydrogen production fluidized bed model according to the third preset parameter table;

[0240] A third preset parameter table is obtained, in which parameters for configuring the third boundary condition, such as reaction temperature, inlet superficial gas velocity and other parameters are stored. After obtaining the third preset parameter table, the third boundary condition of the second methanol steam reforming hydrogen production fluidized bed model is configured by the parameters in the third preset parameter table, so as to facilitate numerical simulation of the second methanol steam reforming hydrogen production fluidized bed model under the third boundary condition.

[0241] S218, performing numerical simulation on the second methanol steam reforming hydrogen production fluidized bed model under the third boundary condition, and obtaining numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model;

[0242] After the second methanol steam reforming hydrogen production fluidized bed model is configured according to the third boundary condition, the second methanol steam reforming hydrogen production fluidized bed model is numerically simulated, and the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model are obtained, so as to determine the target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model, that is, to optimize the parameters and obtain the optimal parameters.

[0243] S219, obtaining preset indicators, and determining target parameters of the second methanol steam reforming hydrogen production fluidized bed model according to the preset indicators and the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model.

[0244] The preset indicators include methanol conversion rate, outlet carbon monoxide content, and carbon dioxide selectivity. The target parameters of the second methanol steam reforming hydrogen production fluidized bed model are determined according to the preset indicators and the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model. The target parameters include reaction temperature, inlet superficial gas velocity, and carbon dioxide adsorbent particle size. The simulation results of the second methanol steam reforming hydrogen production fluidized bed model meet the preset indicators by adjusting the parameter values ​​of reaction temperature, inlet superficial gas velocity, and carbon dioxide adsorbent particle size.

[0245] It should be understood that although Figure 1-2 The steps in the flowchart are shown in sequence as indicated by the arrows, but these steps are not necessarily executed in the order indicated by the arrows. Unless otherwise specified in this document, there is no strict order restriction for the execution of these steps, and these steps can be executed in other orders. Moreover, Figure 1-2 At least part of the steps may include multiple sub-steps or multiple stages. These sub-steps or stages are not necessarily executed at the same time, but can be executed at different times. The execution order of these sub-steps or stages is not necessarily sequential, but can be executed in turn or alternately with other steps or at least part of the sub-steps or stages of other steps.

[0246] Embodiment 3

[0247] Reference Fig.17 As shown, Fig.17 This is a system structure diagram of the methanol steam reforming hydrogen production parameter optimization system provided in an embodiment of the present application.

[0248] The methanol steam reforming hydrogen production parameter optimization system of this embodiment includes:

[0249] A first model module is used to obtain a target partition drag model, establish a first methanol steam reforming hydrogen production fluidized bed model based on the target partition drag model, and perform model verification on the first methanol steam reforming hydrogen production fluidized bed model;

[0250] The methanol steam reforming hydrogen production fluidized bed model in the methanol steam reforming hydrogen production parameter optimization method of the present application adopts a partitioned drag model. Therefore, it is necessary to first obtain the target partitioned drag model through the first model module, and then establish the first methanol steam reforming hydrogen production fluidized bed model based on the target partitioned drag model through the first model module. The drag prediction of the target partitioned drag model is relatively accurate and can accurately predict the distribution of particles. Therefore, the drag prediction accuracy of the first methanol steam reforming hydrogen production fluidized bed model established based on the target partitioned drag model is higher, and it can provide effective theoretical guidance for actual hydrogen production.

[0251] A second model module is used for setting the particles of the first methanol steam reforming hydrogen production fluidized bed model as catalyst particles and carbon dioxide adsorbent particles to form a second methanol steam reforming hydrogen production fluidized bed model after the first methanol steam reforming hydrogen production fluidized bed model is verified;

[0252] After the first methanol steam reforming hydrogen production fluidized bed model is verified, the particles (solid phase) of the first methanol steam reforming hydrogen production fluidized bed model can be set as catalyst particles and carbon dioxide adsorbent particles, and the fluidizing medium (gas phase) of the first methanol steam reforming hydrogen production fluidized bed model can be set to methanol vapor through the second model module to form a second methanol steam reforming hydrogen production fluidized bed model.

[0253] The target parameter module is used to perform numerical simulation on the second methanol steam reforming hydrogen production fluidized bed model to determine the target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model.

[0254] After obtaining the second methanol steam reforming hydrogen production fluidized bed model, the second methanol steam reforming hydrogen production fluidized bed model can be numerically simulated through the target parameter module, and then the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model can be obtained, so as to determine the target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model, and the target parameters are parameters that optimize the hydrogen production and carbon dioxide capture rate of the second methanol steam reforming hydrogen production fluidized bed model.

[0255] The specific definition of the methanol steam reforming hydrogen production parameter optimization system can be found in the above definition of the method, which will not be repeated here. Each module in the above-mentioned methanol steam reforming hydrogen production parameter optimization system can be implemented in whole or in part by software, hardware and a combination thereof. The above-mentioned modules can be embedded in or independent of the processor in the computer device in the form of hardware, or can be stored in the memory in the computer device in the form of software, so that the processor can call and execute the operations corresponding to the above modules.

[0256] The technical features of the above embodiments may be combined arbitrarily. To make the description concise, not all possible combinations of the technical features in the above embodiments are described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification.

[0257] The above-mentioned embodiments only express several implementation methods of the present application, and the descriptions thereof are relatively specific and detailed, but they cannot be understood as limiting the scope of the invention patent. It should be pointed out that, for a person of ordinary skill in the art, several variations and improvements can be made without departing from the concept of the present application, and these all belong to the protection scope of the present application. Therefore, the protection scope of the patent of the present application shall be subject to the attached claims.

Claims

1. A method for optimizing parameters of methanol steam reforming hydrogen production, characterized in that: The method comprises: Acquire a target partition drag model, establish a first methanol steam reforming hydrogen production fluidized bed model based on the target partition drag model, and perform model verification on the first methanol steam reforming hydrogen production fluidized bed model; After the first methanol steam reforming hydrogen production fluidized bed model is verified, the particles of the first methanol steam reforming hydrogen production fluidized bed model are set to catalyst particles and carbon dioxide adsorbent particles to form a second methanol steam reforming hydrogen production fluidized bed model; A numerical simulation is performed on the second fluidized bed model for producing hydrogen through steam reforming of methanol to determine target parameters according to the numerical simulation results of the second fluidized bed model for producing hydrogen through steam reforming of methanol.

2. The method for optimizing parameters of methanol steam reforming hydrogen production according to claim 1, characterized in that: Before obtaining the target partition drag model, the method further includes: Predetermining a plurality of particle volume fraction intervals according to the particle volume fraction, and dividing the fluidized bed model according to the particle volume fraction intervals to form a partitioned drag model; Establishing a first fluidized bed simulation model based on the partition drag model, setting the fluidizing medium of the first fluidized bed simulation model to air, and setting the particles of the first fluidized bed simulation model to glass bead particles; Performing model verification on the first fluidized bed simulation model, and after the first fluidized bed simulation model passes the verification, determining a particle volume fraction interval corresponding to the verified first fluidized bed simulation model; The particle volume fraction interval corresponding to the verified first fluidized bed simulation model is used as the target particle volume fraction interval, so as to determine the target partition drag model according to the target particle volume fraction interval.

3. The method for optimizing parameters of methanol steam reforming hydrogen production according to claim 2, characterized in that: The step of establishing a first fluidized bed simulation model based on the partition drag model, setting the fluidizing medium of the first fluidized bed simulation model to air, and setting the particles of the first fluidized bed simulation model to glass bead particles comprises: Establishing a first fluidized bed physical model, and meshing the first fluidized bed physical model to form a first mesh model; A first fluidized bed simulation model is established based on the partition drag model and the first grid model, and the fluidizing medium of the first fluidized bed simulation model is set to air, and the particles of the first fluidized bed simulation model are set to glass bead particles.

4. The method for optimizing parameters of methanol steam reforming hydrogen production according to claim 2, characterized in that: The performing model verification on the first fluidized bed simulation model comprises: Obtaining a first preset parameter table, and configuring a first boundary condition of the first fluidized bed simulation model according to the first model preset parameter table; Performing numerical simulation on the first fluidized bed simulation model under the first boundary condition to obtain numerical simulation results of the first fluidized bed simulation model; performing a model test on the first fluidized bed simulation model under the first boundary condition to obtain a model test result of the first fluidized bed simulation model; The first fluidized bed simulation model is verified according to the numerical simulation results and model test results of the first fluidized bed simulation model.

5. The method for optimizing parameters of methanol steam reforming hydrogen production according to claim 1, characterized in that: The target partition drag model includes a dense phase region, a transition phase region and a dilute phase region. The drag calculation model of the dense phase region is the Ergun model, the drag calculation model of the transition phase region is the Koch-Hill model, and the drag calculation model of the dilute phase region is the Wen-Yu model. Corresponding conversion functions are set between the dense phase region and the transition phase region and between the transition phase region and the dilute phase region.

6. The method for optimizing parameters of methanol steam reforming hydrogen production according to claim 1, characterized in that: The step of establishing a first methanol steam reforming hydrogen production fluidized bed model based on the target partition drag model comprises: Establishing a second fluidized bed physical model, and meshing the second fluidized bed physical model to form a second mesh model; The first methanol steam reforming hydrogen production fluidized bed model is established based on the target partition drag model and the second grid model, and the fluidizing medium of the first methanol steam reforming hydrogen production fluidized bed model is set to methanol steam, and the particles of the first methanol steam reforming hydrogen production fluidized bed model are set to catalyst particles.

7. The method for optimizing parameters of methanol steam reforming hydrogen production according to claim 1, characterized in that: The model verification of the first methanol steam reforming hydrogen production fluidized bed model includes: Obtaining a second preset parameter table, and configuring a second boundary condition of the first methanol steam reforming hydrogen production fluidized bed model according to the second preset parameter table; Numerical simulation and model experiment are carried out on the first fluidized bed model of methanol steam reforming hydrogen production under the second boundary condition to verify the first fluidized bed model of methanol steam reforming hydrogen production.

8. The method for optimizing parameters of methanol steam reforming hydrogen production according to claim 7, characterized in that: The method of performing numerical simulation and model experiment on the first fluidized bed model for producing hydrogen by steam reforming of methanol under the second boundary condition to verify the first fluidized bed model for producing hydrogen by steam reforming of methanol includes: Performing numerical simulation on the first methanol steam reforming hydrogen production fluidized bed model under the second boundary condition to obtain numerical simulation results of the first methanol steam reforming hydrogen production fluidized bed model; Conducting a model experiment on the first methanol steam reforming hydrogen production fluidized bed model under the second boundary condition to obtain a model test result of the first methanol steam reforming hydrogen production fluidized bed model; Model verification of the first methanol steam reforming hydrogen production fluidized bed model is performed based on the numerical simulation results of the first methanol steam reforming hydrogen production fluidized bed model and the model test results of the model test.

9. The method for optimizing parameters of methanol steam reforming hydrogen production according to claim 1, characterized in that: The performing of numerical simulation on the second methanol steam reforming hydrogen production fluidized bed model to determine target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model includes: Obtaining a third preset parameter table, and configuring a third boundary condition of the second methanol steam reforming hydrogen production fluidized bed model according to the third preset parameter table; Performing numerical simulation on the second methanol steam reforming hydrogen production fluidized bed model under the third boundary condition, and obtaining numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model; A preset index is obtained, and target parameters of the second methanol steam reforming hydrogen production fluidized bed model are determined according to the preset index and the numerical simulation result of the second methanol steam reforming hydrogen production fluidized bed model.

10. A methanol steam reforming hydrogen production system for implementing the methanol steam reforming hydrogen production parameter optimization method according to any one of claims 1 to 9, characterized in that: include: A first model module is used to obtain a target partition drag model, establish a first methanol steam reforming hydrogen production fluidized bed model based on the target partition drag model, and perform model verification on the first methanol steam reforming hydrogen production fluidized bed model; A second model module is used for setting the particles of the first methanol steam reforming hydrogen production fluidized bed model as catalyst particles and carbon dioxide adsorbent particles to form a second methanol steam reforming hydrogen production fluidized bed model after the first methanol steam reforming hydrogen production fluidized bed model is verified; The target parameter module is used to perform numerical simulation on the second methanol steam reforming hydrogen production fluidized bed model to determine the target parameters according to the numerical simulation results of the second methanol steam reforming hydrogen production fluidized bed model.

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