Method for determining the temperature of coke entering the tuyere raceway of a blast furnace based on process simulation

Abstract

The present application relates to a kind of methods for determining the temperature of coke entering tuyere raceway of blast furnace based on process simulation, comprising: for the industrial blast furnace of given size, geometry modeling, mesh division are carried out;Given coke ratio, yield, assume the physical heat of coke entering tuyere raceway zone, determine input parameter;According to input parameter, calculate and set the solid inlet boundary condition at blast hole and the gas inlet boundary condition before tuyere, and the boundary of tuyere raceway;Preliminary calculation solid phase flow field determines dead stock column region, the structure of three-dimensional layered burden;Carry out gas-solid two-phase flow calculation, determine softening zone, and ensure that the coke balance calculation convergence at tuyere, obtain the temperature of coke entering tuyere raceway;Iterative calculation actual physical heat of coke entering tuyere raceway zone, until actual physical heat and the physical heat of coke entering tuyere raceway zone assumed are equal, update theoretical combustion temperature.The present application realizes the accurate quantification of the temperature of coke entering tuyere raceway.

Description

Technical Field

[0001] This invention relates to the field of blast furnace numerical simulation technology, and in particular to a method for determining the temperature of coke entering the blast furnace tuyeres based on process simulation. Background Technology

[0002] In blast furnace smelting, the intensity of the combustion reaction of coke in the tuyere swirl zone at the bottom of the blast furnace directly affects the stability of the blast furnace thermal regime, the smooth operation of smelting, and the overall energy consumption. The inlet temperature of coke entering the tuyere swirl zone is a key local thermal parameter that determines the combustion reaction rate, gas generation, and heat release efficiency. Accurate quantification of this parameter is crucial for optimizing the blast furnace blast regime, adjusting the amount of injected fuel, reducing the coke ratio, and improving the overall energy consumption of the blast furnace, significantly impacting the theoretical combustion temperature of the blast furnace. Due to the harsh environment inside the blast furnace—high temperatures of 1000℃-2000℃, high pressures of tens to hundreds of kPa, and intense coupling of gas-solid-liquid multiphase flow—and the fact that the tuyere swirl zone is located in the core reaction area near the bottom tuyere, direct measurement is impossible. Furthermore, the empirical formula fitting method is highly limited by the operating conditions of the fitted data, only applicable to specific blast furnace volumes and raw material conditions; the calculation error increases dramatically when the operating conditions change. Furthermore, it cannot reflect the spatial distribution of the flow field and temperature field inside the blast furnace, and the calculation accuracy is far from meeting the needs of refined operation of the blast furnace.

[0003] Existing methods utilize numerical simulation techniques (such as CFD) to model blast furnaces and simulate their production processes. By iteratively solving partial differential equations, they aim to predict the internal flow field, temperature field, and chemical reaction rate of the blast furnace, as well as calculate comprehensive performance indicators. However, the model construction, simulation steps, and calculation results output all serve to optimize furnace parameters such as the aspect ratio and throat-to-waist diameter ratio, and improve overall blast furnace performance indicators such as coke ratio, yield, and tuyere pressure. They do not specifically address the precise quantification of key local thermal parameters in the tuyere swirl zone. Specifically, this manifests in two ways: First, the macroscopic performance indicators and furnace parameters are treated as the ultimate goals of the simulation calculation. Intermediate data supporting the solution of local thermal parameters, such as the physical heat of coke entering the tuyere swirl zone and the theoretical combustion temperature, are not considered as core calculation objects. The model lacks precise solution logic and data extraction systems for these local parameters. Second, only the forward simulation calculations of the multiphase flow field and thermochemical process in the blast furnace were completed. The relationship between the theoretical combustion temperature and the physical heat actually brought in by the coke entering the tuyeres and the temperature of the coke entering the tuyeres cannot be reflected. These thermal parameters cannot be specifically quantified. Summary of the Invention

[0004] To address the shortcomings of existing technologies, this invention provides a method for determining the temperature of coke entering the tuyeres of a blast furnace based on process simulation. This method solves the technical problem that existing technologies cannot accurately quantify the temperature of coke entering the tuyeres due to limitations in design objectives and the lack of key technical means.

[0005] The technical solution adopted in this invention is as follows: This invention provides a method for determining the temperature of coke entering the blast furnace tuyeres based on process simulation, comprising: S1. Perform geometric modeling and mesh generation for an industrial blast furnace of a given size; S2. Given the coke ratio and yield, and assuming the physical heat brought in by the coke entering the tuyere vortex zone, determine the input parameters; S3. Based on the input parameters, calculate and set the solid inlet boundary conditions at the furnace throat and the gas inlet boundary conditions in front of the tuyere, as well as the boundary of the tuyere swirl zone; S4. Perform preliminary calculations of the solid flow field to determine the dead material column region; S5. The structure of the three-dimensional layered furnace charge was determined using the timeline tracing method; S6. Calculate the velocity and temperature distributions of the gas and solid phases without considering the soft melting zone and liquid, and the composition after chemical reaction, and solve for the flow field, temperature field and concentration field of the solid and gas phases until the iteration converges. S7. Determine the initial soft melting zone region based on the solid temperature field obtained after iterative convergence; S8. Considering chemical reactions, the remelting zone, and the liquid, recalculate the velocity distribution and temperature distribution of the gas and solid phases, and calculate the liquid-related parameters based on the shape and location of the remelting zone. Calculate the reduction in ore particle size and coke particle size considering particle pulverization, until the remelting zone region converges. S9. Determine whether the coke balance calculation at the tuyeres has converged. If it has not converged, return to S2 to adjust the yield and recalculate. If it has converged, proceed to the next step. S10. Based on the obtained solid flow field and temperature field, obtain the solid temperature and flow rate at any position in the blast furnace, thereby obtaining the temperature of coke entering the tuyeres swirling zone; S11. Iteratively calculate the actual physical heat brought in by the coke entering the tuyer vortex until the actual physical heat is equal to the assumed physical heat brought in by the coke entering the tuyer vortex, and update the theoretical combustion temperature.

[0006] As a preferred technical solution: Step S4, the dead material column region is calculated through inner loop iteration, including: S41. Calculate the initial solid velocity field at the blast furnace inlet, outlet, and furnace wall under boundary conditions; S42. Define the region where the solid velocity is less than the critical velocity as the dead stock region and calculate its volume Vd1; S43. Use the dead material column region as the boundary condition and recalculate the solid velocity field; S44. Determine the new dead material column region and calculate its volume Vd2, then compare Vd2 with Vd1; S45. Repeat S43 to S44 until the residual meets the requirement: |Vd1-Vd2| / Vd1 is less than the set value.

[0007] The method of determining the structure of three-dimensional layered furnace charge using timeline tracing includes: The timeline at the top of the blast furnace is initialized to 0, and the predicted timeline is obtained using the following formula: t batch =m batch / ρ bulk u feed A throat ; In the formula, t batch The m represents the total time required to fill one layer of ore and one layer of coke. batch ρ represents the total weight of a mineral layer and a coking layer. bulk Represents bulk density, u feed A represents the feed rate. throat Represents the cross-sectional area of ​​the blast furnace throat; t batch Multiplying the radial ore volume fraction by the boundary line between the ore and coke yields the three-dimensional furnace charge layered structure. The ore volume fraction is obtained from the top charge batch weight.

[0008] In step S8, the liquid-related parameters are calculated using a liquid adaptive equilibrium model, including liquid flow parameters, liquid temperature distribution, and liquid composition.

[0009] Step S10 includes: Determine whether the actual physical heat is equal to the assumed physical heat brought in by the coke entering the tuyer vortex. If they are not equal, return to step S2 and replace the assumed physical heat brought in by the coke entering the tuyer vortex with the calculated actual physical heat. Iterate and update the theoretical combustion temperature again until they are equal. Output the final temperature of the coke entering the tuyer vortex and the final theoretical combustion temperature.

[0010] The coke balance calculation includes calculating the total coke consumption, which is calculated based on the reaction rate over the entire computational domain according to the convergence result; during the iterative calculation, the total amount of coke and ore added in the next iteration is determined by using the total coke consumption calculated in the previous iteration, until the difference between the amount of coke charged into the furnace and other coke consumption amounts meets the specified error.

[0011] The input parameters include solid phase parameters and gas phase parameters; the solid phase parameters include ore-to-coke ratio distribution, ore composition, coke composition, ore particle size, coke particle size, ore temperature, coke temperature, ore batch weight, pulverized coal injection rate, and pulverized coal composition; the gas phase parameters include injection parameters, blast rate, blast temperature, and oxygen enrichment rate.

[0012] The gas inlet boundary conditions in front of the air vent include gas composition, gas flow rate, and gas temperature.

[0013] In step S4, the solid flow is regarded as a continuous flow of viscous fluid and is assumed to have high viscosity. The solid flow field and temperature field are obtained by discrete governing equations. In step S6, the solid and gas flow fields, temperature fields and concentration fields are solved by discrete mass conservation equations, momentum conservation equations, energy conservation differential equations, transport equations, state equations, phase conservation equations and timeline equations.

[0014] The softening zone is defined as the region where the solid phase temperature is between 1473K and 1673K.

[0015] The technical solution of the present invention can achieve at least some of the following beneficial effects: This invention addresses the problem that existing technologies lack effective means to measure the temperature of coke entering the tuyere vortex zone, which has long been an unmeasurable and difficult-to-accurate thermal parameter of the blast furnace tuyere vortex zone. It constructs a three-dimensional CFD blast furnace process model to simulate the entire process of multiphase flow coupling, heat and mass transfer, and chemical reactions within the blast furnace. By comprehensively considering carbon balance, heat balance, flow field distribution within the furnace, and heat transfer laws, the temperature of coke entering the tuyere vortex zone is accurately quantified, thereby obtaining the precise theoretical combustion temperature of the blast furnace.

[0016] Compared with traditional methods, this invention does not require instrument measurement, thus avoiding the errors caused by it. The calculation results are accurate, providing reliable data support for the optimization of blast furnace theoretical design, blast furnace smelting efficiency improvement and energy consumption reduction.

[0017] This invention's method is adaptable to various types of blast furnaces and different injection and blasting regimes, and changes in operating conditions do not require readjustment of the calculation system. This invention's method is low-cost and provides an effective path for the industrialization of low-carbon metallurgy. Attached Figure Description

[0018] Figure 1 This is a flowchart illustrating the method of an embodiment of the present invention.

[0019] Figure 2 This is a schematic diagram of a three-dimensional assembly model of a blast furnace according to an embodiment of the present invention.

[0020] Figure 3This is a schematic diagram showing the temperature of coke entering the tuyeres' swirling zone at different injection rates, as described in this invention example.

[0021] Figure 4 This is a schematic diagram of the theoretical combustion temperature under different injection rates in an example of the present invention.

[0022] Figure 5 This is a schematic diagram showing the temperature of coke entering the vortex zone at different blowing temperatures, as described in this invention example.

[0023] Figure 6 This is a schematic diagram of the theoretical combustion temperature at different injection temperatures in an example of the present invention.

[0024] Figure 7 This is a schematic diagram showing the temperature of coke entering the vortex zone under different CO2 injection concentrations in an example of the present invention.

[0025] Figure 8 This is a schematic diagram illustrating the theoretical combustion temperature under different CO2 injection concentrations in an example of the present invention. Detailed Implementation

[0026] The specific embodiments of the present invention are described below with reference to the accompanying drawings.

[0027] See Figure 1 This embodiment provides a method for determining the temperature of coke entering the blast furnace tuyeres based on process simulation, including the following steps: S1. Perform geometric modeling and mesh generation for an industrial blast furnace of a given size; S2. Given the coke ratio and yield, and assuming the physical heat brought in by the coke entering the tuyere vortex zone, determine the input parameters; S3. Based on the input parameters, calculate and set the solid inlet boundary conditions at the furnace throat and the gas inlet boundary conditions in front of the tuyere, as well as the boundary of the tuyere swirl zone; S4. Perform preliminary calculations of the solid flow field to determine the dead material column region; S5. The structure of the three-dimensional layered furnace charge was determined using the timeline tracing method; S6. Calculate the velocity and temperature distributions of the gas and solid phases without considering the soft melting zone and liquid, and the composition after chemical reaction, and solve for the flow field, temperature field and concentration field of the solid and gas phases until the iteration converges. S7. Determine the initial soft melting zone region based on the solid temperature field obtained after iterative convergence; S8. Considering chemical reactions, the remelting zone, and the liquid, recalculate the velocity distribution and temperature distribution of the gas and solid phases, and calculate the liquid-related parameters based on the shape and location of the remelting zone. Calculate the reduction in ore particle size and coke particle size considering particle pulverization, until the remelting zone region converges. S9. Determine whether the coke balance calculation at the tuyeres has converged. If it has not converged, return to S2 to adjust the yield and recalculate. If it has converged, proceed to the next step. S10. Based on the obtained solid flow field and temperature field, obtain the solid temperature and flow rate at any position in the blast furnace, thereby obtaining the temperature of coke entering the tuyeres swirling zone; S11. Iteratively calculate the actual physical heat brought in by the coke entering the tuyer vortex until the actual physical heat is equal to the assumed physical heat brought in by the coke entering the tuyer vortex, and update the theoretical combustion temperature.

[0028] As a preferred method, step S1 involves establishing a three-dimensional geometric model for oxygen blast furnaces with different injection regimes. (See [link]) Figure 2 . Figure 2 Figures (a) and (b) show the geometric dimensions of the blast furnace and a schematic diagram of a one-seventh-scale model of the blast furnace, respectively. The specific geometric dimensions are: throat diameter 4.1m, waist diameter 6m, hearth diameter 5.2m, throat height 1.8m, body height 9.3m, belly height 1.2m, waist height 3.0m, and hearth height 1.6m. The blast furnace volume is 380m³. 3 ; As a preferred method, the input parameters determined in step S2 include solid-phase parameters and gas-phase parameters; the solid-phase parameters include ore-to-coke ratio distribution, ore composition, coke composition, ore particle size, coke particle size, ore temperature, coke temperature, ore batch weight, pulverized coal injection rate, and pulverized coal composition; the gas-phase parameters include injection parameters, blast rate, blast temperature, and oxygen enrichment rate; for the three different injection regimes existing in the oxygen blast furnace, corresponding injection parameters are set as follows: (1) Keep the blowing temperature and composition constant, and the blowing rate 4.3 Nm 3 / s~18.3 Nm 3 / s, interval 1 Nm 3 / s; wherein the preferred blowing temperature is 1373K, and the blowing components, by concentration, are: CO2 1.0%, CO 88.4%, H2 8.48%, N2 0.79%, H2O 1.33%.

[0029] (2) Keep the blowing rate and composition constant, and the blowing temperature 1073K~2073K, with an interval of 100K; wherein the blowing rate is preferably 10.3 Nm 3 / s, the sprayed components are the same as in case (1).

[0030] (3) Keep the injection rate and temperature constant, and the injection composition: CO2 concentration is 1%~9%, with an interval of 1%; the injection rate is the same as in case (2), and the injection temperature is the same as in case (1). In all three cases, CO+CO2=89.4%.

[0031] Table 1 Input Parameters for Blast Furnace Simulation

[0032] As a preferred approach, in step S2, it is assumed that the physical heat Q1 brought in by the coke entering the tuyer vortex zone is 2430 kJ / kg.

[0033] As a preferred embodiment, the gas inlet boundary conditions before the air vent in step S3 include theoretical combustion temperature, gas composition, and gas flow rate.

[0034] As a preferred method, step S4 calculates the dead material column region through an inner loop iteration, including: S41. Calculate the initial solid velocity field at the blast furnace inlet, outlet, and furnace wall under boundary conditions; S42. Define the region where the solid velocity is less than the critical velocity as the dead stock region and calculate its volume Vd1; S43. Use the dead material column region as the boundary condition and recalculate the solid velocity field; S44. Determine the new dead material column region and calculate its volume Vd2, then compare Vd2 with Vd1; S45. Repeat S43 to S44 until the residual meets the requirement: |Vd1-Vd2| / Vd1 is less than the set value, which is preferably 0.001.

[0035] As a preferred approach, in step S4, the solid flow is treated as a continuous flow of a viscous fluid, and it is assumed to have high viscosity. The solid flow field and temperature field are obtained by discrete governing equations.

[0036] As a preferred method, step S5, which uses a timeline tracing method to determine the structure of the three-dimensional layered furnace charge, includes: The timeline at the top of the blast furnace is initialized to 0, and the predicted timeline is obtained using the following formula: t batch =m batch / ρ bulk u feed A throat ; In the formula, t batch The m represents the total time required to fill one layer of ore and one layer of coke. batch ρ represents the total weight of a mineral layer and a coking layer. bulk Represents bulk density, u feed A represents the feed rate. throat Represents the cross-sectional area of ​​the blast furnace throat; t batch After multiplying by the radial ore volume fraction, the blast furnace grid is marked along the height direction; In the calculation results of the two time nodes, the regions with the same marked integer are identified as coke layers, while the remaining regions are ore layers, thus obtaining the structure of three-dimensional layered furnace charge.

[0037] As a preferred method, in step S6, the solid and gas phase flow fields, temperature fields, and concentration fields are solved by discrete mass conservation equations, momentum conservation equations, energy conservation differential equations, transport equations, state equations, phase conservation equations, and timeline equations.

[0038] As a preferred embodiment, in step S7, the initial softening zone region is defined as the region where the solid phase temperature is between 1473K and 1673K.

[0039] As a preferred method, in step S8, the liquid-related parameters are calculated using a liquid adaptability balance model, which includes liquid flow parameters, liquid temperature distribution, and liquid composition.

[0040] The liquid adaptive force balance model includes:

[0041] in, The force exerted by the gas on the liquid. The force exerted by a solid on a liquid. C is the force exerted by gravity on the liquid. DG and C DS The drag coefficients for gases and solids are A and A, respectively. g-l and A s-l These represent the effective contact areas of gas-liquid and solid-liquid, respectively, ρ g and ρ l These represent the densities of gases and liquids, U. g and U l The velocity of the gas and the velocity of the liquid are respectively, g is the acceleration due to gravity, and h is the velocity of the liquid. d This refers to the dynamic liquid holdup.

[0042] Specifically, in step S9, the coke balance calculation includes calculating the total coke consumption, which is calculated based on the reaction rate over the entire computational domain according to the convergence result; during the iterative calculation process, the total amount of coke and ore added in the next iteration is determined by using the total coke consumption calculated in the previous iteration, until the difference between the amount of coke charged into the furnace and the coke consumption of other items meets the specified error.

[0043] Specifically, carbon in the blast furnace is mainly consumed through the following chemical reactions: direct reduction, solvent loss reaction, combustion in the tuyeres, and carburizing. The amount of coke (A) charged into the furnace is calculated as follows: carbon consumed by solvent loss reaction (B) + carbon consumed by direct reduction (C) + carbon consumed by water-gas reaction (D) + carbon consumed by silica reduction (E) + carbon consumed by combustion (F) + carbon consumed by carburizing (G). In each iteration, the total coke consumption (=B+C+D+E+F+G) is calculated based on the reaction rate over the entire computational domain according to the convergence result. This total coke consumption is used to determine the total amount of coke (A) and ore added in the next iteration, and this process is repeated until A=B+C+D+E+F+G meets a specified error. This error is preferably set to 0.1 kg / tHM. The coke consumption caused by carburizing is considered a constant.

[0044] Based on this, this embodiment also implements a method for determining the yield. By adjusting the yield, the solid charge rate at the furnace top is adjusted to control the input of coke. When the model converges, the yield is determined.

[0045] As a preferred embodiment, step S10 includes: Determine whether the actual physical heat Q2 is equal to the assumed physical heat Q1 brought in by the coke entering the tuyer vortex. If they are not equal, return to step S2 and replace the assumed physical heat Q1 brought in by the coke entering the tuyer vortex with the calculated actual physical heat Q2. Iterate and update the theoretical combustion temperature again until the actual physical heat is equal to the assumed physical heat. Output the final temperature of the coke entering the tuyer vortex and calculate the final theoretical combustion temperature.

[0046] The theoretical combustion temperature represents the temperature achievable by the combustion and oxidation of carbon into CO in the tuyeres' swirling zone, and the temperature reached by the gas formed when all the physical heat brought in by the blast and fuel is used to heat the gas. In the blast furnace process model, the conditions for the reducing gas generated in the tuyeres are approximated using heat and mass balance, and this is considered as the gas phase input, while a solid (coke) outlet is introduced. The outlet boundary essentially represents the simplified boundary of the tuyeres. Therefore, the solid flow rate at the outlet, which is the remaining charge coke after chemical reaction and carburizing, should correspond to the amount of coke at the tuyeres (the amount of coke burned per ton of molten iron in the swirling zone). Otherwise, the coke balance is not satisfied. Based on this, the theoretical combustion temperature is calculated iteratively. By calculating the actual physical heat brought in by the coke entering the tuyeres' swirling zone, the heat used to heat the gas can be obtained, and the accurate theoretical combustion temperature can be calculated accordingly.

[0047] Numerical simulations show the trends of coke temperature entering the tuyer vortex zone and theoretical combustion temperature under different injection rates, as follows: Figure 3 and Figure 4As shown in the figure, as the injection rate increases, the temperature of coke entering the swirl zone decreases, which is consistent with the downward trend of the theoretical combustion temperature. This is because the increased injection rate leads to an increase in the CO2 content introduced per unit time, which in turn increases the rate of endothermic dissolution reaction, resulting in a decrease in the temperature of the lower part of the blast furnace.

[0048] The trends of coke temperature entering the tuyeres and theoretical combustion temperature under different injection temperatures are shown in the following figures. Figure 5 and Figure 6 As shown in the figure, as the injection temperature increases, the temperature of coke entering the tuyeres gradually rises, and the theoretical combustion temperature also increases. This is because increasing the injection temperature directly introduces more heat into the blast furnace, causing the temperature in the lower part of the blast furnace to rise.

[0049] The trends of temperature variation of coke entering the tuyer vortex zone and theoretical combustion temperature under different CO2 injection concentrations are shown in the figure. Figure 7 and Figure 8 As shown in the figure, with the increase of CO2 injection concentration, the temperature of coke entering the tuyeres and the theoretical combustion temperature both decrease. This is because the increase in CO2 concentration directly promotes the dissolution reaction, resulting in a decrease in the temperature of the lower part of the blast furnace.

[0050] It will be understood by those skilled in the art that the above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention. Although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art can still modify the technical solutions described in the foregoing embodiments or make equivalent substitutions for some of the technical features. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the protection scope of the present invention.

Claims

1. A method for determining the temperature of coke entering the blast furnace tuyeres based on process simulation, characterized in that, include: S1. Perform geometric modeling and mesh generation for an industrial blast furnace of a given size; S2. Given the coke ratio and yield, and assuming the physical heat brought in by the coke entering the tuyere vortex zone, determine the input parameters; S3. Based on the input parameters, calculate and set the solid inlet boundary conditions at the furnace throat and the gas inlet boundary conditions in front of the tuyere, as well as the boundary of the tuyere swirl zone; S4. Perform preliminary calculations of the solid flow field to determine the dead material column region; S5. The structure of the three-dimensional layered furnace charge was determined using the timeline tracing method; S6. Calculate the velocity and temperature distributions of the gas and solid phases without considering the soft melting zone and liquid, and the composition after chemical reaction, and solve for the flow field, temperature field and concentration field of the solid and gas phases until the iteration converges. S7. Determine the initial soft melting zone region based on the solid temperature field obtained after iterative convergence; S8. Considering chemical reactions, the remelting zone, and the liquid, recalculate the velocity distribution and temperature distribution of the gas and solid phases, and calculate the liquid-related parameters based on the shape and location of the remelting zone. Calculate the reduction in ore particle size and coke particle size considering particle pulverization, until the remelting zone region converges. S9. Determine whether the coke balance calculation at the tuyeres has converged. If it has not converged, return to S2 to adjust the yield and recalculate. If it has converged, proceed to the next step. S10. Based on the obtained solid flow field and temperature field, obtain the solid temperature and flow rate at any position in the blast furnace, thereby obtaining the temperature of coke entering the tuyeres swirling zone; S11. Iteratively calculate the actual physical heat brought in by the coke entering the tuyer vortex until the actual physical heat is equal to the assumed physical heat brought in by the coke entering the tuyer vortex, and update the theoretical combustion temperature.

2. The method according to claim 1, characterized in that, Step S4, calculate the dead material column region through inner loop iteration, including: S41. Calculate the initial solid velocity field at the blast furnace inlet, outlet, and furnace wall under boundary conditions; S42. Define the region where the solid velocity is less than the critical velocity as the dead stock region and calculate its volume Vd1; S43. Use the dead material column region as the boundary condition and recalculate the solid velocity field; S44. Determine the new dead material column region and calculate its volume Vd2, then compare Vd2 with Vd1; S45. Repeat S43 to S44 until the residual meets the requirement: |Vd1-Vd2| / Vd1 is less than the set value.

3. The method according to claim 1, characterized in that, The method of determining the structure of three-dimensional layered furnace charge using timeline tracing includes: The timeline at the top of the blast furnace is initialized to 0, and the predicted timeline is obtained using the following formula: t batch =m batch / ρ bulk u feed A throat ; In the formula, t batch The m represents the total time required to fill one layer of ore and one layer of coke. batch ρ represents the total weight of a mineral layer and a coking layer. bulk Represents bulk density, u feed A represents the feed rate. throat Represents the cross-sectional area of ​​the blast furnace throat; t batch Multiplying the radial ore volume fraction by the boundary line between the ore and coke yields the three-dimensional furnace charge layered structure. The ore volume fraction is obtained from the top charge batch weight.

4. The method according to claim 1, characterized in that, In step S8, the liquid-related parameters are calculated using a liquid adaptive equilibrium model, including liquid flow parameters, liquid temperature distribution, and liquid composition.

5. The method according to claim 1, characterized in that, Step S10 includes: Determine whether the actual physical heat is equal to the assumed physical heat brought in by the coke entering the tuyer vortex. If they are not equal, return to step S2 and replace the assumed physical heat brought in by the coke entering the tuyer vortex with the calculated actual physical heat. Iterate and update the theoretical combustion temperature again until they are equal. Output the final temperature of the coke entering the tuyer vortex and the final theoretical combustion temperature.

6. The method according to claim 1, characterized in that, The coke balance calculation includes calculating the total coke consumption, which is calculated based on the reaction rate over the entire computational domain according to the convergence result; during the iterative calculation, the total amount of coke and ore added in the next iteration is determined by using the total coke consumption calculated in the previous iteration, until the difference between the amount of coke charged into the furnace and other coke consumption amounts meets the specified error.

7. The method according to claim 1, characterized in that, The input parameters include solid phase parameters and gas phase parameters; the solid phase parameters include ore-to-coke ratio distribution, ore composition, coke composition, ore particle size, coke particle size, ore temperature, coke temperature, ore batch weight, pulverized coal injection rate, and pulverized coal composition; the gas phase parameters include injection parameters, blast rate, blast temperature, and oxygen enrichment rate.

8. The method according to claim 7, characterized in that, The gas inlet boundary conditions in front of the air vent include gas composition, gas flow rate, and gas temperature.

9. The method according to claim 1, characterized in that, In step S4, the solid flow is regarded as a continuous flow of viscous fluid and is assumed to have high viscosity. The solid flow field and temperature field are obtained by discrete governing equations. In step S6, the solid and gas flow fields, temperature fields and concentration fields are solved by discrete mass conservation equations, momentum conservation equations, energy conservation differential equations, transport equations, state equations, phase conservation equations and timeline equations.

10. The method according to claim 1, characterized in that, The softening zone is defined as the region where the solid phase temperature is between 1473K and 1673K.

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