Method and apparatus for predicting temperature of molten iron in blast furnace smelting, electronic device, and storage medium

Abstract

The present invention provides a method and apparatus for predicting the temperature of molten iron in blast furnace smelting, an electronic device, and a storage medium. The method comprises: acquiring original fuel parameters, blast parameters, coal gas blowing parameters, furnace top coal gas parameters, and slag iron parameters in a blast furnace smelting process; on the basis of the original fuel parameters, the blast parameters, and the coal gas blowing parameters, determining the furnace bosh coal gas amount, the furnace bosh coal gas component, and the theoretical coal gas combustion temperature at a tuyere rotation area; determining the direct reduction degree of iron ore on the basis of the furnace top coal gas parameters, the slag iron parameters, the furnace bosh coal gas amount, and the furnace bosh coal gas component; determining a gas-liquid heat exchange coefficient on the basis of the theoretical coal gas combustion temperature, the furnace bosh coal gas component, the slag iron parameters, and the coal gas component after direct direction; and on the basis of the gas-liquid heat exchange coefficient, the direct reduction degree of iron ore, the theoretical coal gas combustion temperature, and the slag iron parameters, performing iterative solution of the molten iron temperature and the coal gas temperature, so as to complete prediction of the temperature of molten iron in the blast furnace smelting. The accuracy of molten iron temperature prediction can be improved, and a good basis is provided for blast furnace smelting control, ensuring stable and smooth operation of a blast furnace.

Description

Method, device, electronic device and storage medium for predicting molten iron temperature in blast furnace smelting Technical Field

[0001] The present application relates to the technical field of blast furnace smelting, and in particular to a method, device, electronic equipment and storage medium for predicting the temperature of molten iron in blast furnace smelting. Background Art

[0002] During the blast furnace smelting process, molten iron temperature reflects the heat balance within the furnace and the reduction state of the iron ore. Furthermore, gas injection is a key technology for achieving carbon reduction in blast furnaces, and maintaining a stable molten iron temperature is crucial for stable and smooth blast furnace operation under gas injection conditions. Therefore, effectively and accurately predicting molten iron temperature is crucial for controlling blast furnace operations.

[0003] At present, most related technologies determine the temperature variation pattern of molten iron from historical operating data and then predict the molten iron temperature. However, they do not take real-time parameters into consideration sufficiently, which affects the accuracy of the prediction and makes it difficult to reasonably predict the molten iron temperature under gas injection conditions.

[0004] Summary of the Invention

[0005] In view of the shortcomings of the existing technology mentioned above, the present application provides a method, device, electronic equipment and storage medium for predicting the temperature of molten iron in blast furnace smelting to solve the technical problems that the above-mentioned related technologies do not give sufficient consideration to real-time parameters when predicting the temperature of molten iron, which affects the accuracy of the prediction and makes it difficult to reasonably predict the temperature of molten iron under gas injection conditions.

[0006] The present application provides a method for predicting the temperature of molten iron in blast furnace smelting, the method comprising: obtaining raw fuel parameters, blast parameters, gas injection parameters, furnace top gas parameters and slag iron parameters in the blast furnace smelting process; determining the total heat income, bosh gas volume and bosh gas composition of the tuyere swirl zone according to the raw fuel parameters, the blast parameters and the gas injection parameters, and determining the theoretical combustion temperature of the gas in the tuyere swirl zone according to the total heat income, the bosh gas volume and the bosh gas composition; determining the theoretical combustion temperature of the gas in the tuyere swirl zone according to the total heat income, the bosh gas volume and the bosh gas composition; determining the theoretical combustion temperature of the gas in the tuyere swirl zone according to the top gas parameters, the slag iron parameters, the bosh gas volume and the bosh gas composition. direct reduction degree; determining the gas-liquid heat exchange coefficient according to the theoretical combustion temperature of the gas, the bosh gas composition, the slag-iron parameters and the gas composition after direct reduction at the direct reduction position, wherein the gas composition after direct reduction is determined based on the top gas parameters, or the gas composition after direct reduction is determined based on the top gas parameters, the bosh gas volume and the bosh gas composition; based on the gas-liquid heat exchange coefficient, the direct reduction degree of the iron ore, the theoretical combustion temperature of the gas and the slag-iron parameters, performing iterative solution for the molten iron temperature and the gas temperature until the first convergence condition is met, thereby completing the prediction of the molten iron temperature for blast furnace smelting.

[0007] In one embodiment of the present application, the total heat income, the amount of furnace gas and the composition of furnace gas in the tuyere swirl zone are determined according to the raw fuel parameters, the blast parameters and the gas injection parameters, so as to determine the theoretical combustion temperature of the gas in the tuyere swirl zone according to the total heat income, the amount of furnace gas and the composition of furnace gas, including: determining the volume of gas participating in the chemical reaction, the volume of gas not participating in the chemical reaction and the volume of gas generated by the chemical reaction in the tuyere swirl zone according to the raw fuel parameters, the blast parameters and the gas injection parameters; calculating the chemical reaction release temperature of the tuyere swirl zone based on the volume of gas participating in the chemical reaction Heat, and the total heat income is calculated based on the coke sensible heat, blast sensible heat, gas sensible heat and the heat released by the chemical reaction in the tuyere swirl zone, the coke sensible heat is determined based on the raw fuel parameters, the blast sensible heat is determined based on the blast parameters, and the gas sensible heat is determined based on the gas injection parameters; the bosh gas volume and the bosh gas composition are calculated based on the gas volume generated by the chemical reaction and the gas volume not participating in the chemical reaction; the theoretical gas combustion temperature is iteratively solved based on the bosh gas volume, the bosh gas composition and the total heat income until the second convergence condition is met, so as to obtain the theoretical gas combustion temperature.

[0008] In one embodiment of the present application, before calculating the total heat income based on the coke sensible heat, blast sensible heat, gas sensible heat and the heat released by the chemical reaction in the tuyere swirl zone, the method includes: determining the coke specific heat capacity based on the preset coke temperature and coke composition, so as to calculate the coke sensible heat based on the preset coke temperature, the coke specific heat capacity and the coke usage, and the raw fuel parameters include the coke composition and the coke usage; determining the blast specific heat capacity based on the blast temperature and blast composition, so as to calculate the blast sensible heat based on the blast specific heat capacity, the blast volume and the blast temperature, and the blast parameters include the blast composition, the blast temperature and the blast volume; determining the injected coal gas specific heat capacity based on the preset injected coal gas temperature and injected coal gas composition, so as to calculate the coal gas sensible heat based on the preset injected coal gas temperature, the injected coal gas specific heat capacity and the coal gas injection volume, and the coal gas injection parameters include the injected coal gas composition and the coal gas injection volume.

[0009] In one embodiment of the present application, the theoretical combustion temperature of the gas is iteratively solved based on the bosh gas volume, the bosh gas composition and the total heat income until the second convergence condition is met to obtain the theoretical combustion temperature of the gas, including: determining the initial bosh gas specific heat capacity of the tuyere swirl zone based on the bosh gas composition and the preset theoretical combustion temperature of the gas, and calculating the initial theoretical combustion temperature of the gas based on the total heat income, the bosh gas volume and the initial bosh gas specific heat capacity; using the initial theoretical combustion temperature of the gas as the theoretical combustion temperature of the gas before iteration, determining the iterative bosh gas specific heat capacity of the tuyere swirl zone based on the bosh gas composition and the theoretical combustion temperature of the gas before iteration, and calculating the initial theoretical combustion temperature of the gas based on the total heat income, the bosh gas volume and the initial The iterative furnace bosh gas specific heat capacity is used to calculate the theoretical combustion temperature of the gas after iteration; the difference between the theoretical combustion temperature of the gas before iteration and the theoretical combustion temperature of the gas after iteration is calculated to obtain the iterative temperature difference of the theoretical combustion temperature of the gas; if the iterative temperature difference of the theoretical combustion temperature of the gas is less than or equal to the second preset temperature difference threshold, the second convergence condition is met, and the theoretical combustion temperature of the gas after iteration is used as the theoretical combustion temperature of the gas; if the iterative temperature difference of the theoretical combustion temperature of the gas is greater than the second preset temperature difference threshold, the theoretical combustion temperature of the gas is iteratively solved based on the furnace bosh gas amount, the furnace bosh gas composition, the total heat income and the theoretical combustion temperature of the gas after iteration until the second convergence condition is met to obtain the theoretical combustion temperature of the gas.

[0010] In one embodiment of the present application, the direct reduction degree of iron ore is determined according to the top gas parameters, the slag iron parameters, the bosh gas amount and the bosh gas composition, including: determining the amount of carbon monoxide in the bosh gas based on the bosh gas amount and the bosh gas composition, and determining the total amount of carbon monoxide and carbon dioxide in the top gas based on the top gas amount and the top gas composition, so as to determine the total amount of carbon monoxide generated by direct reduction according to the amount of carbon monoxide in the bosh gas and the total amount of carbon monoxide and carbon dioxide in the top gas, wherein the top gas parameters include the top gas amount and the top gas composition; The mass of trace elements in the molten iron and the mass of iron in the molten iron are determined based on the molten iron composition and the molten iron output, and the amount of carbon monoxide generated by direct reduction of trace element oxides is determined based on the mass of the trace elements in the molten iron, so as to determine the amount of carbon monoxide generated by direct reduction of iron ore according to the total amount of carbon monoxide generated by direct reduction and the amount of carbon monoxide generated by direct reduction of trace element oxides, wherein the slag iron parameters include the molten iron composition and the molten iron output; the direct reduction degree of the iron ore is calculated based on the amount of carbon monoxide generated by direct reduction of the iron ore, the mass of the iron in the molten iron and the mass of iron in the preset hot-pressed iron blocks.

[0011] In one embodiment of the present application, before determining the gas-liquid heat exchange coefficient, the method includes: determining the total amount of carbon monoxide and carbon dioxide in the top gas, the total amount of water and hydrogen in the top gas, and the amount of nitrogen in the top gas based on the top gas amount and the top gas composition, wherein the top gas parameters include the top gas amount and the top gas composition; using the top gas amount as the direct reduction gas amount, the total amount of carbon monoxide and carbon dioxide in the top gas as the carbon monoxide amount in the direct reduction gas, the total amount of water and hydrogen in the top gas as the hydrogen amount in the direct reduction gas, and the nitrogen amount in the top gas as the nitrogen amount in the direct reduction gas; and determining the direct reduction gas composition based on the direct reduction gas amount, the carbon monoxide amount in the direct reduction gas, the hydrogen amount in the direct reduction gas, and the nitrogen amount in the direct reduction gas.

[0012] In one embodiment of the present application, before determining the gas-liquid heat exchange coefficient, the method includes: determining the total amount of carbon monoxide and carbon dioxide in the top gas based on the top gas amount and the top gas composition, wherein the top gas parameters include the top gas amount and the top gas composition; determining the amount of hydrogen in the bosh gas and the amount of nitrogen in the bosh gas based on the bosh gas amount and the bosh gas composition; using the top gas amount as the direct reduction gas amount, the total amount of carbon monoxide and carbon dioxide in the top gas as the amount of carbon monoxide in the direct reduction gas, the amount of hydrogen in the bosh gas as the amount of hydrogen in the direct reduction gas, and the amount of nitrogen in the bosh gas as the amount of nitrogen in the direct reduction gas; determining the direct reduction gas composition based on the direct reduction gas amount, the amount of carbon monoxide in the direct reduction gas, the amount of hydrogen in the direct reduction gas, and the amount of nitrogen in the direct reduction gas.

[0013] In one embodiment of the present application, the gas-liquid heat exchange coefficient is determined based on the theoretical combustion temperature of the coal gas, the bosh gas composition, the slag iron parameters and the direct reduction gas composition of the direct reduction position, including: interpolating the coal gas composition of the bosh gas and the coal gas composition after direct reduction to obtain the coal gas composition of the dripping zone; determining the gas-liquid heat exchange coefficient of the tuyere vortex zone based on the equivalent particle size of slag iron, the coal gas thermal conductivity of the tuyere vortex zone and the Nusselt number of the tuyere vortex zone, the coal gas thermal conductivity of the tuyere vortex zone and the Nusselt number of the tuyere vortex zone are both determined based on the bosh gas composition and the theoretical combustion temperature of the gas, and the equivalent particle size of slag iron is determined based on the The slag and iron parameters are determined; the gas-liquid heat exchange coefficient at the direct reduction position is determined according to the equivalent particle size of the slag and iron, the thermal conductivity of the coal gas at the direct reduction position, and the Nusselt number of the direct reduction position, and the coal gas thermal conductivity at the direct reduction position and the Nusselt number of the direct reduction position are both determined based on the coal gas composition after direct reduction and the theoretical combustion temperature of the coal gas; the gas-liquid heat exchange coefficient of the dripping zone is determined according to the equivalent particle size of the slag and iron, the thermal conductivity of the coal gas in the dripping zone, and the Nusselt number of the dripping zone, and the coal gas thermal conductivity of the dripping zone and the Nusselt number of the dripping zone are both determined based on the coal gas composition in the dripping zone and the theoretical combustion temperature of the coal gas.

[0014] In one embodiment of the present application, based on the gas-liquid heat exchange coefficient, the direct reduction degree of the iron ore, the theoretical combustion temperature of the coal gas and the slag iron parameters, the molten iron temperature and the coal gas temperature are iteratively solved until the first convergence condition is met, and the molten iron temperature prediction is completed, including: determining the direct reduction heat consumption according to the molten iron composition and the direct reduction degree of the iron ore, and the slag iron parameters include the molten iron composition; based on the coal gas phase temperature, the molten iron phase temperature, the gas-liquid heat exchange coefficient and the direct reduction heat consumption, and according to the coal gas phase energy conservation relationship and the molten iron phase energy conservation relationship, the molten iron temperature and the coal gas temperature are iteratively solved to obtain the molten iron temperature in the tuyere raceway before iteration, the molten iron temperature in the tuyere raceway after iteration, and the coal gas temperature before and after direct reduction. The gas temperature and the gas temperature after direct reduction after iteration, the initial value of the gas phase temperature is the theoretical combustion temperature of the gas, and the initial value of the molten iron phase temperature is the preset molten iron temperature after direct reduction; determine the difference between the molten iron temperature in the tuyere raceway before iteration and the molten iron temperature in the tuyere raceway after iteration as the iterative temperature difference of molten iron temperature, and determine the difference between the gas temperature after direct reduction before iteration and the gas temperature after direct reduction after iteration as the iterative temperature difference of gas temperature; if the iterative temperature difference of molten iron temperature and the iterative temperature difference of gas temperature are both less than or equal to the first preset temperature difference threshold, then the first convergence condition is met, and the molten iron temperature in the tuyere raceway after iteration is used as the final prediction result of molten iron temperature prediction.

[0015] In one embodiment of the present application, a device for predicting the temperature of molten iron in blast furnace smelting is also provided, and the device includes: a smelting data acquisition module for acquiring raw fuel parameters, blast parameters, gas injection parameters, furnace top gas parameters and slag iron parameters of the blast furnace smelting process; a theoretical combustion temperature determination module for determining the total heat income, the furnace bosh gas volume and the furnace bosh gas composition of the tuyere swirl zone according to the raw fuel parameters, the blast parameters and the gas injection parameters, so as to determine the theoretical combustion temperature of the gas in the tuyere swirl zone according to the total heat income, the furnace bosh gas volume and the furnace bosh gas composition; a direct reduction degree determination module for determining the theoretical combustion temperature of the gas in the tuyere swirl zone according to the top gas parameters, the slag iron parameters, the furnace bosh gas volume and the furnace bosh gas composition. The bosh gas composition is used to determine the direct reduction degree of the iron ore; a heat exchange coefficient determination module is used to determine the gas-liquid heat exchange coefficient according to the theoretical combustion temperature of the gas, the bosh gas composition, the slag iron parameters and the gas composition after direct reduction at the direct reduction position, wherein the gas composition after direct reduction is determined based on the furnace top gas parameters, or the gas composition after direct reduction is determined based on the furnace top gas parameters, the bosh gas volume and the bosh gas composition; an iterative solution module is used to iteratively solve the molten iron temperature and the gas temperature based on the gas-liquid heat exchange coefficient, the direct reduction degree of the iron ore, the theoretical combustion temperature of the gas and the slag iron parameters until the first convergence condition is met, thereby completing the prediction of the molten iron temperature in blast furnace smelting.

[0016] In one embodiment of the present application, an electronic device is also provided, which includes: one or more processors; a storage device for storing one or more programs, and when the one or more programs are executed by the one or more processors, the electronic device implements the blast furnace smelting molten iron temperature prediction method as described above.

[0017] In one embodiment of the present application, a computer-readable storage medium is further provided, on which a computer program is stored. When the computer program is executed by a computer processor, the computer executes the above-mentioned method for predicting the temperature of molten iron in blast furnace smelting.

[0018] The beneficial effects of the present invention are as follows: The present invention provides a method, device, electronic device and storage medium for predicting the temperature of molten iron in blast furnace smelting. The method calculates by using the raw fuel parameters, blast parameters, gas injection parameters, furnace top gas parameters and slag iron parameters of the blast furnace smelting process to obtain the theoretical combustion temperature of gas, the gas-liquid heat exchange coefficient and the direct reduction degree of iron ore, thereby iteratively solving the molten iron temperature and the gas temperature. It can realize the prediction of the molten iron temperature in blast furnace smelting under various working conditions such as gas injection conditions, and improve the accuracy of the molten iron temperature prediction, providing a good basis for the operation control of blast furnace smelting to ensure the stable and smooth operation of the blast furnace.

[0019] It should be understood that the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the present application. BRIEF DESCRIPTION OF THE DRAWINGS

[0020] FIG1 is a flow chart of a method for predicting the temperature of molten iron in a blast furnace according to an exemplary embodiment of the present application;

[0021] FIG2 is a schematic structural diagram of a water temperature prediction system for a blast furnace iron smelting process according to a specific embodiment of the present application;

[0022] 3 is a schematic diagram of a blast furnace iron smelting process water temperature prediction system in a specific embodiment of the embodiment shown in FIG2 ;

[0023] FIG4 is a block diagram of a device for predicting the temperature of molten iron in a blast furnace according to an exemplary embodiment of the present application;

[0024] FIG5 is a schematic structural diagram of an electronic device according to an exemplary embodiment of the present application. DETAILED DESCRIPTION

[0025] The following describes the embodiments of the present application through specific examples. Those skilled in the art can easily understand the other advantages and effects of the present application from the content disclosed in this specification. The present application can also be implemented or applied through other different specific embodiments. The details in this specification can also be modified or changed based on different viewpoints and applications without departing from the spirit of the present application. It should be noted that the following embodiments and features in the embodiments can be combined with each other unless they conflict.

[0026] It should be noted that the illustrations provided in the following embodiments are only schematic illustrations of the basic concept of the present application. Therefore, the illustrations only show components related to the present application and are not drawn according to the number, shape and size of components in actual implementation. In actual implementation, the type, quantity and proportion of each component can be changed at will, and the component layout type may also be more complicated.

[0027] It should be noted that in this application, "first," "second," and the like are merely used to distinguish similar objects, and do not limit the order or precedence of similar objects. The variations of "including," "having," and the like indicate that the scope of the subject of the term is not exclusive, in addition to the examples shown in the term.

[0028] It should be understood that the various numbers, step numbers, and other reference numerals in this application are provided for ease of description and are not intended to limit the scope of this application. The order of reference numerals in this application does not necessarily imply a specific order of execution; the order of execution of each process is determined by its function and inherent logic.

[0029] In the following description, a large number of details are discussed to provide a more thorough explanation of the embodiments of the present application. However, it is obvious to those skilled in the art that the embodiments of the present application can be implemented without these specific details. In other embodiments, well-known structures and devices are shown in the form of block diagrams rather than in detail to avoid making the embodiments of the present application difficult to understand.

[0030] The embodiments of the present application respectively propose a method for predicting the temperature of molten iron in blast furnace smelting, a device for predicting the temperature of molten iron in blast furnace smelting, an electronic device, a computer-readable storage medium and a computer program product. These embodiments will be described in detail below.

[0031] In one embodiment of the present application, a method for predicting the temperature of molten iron in blast furnace smelting is proposed, comprising: obtaining raw fuel parameters, blast parameters, gas injection parameters, top gas parameters and slag iron parameters in the blast furnace smelting process; determining the total heat income, bosh gas volume and bosh gas composition of the tuyere swirl zone according to the raw fuel parameters, blast parameters and gas injection parameters, and determining the theoretical combustion temperature of the gas in the tuyere swirl zone according to the total heat income, bosh gas volume and bosh gas composition; determining the theoretical combustion temperature of the gas in the tuyere swirl zone according to the total heat income, bosh gas volume and bosh gas composition; determining the theoretical combustion temperature of the gas in the tuyere swirl zone according to the top gas parameters, slag iron parameters, bosh gas volume and bosh gas composition. Determine the direct reduction degree of iron ore; determine the gas-liquid heat exchange coefficient based on the theoretical combustion temperature of coal gas, the composition of furnace bosh gas, the slag iron parameters and the composition of the direct reduction gas at the direct reduction position, the gas-liquid heat exchange coefficient is determined, the composition of the direct reduction gas is determined based on the furnace top gas parameters, or the composition of the direct reduction gas is determined based on the furnace top gas parameters, the furnace bosh gas volume and the furnace bosh gas composition; based on the gas-liquid heat exchange coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of coal gas and the slag iron parameters, iteratively solve the molten iron temperature and the coal gas temperature until the first convergence condition is met, and complete the prediction of the molten iron temperature of blast furnace smelting. It can be seen that the technical solution of the embodiment of the present application can realize the prediction of the molten iron temperature of blast furnace smelting under various working conditions such as gas injection working conditions, and improve the accuracy of the molten iron temperature prediction, providing a good basis for the operation control of blast furnace smelting to ensure the stable and smooth operation of the blast furnace.

[0032] Please refer to Figure 1, which is a flow chart of a method for predicting the temperature of molten iron in a blast furnace, according to an exemplary embodiment of the present application. As shown in Figure 1, in an exemplary embodiment, the method for predicting the temperature of molten iron in a blast furnace includes at least steps S110 to S150, which are described in detail as follows:

[0033] Step S110, obtaining raw fuel parameters, blast parameters, gas injection parameters, top gas parameters and slag and iron parameters of the blast furnace smelting process.

[0034] In one embodiment of the present application, the raw fuel parameters refer to the raw fuel composition and raw fuel usage, and may include at least one of the coke composition and coke usage, the pulverized coal composition and pulverized coal usage, etc. The raw fuel composition refers to the ratio of substances in the raw fuel to the raw fuel. For example, the coke composition may include the ratio of C (carbon), H (hydrogen), O (oxygen), N (nitrogen), S (sulfur), volatile matter, ash, etc. in the coke, and the pulverized coal composition may include the ratio of C, H, O, N, S, volatile matter, ash, etc. in the pulverized coal.

[0035] The blast parameters may include at least one of blast volume, blast temperature, blast composition, etc., wherein the blast composition may include at least one of blast humidity, oxygen enrichment rate, etc.

[0036] Gas injection parameters include at least one of the following: the type of injection medium, the composition of the injected gas, the gas injection rate, and the injected gas temperature. The type of injection medium includes a mixture of one or more of coke oven gas, converter gas, decarbonized blast furnace gas, natural gas, pure hydrogen, chemical tail gas, shale gas, and the like. The composition of the injected gas refers to the ratio of substances in the injected gas. For example, the composition of the injected gas may include the ratio of H2 (hydrogen), CO (carbon monoxide), CO2 (carbon dioxide), CH4 (methane), N2 (nitrogen), and O2 (oxygen).

[0037] Top gas parameters include at least one of top gas composition and top gas volume. Top gas composition refers to the ratio of substances in the top gas. For example, top gas composition may include the ratio of H2, CO, CO2, N2, etc. in the top gas.

[0038] The slag parameters include at least one of the following: molten iron composition (i.e., slag composition), molten iron output, and slag production (i.e., slag volume). Molten iron composition refers to the ratio of substances in the molten iron. For example, the molten iron composition may include the ratios of Fe (iron), C, Si (silicon), Mn (manganese), P (phosphorus), S, and Ti (titanium).

[0039] It should be understood that the raw fuel parameters, blast parameters, gas injection parameters, top gas parameters and slag iron parameters are real-time data of the blast furnace smelting process, which can directly and in real time reflect the smelting conditions in the blast furnace. Therefore, the molten iron temperature can be accurately predicted based on the raw fuel parameters, blast parameters, gas injection parameters, top gas parameters and slag iron parameters.

[0040] Step S120, determining the total heat income, bosh gas volume and bosh gas composition of the tuyere swirl zone based on the raw fuel parameters, blast parameters and gas injection parameters, so as to determine the theoretical combustion temperature of the gas in the tuyere swirl zone based on the total heat income, bosh gas volume and bosh gas composition.

[0041] In one embodiment of the present application, the blast furnace includes five zones, namely, from top to bottom, the block zone, the soft melting zone, the dripping zone, the tuyere vortex zone and the slag zone, which are distributed at different height positions inside the blast furnace. The block zone is used for evaporation of moisture in the charge and thermal decomposition, iron ore reduction, heat exchange between the charge and coal gas, etc. The charge is softened in the soft melting zone, and the lower boundary of the soft melting zone begins to melt and drip, and the direct reduction reaction of blast furnace ironmaking is carried out to form initial slag. Therefore, the lower boundary of the soft melting zone is the direct reduction position. In the dripping zone, various chemical reactions occur between the dripping liquid slag and the coal gas and solid carbon. In the tuyere vortex zone, the injected fuel and the hot air undergo a combustion reaction to produce high-temperature coal gas. In the slag zone, slag-metal reaction occurs at the interface between the slag and iron layers and when the iron droplets pass through the slag layer.

[0042] The slag in the tuyere raceway is liquid, and liquid slag is molten iron. Accordingly, the molten iron temperature refers to the slag temperature of the liquid slag in the tuyere raceway. Due to heat exchange between molten iron and coal gas, the molten iron temperature is affected by the theoretical combustion temperature of the coal gas in the tuyere raceway. Therefore, it is necessary to determine the theoretical combustion temperature of the coal gas. This can be determined by determining the total heat input, bosh gas volume, and bosh gas composition of the tuyere raceway based on the raw fuel parameters, air blast parameters, and coal gas injection parameters.

[0043] In one embodiment of the present application, step S120 includes: determining the volume of gas participating in the chemical reaction, the volume of gas not participating in the chemical reaction and the volume of gas generated by the chemical reaction in the tuyere vortex zone based on the raw fuel parameters, blast parameters and gas injection parameters; calculating the heat released by the chemical reaction in the tuyere vortex zone based on the volume of gas participating in the chemical reaction, and calculating the total heat income based on the coke sensible heat, blast sensible heat, gas sensible heat and the heat released by the chemical reaction in the tuyere vortex zone, the coke sensible heat is determined based on the raw fuel parameters, the blast sensible heat is determined based on the blast parameters, and the gas sensible heat is determined based on the gas injection parameters; calculating the furnace bosh gas volume and the furnace bosh gas composition based on the gas volume generated by the chemical reaction and the gas volume not participating in the chemical reaction; iteratively solving the theoretical combustion temperature of the gas based on the furnace bosh gas volume, the furnace bosh gas composition and the total heat income until the second convergence condition is met to obtain the theoretical combustion temperature of the gas.

[0044] In this embodiment, please refer to Table 1, which is a table of chemical reactions and thermal effects in the tuyere raceway in a specific embodiment of the present application. As shown in Table 1, in the tuyere raceway, the injected coal gas, injected coal powder and the elemental carbon or CO2 or H2O (water) or CH4 or chemical C x H y O m N n After contact with oxygen or other substances, combustion and other chemical reactions occur, all of them are converted into CO, H2 and N2, and the thermal effects of different chemical reactions are different.

[0045] Table 1

[0046] Therefore, the heat released by the chemical reaction in the tuyere raceway is calculated as follows: Q2 = aΔH C1 +bΔH C2 +cΔH CH4 +dΔH C3 +eΔH C4 Formula (1)

[0047] Where Q2 is the heat released by the chemical reaction in the tuyere raceway, a, b, c, d, e are the reaction participation amounts corresponding to reactions 1-5 in Table 1, ΔH C1 , ΔH C2 , ΔH CH4 , ΔH C3 , ΔH C4 The thermal effects corresponding to reactions 1-5 in Table 1 are shown in order. The values ​​of a, b, and c depend on the volume of CO2, H2O, and CH4 in the injected coal gas, and the values ​​of d and e depend on the total amount of oxygen entering the blast furnace. It should be noted that when calculating the heat released by the chemical reaction in the tuyere raceway, O2 preferentially reacts with CH4 and C x H y O m N n The gases react and finally react with solid carbon C. The combustion priority among coal gas, coal powder, coke and oxygen is: coal gas > coal powder > coke, and the coal powder burnout rate is 70-84%.

[0048] Therefore, when calculating the heat released by the chemical reaction in the tuyere raceway, we can first determine the volume of the gas involved in the chemical reaction in the tuyere raceway, including the volume of CO2, H2O, CH4, C x H y O m N n Volume and O2 volume. Specifically, it can be based on the CO2 ratio, H2O ratio, CH4 ratio, C x H y O m Nn ratio and gas injection volume, determine the volume of CO2, H2O, CH4 and C in the injected gas x H y O m N n Volume, wherein the gas injection parameters include the injected gas composition and the gas injection amount. The O2 volume in the injected gas is determined based on the O2 ratio in the injected gas composition and the gas injection amount; the O2 volume in the blast is determined based on the O2 ratio in the blast composition and the blast amount, wherein the blast parameters include the blast composition and the blast amount; the O2 volume in coke is determined based on the O2 ratio in the coke composition and the coke usage, and the O2 volume in pulverized coal is determined based on the O2 ratio in the pulverized coal composition and the pulverized coal usage, wherein the raw fuel parameters include the coke composition and the coke usage, the pulverized coal composition and the pulverized coal usage. The total amount of oxygen entering the blast furnace is calculated based on the O2 volume in the injected gas, the O2 volume in the blast, the O2 volume in the coke, and the O2 volume in the pulverized coal, and the calculation method is as follows:

[0049] Among them, V t is the total amount of oxygen entering the blast furnace, is the volume of O2 in the blast, is the volume of O2 in the injected gas, is the volume of O2 in coke, is the volume of O2 in pulverized coal.

[0050] After obtaining the heat released by the chemical reaction in the tuyere raceway, the total heat income of the tuyere raceway is calculated based on the coke sensible heat, blast sensible heat, gas sensible heat and the heat released by the chemical reaction in the tuyere raceway. The calculation method is as follows: Q = Q1 + Q2 + Q3 + Q4 Formula (3)

[0051] Where Q is the total heat input in the tuyere vortex zone, Q1 is the blast sensible heat, Q2 is the heat released by chemical reactions in the tuyere vortex zone, Q3 is the gas sensible heat, and Q4 is the coke sensible heat. Blast sensible heat is determined based on blast parameters, gas sensible heat is determined based on gas injection parameters, and coke sensible heat is determined based on raw fuel parameters.

[0052] The bosh gas in the tuyere vortex zone includes gases produced by chemical reactions and gases that do not participate in the chemical reactions. The volume of gases produced by the chemical reactions in the tuyere vortex zone, including the volume of CO and the volume of H2, can be determined based on the volume of gases participating in the chemical reactions in the tuyere vortex zone and the reaction formulas in Table 1. Since pulverized coal, injected coal gas, and blast contain N2, according to Table 1, there is no N2 in the gases participating in the chemical reactions. The volume of N2 in pulverized coal, injected coal gas, and blast can be determined as the volume of gases that do not participate in the chemical reactions. The volume of N2 in pulverized coal can be determined based on the proportion of N2 in the pulverized coal component and the amount of pulverized coal used, the volume of N2 in the injected coal gas can be determined based on the proportion of N2 in the injected coal gas component and the amount of gas injected, and the volume of N2 in the blast can be determined based on the proportion of N2 in the blast component and the amount of blast. Then, the amount of bosh gas can be calculated based on the volume of gases produced by the chemical reactions and the volume of gases that do not participate in the chemical reactions. The calculation method is as follows:

[0053] Among them, V G is the amount of bosh gas, is the volume of CO produced after the coke reacts in the tuyere raceway, is the volume of CO produced by the reaction of pulverized coal in the tuyere vortex zone, is the volume of CO produced after the injected coal gas reacts in the vortex zone of the tuyere, is the volume of CO produced by the reaction of water in the blast in the vortex zone of the tuyere, is the volume of H2 produced by the reaction between the moisture in the pulverized coal and the hydrogen in the volatile matter in the tuyere vortex zone, is the volume of H2 produced by the reaction of water in the vortex zone of the tuyere, It is the volume of H2 produced by the reaction between water in the injected coal gas and hydrogen-containing gas (such as methane, ethane, ethylene, etc.) in the tuyere vortex zone. is the volume of N2 in pulverized coal, is the volume of N2 in the injected gas, is the volume of N2 in the blast. Schematically, Including the volume of CO produced by the reaction of fixed carbon in pulverized coal, carbon in volatile matter and water, Including coal powder volatilization and the volume of N2 in coal powder carrier gas.

[0054] As can be seen from formula (4), the bosh gas includes CO, H2 and N2. The volume of CO, H2 and N2 in the bosh gas can be determined according to the volume of gas generated by the chemical reaction and the volume of gas not participating in the chemical reaction. The CO ratio in the bosh gas is calculated according to the volume of CO in the bosh gas and the amount of bosh gas. The H2 ratio in the bosh gas is calculated according to the volume of H2 in the bosh gas and the amount of bosh gas. The N2 ratio in the bosh gas is calculated according to the volume of N2 in the bosh gas and the amount of bosh gas. The CO ratio, H2 ratio and N2 volume in the bosh gas are used as the bosh gas components.

[0055] After obtaining the total heat income, bosh gas volume, and bosh gas composition, the theoretical gas combustion temperature is iteratively solved based on the bosh gas volume, bosh gas composition, and total heat income until a second convergence condition is met to obtain the theoretical gas combustion temperature. Illustratively, the second convergence condition can be that the number of iterations of the iterative solution for the theoretical gas combustion temperature meets a second preset number of iterations, or that the iterative temperature difference of the theoretical gas combustion temperature is less than or equal to a second preset temperature difference threshold, or other convergence conditions, which are not limited here. By using the sum of the coke sensible heat, blast sensible heat, gas sensible heat, and heat released by chemical reactions as the total heat income, the heat released is fully considered, thereby improving the accuracy of the theoretical gas combustion temperature calculation.

[0056] In one embodiment of the present application, before calculating the total heat income based on the coke sensible heat, blast sensible heat, gas sensible heat and heat released by the chemical reaction in the tuyere swirl zone, the method includes: determining the coke specific heat capacity based on the preset coke temperature and coke composition, so as to calculate the coke sensible heat based on the preset coke temperature, coke specific heat capacity and coke usage, and the raw fuel parameters include coke composition and coke usage; determining the blast specific heat capacity based on the blast temperature and blast composition, so as to calculate the blast sensible heat based on the blast specific heat capacity, blast volume and blast temperature, and the blast parameters include blast composition, blast temperature and blast volume; determining the injected coal gas specific heat capacity based on the preset injected coal gas temperature and injected coal gas composition, so as to calculate the coal gas sensible heat based on the preset injected coal gas temperature, injected coal gas specific heat capacity and coal gas injection volume, and the coal gas injection parameters include injected coal gas composition and coal gas injection volume.

[0057] In this embodiment, blast air, coke, and injected coal gas are all composed of different substances. The specific heat capacity of different substances is different, and the specific heat capacity of the same substance at different temperatures is also different. Therefore, the relationship between the specific heat capacity of different substances and temperature can be established in advance.

[0058] When calculating the sensible heat of the blast, first determine the specific heat of each substance in the blast at the blast temperature based on the preset relationship between the specific heat and temperature of different substances and the blast temperature in the blast parameters. Then calculate the specific heat of the blast based on the specific heat of each substance in the blast at the blast temperature and the proportion of each substance in the blast composition in the blast parameters. Finally, calculate the sensible heat of the blast based on the specific heat of the blast, the blast temperature and the blast volume in the blast parameters. The calculation method is as follows: Q1=C b V b T b Formula (5)

[0059] Among them, Q1 is the sensible heat of the blast, C b is the blast specific heat capacity, V b is the blast volume, T b is the blast temperature.

[0060] When calculating the sensible heat of the gas, first determine the specific heat capacity of each substance in the injected gas at the preset gas injection temperature based on the preset relationship between the specific heat capacity of different substances and temperature and the preset gas injection temperature. Then, calculate the specific heat capacity of the injected gas based on the specific heat capacity of each substance in the injected gas at the preset gas injection temperature and the proportion of each substance in the injected gas composition in the gas injection parameters. Finally, calculate the sensible heat of the gas based on the specific heat capacity of the injected gas, the preset gas injection temperature, and the gas injection amount in the gas injection parameters. The calculation method is as follows: Q3 = C gi V gi T gi Formula (6)

[0061] Among them, Q3 is the sensible heat of gas, C gi is the specific heat capacity of the injected gas, V gi is the gas injection rate, T gi It is the preset injection gas temperature.

[0062] When calculating the sensible heat of coke, first determine the specific heat capacity of each substance in the coke at the preset coke temperature based on the preset relationship between the specific heat capacity of different substances and temperature and the preset coke temperature. Then calculate the specific heat capacity of coke based on the specific heat capacity of each substance in the coke at the preset coke temperature and the proportion of each substance in the coke composition in the raw fuel parameters. Finally, calculate the sensible heat of coke based on the specific heat capacity of coke, the preset coke temperature and the coke usage in the raw fuel parameters. The calculation method is as follows: Q4=C coke m coke T coke Formula (7)

[0063] Among them, Q4 is the sensible heat of coke, C coke is the specific heat capacity of coke, m coke is the amount of coke used, T cokeThe preset coke temperature can be any temperature value between 1400° C. and 1500° C., or other temperature values, which are not limited here.

[0064] This embodiment takes into account the effects of temperature and the proportions of various substances on the specific heat capacities of blast air, coal gas, and coke. The specific heat capacities of blast air, coal gas, and coke are determined by temperature and the proportions of various substances, thereby improving the accuracy of the specific heat capacities of blast air, coal gas, and coke, and thereby improving the accuracy of the calculation of the sensible heat of blast air, coal gas, and coke.

[0065] In one embodiment of the present application, the theoretical combustion temperature of the gas is iteratively solved based on the bosh gas volume, bosh gas composition and total heat income until the second convergence condition is met to obtain the theoretical combustion temperature of the gas, including: determining the initial bosh gas specific heat capacity of the tuyere swirl zone based on the bosh gas composition and the preset theoretical combustion temperature of the gas, and calculating the initial theoretical combustion temperature of the gas based on the total heat income, the bosh gas volume and the initial bosh gas specific heat capacity; using the initial theoretical combustion temperature of the gas as the theoretical combustion temperature of the gas before iteration, determining the iterative bosh gas specific heat capacity of the tuyere swirl zone based on the bosh gas composition and the theoretical combustion temperature of the gas before iteration, and calculating the initial theoretical combustion temperature of the gas based on the total heat income, the bosh gas volume and the initial theoretical combustion temperature of the gas and the iterative bosh gas specific heat capacity to calculate the theoretical combustion temperature of the gas after iteration; calculate the difference between the theoretical combustion temperature of the gas before iteration and the theoretical combustion temperature of the gas after iteration to obtain the iterative temperature difference of the theoretical combustion temperature of the gas; if the iterative temperature difference of the theoretical combustion temperature of the gas is less than or equal to the second preset temperature difference threshold, the second convergence condition is met, and the theoretical combustion temperature of the gas after iteration is used as the theoretical combustion temperature of the gas; if the iterative temperature difference of the theoretical combustion temperature of the gas is greater than the second preset temperature difference threshold, the theoretical combustion temperature of the gas is iteratively solved based on the bosh gas volume, bosh gas composition, total heat income and the theoretical combustion temperature of the gas after iteration until the second convergence condition is met to obtain the theoretical combustion temperature of the gas.

[0066] In this embodiment, the calculation formula of the theoretical combustion temperature of coal gas is as follows:

[0067] Among them, T f is the theoretical combustion temperature of gas, Q is the total heat input, V G is the amount of bosh gas, C G is the specific heat capacity of the bosh gas.

[0068] Based on this, the iterative solution process for the theoretical combustion temperature of gas can be:

[0069] 1. Preset a temperature value as the preset theoretical combustion temperature of coal gas. Determine the specific heat capacity of each substance in the bosh gas at the preset theoretical combustion temperature of coal gas based on the relationship between the specific heat capacity of different substances and temperature and the preset theoretical combustion temperature of coal gas. Calculate the initial specific heat capacity of coal gas based on the specific heat capacity of each substance in the bosh gas at the preset theoretical combustion temperature of coal gas and the proportion of each substance in the composition of coal gas. Substitute the total heat income, the amount of coal gas and the initial specific heat capacity of coal gas into formula (8) to calculate the initial theoretical combustion temperature of coal gas, and use the initial theoretical combustion temperature of coal gas as the theoretical combustion temperature of coal gas before iteration.

[0070] 2. Determine the specific heat capacity of each substance in the bosh gas at the theoretical combustion temperature before iteration based on the preset relationship between the specific heat capacity of different substances and temperature and the theoretical combustion temperature of the gas before iteration; calculate the iterative bosh gas specific heat capacity based on the specific heat capacity of each substance in the bosh gas at the theoretical combustion temperature before iteration and the proportion of each substance in the bosh gas composition; substitute the total heat income, the bosh gas volume and the iterative bosh gas specific heat capacity into formula (8) to calculate the theoretical combustion temperature of the gas after iteration.

[0071] 3. Calculate the difference between the theoretical combustion temperature of the gas before iteration and the theoretical combustion temperature of the gas after iteration as the iterative temperature difference of the theoretical combustion temperature of the gas, and compare the iterative temperature difference of the theoretical combustion temperature of the gas with a second preset temperature difference threshold.

[0072] 4. If the iterative temperature difference of the theoretical gas combustion temperature is less than or equal to the second preset temperature difference threshold, it means that the second convergence condition is met, and the theoretical gas combustion temperature after the iteration is used as the theoretical gas combustion temperature. Otherwise, the theoretical gas combustion temperature after the iteration is used as the new theoretical gas combustion temperature before the iteration, and the contents of 2-3 are repeated until the second convergence condition is met. The theoretical gas combustion temperature after the iteration obtained by the last iterative solution of the theoretical gas combustion temperature is used as the theoretical gas combustion temperature.

[0073] By iteratively solving the theoretical combustion temperature of coal gas, the accuracy of the theoretical combustion temperature of coal gas is improved, and the accuracy of molten iron temperature prediction is further improved.

[0074] Step S130, determining the direct reduction degree of the iron ore based on top gas parameters, slag and iron parameters, bosh gas volume and bosh gas composition.

[0075] In one embodiment of the present application, since the direct reduction of elements such as Fe, Si, Mn, S, and P in molten iron consumes heat, the reduction of these elements also affects the molten iron temperature. Therefore, it is necessary to determine the direct reduction degree of the iron ore. This can be calculated based on top gas parameters, slag and iron parameters, bosh gas volume, and bosh gas composition.

[0076] In one embodiment of the present application, step S130 includes: determining the amount of carbon monoxide in the bosh gas based on the bosh gas amount and the bosh gas composition, and determining the total amount of carbon monoxide and carbon dioxide in the top gas based on the top gas amount and the top gas composition, so as to determine the total amount of carbon monoxide generated by direct reduction according to the amount of carbon monoxide in the bosh gas and the total amount of carbon monoxide and carbon dioxide in the top gas, and the top gas parameters include the top gas amount and the top gas composition; determining the mass of trace elements in the molten iron and the mass of iron in the molten iron based on the molten iron composition and the molten iron output, and determining the amount of carbon monoxide generated by direct reduction of trace element oxides based on the mass of trace elements in the molten iron, so as to determine the amount of carbon monoxide generated by direct reduction of iron ore according to the total amount of carbon monoxide generated by direct reduction and the amount of carbon monoxide generated by direct reduction of trace element oxides, and the slag iron parameters include the molten iron composition and the molten iron output; calculating the direct reduction degree of iron ore based on the amount of carbon monoxide generated by direct reduction of iron ore, the mass of iron in the molten iron and the mass of iron in the preset hot-pressed iron blocks.

[0077] In this embodiment, the volume of CO in the bosh gas, i.e., the amount of CO, is calculated based on the CO ratio in the bosh gas composition and the amount of bosh gas. The volume of CO in the top gas is calculated based on the CO ratio in the top gas composition and the amount of top gas. The volume of CO2 in the top gas is calculated based on the CO2 ratio in the top gas composition and the amount of top gas. The sum of the volume of CO in the top gas and the volume of CO2 in the top gas is calculated to be the total amount of CO and CO2 in the top gas. The difference between the total amount of CO and CO2 in the top gas and the amount of CO in the bosh gas is calculated as the total amount of CO generated by direct reduction, and the calculation method is as follows: V1 = V CO+CO2 -V COb Formula (9)

[0078] Among them, V1 is the total amount of CO generated by direct reduction, V CO+CO2 is the total amount of CO and CO2 in the top gas, V COb is the amount of CO in the bosh gas.

[0079] It should be understood that during the direct reduction reaction, the iron ore undergoes a direct reduction reaction to generate a reduction product of the Fe element, and the trace element oxides undergo a direct reduction reaction to generate trace element reduction products, wherein the trace elements in the molten iron include elements such as Si, Mn, P, Ti, and S. Correspondingly, the trace element oxides include oxides of elements such as Si, Mn, P, Ti, and S, and the trace element reduction products include reduction products of elements such as Si, Mn, P, Ti, and S. Therefore, the mass of the trace elements in the molten iron, such as the mass of Si, the mass of Mn, the mass of P, the mass of Ti, and the mass of S, can be determined based on the proportion of the trace elements in the molten iron composition, such as the proportion of Si, the proportion of Mn, the proportion of P, the proportion of Ti, and the proportion of S, and the molten iron output, thereby calculating the amount of CO generated by the direct reduction of the trace element oxides such as Si, Mn, P, Ti, and S according to the mass of the trace elements such as Si, Mn, P, Ti, and S in the molten iron, and the calculation method is as follows:

[0080] Among them, V2 is the amount of CO generated by direct reduction of trace element oxides such as Si, Mn, P, Ti, and S, m [Si] is the mass of Si in molten iron, m [Mn] is the mass of Mn in molten iron, m [P] is the mass of P in the molten iron, m [Ti] is the mass of Ti in molten iron, m [S] is the mass of S in molten iron.

[0081] The difference between the total amount of CO generated by direct reduction and the amount of CO generated by direct reduction of trace element oxides is calculated as the amount of CO generated by direct reduction of iron ore. The calculation method is as follows: V3 = V1 - V2 Formula (11)

[0082] Among them, V3 is the amount of CO generated by direct reduction of iron ore, V1 is the total amount of CO generated by direct reduction, and V2 is the amount of CO generated by direct reduction of trace element oxides.

[0083] The mass of iron in the molten iron is determined based on the proportion of iron in the molten iron composition and the molten iron output. The direct reduction degree of the iron ore is calculated based on the amount of CO generated by direct reduction of the iron ore, the mass of iron in the molten iron, and the mass of iron in the preset hot briquette. The calculation method is as follows:

[0084] Where Rd is the direct reduction degree of iron ore, V3 is the amount of CO generated by direct reduction of iron ore, m [Fe] is the mass of iron in molten iron, m l The iron content of the hot briquette iron used in the blast furnace is the mass of iron in the preset hot briquette iron.

[0085] This embodiment takes into account the reducibility of trace element oxides. By determining the total amount of CO generated by direct reduction and the amount of CO generated by direct reduction of trace element oxides, the amount of CO generated by direct reduction of iron ore is further determined. The direct reduction degree of iron ore is calculated based on the amount of CO generated by direct reduction of iron ore, thereby improving the accuracy of the direct reduction degree of iron ore.

[0086] Step S140 , determining the gas-liquid heat exchange coefficient according to the theoretical combustion temperature of the gas, the amount of the bosh gas, the composition of the bosh gas, the slag and iron parameters, and the composition of the gas after direct reduction at the direct reduction position.

[0087] In one embodiment of the present application, since heat exchange occurs between molten iron and coal gas, the accuracy of molten iron temperature prediction is also related to the gas-liquid heat exchange coefficient. The gas-liquid heat exchange coefficient can be calculated based on the theoretical coal gas combustion temperature, the bosh gas volume, the bosh gas composition, the slag and iron parameters, and the direct reduction gas composition at the direct reduction location. Since the direct reduction gas volume is equal to the top gas volume, the volume of CO in the direct reduction gas is equal to the sum of the volumes of CO and CO2 in the top gas, the volume of H2 in the direct reduction gas is equal to the sum of the volumes of H2 and H2O in the top gas or the volume of H2 in the bosh gas, and the volume of N2 in the direct reduction gas is equal to the volume of N2 in the top gas or the volume of N2 in the bosh gas. Therefore, the direct reduction gas composition can be determined based on the top gas parameters, or the direct reduction gas composition can be determined based on the top gas parameters, the bosh gas volume, and the bosh gas composition.

[0088] In one embodiment of the present application, before determining the gas-liquid heat exchange coefficient, the method includes: determining the total amount of carbon monoxide and carbon dioxide in the top gas, the total amount of water and hydrogen in the top gas, and the amount of nitrogen in the top gas based on the top gas amount and the top gas composition, wherein the top gas parameters include the top gas amount and the top gas composition; using the top gas amount as the gas amount after direct reduction, the total amount of carbon monoxide and carbon dioxide in the top gas as the amount of carbon monoxide in the gas after direct reduction, the total amount of water and hydrogen in the top gas as the amount of hydrogen in the gas after direct reduction, and the amount of nitrogen in the top gas as the amount of nitrogen in the gas after direct reduction; determining the gas composition after direct reduction based on the gas amount after direct reduction, the amount of carbon monoxide in the gas after direct reduction, the amount of hydrogen in the gas after direct reduction, and the amount of nitrogen in the top gas.

[0089] In this embodiment, the composition of the gas after direct reduction can be accurately determined based on the relationship between the top gas and the gas after direct reduction.

[0090] First, the volume of H2 in the top gas can be calculated based on the H2 ratio and the amount of top gas in the top gas composition, and the volume of H2O in the top gas can be calculated based on the H2O ratio and the amount of top gas in the top gas composition. The sum of the volume of H2 in the top gas and the volume of H2O in the top gas is the total amount of H2O and H2 in the top gas; the volume of CO in the top gas can be calculated based on the CO ratio and the amount of top gas in the top gas composition, and the volume of CO2 in the top gas can be calculated based on the CO2 ratio and the amount of top gas in the top gas composition. The sum of the volume of CO in the top gas and the volume of CO2 in the top gas is the total amount of CO and CO2 in the top gas; the volume of N2 in the top gas, i.e., the amount of N2 in the top gas, can be calculated based on the N2 ratio and the amount of top gas in the top gas composition.

[0091] Then, the amount of top gas is taken as the amount of gas after direct reduction, the total amount of CO and CO2 in the top gas is taken as the amount of CO in the gas after direct reduction, the total amount of H2O and H2 in the top gas is taken as the amount of H2 in the gas after direct reduction, and the amount of N2 in the top gas is taken as the amount of N2 in the gas after direct reduction.

[0092] Finally, the H2 ratio in the direct reduction gas is determined according to the H2 amount in the direct reduction gas and the amount of direct reduction gas, the CO ratio in the direct reduction gas is determined according to the CO amount in the direct reduction gas and the amount of direct reduction gas, and the N2 ratio in the direct reduction gas is determined according to the N2 amount in the direct reduction gas and the amount of direct reduction gas, so as to use the H2 ratio in the direct reduction gas, the CO ratio in the direct reduction gas and the N2 ratio in the direct reduction gas as the components of the direct reduction gas.

[0093] In another embodiment of the present application, before determining the gas-liquid heat exchange coefficient, the method includes: determining the total amount of carbon monoxide and carbon dioxide in the top gas based on the top gas amount and the top gas composition, wherein the top gas parameters include the top gas amount and the top gas composition; determining the amount of hydrogen in the bosh gas and the amount of nitrogen in the bosh gas based on the bosh gas amount and the bosh gas composition; using the top gas amount as the gas amount after direct reduction, the total amount of carbon monoxide and carbon dioxide in the top gas as the amount of carbon monoxide in the gas after direct reduction, the amount of hydrogen in the bosh gas as the amount of hydrogen in the gas after direct reduction, and the amount of nitrogen in the bosh gas as the amount of nitrogen in the gas after direct reduction; determining the gas composition after direct reduction based on the gas amount after direct reduction, the amount of carbon monoxide in the gas after direct reduction, the amount of hydrogen in the gas after direct reduction, and the amount of nitrogen in the gas after direct reduction.

[0094] In this embodiment, the composition of the gas after direct reduction can be accurately determined based on the relationship between the top gas, the bosh gas and the gas after direct reduction.

[0095] First, the volume of CO in the top gas is calculated based on the CO ratio in the top gas composition and the amount of top gas, and the volume of CO2 in the top gas is calculated based on the CO2 ratio in the top gas composition and the amount of top gas. The sum of the volume of CO in the top gas and the volume of CO2 in the top gas is the total amount of CO and CO2 in the top gas; the volume of H2 in the bosh gas, i.e., the amount of H2 in the bosh gas, is determined based on the H2 ratio in the bosh gas composition and the amount of bosh gas; and the volume of N2 in the bosh gas, i.e., the amount of N2 in the bosh gas, is determined based on the N2 ratio in the bosh gas composition and the amount of bosh gas.

[0096] Then, the amount of top gas is taken as the amount of gas after direct reduction, the total amount of CO and CO2 in the top gas is taken as the amount of CO in the gas after direct reduction, the amount of H2 in the bosh gas is taken as the amount of H2 in the gas after direct reduction, and the amount of N2 in the bosh gas is taken as the amount of N2 in the gas after direct reduction.

[0097] Finally, the H2 ratio in the direct reduction gas is determined according to the H2 amount in the direct reduction gas and the amount of direct reduction gas, the CO ratio in the direct reduction gas is determined according to the CO amount in the direct reduction gas and the amount of direct reduction gas, and the N2 ratio in the direct reduction gas is determined according to the N2 amount in the direct reduction gas and the amount of direct reduction gas, so as to use the H2 ratio in the direct reduction gas, the CO ratio in the direct reduction gas and the N2 ratio in the direct reduction gas as the components of the direct reduction gas.

[0098] In one embodiment of the present application, step S140 includes: interpolating the composition of the bosh gas and the composition of the gas after direct reduction to obtain the gas composition of the dripping zone; determining the gas-liquid heat exchange coefficient of the tuyere vortex zone according to the equivalent particle size of slag iron, the thermal conductivity of the gas in the tuyere vortex zone and the Nusselt number of the tuyere vortex zone, the thermal conductivity of the gas in the tuyere vortex zone and the Nusselt number of the tuyere vortex zone are both determined based on the bosh gas composition and the theoretical combustion temperature of the gas, and the equivalent particle size of slag iron is determined based on the slag iron parameters; determining the gas-liquid heat exchange coefficient of the tuyere vortex zone according to the equivalent particle size of slag iron, the thermal conductivity of the gas in the tuyere vortex zone and the Nusselt number of the tuyere vortex zone The gas-liquid heat transfer coefficient at the direct reduction position is determined based on the gas thermal conductivity at the direct reduction position and the Nusselt number at the direct reduction position. Both the gas thermal conductivity and the Nusselt number at the direct reduction position are determined based on the gas composition after direct reduction and the theoretical combustion temperature of the gas. The gas-liquid heat transfer coefficient in the dripping zone is determined based on the equivalent particle size of slag and iron, the gas thermal conductivity and the Nusselt number of the dripping zone. Both the gas thermal conductivity and the Nusselt number of the dripping zone are determined based on the gas composition and the theoretical combustion temperature of the gas in the dripping zone.

[0099] In this embodiment, the dripping zone is the area between the tuyere swirl zone and the direct reduction position. Since the gas composition at different height positions of the dripping zone from the direct reduction position to the tuyere swirl zone is different, and the gas-liquid heat exchange coefficient of different gas compositions is also different, in order to improve the accuracy of molten iron temperature prediction, it is also necessary to determine the gas-liquid heat exchange coefficient at different height positions of the dripping zone.

[0100] Schematically, the gas-liquid heat transfer coefficient can be determined by the correction factor, gas thermal conductivity, slag iron equivalent particle size and Nusselt number. The calculation method of gas-liquid heat transfer coefficient is as follows: h g-l =γ·k g Nu / d l Formula (13)

[0101] Among them, h g-l is the gas-liquid heat transfer coefficient, γ is the correction coefficient, k g is the thermal conductivity of gas, Nu is the Nusselt number, d l is the equivalent particle size of slag and iron.

[0102] The Nusselt number is calculated as follows: Nu=2.0+0.6(9Re p ) 1 / 2 Pr 1 / 3 Formula (14)

[0103] Among them, Nu is the Nusselt number, Re p is the Reynolds number, and Pr is the Prandtl number.

[0104] The Reynolds number is calculated as follows: p =ρ g d s u g / μ g Formula (15)

[0105] Among them, Re p is the Reynolds number, ρ g is the gas density, d s is the characteristic length, u g is the gas flow rate, μ g is the gas viscosity.

[0106] The Prandtl number is calculated as follows: Pr = u g C G / k g Formula (16)

[0107] Where Pr is the Prandtl number, u g is the gas flow rate, C G is the specific heat capacity of gas, k g is the thermal conductivity of gas.

[0108] It should be noted that the thermal conductivity, density, viscosity and specific heat of gas are all related to the gas composition and temperature. The relationship between the thermal conductivity and composition of gas is as follows: g =m CO1 k CO +m H21 k H2 +m N21 k N2 Formula (17)

[0109] Among them, k g is the thermal conductivity of gas, m CO1 is the CO ratio in coal gas, m H21 is the H2 ratio in coal gas, m N21 is the ratio of N2 in coal gas, k CO is the thermal conductivity of CO, k H2 is the thermal conductivity of H2, k N2 is the thermal conductivity of N2.

[0110] The relationship between gas density and gas composition is as follows: ρ g =m CO1 ρ CO +m H21 ρ H2 +m N21 ρ N2 Formula (18)

[0111] Among them, ρ g is the gas density, m CO1 is the CO ratio in coal gas, m H21 is the H2 ratio in coal gas, m N21 is the proportion of N2 in coal gas, ρ CO is the CO density, ρ H2 is the H2 density, ρ N2 is the N2 density.

[0112] The relationship between gas viscosity and gas composition is as follows: μ g =m CO1 μ CO +m H21 μ H2 +m N21 μ N2 Formula (19)

[0113] Among them, μ g is the gas viscosity, m CO1 is the CO ratio in coal gas, m H21 is the H2 ratio in coal gas, m N21 is the proportion of N2 in coal gas, μ CO is CO viscosity, μ H2is H2 viscosity, μ N2 is the N2 viscosity.

[0114] The relationship between the specific heat capacity of coal gas and its composition is as follows: C G =m CO1 C CO +m H21 C H2 +m N21 C N2 Formula (20)

[0115] Among them, C G is the specific heat capacity of gas, m CO1 is the CO ratio in coal gas, m H21 is the H2 ratio in coal gas, m N21 is the ratio of N2 in coal gas, C CO is the specific heat capacity of CO, C H2 is the specific heat capacity of H2, C N2 is the specific heat capacity of N2.

[0116] Schematically, the process for determining the gas-liquid heat exchange coefficient in the tuyere vortex zone can be:

[0117] According to the theoretical combustion temperature of coal gas and the preset corresponding relationship between the specific heat capacity of each substance and temperature, the specific heat capacity of CO, the specific heat capacity of H2 and the specific heat capacity of N2 are determined, and the specific heat capacity of CO, the specific heat capacity of H2 and the specific heat capacity of N2 as well as the CO ratio, H2 ratio and N2 ratio in the furnace gas composition are substituted into formula (20) to obtain the specific heat capacity of coal gas in the tuyere swirling zone; according to the theoretical combustion temperature of coal gas and the preset corresponding relationship between the viscosity of each substance and temperature, the viscosity of CO, the viscosity of H2 and the viscosity of N2 as well as the CO ratio, H2 ratio and N2 ratio in the furnace gas composition are substituted into formula (19) to obtain the coal gas viscosity in the tuyere swirling zone; according to the theoretical combustion temperature of coal gas and the preset corresponding relationship between the viscosity of each substance and temperature, the viscosity of CO, the viscosity of H2 and the viscosity of N2 as well as the CO ratio, H2 ratio and N2 ratio in the furnace gas composition are substituted into formula (19) to obtain the coal gas viscosity in the tuyere swirling zone The CO density, H2 density and N2 density are determined based on the theoretical combustion temperature and the preset correspondence between the density of each substance and the temperature. The CO density, H2 density and N2 density as well as the CO ratio, H2 ratio and N2 ratio in the furnace bosh gas composition are substituted into formula (18) to obtain the gas density in the tuyere swirling zone. The thermal conductivity of CO, H2 thermal conductivity and N2 thermal conductivity are determined based on the theoretical combustion temperature of the gas and the preset correspondence between the thermal conductivity of each substance and the temperature. The thermal conductivity of CO, H2 thermal conductivity and N2 thermal conductivity as well as the CO ratio, H2 ratio and N2 ratio in the furnace bosh gas composition are substituted into formula (17) to obtain the gas thermal conductivity in the tuyere swirling zone. Substitute the thermal conductivity and specific heat of the gas in the tuyere vortex zone into formula (16) to obtain the Prandtl number of the tuyere vortex zone, and substitute the gas density and gas viscosity in the tuyere vortex zone into formula (15) to obtain the Rayleigh number of the tuyere vortex zone, wherein the gas flow rate is obtained by dividing the gas volume by the cross-sectional area of ​​the blast furnace at the calculated position, and the cross-sectional area is determined by the blast furnace type structure, the characteristic length is the equivalent particle size of slag iron, and the equivalent particle size of slag iron is determined based on the density of molten iron, the density of liquid slag, the blast furnace type structure and the slag volume in the slag iron parameters; substitute the Prandtl number and Rayleigh number of the tuyere vortex zone into formula (14) to obtain the Nusselt number of the tuyere vortex zone; substitute the thermal conductivity and Nusselt number of the gas in the tuyere vortex zone into formula (13) to obtain the gas-liquid heat exchange coefficient of the tuyere vortex zone, wherein the correction coefficient can be preset, can be any value between 0.2 and 0.5, or other values, which are not limited here.

[0118] Accordingly, according to the above method, based on the theoretical combustion temperature of coal gas, slag iron parameters and the composition of coal gas after direct reduction, the gas-liquid heat exchange coefficient at the direct reduction position is calculated, which will not be repeated here.

[0119] The gas composition of the bosh gas and the gas composition after direct reduction are interpolated to obtain the gas composition of the dripping zone. This dripping zone gas composition includes the gas composition at different heights within the dripping zone. Similarly, the gas-liquid heat exchange coefficient at different heights within the dripping zone is calculated based on the theoretical combustion temperature of the gas, slag and iron parameters, and the gas composition at different heights within the dripping zone. This is not further detailed here. By determining the gas-liquid heat exchange coefficient at different heights within the dripping zone, the accuracy of the molten iron temperature prediction is further improved.

[0120] Step S150, based on the gas-liquid heat exchange coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of coal gas and the slag iron parameters, iteratively solve the molten iron temperature and the coal gas temperature until the first convergence condition is met, completing the prediction of the blast furnace smelting molten iron temperature.

[0121] In one embodiment of the present application, a temperature value can be preset for the molten iron temperature at the direct reduction blast furnace position as the preset molten iron temperature after direct reduction. Based on the gas-liquid heat exchange coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of coal gas, the preset molten iron temperature after direct reduction and the slag iron parameters, and using the coal gas phase energy conservation relationship and the molten iron phase energy conservation relationship, the molten iron temperature and the coal gas temperature are iteratively solved until the first convergence condition is met to obtain the coal gas temperature at the direct reduction position and the molten iron temperature in the tuyere swirl zone. Schematically, the first convergence condition can be that the number of iterations of the iterative solution of the molten iron temperature and the coal gas temperature meets the first preset number of iterations, or that the iterative temperature difference of the coal gas temperature and the iterative temperature difference of the molten iron temperature are both less than or equal to the first preset temperature difference threshold, or other convergence conditions, which are not limited here.

[0122] In one embodiment of the present application, step S150 includes: determining the direct reduction heat consumption according to the molten iron composition and the direct reduction degree of the iron ore, wherein the slag iron parameter includes the molten iron composition; performing iterative solution of the molten iron temperature and the gas temperature based on the coal gas phase temperature, the molten iron phase temperature, the gas-liquid heat exchange coefficient and the direct reduction heat consumption, and according to the coal gas phase energy conservation relationship and the molten iron phase energy conservation relationship, obtaining the molten iron temperature in the tuyere raceway before iteration, the molten iron temperature in the tuyere raceway after iteration, the coal gas temperature after direct reduction before iteration and the coal gas temperature after direct reduction after iteration, and the initial value of the coal gas phase temperature is The theoretical combustion temperature of coal gas, the initial value of the molten iron phase temperature is the preset molten iron temperature after direct reduction; determine the difference between the molten iron temperature in the tuyere raceway before iteration and the molten iron temperature in the tuyere raceway after iteration as the iterative temperature difference of molten iron temperature, and determine the difference between the coal gas temperature after direct reduction before iteration and the coal gas temperature after direct reduction after iteration as the iterative temperature difference of coal gas temperature; if the iterative temperature difference of molten iron temperature and the iterative temperature difference of coal gas temperature are both less than or equal to the first preset temperature difference threshold, the first convergence condition is met, and the molten iron temperature in the tuyere raceway after iteration is used as the final prediction result of molten iron temperature prediction.

[0123] In this embodiment, the law of conservation of energy has the following characteristics: the heat consumption generated by the direct reduction of iron ore and oxides of trace elements such as Si, Mn, S, P, and Ti is included in the change of coal gas energy; the law of conservation of energy is related to the flow rate, heat capacity, and density of coal gas and slag iron; the calculation range of energy conservation includes the area corresponding to the beginning of melting of iron slag to the surface of the furnace pool, and the melting temperature of iron slag is between 1300 and 1400°C.

[0124] Therefore, the energy conservation relationship of the coal gas phase and the molten iron phase can be used to iteratively solve the molten iron temperature and coal gas temperature based on the coal gas phase temperature, the molten iron phase temperature, the gas-liquid heat exchange coefficient, and the direct reduction heat consumption. The expression of the coal gas phase energy conservation relationship is as follows:

[0125] Among them, ρ g is the gas density, u g is the gas flow rate, C g is the specific heat capacity of gas, T g is the gas phase temperature, z is the length of the solution grid, h g-l is the gas-liquid heat transfer coefficient, A is the specific surface area, T l is the molten iron phase temperature, Q Rd is the heat consumption of direct reduction, V a The volume of the solution area.

[0126] The expression of the energy conservation relationship of molten iron phase is as follows:

[0127] Among them, ρ l is the density of molten iron, u l is the molten iron flow rate, C l is the specific heat capacity of molten iron, T l is the molten iron phase temperature, T g is the gas phase temperature, z is the length of the solution grid, h g-l is the gas-liquid heat transfer coefficient, and A is the specific surface area.

[0128] It should be noted that the methods for determining gas density and specific heat capacity are described in the previous examples and will not be repeated here. The specific surface area can be determined based on the equivalent particle size of slag and iron; the volume of the solution region can be preset; the gas flow rate, slag and iron flow rate, and equivalent particle size of slag and iron are all related to the blast furnace type and can be determined in advance based on the blast furnace structure; the direct reduction heat consumption can be determined based on the direct reduction degree of the iron ore and the molten iron composition in the slag and iron parameters.

[0129] Please refer to Table 2, which shows the direct reduction chemical reactions and thermal effects in a specific embodiment of the present application. As shown in Table 2, oxides of elements such as Fe, Si, Mn, P, Ti, and S undergo direct reduction reactions to generate reduction products of the elements such as Fe, Si, Mn, P, Ti, and S.

[0130] Table 2

[0131] Based on this, the heat consumption of direct reduction is calculated as follows:

[0132] Among them, Q Rd is the heat consumption of direct reduction, ΔH Fe is the reaction heat effect of direct reduction of Fe element, Rd is the direct reduction degree of iron ore, m [Fe] is the mass of iron in molten iron, M 矿 is the ore ratio, ω Fe is the mass fraction of Fe in the mixed ore, ω FeS is the mass fraction of FeS (ferrous sulfide) in the mixed ore, ΔH Si is the reaction heat effect of direct reduction of Si element, m [Si] is the mass of Si in molten iron, ΔH Mn is the heat effect of direct reduction of Mn element, m [Mn] is the mass of Mn in molten iron, ΔH P is the heat effect of direct reduction of P element, m [P] is the mass of P in the molten iron, ΔH Ti is the heat effect of direct reduction of Ti element, m [Ti] is the mass of Ti in molten iron, ΔH S is the heat effect of direct reduction of S element, m [S] is the mass of S in the molten iron. The ore ratio, the mass fraction of Fe and the mass fraction of FeS can be preset.

[0133] Schematically, the dripping zone is gridded along the height direction, the theoretical combustion temperature of the gas is used as the initial value of the gas phase temperature, and the preset molten iron temperature after direct reduction is used as the initial value of the molten iron phase temperature. Equations (21) and (22) are used for iterative solution to obtain the solution results, including the gas temperature after direct reduction before iteration, the molten iron temperature in the tuyere vortex zone before iteration, the gas temperature after direct reduction after iteration, and the molten iron temperature in the tuyere vortex zone after iteration. If the difference between the gas temperature after direct reduction before iteration and the gas temperature after direct reduction after iteration, i.e., the iterative temperature difference of the gas temperature, and the difference between the molten iron temperature in the tuyere vortex zone before iteration and the molten iron temperature in the tuyere vortex zone after iteration, i.e., the iterative temperature difference of the molten iron temperature, are both less than or equal to the first preset temperature difference threshold, then the first convergence condition is met, and the molten iron temperature in the tuyere vortex zone after iteration is used as the final prediction result of the molten iron temperature prediction. On the contrary, the iterative solution is performed again using equations (21) and (22) until the second convergence condition is met, and the final molten iron temperature in the tuyere raceway after the iteration is used as the final prediction result of the molten iron temperature prediction. Schematically, the preset molten iron temperature after direct reduction can be 1350°C, or any temperature value between 1300 and 1500°C, or other temperature values, which are not limited here. The second preset temperature difference threshold can be 0.01°C, or any temperature value between 0.01 and 0.05°C, or other temperature values, which are not limited here.

[0134] Utilizing the energy conservation relationships of the coal gas phase and the molten iron phase, the molten iron temperature and coal gas temperature are iteratively solved through the theoretical combustion temperature of coal gas, the direct reduction degree of iron ore, and the gas-liquid heat exchange coefficient at different heights. The convergence is performed based on the error before and after the iteration, further improving the accuracy of the molten iron temperature prediction.

[0135] In a specific embodiment of the present application, a 2300m 3 For example, the blast furnace has a utilization coefficient of 3.7t / (d·m 3 ), further illustrate the solution of this application.

[0136] The temperature of molten iron in a conventional blast furnace without gas injection is predicted as follows:

[0137] Please refer to Table 3, which is a table of raw fuel parameters in a specific embodiment of the present application. As shown in Table 3, the raw fuel parameters may include coke composition and coke amount, and PCI coal composition and amount. The coke composition may include the ratio of C, H, O, N, S, volatile matter, and ash in the coke, and the PCI coal composition may include the ratio of C, H, O, N, S, volatile matter, and ash in the PCI coal.

[0138] Table 3

[0139] Please refer to Table 4, which is a table of blast parameters in a specific embodiment of the present application. As shown in Table 4, the blast parameters may include blast volume, blast temperature, blast humidity, and oxygen enrichment rate.

[0140] Table 4

[0141] Please refer to Table 5, which is a table of top gas parameters in a specific embodiment of the present application. As shown in Table 5, the top gas parameters may include the amount of top gas and the ratios of CO, CO2, H2, and N2 in the top gas.

[0142] Table 5

[0143] Please refer to Table 6, which is a table of slag parameters in a specific embodiment of the present application. As shown in Table 6, the slag parameters may include the amount of slag and the proportions of Fe, C, Si, Mn, P, S, and Ti in the molten iron.

[0144] Table 6

[0145] According to Table 4, the sensible heat Q1 brought into the blast furnace by the blast is calculated to be 2.00 GJ / t, and the oxygen content available for the combustion of pulverized coal and coke in the tuyere gyrotron of the blast furnace is 239.20 m 3 / t, it is calculated that the total heat Q2 released by the combustion of coal powder, coke or other reactions in the tuyere raceway is 2.41GJ / t. The temperature of coke entering the combustion zone is about 1400℃, the amount of coke burned in the tuyere is 173.46kg / t, and the sensible heat Q4 brought into the tuyere raceway by coke is 0.29GJ / t. Therefore, the total heat input Q of the tuyere raceway is 4.70GJ / t. According to Tables 3 and 4, using the law of conservation of matter in the tuyere raceway, the contents of CO, H2 and N2 in the bosh gas are 41.67%, 6.95% and 51.38% respectively, and the amount of bosh gas is 1193.88m 3 / t. Therefore, the theoretical combustion temperature of the coal gas is calculated to be 2252℃.

[0146] According to Table 5 and Table 6, the direct reduction degree of iron ore Rd is 0.451, and the CO, H2, and N2 in the coal gas after direct reduction are 48.92%, 6.09%, and 44.99%, respectively. According to Table 6 and the theoretical combustion temperature and the amount of coal gas in the furnace, the furnace Reynolds number Re is calculated. p is 30883, the Prandtl number Pr is 0.362, and the Nusselt number Nu is 227.54. Therefore, the gas-liquid heat transfer coefficient h between the coal gas and the slag iron droplets is g-l 26.89W / (m 2.K). Through iterative solution and calculation based on the law of energy conservation, the molten iron temperature, i.e., the molten iron temperature in the tuyere raceway, is obtained to be 1521.20°C, which is close to the average molten iron temperature of 1520°C in the corresponding blast furnace. The gas temperature after direct reduction is 1897.20°C.

[0147] Since gas injection is implemented during the blast furnace smelting process, and the injection process causes changes in blast and furnace top parameters, the blast furnace molten iron temperature prediction under gas injection conditions is as follows:

[0148] Please refer to Table 7, which is a table of gas injection parameters in a specific embodiment of the present application. As shown in Table 7, the gas injection parameters may include the gas injection amount and the ratios of H2, CO, CO2, CH4, nitrogen, and O2 in the injected gas.

[0149] Table 7

[0150] Please refer to Table 8, which is a table of blast parameters under gas injection conditions in a specific embodiment of the present application. As shown in Table 8, the blast parameters under gas injection conditions, including blast volume, blast humidity, and oxygen enrichment rate, have changed from the corresponding values ​​in Table 4.

[0151] Table 8

[0152] Please refer to Table 9, which is a table of top gas parameters under gas injection conditions in a specific embodiment of the present application. As shown in Table 9, the top gas composition and top gas volume in the top gas parameters under gas injection conditions have changed from the corresponding values ​​in Table 5.

[0153] According to Table 3, Table 7 and Table 8, using the law of conservation of matter in the tuyere raceway, the contents of CO, H2 and N2 in the bosh gas are 43.71%, 9.61% and 46.68% respectively, and the amount of bosh gas is 1197.4m 3 / t, the theoretical combustion temperature of the coal gas is calculated to be 2163°C. According to Table 9, Table 6 and the composition of the furnace gas, the direct reduction degree of iron ore Rd is 0.39, and the CO, H2, and N2 contents in the coal gas after direct reduction are 49.90%, 8.55%, and 41.54%, respectively. The gas-liquid heat exchange coefficient h between the coal gas and the slag iron droplets is calculated to be g-l 28.654W / (m 2 .K). Therefore, through iterative solution and calculation based on energy conservation, the molten iron temperature is obtained to be 1510.61℃, and the gas temperature after direct reduction is 1753.63℃.

[0154] Please refer to Figure 2, which is a structural diagram of a water temperature prediction system for a blast furnace iron smelting process shown in a specific embodiment of the present application. As shown in Figure 2, the water temperature prediction system for a blast furnace iron smelting process includes a data acquisition subsystem, a physical property database, a tuyere area heat balance calculation subsystem, a direct reduction calculation subsystem, and an iterative solution subsystem. Among them, the data acquisition subsystem is used to obtain smelting data in the blast furnace smelting process, and the smelting data include raw material parameters, blast parameters, gas injection parameters, top gas parameters, and slag parameters; the physical property database is used to collect and store the specific heat capacity, density, dynamic viscosity, thermal conductivity of various gases, as well as the specific heat capacity, density, thermal conductivity, etc. of various solid phase substances; the tuyere area heat balance calculation subsystem is used to calculate the thermal equilibrium state of the tuyere area; the direct reduction calculation subsystem is used to calculate the direct reduction degree of iron ore; the iterative solution subsystem is used to judge the convergence of the molten iron temperature result and obtain the molten iron temperature value.

[0155] Please refer to Figure 3, which is a schematic diagram of the hot iron temperature prediction process of the blast furnace smelting process in a specific embodiment of the water temperature prediction system of the blast furnace iron smelting process shown in Figure 2. As shown in Figure 3, the hot iron temperature prediction process of the blast furnace smelting process includes:

[0156] 1. Real-time acquisition of smelting data during the blast furnace smelting process, including raw material parameters, blast parameters, gas injection parameters, top gas parameters, and slag and iron parameters;

[0157] 2. Based on the raw fuel parameters, blast parameters, and gas injection parameters, calculate the theoretical combustion temperature of the gas in the tuyere vortex zone, the amount of bosh gas, and the composition of the bosh gas;

[0158] 3. Calculate the direct reduction degree of iron ore, the gas composition and gas volume after direct reduction based on the top gas parameters, slag iron parameters and bosh gas composition;

[0159] 4. Calculate the gas-liquid heat exchange coefficient between gas, molten iron and slag based on the physical phase database, theoretical combustion temperature of gas, bosh gas volume, and slag and iron parameters;

[0160] 5. Based on the law of conservation of heat, an iterative solution is performed to obtain the molten iron temperature and the gas temperature after direct reduction.

[0161] For the detailed process in the flow chart of Figure 3, please refer to the records in the aforementioned embodiments, which will not be described in detail here. The technical solution of this embodiment uses the smelting data of the blast furnace smelting process acquired in real time to calculate the theoretical combustion temperature of the coal gas in the tuyere swirl zone, the degree of iron ore reduction, and the gas-liquid heat exchange coefficient, and then iteratively solves the molten iron temperature and coal gas temperature to complete the prediction of the blast furnace smelting molten iron temperature. It can obtain the molten iron temperature in the blast furnace smelting process under various working conditions, help the operator judge the heat status in the blast furnace, ore reduction and other information, and provide a guarantee for the stable and smooth operation of conventional blast furnaces and low-carbon blast furnaces.

[0162] Please refer to Figure 4, which is a block diagram of a device for predicting the temperature of molten iron in a blast furnace according to an exemplary embodiment of the present application. As shown in Figure 4, the exemplary device for predicting the temperature of molten iron in a blast furnace includes:

[0163] The smelting data acquisition module 410 is configured to obtain the raw fuel parameters, blast parameters, gas injection parameters, top gas parameters and slag iron parameters of the blast furnace smelting process; the theoretical combustion temperature determination module 420 is configured to determine the total heat income, bosh gas volume and bosh gas composition of the tuyere swirl zone according to the raw fuel parameters, blast parameters and gas injection parameters, and to determine the theoretical combustion temperature of the gas in the tuyere swirl zone according to the total heat income, bosh gas volume and bosh gas composition; the direct reduction degree determination module 430 is configured to determine the direct reduction degree of iron ore according to the top gas parameters, slag iron parameters, bosh gas volume and bosh gas composition. Reduction degree; a heat transfer coefficient determination module 440 is configured to determine the gas-liquid heat transfer coefficient based on the theoretical combustion temperature of the gas, the composition of the furnace bosh gas, the slag iron parameters and the composition of the gas after direct reduction at the direct reduction position, the gas composition after direct reduction is determined based on the furnace top gas parameters, or the gas composition after direct reduction is determined based on the furnace top gas parameters, the furnace bosh gas volume and the furnace bosh gas composition; an iterative solution module 450 is configured to iteratively solve the molten iron temperature and the gas temperature based on the gas-liquid heat transfer coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of the gas and the slag iron parameters until the first convergence condition is met, thereby completing the prediction of the molten iron temperature for blast furnace smelting.

[0164] It should be noted that the blast furnace smelting molten iron temperature prediction device provided in the above embodiment and the blast furnace smelting molten iron temperature prediction method provided in the above embodiment belong to the same concept, wherein the specific manner in which each module and unit performs the operation has been described in detail in the method embodiment and will not be repeated here. In actual application, the blast furnace smelting molten iron temperature prediction device provided in the above embodiment can allocate the above functions to different functional modules as needed, that is, divide the internal structure of the device into different functional modules to complete all or part of the functions described above, and this is not limited here.

[0165] This embodiment also provides an electronic device, including: one or more processors; a storage device for storing one or more programs, when the one or more programs are executed by the one or more processors, the electronic device implements the blast furnace smelting molten iron temperature prediction method provided in the above-mentioned embodiments.

[0166] Please refer to Figure 5, which is a schematic diagram of the structure of an electronic device according to an exemplary embodiment of the present application. It should be noted that the electronic device 500 shown in Figure 5 is only an example and should not bring any limitation to the functions and scope of use of the embodiments of the present application.

[0167] As shown in Figure 5, the electronic device 500 includes a processor 501, a memory 502 and a communication bus 503; the communication bus 503 is used to connect the processor 501 and the memory 502; the processor 501 is used to execute the computer program stored in the memory 502 to implement one or more methods in the above embodiments.

[0168] This embodiment further provides a computer-readable storage medium having a computer program stored thereon. When executed by a computer processor, the computer program causes the computer to execute the aforementioned method for predicting the temperature of molten iron in a blast furnace. The computer-readable storage medium may be included in the electronic device described in the above embodiment, or may exist independently and not be incorporated into the electronic device.

[0169] This embodiment further provides a computer program product or computer program, which includes computer instructions stored in a computer-readable storage medium. A processor of a computer device reads the computer instructions from the computer-readable storage medium and executes the computer instructions, causing the computer device to perform the method for predicting molten iron temperature in blast furnace smelting provided in each of the above embodiments.

[0170] The electronic device provided in this embodiment includes a processor, a memory, a transceiver and a communication interface. The memory and the communication interface are connected to the processor and the transceiver and complete communication with each other. The memory is used to store computer programs, the communication interface is used to communicate, and the processor and the transceiver are used to run the computer program so that the electronic device executes each step of the above method.

[0171] In this embodiment, the memory may include a random access memory (RAM), and may also include a non-volatile memory (non-volatile memory), such as at least one disk storage.

[0172] The above-mentioned processor can be a general-purpose processor, including a central processing unit (CPU), a network processor (NP), etc.; it can also be a digital signal processor (DSP), an application-specific integrated circuit (ASIC), a field-programmable gate array (FPGA) or other programmable logic devices, discrete gate or transistor logic devices, and discrete hardware components.

[0173] Regarding the computer-readable storage medium in this embodiment, those skilled in the art will understand that all or part of the steps in implementing the above-described method embodiments can be accomplished by hardware associated with the computer program. The aforementioned computer program can be stored in a computer-readable storage medium. When executed, the program performs the steps of the above-described method embodiments. The aforementioned storage medium includes various media capable of storing program code, such as ROM (read-only memory), RAM (random access memory), magnetic disks, or optical disks.

[0174] The above embodiments are merely illustrative of the principles and effects of this application and are not intended to limit this application. Anyone skilled in the art may modify or alter the above embodiments without departing from the spirit and scope of this application. Therefore, any equivalent modifications or alterations accomplished by a person of ordinary skill in the art without departing from the spirit and technical concepts disclosed in this application shall be covered by the claims of this application.

Claims

1. A method for predicting the temperature of molten iron in blast furnace smelting, characterized in that: The method comprises: Obtaining raw fuel parameters, blast parameters, gas injection parameters, top gas parameters and slag iron parameters in the blast furnace smelting process; Determine the total heat income, the amount of bosh gas and the composition of the bosh gas in the tuyere whirlpool area according to the raw fuel parameters, the blast parameters and the gas injection parameters, and determine the theoretical combustion temperature of the gas in the tuyere whirlpool area according to the total heat income, the amount of bosh gas and the composition of the bosh gas; Determining the direct reduction degree of the iron ore according to the furnace top gas parameters, the slag iron parameters, the bosh gas volume and the bosh gas composition; Determine the gas-liquid heat exchange coefficient according to the theoretical combustion temperature of the coal gas, the bosh gas composition, the slag iron parameters and the composition of the coal gas after direct reduction at the direct reduction position, wherein the composition of the coal gas after direct reduction is determined based on the furnace top gas parameters, or the composition of the coal gas after direct reduction is determined based on the furnace top gas parameters, the bosh gas volume and the bosh gas composition; Based on the gas-liquid heat exchange coefficient, the direct reduction degree of the iron ore, the theoretical combustion temperature of the coal gas and the slag iron parameters, the molten iron temperature and the coal gas temperature are iteratively solved until the first convergence condition is met, thereby completing the prediction of the molten iron temperature for blast furnace smelting.

2. The method for predicting the temperature of molten iron in blast furnace smelting according to claim 1, characterized in that: According to the raw fuel parameters, the blast parameters and the gas injection parameters, the total heat income, the amount of bosh gas and the composition of the bosh gas in the tuyere whirlpool zone are determined, and according to the total heat income, the amount of bosh gas and the composition of the bosh gas, the theoretical combustion temperature of the gas in the tuyere whirlpool zone is determined, including: Determine the volume of gas participating in the chemical reaction, the volume of gas not participating in the chemical reaction and the volume of gas generated by the chemical reaction in the tuyere whirlpool area according to the raw fuel parameters, the blast parameters and the gas injection parameters; The heat released by the chemical reaction in the tuyere raceway is calculated based on the volume of the gas involved in the chemical reaction, and the total heat income is calculated based on the coke sensible heat, blast sensible heat, gas sensible heat and the heat released by the chemical reaction in the tuyere raceway, wherein the coke sensible heat is determined based on the raw fuel parameters. The blast sensible heat is determined based on the blast parameters, and the gas sensible heat is determined based on the gas injection parameters; Calculating the amount of the bosh gas and the composition of the bosh gas according to the volume of the gas generated by the chemical reaction and the volume of the gas not involved in the chemical reaction; The theoretical combustion temperature of the gas is iteratively solved based on the amount of the bosh gas, the composition of the bosh gas and the total heat income until the second convergence condition is met to obtain the theoretical combustion temperature of the gas.

3. The method for predicting the temperature of molten iron in blast furnace smelting according to claim 2, characterized in that: Before calculating the total heat income based on the coke sensible heat, blast sensible heat, gas sensible heat and the heat released by the chemical reaction in the tuyere raceway, the method comprises: Determine the coke specific heat capacity according to a preset coke temperature and coke composition, so as to calculate the coke sensible heat according to the preset coke temperature, the coke specific heat capacity and the coke dosage, wherein the raw fuel parameters include the coke composition and the coke dosage; Determine the blast specific heat capacity according to the blast temperature and the blast composition, so as to calculate the blast sensible heat according to the blast specific heat capacity, the blast volume and the blast temperature, wherein the blast parameters include the blast composition, the blast temperature and the blast volume; The specific heat capacity of the injected gas is determined based on the preset injected gas temperature and the injected gas composition, and the sensible heat of the gas is calculated based on the preset injected gas temperature, the injected gas specific heat capacity and the gas injection amount. The gas injection parameters include the injected gas composition and the gas injection amount.

4. The method for predicting the temperature of molten iron in blast furnace smelting according to claim 2, characterized in that: Iteratively solving the theoretical combustion temperature of the gas based on the amount of the bosh gas, the composition of the bosh gas and the total heat income until the second convergence condition is met, and obtaining the theoretical combustion temperature of the gas, including: Determine the initial bosh gas specific heat capacity of the tuyere whirlpool zone according to the bosh gas composition and the preset gas theoretical combustion temperature, and calculate the initial gas theoretical combustion temperature according to the total heat income, the bosh gas volume and the initial bosh gas specific heat capacity; The initial theoretical combustion temperature of coal gas is taken as the theoretical combustion temperature of coal gas before iteration. The iterative bosh gas specific heat capacity of the tuyere raceway is determined based on the bosh gas composition and the iterative bosh gas theoretical combustion temperature, and the iterative bosh gas theoretical combustion temperature is calculated based on the total heat income, the bosh gas volume and the iterative bosh gas specific heat capacity; Calculating the difference between the theoretical combustion temperature of the coal gas before the iteration and the theoretical combustion temperature of the coal gas after the iteration to obtain an iterative temperature difference of the theoretical combustion temperature of the coal gas; If the iterative temperature difference of the theoretical combustion temperature of coal gas is less than or equal to the second preset temperature difference threshold, the second convergence condition is met, and the theoretical combustion temperature of coal gas after iteration is used as the theoretical combustion temperature of coal gas; If the iterative temperature difference of the theoretical combustion temperature of the coal gas is greater than the second preset temperature difference threshold, the theoretical combustion temperature of the coal gas is iteratively solved based on the furnace gas volume, the furnace gas composition, the total heat income and the iterative theoretical combustion temperature of the coal gas until the second convergence condition is met to obtain the theoretical combustion temperature of the coal gas.

5. The method for predicting the temperature of molten iron in blast furnace according to any one of claims 1 to 4, characterized in that: Determining the direct reduction degree of the iron ore according to the furnace top gas parameters, the slag iron parameters, the bosh gas volume and the bosh gas composition includes: determining the amount of carbon monoxide in the bosh gas based on the bosh gas amount and the bosh gas composition, and determining the total amount of carbon monoxide and carbon dioxide in the top gas based on the top gas amount and the top gas composition, so as to determine the total amount of carbon monoxide generated by direct reduction according to the amount of carbon monoxide in the bosh gas and the total amount of carbon monoxide and carbon dioxide in the top gas, wherein the top gas parameters include the top gas amount and the top gas composition; Determine the mass of trace elements in the molten iron and the mass of iron in the molten iron based on the composition of the molten iron and the output of the molten iron, and determine the amount of carbon monoxide generated by direct reduction of trace element oxides based on the mass of the trace elements in the molten iron, so as to determine the amount of carbon monoxide generated by direct reduction of iron ore according to the total amount of carbon monoxide generated by direct reduction and the amount of carbon monoxide generated by direct reduction of the trace element oxides, wherein the slag iron parameters include the composition of the molten iron and the output of the molten iron; Based on the amount of carbon monoxide generated by direct reduction of the iron ore, the quality of the iron in the molten iron and the preset heat The mass of iron in the iron blocks is used to calculate the direct reduction degree of the iron ore.

6. The method for predicting the temperature of molten iron in blast furnace according to any one of claims 1 to 4, characterized in that: Before determining the gas-liquid heat transfer coefficient, the method includes: Determining the total amount of carbon monoxide and carbon dioxide in the top gas, the total amount of water and hydrogen in the top gas, and the amount of nitrogen in the top gas based on the top gas amount and the top gas composition, wherein the top gas parameters include the top gas amount and the top gas composition; The amount of the furnace top gas is taken as the amount of coal gas after direct reduction, the total amount of carbon monoxide and carbon dioxide in the furnace top gas is taken as the amount of carbon monoxide in the coal gas after direct reduction, the total amount of water and hydrogen in the furnace top gas is taken as the amount of hydrogen in the coal gas after direct reduction, and the amount of nitrogen in the furnace top gas is taken as the amount of nitrogen in the coal gas after direct reduction; The composition of the coal gas after direct reduction is determined based on the amount of the coal gas after direct reduction, the amount of carbon monoxide in the coal gas after direct reduction, the amount of hydrogen in the coal gas after direct reduction, and the amount of nitrogen in the coal gas after direct reduction.

7. The method for predicting the temperature of molten iron in blast furnace smelting according to any one of claims 1 to 4, characterized in that: Before determining the gas-liquid heat transfer coefficient, the method includes: Determining the total amount of carbon monoxide and carbon dioxide in the top gas based on the top gas volume and the top gas composition, wherein the top gas parameters include the top gas volume and the top gas composition; Determining the amount of hydrogen in the bosh gas and the amount of nitrogen in the bosh gas based on the amount of bosh gas and the composition of the bosh gas; The amount of the furnace top gas is taken as the amount of the coal gas after direct reduction, the total amount of carbon monoxide and carbon dioxide in the furnace top gas is taken as the amount of carbon monoxide in the coal gas after direct reduction, the amount of hydrogen in the bosh gas is taken as the amount of hydrogen in the coal gas after direct reduction, and the amount of nitrogen in the bosh gas is taken as the amount of nitrogen in the coal gas after direct reduction; The amount of direct reduction gas is determined based on the amount of coal gas after direct reduction, the amount of carbon monoxide in the coal gas after direct reduction, the amount of hydrogen in the coal gas after direct reduction, and the amount of nitrogen in the coal gas after direct reduction. Gas composition.

8. The method for predicting the temperature of molten iron in blast furnace smelting according to any one of claims 1 to 4, characterized in that: According to the theoretical combustion temperature of the coal gas, the composition of the bosh coal gas, the slag iron parameters and the composition of the coal gas after direct reduction at the direct reduction position, the gas-liquid heat exchange coefficient is determined, including: Performing interpolation calculation on the bosh gas composition and the direct reduction gas composition to obtain the gas composition of the dripping zone; Determine the gas-liquid heat exchange coefficient of the tuyere vortex zone according to the slag iron equivalent particle size, the gas thermal conductivity of the tuyere vortex zone and the Nusselt number of the tuyere vortex zone, wherein the gas thermal conductivity of the tuyere vortex zone and the Nusselt number of the tuyere vortex zone are both determined based on the bosh gas composition and the theoretical combustion temperature of the gas, and the slag iron equivalent particle size is determined based on the slag iron parameters; Determine the gas-liquid heat exchange coefficient at the direct reduction position according to the equivalent particle size of slag iron, the thermal conductivity of the coal gas at the direct reduction position and the Nusselt number at the direct reduction position, wherein the thermal conductivity of the coal gas at the direct reduction position and the Nusselt number at the direct reduction position are both determined based on the composition of the coal gas after direct reduction and the theoretical combustion temperature of the coal gas; The gas-liquid heat exchange coefficient of the dripping zone is determined according to the equivalent particle size of the slag iron, the coal gas thermal conductivity of the dripping zone and the Nusselt number of the dripping zone. The coal gas thermal conductivity of the dripping zone and the Nusselt number of the dripping zone are both determined based on the coal gas composition of the dripping zone and the theoretical combustion temperature of the coal gas.

9. The method for predicting the temperature of molten iron in blast furnace smelting according to claim 8, characterized in that: Based on the gas-liquid heat exchange coefficient, the direct reduction degree of the iron ore, the theoretical combustion temperature of the coal gas and the slag iron parameters, the molten iron temperature and the coal gas temperature are iteratively solved until the first convergence condition is met, and the molten iron temperature prediction is completed, including: Determining the heat consumption for direct reduction according to the composition of the molten iron and the direct reduction degree of the iron ore, wherein the slag iron parameters include the composition of the molten iron; Based on the coal gas phase temperature, the molten iron phase temperature, the gas-liquid heat exchange coefficient and the direct reduction heat consumption, And according to the energy conservation relationship of the coal gas phase and the energy conservation relationship of the molten iron phase, the molten iron temperature and the coal gas temperature are iteratively solved to obtain the molten iron temperature in the tuyere vortex zone before iteration, the molten iron temperature in the tuyere vortex zone after iteration, the coal gas temperature after direct reduction before iteration, and the coal gas temperature after direct reduction after iteration, the initial value of the coal gas phase temperature is the theoretical combustion temperature of the coal gas, and the initial value of the molten iron phase temperature is the preset molten iron temperature after direct reduction; Determine the difference between the molten iron temperature in the tuyere raceway before the iteration and the molten iron temperature in the tuyere raceway after the iteration as the molten iron temperature iteration temperature difference, and determine the difference between the coal gas temperature after direct reduction before the iteration and the coal gas temperature after direct reduction after the iteration as the coal gas temperature iteration temperature difference; If the iterative temperature difference of the molten iron temperature and the iterative temperature difference of the coal gas temperature are both less than or equal to the first preset temperature difference threshold, the first convergence condition is met, and the molten iron temperature in the tuyere raceway after the iteration is used as the final prediction result of the molten iron temperature prediction.

10. A device for predicting the temperature of molten iron in blast furnace smelting, characterized in that: The device comprises: The smelting data acquisition module is used to obtain the raw fuel parameters, blast parameters, gas injection parameters, top gas parameters and slag iron parameters of the blast furnace smelting process; a module for determining a theoretical combustion temperature, for determining a total heat income, a bosh gas volume and a bosh gas composition of a tuyere whirlpool zone according to the raw fuel parameter, the blast parameter and the gas injection parameter, so as to determine a theoretical combustion temperature of the gas in the tuyere whirlpool zone according to the total heat income, the bosh gas volume and the bosh gas composition; A direct reduction degree determination module, used to determine the direct reduction degree of the iron ore according to the furnace top gas parameters, the slag iron parameters, the bosh gas volume and the bosh gas composition; a heat exchange coefficient determination module, for determining the gas-liquid heat exchange coefficient according to the theoretical combustion temperature of the coal gas, the bosh coal gas composition, the slag iron parameters and the composition of the coal gas after direct reduction at the direct reduction position, wherein the composition of the coal gas after direct reduction is determined based on the furnace top gas parameters, or the composition of the coal gas after direct reduction is determined based on the furnace top gas parameters, the bosh coal gas volume and the bosh coal gas composition; The iterative solution module is used to iteratively solve the molten iron temperature and the coal gas temperature based on the gas-liquid heat exchange coefficient, the direct reduction degree of the iron ore, the theoretical combustion temperature of the coal gas and the slag iron parameters until The first convergence condition is met and the prediction of molten iron temperature in blast furnace smelting is completed.

11. An electronic device, characterized in that: The electronic device comprises: one or more processors; A storage device for storing one or more programs, which, when executed by the one or more processors, enables the electronic device to implement the method for predicting the temperature of molten iron in blast furnace smelting as described in any one of claims 1-9.

12. A computer-readable storage medium, characterized in that: A computer program is stored thereon, and when the computer program is executed by a processor of a computer, the computer is caused to execute a method for predicting the temperature of molten iron in blast furnace smelting as described in any one of claims 1-9.

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