Blast furnace smelting molten iron temperature prediction method and device, electronic equipment and storage medium

Abstract

The present application provides a kind of blast furnace smelting molten iron temperature prediction method, device, electronic equipment and storage medium, the method includes obtaining the raw fuel parameters of blast furnace smelting process, blast parameter, coal gas injection parameter, top gas parameter and slag iron parameter, according to raw fuel parameters, blast parameter and coal gas injection parameter determines the amount of furnace bosh gas, bosh gas composition and gas theoretical combustion temperature of wind port convolute area, according to top gas parameter, slag iron parameter, bosh gas amount and bosh gas composition determines iron ore direct reduction degree, according to gas theoretical combustion temperature, bosh gas composition, slag iron parameter and direct reduction after gas composition determines gas-liquid heat exchange coefficient, based on gas-liquid heat exchange coefficient, iron ore direct reduction degree, gas theoretical combustion temperature and slag iron parameter carry out molten iron temperature and gas temperature iterative solution, complete blast furnace smelting molten iron temperature prediction;It can improve molten iron temperature prediction accuracy, provide good basis for blast furnace smelting control, ensure that blast furnace is stable and goes along.

Description

Technical Field

[0001] This application relates to the field of blast furnace smelting technology, specifically to a method, apparatus, electronic device, and storage medium for predicting the temperature of molten iron in blast furnace smelting. Background Technology

[0002] In the blast furnace smelting process, the temperature of molten iron reflects the heat balance and iron ore reduction state within the furnace. Meanwhile, gas injection technology is a key technology for reducing carbon emissions in the blast furnace, and maintaining a stable molten iron temperature is crucial for the stable operation of the blast furnace under gas injection conditions. Therefore, effectively and accurately predicting the temperature of molten iron is of significant guiding importance for the operational control of blast furnace smelting.

[0003] Currently, most related technologies determine the temperature variation patterns of molten iron from historical operating data and then predict the temperature of molten iron. However, they do not take into account real-time parameters enough, which affects the accuracy of the prediction and makes it difficult to make reasonable predictions of the temperature of molten iron under gas injection conditions. Summary of the Invention

[0004] In view of the shortcomings of the prior art described above, this application provides a method, apparatus, electronic device and storage medium for predicting the temperature of molten iron in blast furnace smelting, so as to solve the technical problem that the above-mentioned related technologies do not consider real-time parameters enough 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 the gas injection condition.

[0005] This application provides a method for predicting the temperature of molten iron in blast furnace smelting. The method includes: acquiring raw material parameters, blast parameters, gas injection parameters, furnace top gas parameters, and slag-iron parameters for the blast furnace smelting process; determining the total heat input, furnace belly gas volume, and furnace belly gas composition in the tuyeres based on the raw material parameters, blast parameters, and gas injection parameters, and determining the theoretical combustion temperature of the gas in the tuyeres based on the total heat input, furnace belly gas volume, and furnace belly gas composition; and determining the iron ore direct current based on the furnace top gas parameters, slag-iron parameters, furnace belly gas volume, and furnace belly gas composition. The reduction degree is determined; based on the theoretical combustion temperature of the gas, the composition of the furnace gas, the slag and iron parameters, and the composition of the gas after direct reduction at the direct reduction location, the gas-liquid heat transfer coefficient is determined. The composition of the gas after direct reduction is determined based on the furnace top gas parameters, or the composition of the gas after direct reduction is determined based on the furnace top gas parameters, the furnace gas quantity, and the furnace gas composition. Based on the gas-liquid heat transfer coefficient, the direct reduction degree of the iron ore, the theoretical combustion temperature of the gas, and the slag and iron parameters, the molten iron temperature and gas temperature are iteratively solved until the first convergence condition is met, thus completing the prediction of the molten iron temperature in blast furnace smelting.

[0006] In one embodiment of this application, the total heat input, furnace gas volume, and furnace gas composition of the tuyeres' swirl zone are determined based on the raw material parameters, the blast parameters, and the gas injection parameters. The theoretical combustion temperature of the gas in the tuyeres' swirl zone is then determined based on the total heat input, the furnace gas volume, and the furnace gas composition. This 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 produced by the chemical reaction in the tuyeres' swirl zone based on the raw material parameters, the blast parameters, and the gas injection parameters; and calculating the chemical reaction release in the tuyeres' swirl zone based on the volume of gas participating in the chemical reaction. The heat is calculated based on the sensible heat of coke, sensible heat of blast, sensible heat of gas, and heat released by the chemical reaction in the tuyeres. The sensible heat of coke is determined based on the raw material parameters, the sensible heat of blast is determined based on the blast parameters, and the sensible heat of gas is determined based on the gas injection parameters. The volume of gas produced by the chemical reaction and the volume of gas that did not participate in the chemical reaction are used to calculate the volume and composition of the gas in the furnace. The theoretical combustion temperature of the gas is iteratively solved based on the volume, composition, and total heat income until the second convergence condition is met, thus obtaining the theoretical combustion temperature of the gas.

[0007] In one embodiment of this application, before calculating the total heat input based on the sensible heat of coke, sensible heat of blast, sensible heat of coal gas, and heat released by the chemical reaction in the vortex zone, the method includes: determining the specific heat capacity of coke based on a preset coke temperature and coke composition, so as to calculate the sensible heat of coke based on the preset coke temperature, the specific heat capacity of coke, and the amount of coke used, wherein the raw material parameters include the coke composition and the amount of coke used; determining the specific heat capacity of blast based on blast temperature and blast composition, so as to calculate the sensible heat of blast based on the specific heat capacity of blast, blast volume, and blast temperature, wherein the blast parameters include the blast composition, the blast temperature, and the blast volume; determining the specific heat capacity of injected coal gas based on a preset injected coal gas temperature and injected coal gas composition, so as to calculate the sensible heat of coal gas based on the preset injected coal gas temperature, the specific heat capacity of injected coal gas, and the coal gas injection volume, wherein the coal gas injection parameters include the injected coal gas composition and the coal gas injection volume.

[0008] In one embodiment of this application, the theoretical combustion temperature of the gas is iteratively solved based on the furnace gas volume, the furnace gas composition, and the total heat input until a second convergence condition is met, thereby obtaining the theoretical combustion temperature of the gas. This includes: determining the initial specific heat capacity of the furnace gas in the tuyeres' swirl zone based on the furnace gas composition and a preset theoretical combustion temperature; calculating the initial theoretical combustion temperature of the gas based on the total heat input, the furnace gas volume, and the initial specific heat capacity of the furnace gas; using the initial theoretical combustion temperature of the gas as the theoretical combustion temperature of the gas before iteration; determining the iterative specific heat capacity of the furnace gas in the tuyeres' swirl zone based on the furnace gas composition and the iterative specific heat capacity of the gas before iteration; and calculating the iterative theoretical combustion temperature of the gas based on the total heat input, the furnace gas volume, and the initial theoretical combustion temperature of the gas before iteration. The specific heat capacity of the furnace gas is iterated 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 taken 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 gas volume, the furnace gas composition, the total heat input, and the theoretical combustion temperature of the gas after iteration until the second convergence condition is met, and the theoretical combustion temperature of the gas is obtained.

[0009] In one embodiment of this application, determining the direct reduction degree of iron ore based on the top gas parameters, the slag-iron parameters, the amount of belly gas, and the composition of the belly gas includes: determining the amount of carbon monoxide in the belly gas based on the amount of belly gas and the composition of the belly gas, and determining the total amount of carbon monoxide and carbon dioxide in the top gas based on the amount of top gas and the composition of the top gas, so as to determine the total amount of carbon monoxide generated by direct reduction based on the amount of carbon monoxide in the belly gas and the total amount of carbon monoxide and carbon dioxide in the top gas, wherein the top gas parameters include the amount of top gas and the composition of the top gas; The mass of trace elements and the mass of iron in the molten iron are determined based on the composition and output of the molten iron. The amount of carbon monoxide generated by the direct reduction of trace element oxides is then determined based on the mass of the trace elements in the molten iron. Based on the total amount of carbon monoxide generated by the direct reduction and the amount of carbon monoxide generated by the direct reduction of trace element oxides, the amount of carbon monoxide generated by the direct reduction of iron ore is determined. The slag-iron parameters include the composition and output of the molten iron. The degree of direct reduction of the iron ore is calculated based on the amount of carbon monoxide generated by the direct reduction of iron ore, the mass of iron in the molten iron, and the mass of iron in a preset hot-pressed iron block.

[0010] In one embodiment of this application, before determining the gas-liquid heat transfer coefficient, the method includes: determining the total amount of carbon monoxide and carbon dioxide, the total amount of water and hydrogen, and the amount of nitrogen in the top gas based on the top gas quantity and composition, wherein the top gas parameters include the top gas quantity and the top gas composition; using the top gas quantity as the direct-reduction gas quantity, the total amount of carbon monoxide and carbon dioxide in the top gas as the carbon monoxide content in the direct-reduction gas, the total amount of water and hydrogen in the top gas as the hydrogen content in the direct-reduction gas, and the nitrogen content in the top gas as the nitrogen content in the direct-reduction gas; and determining the direct-reduction gas composition based on the direct-reduction gas quantity, the carbon monoxide content, the hydrogen content, and the nitrogen content.

[0011] In one embodiment of this application, 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 and nitrogen in the belly gas based on the belly gas volume and the belly gas composition; using the top gas volume as the direct-reduction gas volume, the total amount of carbon monoxide and carbon dioxide in the top gas as the carbon monoxide content in the direct-reduction gas, the amount of hydrogen in the belly gas as the hydrogen content in the direct-reduction gas, and the amount of nitrogen in the belly gas as the nitrogen content in the direct-reduction gas; and determining the direct-reduction gas composition based on the direct-reduction gas volume, the carbon monoxide content, the hydrogen content, and the nitrogen content.

[0012] In one embodiment of this application, the gas-liquid heat transfer coefficient is determined based on the theoretical combustion temperature of the gas, the composition of the gas in the furnace belly, the slag and iron parameters, and the composition of the gas after direct reduction at the direct reduction location. This includes: interpolating the composition of the gas in the furnace belly and the composition of the gas after direct reduction to obtain the gas composition of the drip zone; determining the gas-liquid heat transfer coefficient of the tuyeres based on the equivalent particle size of the slag and iron, the thermal conductivity of the gas in the tuyeres' swirling zone, and the Nusselt number of the tuyeres' swirling zone. The thermal conductivity of the gas in the tuyeres' swirling zone and the Nusselt number of the tuyeres' swirling zone are both determined based on the composition of the gas in the furnace belly and the theoretical combustion temperature of the gas. The equivalent particle size of the slag and iron is based on the... The slag and iron parameters are determined as follows: The gas-liquid heat transfer coefficient at the direct reduction position is determined based on the equivalent particle size of the slag and iron, the thermal conductivity of the gas at the direct reduction position, and the Nusselt number at the direct reduction position. Both the thermal conductivity of the gas at the direct reduction position and the Nusselt number at the direct reduction position are determined based on the composition of the gas after direct reduction and the theoretical combustion temperature of the gas. The gas-liquid heat transfer coefficient at the dripping zone is determined based on the equivalent particle size of the slag and iron, the thermal conductivity of the gas at the dripping zone, and the Nusselt number at the dripping zone. Both the thermal conductivity of the gas at the dripping zone and the Nusselt number at the dripping zone are determined based on the composition of the gas at the dripping zone and the theoretical combustion temperature of the gas.

[0013] In one embodiment of this application, based on the gas-liquid heat transfer 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 coal gas temperature are iteratively solved until a first convergence condition is met, thus completing the prediction of the molten iron temperature. This includes: determining the direct reduction heat consumption based on the molten iron composition and the direct reduction degree of the iron ore, wherein the slag-iron parameters include the molten iron composition; and iteratively solving the molten iron temperature and coal gas temperature based on the coal gas phase temperature, the molten iron phase temperature, the gas-liquid heat transfer coefficient, and the direct reduction heat consumption, and according to the energy conservation relationship between the coal gas phase and the molten iron phase, to obtain the molten iron temperature in the tuyeres before iteration, the molten iron temperature in the tuyeres after iteration, and the coal gas temperature after direct reduction before iteration. The initial values ​​of the gas phase temperature and the molten iron phase temperature are: the initial value of the gas phase temperature and the initial value of the molten iron phase temperature. The difference between the molten iron temperature in the tuyeres before iteration and the molten iron temperature in the tuyeres after iteration is determined as the molten iron temperature iteration difference. The difference between the molten iron temperature in the tuyeres before iteration and the molten iron temperature in the tuyeres after iteration is also determined as the gas temperature iteration difference. If both the molten iron temperature iteration difference and the gas temperature iteration difference are less than or equal to a first preset temperature difference threshold, then the first convergence condition is met, and the molten iron temperature in the tuyeres after iteration is taken as the final prediction result for the molten iron temperature prediction.

[0014] In one embodiment of this application, a blast furnace smelting hot metal temperature prediction device is also provided. The device includes: a smelting data acquisition module, used to acquire raw material parameters, blast parameters, gas injection parameters, furnace top gas parameters, and slag-iron parameters during the blast furnace smelting process; a theoretical combustion temperature determination module, used to determine the total heat input, furnace belly gas volume, and furnace belly gas composition in the tuyeres based on the raw material parameters, blast parameters, and gas injection parameters, so as to determine the theoretical combustion temperature of the gas in the tuyeres based on the total heat input, furnace belly gas volume, and furnace belly gas composition; and a direct reduction degree determination module, used to determine the blast furnace top gas parameters, slag-iron parameters, furnace belly gas volume, and slag-iron parameters based on the blast furnace top gas parameters, slag-iron parameters, furnace belly gas volume, and slag-iron parameters. The module determines the direct reduction degree of iron ore based on the composition of the blast furnace gas. A heat transfer coefficient determination module is used to determine the gas-liquid heat transfer coefficient based on the theoretical combustion temperature of the gas, the composition of the blast furnace gas, the slag-iron parameters, and the composition of the gas after direct reduction at the direct reduction location. The composition of the gas after direct reduction is determined based on the parameters of the blast furnace top gas, or iteratively, based on the parameters of the blast furnace top gas, the amount of gas in the blast furnace, and the composition of the gas in the blast furnace. An iterative solution module is used to iteratively solve for the molten iron temperature and 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, thus completing the prediction of the blast furnace molten iron temperature.

[0015] In one embodiment of this application, an electronic device is also provided, the electronic device comprising: one or more processors; and a storage device for storing one or more programs, which, when executed by the one or more processors, cause the electronic device to implement the blast furnace smelting molten iron temperature prediction method as described above.

[0016] In one embodiment of this application, a computer-readable storage medium is also provided, on which a computer program is stored, which, when executed by a computer processor, causes the computer to perform the blast furnace smelting molten iron temperature prediction method as described above.

[0017] The beneficial effects of this invention are as follows: This invention provides a method, device, electronic equipment, and storage medium for predicting the temperature of molten iron in blast furnace smelting. This method calculates the theoretical combustion temperature of the gas, the gas-liquid heat transfer coefficient, and the direct reduction degree of iron ore by utilizing the raw material parameters, blast parameters, gas injection parameters, furnace top gas parameters, and slag-iron parameters of the blast furnace smelting process. This allows for iterative solutions for the molten iron temperature and gas temperature, enabling the prediction of molten iron temperature in blast furnace smelting under various operating conditions, such as gas injection conditions. It also improves the accuracy of molten iron temperature prediction, providing a good basis for the operation and control of blast furnace smelting, and ensuring the stable and smooth operation of the blast furnace.

[0018] It should be understood that the above general description and the following detailed description are exemplary and explanatory only, and do not limit this application. Attached Figure Description

[0019] Figure 1 This is a flowchart illustrating an exemplary embodiment of the present application of a method for predicting the temperature of molten iron in blast furnace smelting;

[0020] Figure 2 This is a schematic diagram of the structure of a water temperature prediction system for blast furnace ironmaking process, shown in a specific embodiment of this application;

[0021] Figure 3 yes Figure 2 The illustrated embodiment shows a schematic diagram of the blast furnace smelting process molten iron temperature prediction system in a specific embodiment.

[0022] Figure 4 This is a block diagram illustrating a blast furnace smelting molten iron temperature prediction device, as shown in an exemplary embodiment of this application.

[0023] Figure 5 This is a schematic diagram illustrating the structure of an electronic device as shown in an exemplary embodiment of this application. Detailed Implementation

[0024] The following specific examples illustrate the implementation of this application. Those skilled in the art can easily understand other advantages and effects of this application from the content disclosed in this specification. This application can also be implemented or applied through other different specific embodiments, and various details in this specification can also be modified or changed based on different viewpoints and applications without departing from the spirit of this application. It should be noted that, unless otherwise specified, the following embodiments and features in the embodiments can be combined with each other.

[0025] It should be noted that the illustrations provided in the following embodiments are only schematic representations of the basic concept of this application. Therefore, the drawings only show the components related to this application and are not drawn according to the actual number, shape and size of the components in the actual implementation. In the actual implementation, the form, quantity and proportion of each component can be arbitrarily changed, and the layout of the components may also be more complex.

[0026] It should be noted that in this application, terms such as "first" and "second" are merely for distinguishing similar objects, and do not limit the order or sequence of similar objects. The variations of "including" and "having" indicate that the scope covered by the subject of the word is not exclusive, except for the examples shown by the word.

[0027] It is understood that the various numerical designations, step numbers, and other identifiers recorded in this application are for descriptive convenience and are not intended to limit the scope of this application. The size of the identifiers in this application does not imply the order of execution; the execution order of each process should be determined by its function and internal logic.

[0028] In the following description, numerous details are explored to provide a more thorough explanation of embodiments of the present application. However, it will be apparent to those skilled in the art that embodiments of the present application may be practiced without these specific details. In other embodiments, well-known structures and devices are shown in block diagram form rather than in detail to avoid obscuring embodiments of the present application.

[0029] The embodiments of this 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.

[0030] In one embodiment of this application, a method for predicting the temperature of molten iron in a blast furnace is proposed, comprising: acquiring raw material parameters, blast parameters, gas injection parameters, top gas parameters, and slag-iron parameters for the blast furnace smelting process; determining the total heat input, furnace gas volume, and furnace gas composition in the tuyeres based on the raw material parameters, blast parameters, and gas injection parameters, so as to determine the theoretical combustion temperature of the gas in the tuyeres based on the total heat input, furnace gas volume, and furnace gas composition; and determining the theoretical combustion temperature of the gas in the tuyeres based on the top gas parameters, slag-iron parameters, furnace gas volume, and furnace gas composition. The direct reduction degree of iron ore is determined; based on the theoretical combustion temperature of the gas, the composition of the gas in the furnace belly, the slag and iron parameters, and the composition of the gas after direct reduction at the direct reduction location, the gas-liquid heat transfer coefficient is determined. The composition of the gas after direct reduction is determined based on the gas parameters at the furnace top, or based on the gas parameters at the furnace top, the gas volume in the furnace belly, and the composition of the gas in the furnace belly. 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 and iron parameters, the molten iron temperature and the gas temperature are iteratively solved until the first convergence condition is met, thus completing the prediction of the molten iron temperature in blast furnace smelting. It is evident that the technical solution of this application embodiment can realize the prediction of the molten iron temperature in blast furnace smelting under various operating conditions, such as gas injection, and improve the accuracy of the molten iron temperature prediction, providing a good basis for the operation and control of blast furnace smelting, and ensuring the stable and smooth operation of the blast furnace.

[0031] Please see Figure 1 , Figure 1 This is a flowchart illustrating an exemplary embodiment of the present application of a method for predicting the temperature of molten iron in blast furnace smelting. Figure 1 As shown, in an exemplary embodiment, the method for predicting the temperature of molten iron in blast furnace smelting includes at least steps S110 to S150, which are described in detail below:

[0032] Step S110: Obtain the raw material parameters, blast parameters, gas injection parameters, furnace top gas parameters, and slag and iron parameters for the blast furnace smelting process.

[0033] In one embodiment of this application, the raw material parameters refer to the composition and quantity of the raw material, which may include at least one of the following: coke composition and quantity, pulverized coal composition and quantity. The raw material composition refers to the proportion of substances in the raw material. For example, the coke composition may include the proportions of C (carbon), H (hydrogen), O (oxygen), N (nitrogen), S (sulfur), volatile matter, and ash in the coke; the pulverized coal composition may include the proportions of C, H, O, N, S, volatile matter, and ash in the pulverized coal.

[0034] The blowing parameters may include at least one of the following: blowing volume, blowing temperature, blowing composition, etc., wherein the blowing composition may include at least one of the following: blowing humidity, oxygen enrichment rate, etc.

[0035] The parameters for coal gas injection include at least one of the following: type of injection medium, composition of injected coal gas, injection volume, and temperature. The type of injection medium includes one or more mixtures of coke oven gas, converter gas, decarbonized blast furnace gas, natural gas, pure hydrogen, chemical tail gas, and shale gas. The composition of injected coal gas refers to the proportion of substances in the injected coal gas. For example, the composition of injected coal gas may include the proportions of H2 (hydrogen), CO (carbon monoxide), CO2 (carbon dioxide), CH4 (methane), N2 (nitrogen), and O2 (oxygen) in the injected coal gas.

[0036] Top gas parameters include at least one of the following: top gas composition and top gas quantity. The top gas composition refers to the proportion of substances in the top gas. For example, the top gas composition may include the proportions of H2, CO, CO2, N2, etc., in the top gas.

[0037] Slag and iron parameters include at least one of the following: molten iron composition (i.e., slag and iron composition), molten iron production, and slag production (i.e., slag quantity). Among these, molten iron composition refers to the proportion of substances in the molten iron. For example, molten iron composition can include the proportions of Fe (iron), C, Si (silicon), Mn (manganese), P (phosphorus), S, and Ti (titanium) in the molten iron.

[0038] It should be understood that the parameters of raw materials, blast furnace, gas injection, furnace top gas, and slag and iron are real-time data of the blast furnace smelting process, which can directly and in real time reflect the smelting situation inside the blast furnace. Therefore, the temperature of molten iron can be accurately predicted based on the parameters of raw materials, blast furnace, gas injection, furnace top gas, and slag and iron.

[0039] Step S120: Based on the raw material parameters, blast parameters, and gas injection parameters, determine the total heat input, furnace gas volume, and furnace gas composition in the tuyeres swirling zone, so as to determine the theoretical combustion temperature of the gas in the tuyeres swirling zone based on the total heat input, furnace gas volume, and furnace gas composition.

[0040] In one embodiment of this application, the blast furnace comprises five zones, from top to bottom: a blocky zone, a softening zone, a dripping zone, a tuyere swirl zone, and a slag-iron zone, distributed at different heights within the blast furnace. The blocky zone is used for burden moisture evaporation and thermal decomposition, iron ore reduction, and heat exchange between the burden and gas. The softening zone softens the burden; melting and dripping begin at the lower boundary of the softening zone, resulting in a direct reduction reaction in blast furnace ironmaking, forming primary slag. Therefore, the lower boundary of the softening zone is the direct reduction location. In the dripping zone, various chemical reactions occur between the dripping liquid slag-iron, gas, and solid carbon. In the tuyere swirl zone, injected fuel reacts with hot blast to produce high-temperature gas. In the slag-iron zone, slag-metal reactions occur at the interface between the slag and iron layers and when iron droplets pass through the slag layer.

[0041] The slag and iron in the tuyere vortex zone are in a liquid state; this liquid slag and iron is molten iron. Accordingly, the molten iron temperature refers to the slag and iron temperature of the liquid slag and iron in the tuyere vortex zone. Because there is heat exchange between the molten iron and the gas, the molten iron temperature is affected by the theoretical combustion temperature of the gas in the tuyere vortex zone. Therefore, it is necessary to determine the theoretical combustion temperature of the gas. This can be done by determining the total heat input of the tuyere vortex zone, the amount of gas in the furnace belly, and the composition of the gas in the furnace belly based on the raw material parameters, blast parameters, and gas injection parameters, thereby determining the theoretical combustion temperature of the gas.

[0042] In one embodiment of this 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 produced by the chemical reaction in the tuyeres swirl zone based on the raw material parameters, blast parameters, and gas injection parameters; calculating the heat released by the chemical reaction in the tuyeres swirl zone based on the volume of gas participating in the chemical reaction, and calculating the total heat input based on the sensible heat of coke, sensible heat of blast, sensible heat of gas, and heat released by the chemical reaction in the tuyeres swirl zone, where the sensible heat of coke is determined based on the raw material parameters, the sensible heat of blast is determined based on the blast parameters, and the sensible heat of gas is determined based on the gas injection parameters; calculating the amount of gas in the furnace and the composition of the gas in the furnace based on the volume of gas produced by the chemical reaction and the volume of gas not participating in the chemical reaction; and iteratively solving for the theoretical combustion temperature of the gas based on the amount of gas in the furnace, the composition of the gas in the furnace, and the total heat input until the second convergence condition is met, thereby obtaining the theoretical combustion temperature of the gas.

[0043] In this embodiment, please refer to Table 1, which is a table of chemical reactions and thermal effects in the tuyeres swirl zone of a specific embodiment of this application. As shown in Table 1, in the tuyeres swirl zone, the elemental carbon, CO2, H2O (water), CH4, or chemical C in the injected gas, injected pulverized coal, and coke... x H y O m N n When it comes into contact with oxygen or other substances, it undergoes combustion and other chemical reactions, and is completely converted into CO, H2 and N2, with different chemical reactions having different thermal effects.

[0044] Table 1

[0045] serial number Reaction thermal effect 1 <![CDATA[C+CO2=2CO]]> <![CDATA[ΔH C1 ]]> 2 <![CDATA[C+H2O=H2+CO]]> <![CDATA[ΔH C2 ]]> 3 <![CDATA[CH4+0.5O2=CO+H2]]> <![CDATA[ΔH CH4 ]]> 4 <![CDATA[C+0.5O2=CO]]> <![CDATA[ΔH C3 ]]> 5 <![CDATA[C x HO m N n +O2=CO+H2+N2]]> <![CDATA[ΔH C4 ]]>

[0046] Therefore, the calculation method for the heat released by the chemical reaction in the wind vortex zone is as follows:

[0047] Q2=aΔH C1 +bΔH C2 +cΔH CH4 +dΔH C3 +eΔH C4 Equation (1)

[0048] Where Q2 represents the heat released by the chemical reaction in the vortex zone, and a, b, c, d, and e are the amounts of reactants involved in reactions 1-5 in Table 1, respectively. ΔH C1 ΔH C2 ΔH CH4 ΔH C3 ΔH C4 The following table shows the heat effects corresponding to reactions 1-5 in Table 1. The values ​​of a, b, and c depend on the volumetric amounts of CO2, H2O, and CH4 in the injected gas, while the values ​​of d and e depend on the total oxygen content entering the blast furnace. It should be noted that when calculating the heat released by the chemical reactions in the tuyeres, O2 preferentially reacts with CH4 and C. x H y O m N n The gaseous components react first, and finally react with solid carbon (C). The combustion priority among coal gas, pulverized coal, coke, and oxygen is: coal gas > pulverized coal > coke, with the pulverized coal burnout rate being 70-84%.

[0049] Therefore, when calculating the heat released by the chemical reaction in the vortex zone, we can first determine the volume of gases participating in the chemical reaction in the vortex zone, including the volume of CO2, H2O, CH4, and C. x H y O m N n Volume and O2 volume. Specifically, this can be based on the proportions of CO2, H2O, CH4, and C in the injected gas composition.x H y O m N n The proportion and injection rate of the coal gas are used to determine the volume of CO2, H2O, CH4, and C in the injected coal gas. x H y O m N n The volume of O2 in the blast furnace is determined by the following parameters: the O2 volume in the blast gas is determined by the O2 ratio in the blast gas composition and the blast volume; the O2 volume in the blast air is determined by the O2 ratio in the blast air composition and the blast volume, where the blast air parameters include the blast air composition and blast volume; the O2 volume in the coke is determined by the O2 ratio in the coke composition and the coke dosage; and the O2 volume in the pulverized coal is determined by the O2 ratio in the pulverized coal composition and the pulverized coal dosage, where the raw material parameters include the coke composition and coke dosage, and the pulverized coal composition and pulverized coal dosage. The total oxygen content entering the blast furnace is calculated based on the O2 volumes in the blast gas, blast air, coke, and pulverized coal, using the following method:

[0050]

[0051] Among them, V t This refers to the total amount of oxygen entering the blast furnace. The volume of O2 in the blower air. This represents the volume of O2 in the injected coal gas. This represents the volume of O2 in the coke. This represents the volume of O2 in the pulverized coal.

[0052] After obtaining the heat released by the chemical reaction in the tuyere swirl zone, the total heat input of the tuyere swirl zone is calculated based on the sensible heat of coke, sensible heat of blast air, sensible heat of gas, and heat released by the chemical reaction. The calculation method is as follows:

[0053] Q = Q1 + Q2 + Q3 + Q4 (Equation 3)

[0054] Where Q represents the total heat input in the tuyere swirl zone, Q1 represents the sensible heat of the blast, Q2 represents the heat released by the chemical reaction in the tuyere swirl zone, Q3 represents the sensible heat of the coal gas, and Q4 represents the sensible heat of the coke. The sensible heat of the blast is determined based on the blast parameters, the sensible heat of the coal gas is determined based on the coal gas injection parameters, and the sensible heat of the coke is determined based on the raw material parameters.

[0055] The gas in the tuyere swirl zone includes gases produced by chemical reactions and gases that do not participate in chemical reactions. The volume of gases produced by chemical reactions in the tuyere swirl zone, including CO and H2, can be determined based on the volume of gases participating in chemical reactions and the reaction formulas in Table 1. Since pulverized coal, injected gas, and blast air contain N2, and Table 1 shows that gases participating in chemical reactions do not contain N2, the volume of N2 in pulverized coal, injected gas, and blast air can be determined as the volume of gases not participating in chemical reactions. Specifically, the volume of N2 in pulverized coal can be determined based on the N2 ratio in the pulverized coal composition and the amount of pulverized coal used; the volume of N2 in injected gas can be determined based on the N2 ratio in the injected gas composition and the gas injection rate; and the volume of N2 in blast air can be determined based on the N2 ratio in the blast air composition and the blast rate. Then, based on the volumes of gases produced by chemical reactions and gases not participating in chemical reactions, the amount of gas in the tuyere swirl zone is calculated as follows:

[0056]

[0057] Among them, V G This refers to the amount of gas in the furnace belly. This represents the volume of CO produced after the coke reacts in the tuyer zone. This refers to the volume of CO produced after the pulverized coal reacts in the tuyeres' swirl zone. This refers to the volume of CO produced after the injected gas reacts in the tuyeres' swirl zone. This refers to the volume of CO produced after the water in the blower reacts in the vortex zone. This refers to the volume of H2 produced after the hydrogen from the moisture and volatiles of pulverized coal reacts in the tuyer swirl zone. The volume of H2 produced after the water in the blower reacts in the vortex zone. This refers to the volume of H2 produced after the reaction of water and hydrogen-containing gases (such as methane, ethane, and ethylene) in the tuyeres of the injected coal gas. The volume of N2 in the pulverized coal. The volume of N2 in the injected gas. This represents the volume of N2 in the blower. (Illustrative) This includes the volume of CO produced by the reaction of fixed carbon in pulverized coal, carbon in volatile matter, and moisture. This includes the volume of N2 in the pulverized coal volatilization and the pulverized coal carrier gas.

[0058] As can be seen from equation (4), the furnace gas includes CO, H2 and N2. The volumes of CO, H2 and N2 in the furnace gas can be determined based on the volume of gas produced by the chemical reaction and the volume of gas that did not participate in the chemical reaction. The proportion of CO in the furnace gas can be calculated based on the volume of CO in the furnace gas and the amount of furnace gas. The proportion of H2 in the furnace gas can be calculated based on the volume of H2 in the furnace gas and the amount of furnace gas. The proportion of N2 in the furnace gas can be calculated based on the volume of N2 in the furnace gas and the amount of furnace gas. The proportions of CO, H2 and N2 in the furnace gas are used as the components of the furnace gas.

[0059] After obtaining the total heat input, the amount of gas in the furnace belly, and the composition of the gas in the furnace belly, the theoretical combustion temperature of the gas is iteratively solved based on the amount of gas in the furnace belly, the composition of the gas in the furnace belly, and the total heat input until the second convergence condition is met, thus obtaining the theoretical combustion temperature of the gas. Illustratively, the second convergence condition can be that the number of iterations in the iterative solution for the theoretical combustion temperature of the gas meets a second preset number of iterations, or that the iterative temperature difference of the theoretical combustion temperature of the gas is less than or equal to a second preset temperature difference threshold, or other convergence conditions, which are not restricted here. By using the sum of the sensible heat of coke, the sensible heat of blast furnace air, the sensible heat of gas, and the heat released by chemical reactions as the total heat input, the released heat is comprehensively considered, improving the accuracy of the calculation of the theoretical combustion temperature of the gas.

[0060] In one embodiment of this application, before calculating the total heat input based on the sensible heat of coke, sensible heat of blast, sensible heat of coal gas, and heat released by chemical reactions in the tuyeres' swirl zone, the method includes: determining the specific heat capacity of coke based on a preset coke temperature and coke composition, so as to calculate the sensible heat of coke based on the preset coke temperature, specific heat capacity of coke, and coke dosage, wherein the raw material parameters include coke composition and coke dosage; determining the specific heat capacity of blast based on blast temperature and blast composition, so as to calculate the sensible heat of blast based on the specific heat capacity of blast, blast volume, and blast temperature, wherein the blast parameters include blast composition, blast temperature, and blast volume; determining the specific heat capacity of injected coal gas based on a preset injected coal gas temperature and injected coal gas composition, so as to calculate the sensible heat of coal gas based on the preset injected coal gas temperature, specific heat capacity of injected coal gas, and coal gas injection volume, wherein the coal gas injection parameters include injected coal gas composition and coal gas injection volume.

[0061] In this embodiment, the blower, coke, and pulverized gas are all composed of different substances, and the specific heat capacity of different substances is different. Furthermore, the specific heat capacity of the same substance is also different at different temperatures. Therefore, the relationship between the specific heat capacity of different substances and temperature can be established in advance.

[0062] When calculating the sensible heat of the blower, firstly, based on the pre-defined relationship between the specific heat capacity of different substances and temperature, and the blower temperature in the blower parameters, determine the specific heat capacity of each substance in the blower at the blower temperature. Then, based on the specific heat capacity of each substance in the blower at the blower temperature and the proportion of each substance in the blower composition in the blower parameters, calculate the specific heat capacity of the blower. Finally, calculate the sensible heat of the blower based on the specific heat capacity, blower temperature, and blower volume in the blower parameters. The calculation method is as follows:

[0063] Q1 = C b V b T b Equation (5)

[0064] Where Q1 is the sensible heat of the blower, C b For the specific heat capacity of the blower air, V b For blower volume, T b This refers to the blower temperature.

[0065] When calculating the sensible heat of coal gas, firstly, based on the preset relationship between the specific heat capacity of different substances and temperature, and the preset temperature of the injected coal gas, determine the specific heat capacity of each substance in the injected coal gas at the preset temperature. Then, based on the specific heat capacity of each substance in the injected coal gas at the preset temperature and the proportion of each substance in the injected coal gas composition in the coal gas injection parameters, calculate the specific heat capacity of the injected coal gas. Finally, calculate the sensible heat of the coal gas based on the specific heat capacity of the injected coal gas, the preset temperature of the injected coal gas, and the coal gas injection rate in the coal gas injection parameters. The calculation method is as follows:

[0066] Q3 = C gi V gi T gi Equation (6)

[0067] Where Q3 is the sensible heat of the gas, C gi V is the specific heat capacity of the injected gas. gi T represents the amount of gas injected. gi This is the preset temperature for the injected gas.

[0068] When calculating the sensible heat of coke, firstly, based on the pre-defined relationship between the specific heat capacity of different substances and temperature, and the pre-defined coke temperature, determine the specific heat capacity of each substance in the coke at the pre-defined coke temperature. Then, based on the specific heat capacity of each substance in the coke at the pre-defined coke temperature and the proportion of each substance in the coke composition in the raw material parameters, calculate the specific heat capacity of the coke. Finally, calculate the sensible heat of the coke based on the specific heat capacity of the coke, the pre-defined coke temperature, and the amount of coke in the raw material parameters. The calculation method is as follows:

[0069] Q4 = C coke m coke T coke Equation (7)

[0070] Where Q4 is the sensible heat of coke, C cokeFor the specific heat capacity of coke, m coke For coke usage, T coke This is the preset coke temperature. It is illustrative; the preset coke temperature can be any temperature value between 1400 and 1500℃, or any other temperature value, without restriction.

[0071] This embodiment considers the effects of temperature and the proportion of each substance on the specific heat capacity of blast air, coal gas, and coke. By determining the specific heat capacity of blast air, coal gas, and coke through temperature and the proportion of each substance, the accuracy of the specific heat capacity of blast air, coal gas, and coke is improved, thereby improving the accuracy of the calculation of the sensible heat of blast air, coal gas, and coke.

[0072] In one embodiment of this application, the theoretical combustion temperature of the gas is iteratively solved based on the gas volume, gas composition, and total heat input until a second convergence condition is met, thus obtaining the theoretical combustion temperature. This includes: determining the initial specific heat capacity of the gas in the tuyeres' swirl zone based on the gas composition and a preset theoretical combustion temperature; calculating the initial theoretical combustion temperature based on the total heat input, gas volume, and initial specific heat capacity; using the initial theoretical combustion temperature as the theoretical combustion temperature before iteration; determining the iterative specific heat capacity of the gas in the tuyeres' swirl zone based on the gas composition and the iterative specific heat capacity before iteration; and calculating the iterative theoretical combustion temperature based on the total heat input, gas volume, and initial specific heat capacity. The specific heat capacity of the gas in the furnace belly 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 taken 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 gas volume in the furnace belly, the gas composition in the furnace belly, the total heat input, and the theoretical combustion temperature of the gas after iteration until the second convergence condition is met, and the theoretical combustion temperature of the gas is obtained.

[0073] In this embodiment, the formula for calculating the theoretical combustion temperature of coal gas is as follows:

[0074]

[0075] Among them, T f Let V be the theoretical combustion temperature of the gas, Q be the total heat input, and V be the total heat input. G C is the amount of gas in the furnace belly. G This refers to the specific heat capacity of the gas in the furnace belly.

[0076] Based on this, the iterative solution process for the theoretical combustion temperature of coal gas can be as follows:

[0077] 1. Set a temperature value as the preset theoretical combustion temperature of coal gas. Determine the specific heat capacity of each substance in the furnace gas at the preset theoretical combustion temperature 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 the furnace gas based on the specific heat capacity of each substance in the furnace gas at the preset theoretical combustion temperature and the proportion of each substance in the furnace gas composition. Substitute the total heat input, the amount of furnace gas, and the initial specific heat capacity of the furnace gas into equation (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.

[0078] 2. Based on the pre-set relationship between the specific heat capacity and temperature of different substances and the theoretical combustion temperature of the gas before iteration, determine the specific heat capacity of each substance in the gas belly at the theoretical combustion temperature of the gas before iteration; based on the specific heat capacity of each substance in the gas belly at the theoretical combustion temperature of the gas before iteration and the proportion of each substance in the gas belly composition, calculate the specific heat capacity of the gas belly after iteration; substitute the total heat input, the amount of gas belly and the specific heat capacity of the gas belly after iteration into equation (8) to calculate the theoretical combustion temperature of the gas after iteration.

[0079] 3. Calculate the difference between the theoretical combustion temperature of the gas before iteration and the theoretical combustion temperature of the gas after iteration, and use it as the iterative temperature difference of the theoretical combustion temperature of the gas. Then compare the iterative temperature difference of the theoretical combustion temperature of the gas with the second preset temperature difference threshold.

[0080] 4. 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, it means that the second convergence condition is met, and the iterative theoretical combustion temperature of the gas is taken as the theoretical combustion temperature of the gas; otherwise, the iterative theoretical combustion temperature of the gas is taken as the new theoretical combustion temperature of the gas before the iteration, and the contents of 2-3 are repeated until the second convergence condition is met, and the iterative theoretical combustion temperature of the gas obtained by the last iteration of the theoretical combustion temperature of the gas is taken as the theoretical combustion temperature of the gas.

[0081] By iteratively solving the theoretical combustion temperature of coal gas, the accuracy of the theoretical combustion temperature of coal gas is improved, which in turn improves the accuracy of the prediction of molten iron temperature.

[0082] Step S130: Determine the direct reduction degree of iron ore based on the parameters of the top gas, slag and iron, the amount of gas in the belly of the furnace, and the composition of the gas in the belly of the furnace.

[0083] In one embodiment of this application, the direct reduction of elements such as Fe, Si, Mn, S, and P in molten iron consumes heat, thus affecting the temperature of the molten iron. Therefore, it is necessary to determine the degree of direct reduction of iron ore, which can be calculated based on the parameters of the top gas, slag and iron parameters, the amount of gas in the furnace belly, and the composition of the furnace belly gas.

[0084] In one embodiment of this application, step S130 includes: determining the amount of carbon monoxide in the furnace belly gas based on the furnace belly gas volume and composition, and determining the total amount of carbon monoxide and carbon dioxide in the furnace top gas based on the furnace top gas volume and composition, so as to determine the total amount of carbon monoxide generated by direct reduction based on the amount of carbon monoxide in the furnace belly gas and the total amount of carbon monoxide and carbon dioxide in the furnace top gas, wherein the furnace top gas parameters include the furnace top gas volume and furnace top gas composition; determining the mass of trace elements and the mass of iron in the molten iron based on the iron composition and iron production, and determining the amount of carbon monoxide generated by the 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 the direct reduction of iron ore based on the total amount of carbon monoxide generated by direct reduction and the amount of carbon monoxide generated by the direct reduction of trace element oxides, wherein the slag-iron parameters include the iron composition and iron production; calculating the degree of direct reduction of iron ore based on the amount of carbon monoxide generated by the direct reduction of iron ore, the mass of iron in the molten iron, and the mass of iron in a preset hot-pressed iron block.

[0085] In this embodiment, the volume of CO in the furnace belly gas (i.e., the amount of CO) is calculated based on the CO proportion and quantity of the furnace belly gas. The volume of CO in the top furnace gas is also calculated based on the CO proportion and quantity of the top furnace gas. Furthermore, the volume of CO2 in the top furnace gas is calculated based on the CO2 proportion and quantity of the top furnace gas. The sum of the CO and CO2 volumes in the top furnace gas is the total amount of CO and CO2 in the top furnace gas. The difference between the total amount of CO and CO2 in the top furnace gas and the amount of CO in the furnace belly gas is used as the total amount of CO directly generated by reduction. The calculation method is as follows:

[0086] V1 = V CO+CO2 -V COb Equation (9)

[0087] Where V1 is the total amount of CO generated by direct reduction, V CO+CO2 V represents the total amount of CO and CO2 in the top gas of the furnace. COb This represents the CO content in the furnace gas.

[0088] It should be understood that in the direct reduction reaction process, iron ore undergoes a direct reduction reaction to produce Fe reduction products, while trace element oxides undergo direct reduction reactions to produce trace element reduction products. The trace elements in the molten iron include Si, Mn, P, Ti, and S, and correspondingly, the trace element oxides include oxides of Si, Mn, P, Ti, and S, while the trace element reduction products include reduction products of Si, Mn, P, Ti, and S. Therefore, the mass of trace elements in the molten iron, such as the proportions of Si, Mn, P, Ti, and S, and the molten iron yield, can be determined based on the proportions of these trace elements. Specifically, the amount of CO produced by the direct reduction of Si, Mn, P, Ti, and S oxides can be calculated based on the mass of these trace elements in the molten iron. The calculation method is as follows:

[0089]

[0090] Where V2 is the amount of CO generated by the direct reduction of oxides of trace elements such as Si, Mn, P, Ti, and S, and m [Si] Let m be the mass of Si in the molten iron. [Mn] Let m be the mass of Mn in the molten iron. [P] Let m be the mass of P in the molten iron. [Ti] Let m be the mass of Ti in the molten iron. [S] Let S be the mass of sulfur in the molten iron.

[0091] The difference between the total CO generated by direct reduction and the CO generated by the direct reduction of trace element oxides is calculated as the CO generated by the direct reduction of iron ore. The calculation method is as follows:

[0092] V3 = V1 - V2 Equation (11)

[0093] Wherein, V3 is the amount of CO generated by the 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 the direct reduction of trace element oxides.

[0094] 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 production. The degree of direct reduction of iron ore is calculated based on the amount of CO generated from the direct reduction of iron ore, the mass of iron in the molten iron, and the mass of iron in the pre-designed hot-pressed iron block. The calculation method is as follows:

[0095]

[0096] Among them, R d V3 represents the degree of direct reduction of iron ore, and m represents the amount of CO generated by the direct reduction of iron ore. [Fe] Let m be the mass of iron in the molten iron. lThe iron content of the hot-pressed iron blocks used in the blast furnace is the mass of iron in the pre-set hot-pressed iron blocks.

[0097] This embodiment takes into account the reducing properties 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 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.

[0098] Step S140: Determine the gas-liquid heat transfer coefficient based on the theoretical combustion temperature of the gas, the amount of gas in the furnace belly, the composition of the gas in the furnace belly, the slag and iron parameters, and the composition of the gas after direct reduction at the direct reduction location.

[0099] In one embodiment of this application, since there is heat exchange between molten iron and gas, the accuracy of molten iron temperature prediction is also related to the gas-liquid heat transfer coefficient. The gas-liquid heat transfer coefficient can be calculated based on the theoretical combustion temperature of the gas, the amount of gas in the furnace belly, the composition of the gas in the furnace belly, the slag-iron parameters, and the composition of the gas after direct reduction at the direct reduction location. Since the amount of gas after direct reduction is equal to the amount of gas at the furnace top, the volume of CO in the gas after direct reduction is equal to the sum of the volumes of CO and CO2 in the furnace top gas, the volume of H2 in the gas after direct reduction is equal to the sum of the volumes of H2 and H2O in the furnace top gas or the volume of H2 in the furnace belly gas, and the volume of N2 in the gas after direct reduction is equal to the volume of N2 in the furnace top gas or the volume of N2 in the furnace belly gas, the composition of the gas after direct reduction can be determined based on the furnace top gas parameters, or based on the furnace top gas parameters, the amount of gas in the furnace belly, and the composition of the gas in the furnace belly.

[0100] In one embodiment of this application, before determining the gas-liquid heat transfer coefficient, the method includes: determining the total amount of carbon monoxide and carbon dioxide, the total amount of water and hydrogen, and the amount of nitrogen in the top gas based on the top gas quantity and composition, wherein the top gas parameters include the top gas quantity and composition; using the top gas quantity as the quantity of gas after direct reduction, the total amount of carbon monoxide and carbon dioxide in the top gas as the amount of carbon monoxide in the directly reduced gas, the total amount of water and hydrogen in the top gas as the amount of hydrogen in the directly reduced gas, and the amount of nitrogen in the top gas as the amount of nitrogen in the directly reduced gas; and determining the composition of the directly reduced gas based on the directly reduced gas quantity, the amount of carbon monoxide, the amount of hydrogen, and the amount of nitrogen.

[0101] In this embodiment, the composition of the directly reduced gas can be accurately determined by the relationship between the top gas and the gas after direct reduction.

[0102] First, the volume of H2 in the top gas can be calculated based on the proportion of H2 and the amount of top gas. The volume of H2O in the top gas can also be calculated based on the proportion of H2O and the amount of top gas. The sum of these two volumes represents the total amount of H2O and H2 in the top gas. Similarly, the volume of CO in the top gas can be calculated based on the proportion of CO and the amount of top gas. The volume of CO2 in the top gas can also be calculated based on the proportion of CO and the amount of top gas. The sum of these two volumes represents the total amount of CO and CO2 in the top gas. Finally, the volume of N2 in the top gas can be calculated based on the proportion of N2 and the amount of top gas, which represents the amount of N2 in the top gas.

[0103] Then, the amount of gas at the top of the furnace is taken as the amount of gas after direct reduction, the total amount of CO and CO2 in the gas at the top of the furnace is taken as the amount of CO in the gas after direct reduction, the total amount of H2O and H2 in the gas at the top of the furnace is taken as the amount of H2 in the gas after direct reduction, and the amount of N2 in the gas at the top of the furnace is taken as the amount of N2 in the gas after direct reduction.

[0104] Finally, the proportion of H2 in the directly reduced coal gas is determined based on the amount of H2 and the amount of directly reduced coal gas. The proportion of CO in the directly reduced coal gas is determined based on the amount of CO and the amount of directly reduced coal gas. The proportion of N2 in the directly reduced coal gas is determined based on the amount of N2 and the amount of directly reduced coal gas. The proportions of H2, CO, and N2 in the directly reduced coal gas are then used as the components of the directly reduced coal gas.

[0105] In another embodiment of this application, 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 composition, wherein the top gas parameters include the top gas volume and composition; determining the amount of hydrogen and nitrogen in the belly gas based on the belly gas volume and composition; using the top gas volume as the direct reduction gas volume, the total amount of carbon monoxide and carbon dioxide in the top gas as the carbon monoxide content in the direct reduction gas, the amount of hydrogen in the belly gas as the hydrogen content in the direct reduction gas, and the amount of nitrogen in the belly gas as the nitrogen content in the direct reduction gas; and determining the direct reduction gas composition based on the direct reduction gas volume, the carbon monoxide content, the hydrogen content, and the nitrogen content.

[0106] In this embodiment, the composition of the directly reduced gas can be accurately determined by the relationship between the top gas, the belly gas, and the gas after direct reduction.

[0107] First, calculate the CO volume in the top gas based on the CO proportion and the amount of top gas. Then, calculate the CO2 volume in the top gas based on the CO2 proportion and the amount of top gas. The sum of the CO and CO2 volumes in the top gas is the total amount of CO and CO2 in the top gas. Next, determine the H2 volume in the belly gas based on the H2 proportion and the amount of belly gas. Finally, determine the N2 volume in the belly gas based on the N2 proportion and the amount of belly gas.

[0108] Then, the amount of gas at the top of the furnace is taken as the amount of gas after direct reduction, the total amount of CO and CO2 in the gas at the top of the furnace is taken as the amount of CO in the gas after direct reduction, the amount of H2 in the gas at the bottom of the furnace is taken as the amount of H2 in the gas after direct reduction, and the amount of N2 in the gas at the bottom of the furnace is taken as the amount of N2 in the gas after direct reduction.

[0109] Finally, the proportion of H2 in the directly reduced coal gas is determined based on the amount of H2 and the amount of directly reduced coal gas. The proportion of CO in the directly reduced coal gas is determined based on the amount of CO and the amount of directly reduced coal gas. The proportion of N2 in the directly reduced coal gas is determined based on the amount of N2 and the amount of directly reduced coal gas. The proportions of H2, CO, and N2 in the directly reduced coal gas are then used as the components of the directly reduced coal gas.

[0110] In one embodiment of this application, step S140 includes: interpolating the composition of the furnace gas and the composition of the gas after direct reduction to obtain the gas composition of the drip zone; determining the gas-liquid heat transfer coefficient of the tuyer zone based on the equivalent particle size of slag and iron, the thermal conductivity of the gas in the tuyer zone, and the Nusselt number of the tuyer zone, wherein the thermal conductivity of the gas in the tuyer zone and the Nusselt number of the tuyer zone are both determined based on the composition of the furnace gas and the theoretical combustion temperature of the gas, and the equivalent particle size of slag and iron is determined based on slag and iron parameters; and based on the equivalent particle size of slag and iron, the gas composition of the tuyer zone, the gas composition of the drip ... The gas-liquid heat transfer coefficient at the direct reduction position is determined by the thermal conductivity of the gas at the reduction position and the Nusselt number at the direct reduction position. Both the thermal conductivity of the gas at the direct reduction position and the Nusselt number at the direct reduction position are determined based on the gas composition and theoretical combustion temperature of the gas after direct reduction. The gas-liquid heat transfer coefficient at the dripping zone is determined by the equivalent particle size of slag and iron, the thermal conductivity of the gas at the dripping zone, and the Nusselt number at the dripping zone. Both the thermal conductivity of the gas at the dripping zone and the Nusselt number at the dripping zone are determined based on the gas composition and theoretical combustion temperature of the gas at the dripping zone.

[0111] In this embodiment, the dripping zone is the area between the tuyere swirling zone and the direct reduction position. Since the gas composition is different at different heights of the dripping zone from the direct reduction position to the tuyere swirling zone, and the gas-liquid heat transfer coefficients of different gas compositions are also different, it is necessary to determine the gas-liquid heat transfer coefficients at different heights of the dripping zone in order to improve the accuracy of molten iron temperature prediction.

[0112] Schematic, the gas-liquid heat transfer coefficient can be determined by a correction factor, the thermal conductivity of the gas, the equivalent particle size of the slag and iron, and the Nusselt number. The calculation method for the gas-liquid heat transfer coefficient is as follows:

[0113] h g-l =γ·k g Nu / d l Equation (13)

[0114] Among them, h g-l γ is the gas-liquid heat transfer coefficient, γ is the correction factor, and k is the liquid-gas heat transfer coefficient. g Where is the thermal conductivity of the gas, Nu is the Nusselt number, and d is the thermal conductivity of the gas. l The equivalent particle size of slag and iron.

[0115] The Nusselt number is calculated as follows:

[0116] Nu = 2.0 + 0.6(9Re) p ) 1 / 2 Pr 1 / 3 Equation (14)

[0117] Where Nu is the Nusselt number, Re p Let be the Reichsau number and Pr be the Prandtl number.

[0118] The Reich number is calculated as follows:

[0119] Re p =ρ g d l u g / μ g Equation (15)

[0120] Among them, Re p Let ρ be the Reynolds number. g Let d be the density of the gas. l u is the equivalent particle size of slag and iron. g Let μ be the gas flow rate. g This refers to the viscosity of the gas.

[0121] Prandtl numbers are calculated as follows:

[0122] Pr = u g C g / k g Equation (16)

[0123] Where Pr is the Prandtl number, u g C is the gas flow rate. g k is the specific heat capacity of coal gas. g The thermal conductivity of the gas is denoted as .

[0124] It should be noted that the thermal conductivity, density, viscosity, and specific heat capacity of coal gas are all related to the composition and temperature of the coal gas. The relationship between the thermal conductivity and the composition of the coal gas is as follows:

[0125] k g =m CO1 k CO +m H21 k H2 +m N21 k N2 Equation (17)

[0126] Where, k g The thermal conductivity of the gas is m. CO1 The proportion of CO in the coal gas, m H21 The proportion of H2 in the gas, m N21 k represents the proportion of N2 in the gas. CO k is the thermal conductivity of CO. H2 Let k be the thermal conductivity of H2. N2 The thermal conductivity of N2 is given.

[0127] The relationship between gas density and gas composition is as follows:

[0128] ρ g =m CO1 ρ CO +m H21 ρ H2 +m N21 ρ N2 Equation (18)

[0129] Where, ρ g For the density of coal gas, m CO1 The proportion of CO in the coal gas, m H21 The proportion of H2 in the gas, m N21 The proportion of N2 in the gas, ρ CO ρ is the density of CO. H2 For the density of H2, ρ N2 The density is N2.

[0130] The relationship between gas viscosity and gas composition is as follows:

[0131] μ g =m CO1 μ CO +m H21 μ H2 +m N21 μN2 Equation (19)

[0132] Where, μ g For the viscosity of the gas, m CO1 The proportion of CO in the coal gas, m H21 The proportion of H2 in the gas, m N21 The proportion of N2 in the gas, μ CO For CO viscosity, μ H2 For H2 viscosity, μ N2 The viscosity is N2.

[0133] The relationship between the specific heat capacity of coal gas and its composition is as follows:

[0134] C g =m CO1 C CO +m H21 C H2 +m N21 C N2 Equation (20)

[0135] Among them, C g For the specific heat capacity of coal gas, m CO1 The proportion of CO in the coal gas, m H21 The proportion of H2 in the gas, m N21 The proportion of N2 in the gas, C CO For CO specific heat capacity, C H2 For H2 specific heat capacity, C N2 This is the specific heat capacity of N2.

[0136] As an illustration, the process for determining the gas-liquid heat transfer coefficient in the vortex zone can be as follows:

[0137] Based on the theoretical combustion temperature of the gas and the pre-set correspondence between the specific heat capacity of each substance and temperature, determine the specific heat capacity of CO, H2, and N2. Substitute the specific heat capacities of CO, H2, and N2, as well as the proportions of CO, H2, and N2 in the gas composition of the furnace belly, into equation (20) to obtain the specific heat capacity of the gas in the tuyeres swirl zone. Based on the theoretical combustion temperature of the gas and the pre-set correspondence between the viscosity of each substance and temperature, determine the viscosity of CO, H2, and N2. Substitute the viscosity of CO, H2, and N2, as well as the proportions of CO, H2, and N2 in the gas composition of the furnace belly, into equation (19) to obtain the viscosity of the gas in the tuyeres swirl zone. Based on the gas... The density of CO, H2, and N2 is determined by the theoretical combustion temperature and the pre-set correspondence between the density of each substance and temperature. The density of CO, H2, and N2, as well as the proportions of CO, H2, and N2 in the gas composition of the furnace belly, are substituted into equation (18) to obtain the gas density in the tuyeres swirling zone. The thermal conductivity of CO, H2, and N2 is determined by the theoretical combustion temperature of the gas and the pre-set correspondence between the thermal conductivity of each substance and temperature. The thermal conductivity of CO, H2, and N2, as well as the proportions of CO, H2, and N2 in the gas composition of the furnace belly, are substituted into equation (17) to obtain the gas thermal conductivity in the tuyeres swirling zone. Substituting the thermal conductivity and specific heat capacity of the gas in the tuyeres into equation (16), the Prandtl number of the tuyeres is obtained. Substituting the gas density and viscosity of the tuyeres into equation (15), the Reilly number of the tuyeres is obtained. The gas flow rate is obtained by dividing the gas volume by the cross-sectional area of ​​the blast furnace at the calculated location. The cross-sectional area is determined by the blast furnace structure. The equivalent particle size of slag and iron is determined based on the molten iron density, liquid slag density, blast furnace structure, and slag quantity in the slag and iron parameters. Substituting the Prandtl number and Reilly number of the tuyeres into equation (14), the Nusselt number of the tuyeres is obtained. Substituting the thermal conductivity and Nusselt number of the gas in the tuyeres into equation (13), the gas-liquid heat transfer coefficient of the tuyeres is obtained. The correction coefficient can be preset and can be any value between 0.2 and 0.5, or other values. No restrictions are imposed here.

[0138] Accordingly, following the above method, the gas-liquid heat transfer coefficient at the direct reduction location is calculated based on the theoretical combustion temperature of the coal gas, slag and iron parameters, and the composition of the coal gas after direct reduction. This will not be elaborated further here.

[0139] Interpolation calculations were performed on the composition of the furnace belly gas and the gas composition after direct reduction to obtain the gas composition of the dripping zone. The gas composition of the dripping zone includes the gas composition at different heights within the dripping zone. Similarly, following the above method, based on the theoretical combustion temperature of the gas, slag-iron parameters, and the gas composition at different heights within the dripping zone, the gas-liquid heat transfer coefficients at different heights within the dripping zone were calculated, which will not be elaborated further here. Determining the gas-liquid heat transfer coefficients at different heights within the dripping zone further improves the accuracy of hot metal temperature prediction.

[0140] Step S150: Based on the gas-liquid heat transfer coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of coal gas, and the slag-iron parameters, iteratively solve for the molten iron temperature and the coal gas temperature until the first convergence condition is met, thus completing the prediction of the molten iron temperature in blast furnace smelting.

[0141] In one embodiment of this application, a preset temperature value can be established for the molten iron temperature at the direct reduction blast furnace location, serving as the preset molten iron temperature after direct reduction. Based on the gas-liquid heat transfer coefficient, the degree of direct reduction of iron ore, the theoretical combustion temperature of the gas, the preset molten iron temperature after direct reduction, and slag-iron parameters, and using the energy conservation relationships of the gas phase and the molten iron phase, the molten iron temperature and gas temperature are iteratively solved until a first convergence condition is met, thus obtaining the gas temperature at the direct reduction location and the molten iron temperature in the tuyeres vortex zone. Illustratively, the first convergence condition may be that the number of iterations for solving the molten iron temperature and gas temperature meets a first preset number of iterations, or that the iterative temperature difference of both the gas temperature and the molten iron temperature is less than or equal to a first preset temperature difference threshold, or other convergence conditions, which are not limited here.

[0142] In one embodiment of this application, step S150 includes: determining the heat consumption for direct reduction based on the composition of molten iron and the degree of direct reduction of iron ore, wherein the slag-iron parameters include the composition of molten iron; based on the gas phase temperature, molten iron phase temperature, gas-liquid heat transfer coefficient, and heat consumption for direct reduction, and according to the energy conservation relationship of the gas phase and the energy conservation relationship of the molten iron phase, iteratively solving for the molten iron temperature and gas temperature, obtaining the molten iron temperature in the tuyeres before iteration, the molten iron temperature in the tuyeres after iteration, the gas temperature after direct reduction before iteration, and the gas temperature after direct reduction after iteration, wherein the initial value of the gas phase temperature is the coal... The initial value of the theoretical combustion temperature of the gas phase and the molten iron phase temperature is the preset molten iron temperature after direct reduction. The difference between the molten iron temperature in the tuyeres before and after iteration is determined as the molten iron temperature iteration difference, and the difference between the gas temperature after direct reduction before and after iteration is determined as the gas temperature iteration difference. If both the molten iron temperature iteration difference and the gas temperature iteration difference are less than or equal to the first preset temperature difference threshold, the first convergence condition is met, and the molten iron temperature in the tuyeres after iteration is taken as the final prediction result of the molten iron temperature prediction.

[0143] 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 start of iron slag melting to the surface of the furnace hearth molten pool, and the iron slag melting temperature is located between 1300 and 1400°C.

[0144] Therefore, the energy conservation relationships of the gas phase and the molten iron phase can be used, and the temperatures of the molten iron and gas phases can be iteratively solved based on the gas phase temperature, the molten iron phase temperature, the gas-liquid heat transfer coefficient, and the direct reduction heat consumption. The expression for the energy conservation relationship of the gas phase is as follows:

[0145]

[0146] Where, ρ g For the density of coal gas, u g C is the gas flow rate. g T represents the specific heat capacity of coal gas. g Let z be the temperature of the gas phase, z be the solution mesh length, and h be the temperature of the gas phase. g-l Where A is the gas-liquid heat transfer coefficient, A is the specific surface area, and T is the gas-liquid heat transfer l Q is the temperature of the molten iron phase. Rd To directly reduce the heat loss, V a To solve for the volume of the region.

[0147] The expression for the energy conservation relationship of molten iron is as follows:

[0148]

[0149] Where, ρ l U is the density of molten iron. l C represents the flow rate of molten iron. l T represents the specific heat capacity of molten iron. l T is the temperature of the molten iron phase. g Let z be the temperature of the gas phase, z be the solution mesh length, and h be the temperature of the gas phase. g-l Let be the gas-liquid heat transfer coefficient, and A be the specific surface area.

[0150] It should be noted that the methods for determining the gas density and specific heat capacity of the gas described in the foregoing embodiments will not be repeated here. 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 according to the blast furnace structure; the direct reduction heat consumption can be determined based on the direct reduction degree of iron ore and the iron composition in the slag and iron parameters.

[0151] Please refer to Table 2, which is a table of direct reduction chemical reactions and thermal effects in a specific embodiment of this 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 elements such as Fe, Si, Mn, P, Ti, and S.

[0152] Table 2

[0153] serial number Reaction thermal effect 1 FeO + C = Fe + CO <![CDATA[ΔH Fe ]]> 2 <![CDATA[SiO2+2C=Si+2CO]]> <![CDATA[ΔH si ]]> 3 MnO + C = Mn + CO <![CDATA[ΔH Mn ]]> 4 <![CDATA[P2O5+5C=2P+5CO]]> <![CDATA[ΔH P ]]> 5 <![CDATA[TiO2+2C=Ti+2CO]]> <![CDATA[ΔH Ti ]]> 6 FeS + CaO + C = Fe + CaS + CO <![CDATA[ΔH S ]]>

[0154] Based on this, the calculation method for direct reduction of heat consumption is as follows:

[0155]

[0156] Among them, Q Rd To directly reduce the heat consumption, ΔH Fe The heat of reaction for the direct reduction of Fe, R d m represents the direct reduction degree of iron ore. [Fe] M represents the mass of iron in molten iron. 矿 For the ore ratio, ω Fe ω represents the mass fraction of Fe in the mixed ore. FeS ΔH represents the mass fraction of FeS (ferrous sulfide) in the mixed ore. Si The heat of reaction for the direct reduction of Si, m [Si] Let ΔH be the mass of Si in the molten iron. Mn The heat of reaction for the direct reduction of Mn, m [Mn] Let ΔH be the mass of Mn in the molten iron. P The heat of reaction for the direct reduction of P element, m [P] Let P be the mass of molten iron, and ΔH be the mass of molten iron. Ti The heat of reaction for the direct reduction of Ti, m [Ti] Let ΔH be the mass of Ti in the molten iron. S The heat of reaction for the direct reduction of sulfur, m [S] The mass of sulfur (S) in the molten iron is given. The ore ratio, the mass fraction of Fe, and the mass fraction of FeS can be preset.

[0157] Indicatively, the dripping zone is divided into grids 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 direct reduction temperature of the molten iron is used as the initial value of the molten iron phase temperature. Equations (21) and (22) are used to iterate and solve the problem to obtain the solution results, including the gas temperature before iteration, the molten iron temperature in the tuyeres before iteration, the gas temperature after iteration, and the molten iron temperature in the tuyeres after iteration. If the difference between the gas temperature before iteration and the gas temperature after iteration is the gas temperature iteration difference, and the difference between the molten iron temperature in the tuyeres before iteration and the molten iron temperature in the tuyeres after iteration is the molten iron temperature iteration difference, both are 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 tuyeres after iteration is taken as the final prediction result of the molten iron temperature prediction. Conversely, equations (21) and (22) are used again for iterative solution until the second convergence condition is met. The final temperature of the molten iron in the tuyeres after iteration is taken as the final prediction result of the molten iron temperature prediction. For illustration, the preset molten iron temperature after direct reduction can be 1350℃, or any temperature value between 1300℃ and 1500℃, or other temperature values; no restrictions are imposed here. The second preset temperature difference threshold can be 0.01℃, or any temperature value between 0.01℃ and 0.05℃, or other temperature values; no restrictions are imposed here either.

[0158] By utilizing the energy conservation relationships of the gas phase and the molten iron phase, the molten iron temperature and gas temperature are iteratively solved using the theoretical combustion temperature of the gas, the direct reduction degree of iron ore, and the gas-liquid heat transfer coefficient at different heights. The convergence is then performed based on the errors before and after the iteration, further improving the accuracy of molten iron temperature prediction.

[0159] In one specific embodiment of this application, a 2300m... 3 Taking the blast furnace as an example, the utilization coefficient is 3.7t / (d·m). 3 (This section provides further details regarding the scheme outlined in this application.)

[0160] The predicted temperature of molten iron in a conventional blast furnace without pulverized gas is as follows:

[0161] Please refer to Table 3, which is a raw material parameter table in a specific embodiment of this application. As shown in Table 3, the raw material parameters may include the coke composition and coke dosage, and the pulverized coal composition and dosage. The coke composition may include the proportions of C, H, O, N, S, volatile matter, and ash in the coke. The pulverized coal composition may include the proportions of C, H, O, N, S, volatile matter, and ash in the pulverized coal.

[0162] Table 3

[0163] name C H O N S Volatile matter Ash Dosage unit ％ ％ ％ ％ ％ ％ ％ kg / t coke 86.50 3.43 2.52 1.70 1.14 1.07 12.40 337.69 Pulverized coal injection 79.32 3.70 4.92 1.29 0.29 13.33 10.19 154.31

[0164] Please refer to Table 4, which is a table of blower parameters in a specific embodiment of this application. As shown in Table 4, the blower parameters may include blower volume, blower temperature, blower humidity, and oxygen enrichment rate.

[0165] Table 4

[0166] name blower volume blower temperature Blower humidity oxygen enrichment rate unit <![CDATA[Nm 3 / min]]> ℃ <![CDATA[g / m 3 ]]> ％ numerical values 5300.20 1220 15.52 8.26

[0167] Please refer to Table 5, which is a table of top gas parameters in a specific embodiment of this application. As shown in Table 5, the top gas parameters may include the amount of top gas and the proportions of CO, CO2, H2, and N2 in the top gas.

[0168] Table 5

[0169] name <![CDATA[H2]]> CO <![CDATA[CO2]]> <![CDATA[CH4]]> <![CDATA[N2]]> <![CDATA[O2]]> Blowing volume unit ％ ％ ％ ％ ％ ％ <![CDATA[m 3 / h]]> numerical values 32.68 34.23 0.94 11.04 20.94 0.17 15000

[0170] Please refer to Table 6, which is a slag-iron parameter table in a specific embodiment of this application. As shown in Table 6, the slag-iron parameters may include the slag quantity and the proportions of Fe, C, Si, Mn, P, S, and Ti in the molten iron.

[0171] Table 6

[0172] name [Fe] [C] [Si] [Mn] [P] [S] [Ti] Slag volume unit ％ ％ ％ ％ ％ ％ ％ kg / t numerical values 94.50 4.20 0.36 0.28 0.14 0.04 0.04 330

[0173] Based on Table 4, the calculated sensible heat Q1 brought into the blast furnace by the blast is 2.00 GJ / t, and the oxygen content available for pulverized coal and coke combustion in the blast furnace tuyeres is 239.20 m³. 3 The total heat Q2 released by the combustion of pulverized coal and coke or other reactions in the tuyere swirl zone is calculated to be 2.41 GJ / t. The coke temperature entering the combustion zone is approximately 1400℃, and the amount of coke burned at the tuyere is 173.46 kg / t. The sensible heat Q4 brought into the tuyere swirl zone by the coke is 0.29 GJ / t. Therefore, the total heat input Q in the tuyere swirl zone is 4.70 GJ / t. Based on Tables 3 and 4, and using the law of conservation of mass in the tuyere swirl zone, the contents of CO, H2, and N2 in the furnace belly gas are found to be 41.67%, 6.95%, and 51.38%, respectively, and the furnace belly gas volume is 1193.88 m³. 3 / t. Therefore, the theoretical combustion temperature of the gas is calculated to be 2252℃.

[0174] Based on Tables 5 and 6, the direct reduceability Rd of iron ore is 0.451. After direct reduction, the CO, H2, and N2 contents in the gas are 48.92%, 6.09%, and 44.99%, respectively. Based on Table 6, the theoretical combustion temperature, and the amount of gas in the furnace belly, the Reynolds number Re in the hearth is calculated. pThe Prandtl number (Pr) is 30883, the Nusselt number (Nu) is 0.362, and the Nusselt number (Nu) is 227.54. Therefore, the gas-liquid heat transfer coefficient h between the gas and the slag-iron droplets is... g-l It is 26.89 W / (m 2 .K). Through iterative calculation based on energy conservation, the molten iron temperature, i.e. the molten iron temperature in the tuyeres, was obtained as 1521.20℃, which is close to the average molten iron temperature of the blast furnace under the corresponding operating conditions, which is 1520℃. After direct reduction, the gas temperature was 1897.20℃.

[0175] Because gas injection is implemented during blast furnace smelting, and this injection process causes changes in blast and furnace top parameters, the predicted blast furnace hot metal temperature under gas injection conditions is as follows:

[0176] Please refer to Table 7, which is a table of gas injection parameters in a specific embodiment of this application. As shown in Table 7, the gas injection parameters may include the gas injection rate and the proportions of H2, CO, CO2, CH4, nitrogen, and O2 in the injected gas.

[0177] Table 7

[0178] name <![CDATA[H2]]> CO <![CDATA[CO2]]> <![CDATA[CH4]]> <![CDATA[N2]]> <![CDATA[O2]]> Blowing volume unit ％ ％ ％ ％ ％ ％ <![CDATA[m 3 / h]]> numerical values 32.68 34.23 0.94 11.04 20.94 0.17 15000

[0179] Please refer to Table 8, which is a table of blower parameters under gas injection conditions in a specific embodiment of this application. As shown in Table 8, the blower volume, blower humidity, and oxygen enrichment rate in the blower parameters under gas injection conditions are different from the corresponding values ​​in Table 4.

[0180] Table 8

[0181] name blower volume blower temperature Blower humidity oxygen enrichment rate unit <![CDATA[Nm 3 / min]]> ℃ <![CDATA[g / m 3 ]]> ％ numerical values 4857.20 1220 14.38 11.06

[0182] Please refer to Table 9, which is a table of furnace top gas parameters under gas injection conditions in a specific embodiment of this application. As shown in Table 9, the furnace top gas composition and furnace top gas quantity in the furnace top gas parameters under gas injection conditions are different from the corresponding values ​​in Table 5.

[0183] Table 9

[0184] name CO CO2 H2 N2 Top gas volume (dry basis) unit ％ ％ ％ ％ Nm3 / t numerical values 28.17 25.16 5.13 41.54 1345.50

[0185] Based on Tables 3, 7, and 8, and using the law of conservation of mass in the tuyere swirl zone, the contents of CO, H2, and N2 in the furnace belly gas were found to be 43.71%, 9.61%, and 46.68%, respectively, and the furnace belly gas volume was 1197.4 m³. 3The theoretical combustion temperature of the gas was calculated to be 2163℃. Based on Tables 9 and 6 and the composition of the furnace gas, the direct reduceability Rd of the iron ore was found to be 0.39. The CO, H2, and N2 contents in the gas after direct reduction were 49.90%, 8.55%, and 41.54%, respectively. The gas-liquid heat transfer coefficient h between the gas and the molten iron droplets was calculated. g-l It is 28.654 W / (m 2 Therefore, through iterative calculation based on energy conservation, the temperature of the molten iron was found to be 1510.61℃, and the temperature of the gas after direct reduction was 1753.63℃.

[0186] Please see Figure 2 , Figure 2 This is a schematic diagram illustrating the structure of a blast furnace ironmaking process water temperature prediction system according to a specific embodiment of this application. Figure 2 As shown, the blast furnace ironmaking process molten iron temperature prediction system 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. The data acquisition subsystem acquires smelting data during the blast furnace smelting process, including raw material parameters, blast parameters, gas injection parameters, furnace top gas parameters, and slag-iron parameters. The physical property database collects and stores the specific heat capacity, density, dynamic viscosity, and thermal conductivity of various gases, as well as the specific heat capacity, density, and thermal conductivity of various solid substances. The tuyere area heat balance calculation subsystem calculates the heat balance state of the tuyere area. The direct reduction calculation subsystem calculates the direct reduction degree of iron ore. The iterative solution subsystem determines the convergence of the molten iron temperature results and obtains the molten iron temperature value.

[0187] Please see Figure 3 , Figure 3 yes Figure 2 The illustrated embodiment shows a schematic diagram of the blast furnace smelting iron temperature prediction system in a specific embodiment, illustrating the blast furnace smelting iron temperature prediction process. (See diagram for details.) Figure 3 As shown, the process for predicting the temperature of molten iron in the blast furnace smelting process includes:

[0188] 1. Real-time acquisition of smelting data during the blast furnace smelting process, including raw material parameters, blast parameters, gas injection parameters, furnace top gas parameters, and slag and iron parameters;

[0189] 2. Based on the raw material parameters, blast parameters, and gas injection parameters, calculate the theoretical combustion temperature of the gas in the tuyeres swirling zone, the gas volume in the furnace belly, and the gas composition in the furnace belly.

[0190] 3. Based on the parameters of the top gas, slag and iron, and the composition of the bottom gas, calculate the degree of direct reduction of iron ore, as well as the composition and quantity of the gas after direct reduction.

[0191] 4. Based on the phase database, theoretical combustion temperature of coal gas, coal gas volume in the furnace belly, and slag and iron parameters, calculate the gas-liquid heat transfer coefficient between coal gas and molten iron and slag.

[0192] 5. Based on the law of conservation of heat, iterative solutions are performed to obtain the temperature of molten iron and the temperature of the gas after direct reduction.

[0193] Figure 3 For detailed procedures, please refer to the descriptions in the aforementioned embodiments; they will not be repeated here. The technical solution of this embodiment uses real-time acquired smelting data from the blast furnace smelting process to determine the theoretical combustion temperature of the gas in the tuyeres, the iron ore reducing power, and the gas-liquid heat transfer coefficient. This data is then used to iteratively solve for the molten iron temperature and gas temperature, enabling prediction of the molten iron temperature during blast furnace smelting. This allows for the acquisition of molten iron temperatures under various operating conditions during the blast furnace smelting process, helping operators assess the thermal state within the blast furnace and information on ore reduction, thus ensuring the stable and smooth operation of both conventional and low-carbon blast furnaces.

[0194] Please see Figure 4 , Figure 4 This is a block diagram illustrating an exemplary embodiment of a blast furnace smelting hot metal temperature prediction device. Figure 4 As shown, the exemplary blast furnace smelting molten iron temperature prediction device includes:

[0195] The smelting data acquisition module 410 is configured to acquire raw material parameters, blast parameters, gas injection parameters, furnace top gas parameters, and slag-iron parameters during the blast furnace smelting process. The theoretical combustion temperature determination module 420 is configured to determine the total heat input, furnace gas volume, and furnace gas composition in the tuyeres based on the raw material parameters, blast parameters, and gas injection parameters, and then determine the theoretical combustion temperature of the gas in the tuyeres based on these parameters. The direct reduction degree determination module 430 is configured to determine the direct reduction degree of iron ore based on the furnace top gas parameters, slag-iron parameters, furnace gas volume, and furnace gas composition. The reduction degree and 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 gas in the furnace belly, the slag and iron parameters, and the composition of the gas after direct reduction at the direct reduction location. The composition of the gas after direct reduction is determined based on the gas parameters at the furnace top, or based on the gas parameters at the furnace top, the gas quantity in the furnace belly, and the composition of the gas in the furnace belly. The iterative solution module 450 is configured to iteratively solve for the molten iron temperature and 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 and iron parameters until the first convergence condition is met, thus completing the prediction of the molten iron temperature in blast furnace smelting.

[0196] It should be noted that the blast furnace smelting molten iron temperature prediction device and the blast furnace smelting molten iron temperature prediction method provided in the above embodiments belong to the same concept. The specific operation methods of each module and unit have been described in detail in the method embodiments and will not be repeated here. In practical applications, the blast furnace smelting molten iron temperature prediction device provided in the above embodiments can be assigned to different functional modules as needed, that is, the internal structure of the device can be divided into different functional modules to complete all or part of the functions described above. This is not a limitation here.

[0197] This embodiment also provides an electronic device, including: one or more processors; and a storage device for storing one or more programs, which, when executed by the one or more processors, enable the electronic device to implement the blast furnace smelting molten iron temperature prediction method provided in the above embodiments.

[0198] Please see Figure 5 , Figure 5 This is a schematic diagram illustrating the structure of an electronic device according to an exemplary embodiment of this application. It should be noted that... Figure 5 The electronic device 500 shown is merely an example and should not impose any limitation on the functionality and scope of use of the embodiments of this application.

[0199] like Figure 5 As shown, 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 a computer program stored in the memory 502 to implement one or more methods as described in the above embodiments.

[0200] This embodiment also provides a computer-readable storage medium storing a computer program thereon. When executed by a computer's processor, the computer program causes the computer to perform the blast furnace smelting molten iron temperature prediction method as described above. This computer-readable storage medium may be included in the electronic device described in the above embodiments, or it may exist independently and not be assembled into the electronic device.

[0201] This embodiment also 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 blast furnace smelting molten iron temperature prediction method provided in the above embodiments.

[0202] 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 between them. The memory is used to store computer programs, the communication interface is used to perform communication, and the processor and the transceiver are used to run the computer programs, so that the electronic device performs the various steps of the above method.

[0203] In this embodiment, the memory may include random access memory (RAM) and may also include non-volatile memory, such as at least one disk storage device.

[0204] The processors mentioned above can be general-purpose processors, including central processing units (CPUs), network processors (NPs), etc.; they can also be digital signal processors (DSPs), application-specific integrated circuits (ASICs), field-programmable gate arrays (FPGAs), or other programmable logic devices, discrete gate or transistor logic devices, or discrete hardware components.

[0205] As will be understood by those skilled in the art, the computer-readable storage medium described in this embodiment allows for the implementation of all or part of the steps in the above method embodiments by computer program-related hardware. The aforementioned computer program can be stored in a computer-readable storage medium. When executed, the program performs the steps of the above method embodiments; and 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.

[0206] The above embodiments are merely illustrative of the principles and effects of this application and are not intended to limit this application. Any person skilled in the art can modify or alter the above embodiments without departing from the spirit and scope of this application. Therefore, all equivalent modifications or alterations made by those skilled in the art without departing from the spirit and technical concept disclosed in this application should still 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 includes: Obtain raw material parameters, blast parameters, gas injection parameters, furnace top gas parameters, and slag and iron parameters for the blast furnace smelting process; Based on the raw material parameters, the blast parameters, and the gas injection parameters, the total heat input, the amount of gas in the furnace belly, and the composition of the gas in the furnace belly are determined, so as to determine the theoretical combustion temperature of the gas in the tuyeres based on the total heat input, the amount of gas in the furnace belly, and the composition of the gas in the furnace belly. Based on the raw material parameters, the blast parameters, and the gas injection parameters, the total heat input, furnace gas volume, and furnace gas composition of the tuyeres' swirl zone are determined. Then, based on the total heat input, the furnace gas volume, and the furnace gas composition, the theoretical combustion temperature of the gas in the tuyeres' swirl zone is determined. This 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 produced by the chemical reaction in the tuyeres' swirl zone based on the raw material parameters, the blast parameters, and the gas injection parameters; calculating the heat released by the chemical reaction in the tuyeres' swirl zone based on the volume of gas participating in the chemical reaction; and determining the char volume of the tuyeres' swirl zone... The total heat input is calculated by considering the sensible heat of coke, the sensible heat of blast, the sensible heat of gas, and the heat released by the chemical reaction. The sensible heat of coke is determined based on the raw material parameters, the sensible heat of blast is determined based on the blast parameters, and the sensible heat of gas is determined based on the gas injection parameters. The volume of gas produced by the chemical reaction and the volume of gas not involved in the chemical reaction are used to calculate the volume and composition of the furnace gas. The theoretical combustion temperature of the gas is iteratively solved based on the volume, composition, and total heat input until the second convergence condition is met, yielding the theoretical combustion temperature of the gas. The formula for calculating the theoretical combustion temperature of the gas is as follows. in, T f The theoretical combustion temperature of the gas is given. Q For the total calorie income, V G The gas volume in the furnace belly is [missing information]. C G The specific heat capacity of the gas in the furnace belly; The direct reduction degree of iron ore is determined based on the parameters of the top gas, the parameters of slag and iron, the amount of gas in the belly of the furnace, and the composition of the gas in the belly of the furnace. The gas-liquid heat transfer coefficient is determined based on the theoretical combustion temperature of the gas, the composition of the gas in the furnace belly, the slag and iron parameters, and the composition of the gas after direct reduction at the direct reduction location; the composition of the gas after direct reduction is determined based on the gas parameters at the furnace top, or the composition of the gas after direct reduction is determined based on the gas parameters at the furnace top, the gas volume in the furnace belly, and the composition of the gas in the furnace belly. Based on the gas-liquid heat transfer coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of coal gas, and the slag-iron parameters, the molten iron temperature and coal gas temperature are iteratively solved until the first convergence condition is met, thus completing the prediction of the molten iron temperature in blast furnace smelting.

2. The method for predicting the temperature of molten iron in blast furnace smelting according to claim 1, characterized in that, Before calculating the total heat input based on the sensible heat of coke, sensible heat of blast air, sensible heat of coal gas, and heat released by the chemical reaction in the tuyeres' swirling zone, the method includes: The specific heat capacity of coke is determined based on the preset coke temperature and coke composition, and the sensible heat of coke is calculated based on the preset coke temperature, the specific heat capacity of coke and the amount of coke used. The raw material parameters include the coke composition and the amount of coke used. The specific heat capacity of the blower is determined based on the blower temperature and blower composition. The sensible heat of the blower is then calculated based on the specific heat capacity, blower volume, and blower temperature. The blower parameters include the blower composition, the blower temperature, and the blower volume. The specific heat capacity of the injected gas is determined based on the preset injected gas temperature and injected gas composition. The sensible heat of the gas is calculated based on the preset injected gas temperature, the specific heat capacity of the injected gas, and the gas injection rate. The gas injection parameters include the injected gas composition and the gas injection rate.

3. The method for predicting the temperature of molten iron in blast furnace smelting according to claim 1, characterized in that, The theoretical combustion temperature of the gas is iteratively solved based on the furnace gas volume, the furnace gas composition, and the total heat input until the second convergence condition is met, thus obtaining the theoretical combustion temperature of the gas, including: The initial specific heat capacity of the tuyeres gas in the tuyeres swirling zone is determined based on the composition of the tuyeres gas and the preset theoretical combustion temperature of the gas. The initial theoretical combustion temperature of the gas is calculated based on the total heat input, the amount of tuyeres gas, and the initial specific heat capacity of the tuyeres gas. The initial theoretical combustion temperature of the gas is used as the theoretical combustion temperature of the gas before iteration. The specific heat capacity of the gas in the tuyeres in the iteration is determined based on the composition of the gas in the furnace belly and the theoretical combustion temperature of the gas before iteration. The theoretical combustion temperature of the gas after iteration is calculated based on the total heat input, the amount of gas in the furnace belly and the specific heat capacity of the gas in the iteration. The difference between the theoretical combustion temperature of the gas before the iteration and the theoretical combustion temperature of the gas after the 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, then the second convergence condition is met, and the iterative theoretical combustion temperature of the gas is taken 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, then the theoretical combustion temperature of the gas is iteratively solved based on the amount of gas in the furnace, the composition of the gas in the furnace, the total heat input, and the iterative theoretical combustion temperature of the gas until the second convergence condition is met, and the theoretical combustion temperature of the gas is obtained.

4. The method for predicting the temperature of molten iron in blast furnace smelting according to any one of claims 1-3, characterized in that, The direct reduction degree of iron ore is determined based on the parameters of the top gas, the parameters of the slag and iron, the amount of gas in the belly of the furnace, and the composition of the gas in the belly of the furnace, including: The amount of carbon monoxide in the furnace belly gas is determined based on the furnace belly gas volume and the furnace belly gas composition, and the total amount of carbon monoxide and carbon dioxide in the furnace top gas is determined based on the furnace top gas volume and the furnace top gas composition. The total amount of carbon monoxide generated by direct reduction is determined based on the amount of carbon monoxide in the furnace belly gas and the total amount of carbon monoxide and carbon dioxide in the furnace top gas. The furnace top gas parameters include the furnace top gas volume and the furnace top gas composition. The mass of trace elements and the mass of iron in the molten iron are determined based on the composition and yield of the molten iron. The amount of carbon monoxide generated by the direct reduction of trace element oxides is then determined based on the mass of the trace elements in the molten iron. Based on the total amount of carbon monoxide generated by direct reduction and the amount of carbon monoxide generated by the direct reduction of trace element oxides, the amount of carbon monoxide generated by the direct reduction of iron ore is determined. The slag-iron parameters include the composition and yield of the molten iron. The trace elements include silicon, manganese, phosphorus, titanium, and sulfur, and the trace element oxides include oxides of silicon, manganese, phosphorus, titanium, and sulfur. The degree of direct reduction of the iron ore is calculated based on the amount of carbon monoxide generated by the direct reduction of the iron ore, the mass of iron in the molten iron, and the mass of iron in the preset hot-pressed iron block.

5. The method for predicting the temperature of molten iron in blast furnace smelting according to any one of claims 1-3, characterized in that, Before determining the gas-liquid heat transfer coefficient, the method includes: The total amount of carbon monoxide and carbon dioxide, the total amount of water and hydrogen, and the amount of nitrogen in the top gas are determined based on the top gas volume and the top gas composition. The top gas parameters include the top gas volume and the top gas composition. The amount of gas at the top of the furnace is taken as the amount of gas after direct reduction. The total amount of carbon monoxide and carbon dioxide in the gas at the top of the furnace is taken as the amount of carbon monoxide in the gas after direct reduction. The total amount of water and hydrogen in the gas at the top of the furnace is taken as the amount of hydrogen in the gas after direct reduction. The amount of nitrogen in the gas at the top of the furnace is taken as the amount of nitrogen in the gas after direct reduction. The composition of the directly reduced coal gas is determined based on the amount of gas produced after direct reduction, the amount of carbon monoxide in the directly reduced coal gas, the amount of hydrogen in the directly reduced coal gas, and the amount of nitrogen in the directly reduced coal gas.

6. The method for predicting the temperature of molten iron in blast furnace smelting according to any one of claims 1-3, characterized in that, Before determining the gas-liquid heat transfer coefficient, the method includes: The total amount of carbon monoxide and carbon dioxide in the top gas is determined based on the top gas volume and top gas composition. The top gas parameters include the top gas volume and top gas composition. The amount of hydrogen and nitrogen in the furnace gas are determined based on the furnace gas volume and the furnace gas composition. The amount of gas at the top of the furnace is taken as the amount of gas after direct reduction. The total amount of carbon monoxide and carbon dioxide in the gas at the top of the furnace is taken as the amount of carbon monoxide in the gas after direct reduction. The amount of hydrogen in the gas at the bottom of the furnace is taken as the amount of hydrogen in the gas after direct reduction. The amount of nitrogen in the gas at the bottom of the furnace is taken as the amount of nitrogen in the gas after direct reduction. The composition of the directly reduced coal gas is determined based on the amount of gas produced after direct reduction, the amount of carbon monoxide in the directly reduced coal gas, the amount of hydrogen in the directly reduced coal gas, and the amount of nitrogen in the directly reduced coal gas.

7. The method for predicting the temperature of molten iron in blast furnace smelting according to any one of claims 1-3, characterized in that, The gas-liquid heat transfer coefficient is determined based on the theoretical combustion temperature of the gas, the composition of the gas in the furnace belly, the slag and iron parameters, and the composition of the gas after direct reduction at the direct reduction location, including: The gas composition in the drip zone is obtained by interpolating the composition of the furnace gas and the composition of the gas after direct reduction. The gas-liquid heat transfer coefficient of the tuyere swirling zone is determined based on the equivalent particle size of slag and iron, the thermal conductivity of the gas in the tuyere swirling zone, and the Nusselt number of the tuyere swirling zone. The thermal conductivity of the gas in the tuyere swirling zone and the Nusselt number of the tuyere swirling zone are both determined based on the composition of the furnace gas and the theoretical combustion temperature of the gas. The equivalent particle size of slag and iron is determined based on the slag and iron parameters. The gas-liquid heat transfer coefficient at the direct reduction position is determined based on the equivalent particle size of the slag and iron, the thermal conductivity of the gas at the direct reduction position, and the Nusselt number at the direct reduction position. Both the thermal conductivity of the gas at the direct reduction position and the Nusselt number at the direct reduction position are determined based on the composition of the gas after direct reduction and the theoretical combustion temperature of the gas. The gas-liquid heat transfer coefficient of the dripping zone is determined based on the equivalent particle size of the slag and iron, the thermal conductivity of the gas in the dripping zone, and the Nusselt number of the dripping zone. Both the thermal conductivity of the gas in the dripping zone and the Nusselt number of the dripping zone are determined based on the gas composition of the dripping zone and the theoretical combustion temperature of the gas.

8. The method for predicting the temperature of molten iron in blast furnace smelting according to claim 7, characterized in that, Based on the gas-liquid heat transfer coefficient, the direct reduceability of the iron ore, the theoretical combustion temperature of the coal gas, and the slag-iron parameters, the molten iron temperature and coal gas temperature are iteratively solved until the first convergence condition is met, thus completing the prediction of the molten iron temperature, including: The heat consumption for direct reduction is determined based on the composition of the molten iron and the direct reduceability of the iron ore, and the slag-iron parameters include the composition of the molten iron. Based on the gas phase temperature, molten iron phase temperature, the gas-liquid heat transfer coefficient, and the direct reduction heat consumption, and according to the energy conservation relationship of the gas phase and the energy conservation relationship of the molten iron phase, the molten iron temperature and gas temperature are iteratively solved to obtain the molten iron temperature in the tuyeres before iteration, the molten iron temperature in the tuyeres after iteration, the gas temperature after direct reduction before iteration, 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. The difference between the molten iron temperature in the tuyeres before the iteration and the molten iron temperature in the tuyeres after the iteration is determined as the molten iron temperature iteration difference, and the difference between the gas temperature after direct reduction before the iteration and the gas temperature after direct reduction after the iteration is determined as the gas temperature iteration difference. If both the iterative temperature difference of the molten iron temperature and the iterative temperature difference of the gas temperature are 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 tuyeres after iteration is taken as the final prediction result of the molten iron temperature prediction.

9. A device for predicting the temperature of molten iron in a blast furnace, characterized in that, The device includes: The smelting data acquisition module is used to acquire raw material parameters, blast parameters, gas injection parameters, furnace top gas parameters, and slag and iron parameters during the blast furnace smelting process. The theoretical combustion temperature determination module is used to determine the total heat input, furnace gas volume and furnace gas composition in the tuyeres swirl zone based on the raw material parameters, the blower parameters and the gas injection parameters, so as to determine the theoretical combustion temperature of the gas in the tuyeres swirl zone based on the total heat input, furnace gas volume and furnace gas composition. Based on the raw material parameters, the blast parameters, and the gas injection parameters, the total heat input, furnace gas volume, and furnace gas composition of the tuyeres' swirl zone are determined. Then, based on the total heat input, the furnace gas volume, and the furnace gas composition, the theoretical combustion temperature of the gas in the tuyeres' swirl zone is determined. This 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 produced by the chemical reaction in the tuyeres' swirl zone based on the raw material parameters, the blast parameters, and the gas injection parameters; calculating the heat released by the chemical reaction in the tuyeres' swirl zone based on the volume of gas participating in the chemical reaction; and determining the char volume of the tuyeres' swirl zone... The total heat input is calculated by considering the sensible heat of coke, the sensible heat of blast, the sensible heat of gas, and the heat released by the chemical reaction. The sensible heat of coke is determined based on the raw material parameters, the sensible heat of blast is determined based on the blast parameters, and the sensible heat of gas is determined based on the gas injection parameters. The volume of gas produced by the chemical reaction and the volume of gas not involved in the chemical reaction are used to calculate the volume and composition of the furnace gas. The theoretical combustion temperature of the gas is iteratively solved based on the volume, composition, and total heat input until the second convergence condition is met, yielding the theoretical combustion temperature of the gas. The formula for calculating the theoretical combustion temperature of the gas is as follows. in, T f The theoretical combustion temperature of the gas is given. Q For the total calorie income, V G The gas volume in the furnace belly is [missing information]. C G The specific heat capacity of the gas in the furnace belly; The direct reduction degree determination module is used to determine the direct reduction degree of iron ore based on the furnace top gas parameters, the slag and iron parameters, the furnace belly gas quantity and the furnace belly gas composition. The heat transfer coefficient determination module is used to determine the gas-liquid heat transfer coefficient based on the theoretical combustion temperature of the gas, the composition of the gas in the furnace belly, the slag and iron parameters, and the composition of the gas after direct reduction at the direct reduction location; the composition of the gas after direct reduction is determined based on the gas parameters at the furnace top, or the composition of the gas after direct reduction is determined based on the gas parameters at the furnace top, the gas volume in the furnace belly, and the composition of the gas in the furnace belly. The iterative solution module is used to iteratively solve for the molten iron temperature and gas temperature based on the gas-liquid heat transfer coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of coal gas, and the slag-iron parameters, until the first convergence condition is met, thus completing the prediction of the molten iron temperature in blast furnace smelting.

10. An electronic device, characterized in that, The electronic device includes: One or more processors; A storage device for storing one or more programs, which, when executed by one or more processors, cause the electronic device to implement the method for predicting molten iron temperature in blast furnace smelting as described in any one of claims 1-8.

11. A computer-readable storage medium, characterized in that, It stores a computer program that, when executed by the computer's processor, causes the computer to perform the method for predicting the temperature of molten iron in blast furnace smelting as described in any one of claims 1-8.

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