Method, apparatus, electronic equipment, and storage medium for predicting ironwater temperature in blast furnace smelting.

Abstract

This invention provides a method, apparatus, electronic equipment, and storage medium for predicting the iron water temperature obtained in blast furnace smelting. This method acquires raw fuel parameters, drum blast parameters, gas injection parameters, top gas parameters, and slag iron parameters in the blast furnace smelting process. Based on the raw fuel parameters, drum blast parameters, and gas injection parameters, the Bosch gas volume, Bosch gas components, and theoretical combustion temperature of the gas in the nozzle rotation area are calculated. Based on the top gas parameters, slag iron parameters, Bosch gas volume, and Bosch gas components, the degree of direct reduction of the iron ore is calculated. Based on the theoretical combustion temperature of the gas, Bosch gas components, slag iron parameters, and gas components after direct reduction, the gas-liquid heat exchange coefficient is calculated. Then, the iron water temperature and gas temperature are repeatedly calculated using the gas-liquid heat exchange coefficient, the degree of direct reduction of the iron ore, the theoretical combustion temperature of the gas, and the slag iron parameters, and the results are obtained to predict the temperature of the iron water obtained in blast furnace smelting. This improves the accuracy of the prediction, provides a good basis for blast furnace smelting, and ensures the stable operation of the blast furnace.

Description

[Technical Field]

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

[0002] In the blast furnace smelting process, the iron-water temperature reflects the thermal equilibrium state within the furnace and the reduction state of the iron ore. Simultaneously, gas injection technology is a key technology for achieving blast furnace decarbonization, and stable iron-water temperature is an essential condition for maintaining stable operation of the blast furnace under gas injection. Therefore, accurately and precisely predicting the iron-water temperature plays an extremely important role in the operational control of blast furnace smelting.

[0003] Currently, many related technologies identify trends in iron-water temperature change from past operational data and then predict the iron-water temperature. However, insufficient consideration of real-time parameters affects the accuracy of the predictions. It is difficult to accurately predict the iron-water temperature under gas injection conditions. [Overview of the Initiative] [Problems that the invention aims to solve]

[0004] Based on the shortcomings of the prior art described above, this application provides a method, apparatus, electronic equipment, and storage medium for predicting iron-water temperature in a blast furnace. This solves the technical problem that real-time parameters are not adequately considered in iron-water temperature prediction, affecting prediction accuracy and making it difficult to appropriately predict iron-water temperature under gas injection conditions. [Means for solving the problem]

[0005] This application provides a method for predicting the temperature of iron water in a blast furnace. This method includes obtaining raw material, fuel, drum blast parameters, gas injection parameters, furnace top gas parameters, and slag iron parameters used in the blast furnace smelting process. Based on the raw material, fuel, drum blast parameters, and gas injection parameters, the total heat, Bosch gas volume, and Bosch gas components of the nozzle rotation region are calculated. The total heat, Bosch gas volume, and Bosch gas components of the nozzle rotation region are calculated using the nozzle rotation gas injection parameters, and these are used to determine the theoretical combustion temperature of the gas in the nozzle rotation region. Furthermore, the degree of direct reduction of iron ore is calculated based on the furnace top gas parameters, slag iron parameters, Bosch gas volume, and Bosch gas components. The gas-liquid heat exchange coefficient is calculated based on the theoretical combustion temperature of the furnace top gas, Bosch gas components, slag iron parameters, and the gas components after direct reduction at the direct reduction position. The gas components after direct reduction are determined based on the furnace top gas parameters, or based on the parameters of the furnace top gas, Bosch gas volume, and Bosch gas components. Using the gas-liquid heat exchange coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of the gas, and the slag iron parameters, the iron-water temperature and gas temperature are repeatedly determined until the first convergence condition is met, and the iron-water temperature during blast furnace smelting is predicted.

[0006] This is an example of an embodiment of the present application. Based on the raw fuel parameters, drum air parameters, and gas injection parameters, the total heat, Bosch gas volume, and Bosch gas components of the nozzle rotation area are calculated. Based on this total heat, Bosch gas volume, and Bosch gas components, the theoretical combustion temperature of the gas in the nozzle rotation area is determined. This process includes calculating the volume of gas participating in the chemical reaction, the volume of gas not participating in the chemical reaction, and the volume of gas generated by the chemical reaction in the nozzle rotation area, based on the raw fuel parameters, drum air parameters, and gas injection parameters. Based on the volume of gas participating in the chemical reaction, the heat generated by the chemical reaction in the drum air nozzle rotation area is calculated. Based on the heat generated by the coke, drum air, gas, and chemical reaction in this rotation area, the total heat is calculated. The heat generated by the coke is calculated based on the parameters of the raw gas, the heat generated by the drum air is calculated based on the drum air parameters, and the heat generated by the gas is calculated based on the gas injection parameters. The Bosch gas volume and Bosch gas components are calculated based on the volume of gas generated by the chemical reaction and the volume of gas not participating in the reaction. Based on the Bosch gas volume, Bosch gas components, and total heat, the theoretical combustion temperature of the gas is repeatedly determined until the second convergence condition is met.

[0007] As one embodiment of this application, the following process is performed before calculating the total heat amount based on the heat generated by coke, the heat generated by the drum breeze, the heat generated by the gas, and the heat generated by chemical reactions in the rotating region of the drum breeze port. First, the specific heat of the coke is calculated based on a preset coke temperature and coke components, and the heat generated by the coke is calculated using this specific heat, the amount of coke used, and the set coke temperature. Here, the raw fuel parameters include the coke components and the amount of coke used. Next, the specific heat of the drum breeze is calculated based on the drum breeze temperature and drum breeze components, and the heat generated by the drum breeze is calculated using this specific heat, the drum breeze volume, and the drum breeze temperature. Here, the drum breeze parameters include the drum breeze components, drum breeze temperature, and drum breeze volume. The specific heat of the blown gas is calculated based on a preset blown gas temperature and components. The specific heat of the blown gas is calculated using this specific heat, the blown gas temperature, and the blown gas injection volume. The blown gas injection parameters include the blown gas components and injection volume.

[0008] In the embodiment of this application, the theoretical combustion temperature of the gas is repeatedly determined based on the Bosch gas quantity, Bosch gas components, and total heat quantity until a second convergence condition is met, and the theoretical combustion temperature is calculated. This process includes determining the specific heat of the initial Bosch gas in the rotating area of ​​the drum vent from the Bosch gas components and a preset theoretical combustion temperature, and calculating the initial theoretical combustion temperature using the total heat quantity, Bosch gas quantity, and initial specific heat. The initial theoretical combustion temperature of the gas is taken as the theoretical combustion temperature of the gas before replacement, and the specific heat of the replacement Bosch gas in the rotating area of ​​the drum vent is calculated based on the Bosch gas components and the theoretical combustion temperature of the gas before replacement. Next, the theoretical combustion temperature of the gas after replacement is calculated using the total heat quantity, Bosch gas quantity, and specific heat of the replacement Bosch gas. The difference between the theoretical combustion temperature of the gas before replacement and the theoretical combustion temperature of the gas after replacement is calculated, and the replacement difference of the theoretical combustion temperature of the gas is calculated. If this replacement difference is less than or equal to the second preset temperature difference threshold, the second convergence condition is met, and the gas theoretical combustion temperature after replacement is adopted as the gas theoretical combustion temperature. If the temperature difference in the theoretical combustion temperature replacement calculation exceeds the second preset threshold, the theoretical combustion temperature replacement calculation is performed using the amount of Bosch gas, gas components, total heat, and the theoretical combustion temperature after iteration, and the results are repeatedly obtained until the second convergence condition is met, thereby calculating the theoretical combustion temperature.

[0009] In the embodiments of this application, the degree of direct reduction of iron ore is determined based on the amount and components of the top gas, using top gas parameters, slag iron parameters, Bosch gas amount, and Bosch gas components. Specifically, the amount of carbon monoxide in the Bosch gas is calculated based on the amount and components of the Bosch gas, and the total amount of carbon monoxide and carbon dioxide in the top gas is calculated based on the amount and components of the top gas. Based on this total amount of carbon monoxide and carbon dioxide, the total amount of carbon monoxide produced by direct reduction is determined. Here, the top gas parameters include the amount and components of the top gas. Based on the components and production amount of iron water, the mass of trace elements and the mass of iron in the iron water are calculated. Furthermore, from the masses of these trace elements, the amount of carbon monoxide produced by directly reducing the oxides of the trace elements is calculated. Based on this total amount of carbon monoxide and the amount of carbon monoxide produced by directly reducing the oxides of the trace elements, the amount of carbon monoxide produced by the direct reduction of iron ore is calculated. The slag iron parameters include the components and production amount of iron water. Then, the degree of direct reduction of iron ore is calculated using the amount of carbon monoxide produced by the direct reduction of iron ore, the mass of iron in the iron water, and the mass of iron in the pre-set hot-pressed iron block.

[0010] In the embodiments of this application, the following procedure is followed before calculating the gas-liquid heat exchange coefficient. First, 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 calculated based on the amount and composition of the top gas. Here, the parameters of the top gas include the amount of top gas and its composition. Next, the amount of top gas is taken as the amount of gas after direct reduction, the total amount of carbon monoxide and carbon dioxide is taken as the amount of carbon monoxide in the gas after direct reduction, the total amount of water and hydrogen is taken as the amount of hydrogen in the gas after direct reduction, and the amount of nitrogen is taken as the amount of nitrogen in the gas after direct reduction. Based on the amount of gas after direct reduction, and the amount of carbon monoxide, hydrogen, and nitrogen within it, the gas composition after direct reduction is determined.

[0011] In the embodiments of this application, the gas-liquid heat exchange coefficient is calculated by following the procedure below. First, the total amount of carbon monoxide and carbon dioxide in the top gas is calculated based on the amount and composition of the top gas. Here, the parameters of the top gas include the amount and composition of the top gas. Next, the amount of hydrogen and nitrogen in the Bosch gas is calculated based on the amount and composition of the Bosch gas. The amount of top gas is taken as the amount of gas after direct reduction, the total amount of carbon monoxide and carbon dioxide in the top gas is taken as the amount of carbon monoxide in the gas after direct reduction, the amount of hydrogen in the Bosch gas is taken as the amount of hydrogen in the gas after direct reduction, and the amount of nitrogen in the Bosch gas is taken as the amount of nitrogen in the gas after direct reduction. The gas composition after direct reduction is determined based on the amount of gas after direct reduction, and the amount of carbon monoxide, hydrogen, and nitrogen within it.

[0012] In the embodiments of this application, the gas-liquid heat exchange coefficient is calculated based on the theoretical combustion temperature of the gas, the Bosch gas components, the slag iron parameters, and the gas components after direct reduction at the direct reduction position. Specifically, the gas components in the drop zone are calculated by interpolating the Bosch gas components and the gas components after direct reduction. Next, the gas-liquid heat exchange coefficient in the nozzle rotation area is calculated based on the equivalent particle size of the slag iron, the thermal conductivity of the gas in the nozzle rotation area, and the number of Nuscelles. Here, the thermal conductivity of the gas and the number of Nuscelles in the nozzle rotation area are calculated based on the Bosch gas components and the theoretical combustion temperature of the gas. The equivalent particle size of the slag iron is calculated based on the slag iron parameters. The gas-liquid heat exchange coefficient at the direct reduction position is calculated based on the equivalent particle size of the slag iron, the thermal conductivity of the gas at the direct reduction position, and the number of Nuscelles at the direct reduction position. The thermal conductivity of the gas and the number of Nuscelles at the direct reduction position are determined based on the gas components after direct reduction and the theoretical combustion temperature of the gas. Furthermore, the gas-liquid heat exchange coefficient of the drop zone is calculated based on the equivalent particle size of the slag iron, the thermal conductivity coefficient of the gas in the drop zone, and the number of Nuscelles in the drop zone. The thermal conductivity coefficient and number of Nuscelles in the drop zone are determined based on the gas components and theoretical combustion temperature of the gas in the drop zone.

[0013] In the embodiments of this application, the ironwater temperature and gas temperature are iteratively determined based on the gas-liquid heat exchange coefficient, the degree of direct reduction of iron ore, the theoretical combustion temperature of the gas, and the slag iron parameters, until a first convergence condition is met, and the ironwater temperature is predicted. This process includes calculating the amount of heat required for direct reduction from the ironwater components and the degree of direct reduction of iron ore. The slag iron parameters include the ironwater components. The ironwater temperature and gas temperature are calculated based on the principle of energy conservation in the gas phase and ironwater phase, using the gas phase temperature, ironwater phase temperature, gas-liquid heat exchange coefficient, and the amount of heat required for direct reduction. This allows for the calculation of the ironwater temperature in the nozzle rotation area before replacement, the ironwater temperature after replacement, the gas temperature after direct replacement before replacement, and the gas temperature after direct reduction after replacement. The initial value of the gas phase temperature is set to the theoretical combustion temperature of the gas, and the initial value of the ironwater phase temperature is set to the ironwater temperature after direct reduction. The difference between the iron-water temperature in the nozzle rotation area before replacement and the iron-water temperature in the nozzle rotation area after replacement is defined as the iron-water temperature change difference, and the difference between the gas temperature after direct reduction before replacement and the gas temperature after direct reduction after replacement is defined as the gas temperature change difference. If both the iron-water temperature change difference and the gas temperature change difference are below the first predetermined temperature difference threshold, the first convergence condition is met, and the iron-water temperature in the nozzle rotation area after replacement is taken as the final prediction result.

[0014] As one example of this application, a blast furnace iron-water temperature prediction device is provided. This device comprises a smelting data acquisition module that acquires raw fuel parameters, drum wind parameters, gas injection parameters, top gas parameters, and slag iron parameters in the blast furnace smelting process; a theoretical combustion temperature determination module that calculates the total heat, Bosch gas volume, and Bosch gas components of the nozzle rotation area based on these parameters and uses them to determine the theoretical combustion temperature of the gas in the nozzle rotation area; and a direct reduction degree determination module that calculates the degree of direct reduction of iron ore based on the top gas parameters, slag iron parameters, Bosch gas volume, and Bosch gas components. The heat exchange coefficient determination module calculates the gas-liquid heat exchange coefficient based on the theoretical combustion temperature of the gas, the Bosch gas components, the slag iron parameters, and the components of the gas after direct reduction at the direct reduction position. The components of the gas after direct reduction are determined based on the top gas parameters, or based on the top gas parameters, Bosch gas volume, and Bosch gas components. The replacement calculation module uses the gas-liquid heat exchange coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of the gas, and the slag iron parameter to repeatedly perform replacement calculations of the iron-water temperature and gas temperature until the first convergence condition is met, thereby predicting the iron-water temperature in blast furnace steelmaking.

[0015] As one embodiment of this application, a type of electronic device is provided. This electronic device comprises one or more processors and one or more program storage devices. These programs are executed by the one or more processors to realize the above-described method for predicting iron water temperature in blast furnace ironmaking.

[0016] As one embodiment of this application, a computer-readable storage medium on which a computer program is recorded is provided. This program is executed by a computer processor to perform the above-described method for predicting iron water temperature in blast furnace ironmaking.

[0017] The main benefit of this invention is to provide a method, apparatus, electronic equipment, and storage medium for predicting the iron-water temperature in a blast furnace. This method calculates the theoretical combustion temperature of the gas, the gas-liquid heat exchange coefficient, and the direct reduction degree of the iron ore using raw fuel parameters, drum wind parameters, gas injection parameters, top gas parameters, and slag iron parameters in the blast furnace smelting process. This allows for the determination of iron-water temperature and gas temperature, enabling prediction of blast furnace smelting iron-water temperature under various conditions, including gas injection conditions. Furthermore, by improving the accuracy of iron-water temperature prediction and providing a suitable basis for controlling the operation of blast furnace smelting, the method ensures stable and smooth operation of the blast furnace.

[0018] The general description above and the detailed description below are illustrative and explanatory only. Please understand that they do not limit this application. [Brief explanation of the drawing]

[0019] [Figure 1] Figure 1 is a flowchart of the iron-water temperature prediction method in blast furnace steelmaking as shown in the embodiment of this application. [Figure 2] Figure 2 is a diagram showing the configuration of a water temperature prediction system in blast furnace steelmaking, as shown in a specific embodiment of this application. [Figure 3] Figure 3 is a schematic diagram of the temperature prediction flow of water and iron in a blast furnace steelmaking process, in one embodiment of the water temperature prediction system for the blast furnace steelmaking process shown in Figure 2. [Figure 4] Figure 4 is a flowchart of a blast furnace iron water temperature prediction device shown in one embodiment of this application. [Figure 5] Figure 5 is a structural diagram of an electronic device shown as an example of an embodiment of this application. [Modes for carrying out the invention]

[0020] The embodiments of this application will be described below using specific examples. Those skilled in the art will be able to easily understand the other advantages and effects of this application from the disclosures herein. This application can also be implemented or applied by other different specific embodiments, and each detail herein may be modified or altered in various ways depending on different viewpoints and applications, as long as it does not contradict the spirit of this application. Furthermore, the following embodiments and features can be combined with each other, as long as they do not contradict each other.

[0021] The drawings of the embodiments shown below are merely illustrations to illustrate the basic concept of this application and do not depict the number, shape, or size of parts that would be used in actual implementation. In actual implementation, the shape, quantity, and proportion of each part can be arbitrarily changed, and the arrangement of parts will be more complex.

[0022] In this application, terms such as "first," "second," etc., are used to distinguish similar subjects and do not limit their order. Furthermore, expressions such as "includes" and "possesses" indicate that the scope is not exclusive, except for the scope indicated by the subject. The identification symbols such as numerical numbers and step numbers described in this application are for ease of explanation and do not limit the scope of this application. The size of the identification symbols in this application does not indicate order, and the execution order of each process is determined based on its function and inherent logic.

[0023] The following description includes many details to provide a more in-depth explanation of the embodiments of this application. However, if you are an expert in this field, you can implement the embodiments of this application even if these specific details are omitted. Furthermore, in order to avoid making the embodiments of this application difficult to understand, the configuration and apparatus of the present invention are not shown in detail in other embodiments, but are instead shown in the form of drawings.

[0024] The embodiments of this application propose a method for predicting iron-water temperature in blast furnace steelmaking, an apparatus for predicting iron-water temperature in blast furnace smelting, electronic equipment, a computer-readable storage medium, and a computer program product, respectively. These embodiments will now be described in detail.

[0025] As an example of an embodiment of this application, a method for predicting the iron-water temperature in a blast furnace is proposed. This method includes obtaining raw fuel parameters, drum blast parameters, gas injection parameters, top gas parameters, and slag iron parameters in the blast furnace smelting process. Based on the raw fuel parameters, drum blast parameters, and gas injection parameters, the total heat amount, Bosch gas amount, and Bosch gas components of the nozzle rotation area are calculated, and these are used to determine the theoretical gas combustion temperature of the nozzle rotation area. Furthermore, the degree of direct reduction of iron ore is calculated based on the top gas parameters, slag iron parameters, Bosch gas amount, and Bosch gas components. The gas-liquid heat exchange coefficient is calculated based on the theoretical gas combustion temperature, Bosch gas composition, slag iron parameters, and the composition of the reduced gas at the direct reduction position. The composition of the gas after direct reduction is determined based on the top gas parameters, or based on the top gas parameters, Bosch gas amount, and Bosch gas composition. Using the gas-liquid heat exchange coefficient, the direct reduction degree of iron ore, the theoretical gas combustion temperature, and slag iron parameters, the iron-water temperature and gas temperature are repeatedly determined until the first convergence condition is met, thereby completing the prediction of the iron-water temperature in blast furnace smelting. The technical configuration in the embodiment of this application can predict the blast furnace iron-water temperature under various conditions, including gas injection conditions, and can also improve the accuracy of the prediction. This provides a suitable basis for controlling the operation of the blast furnace and ensures stable operation of the blast furnace.

[0026] Please refer to Figure 1. Figure 1 is a flowchart of a blast furnace iron-water temperature prediction method illustrating an embodiment of the present application. As shown in Figure 1, the embodiment of the blast furnace iron-water temperature prediction method includes at least steps S110 to S150, which will be described in detail below. In step S110, raw fuel parameters, drum blast parameters, gas injection parameters, top gas parameters, and slag iron parameters are obtained for the blast furnace smelting process.

[0027] In the embodiments of this application, the parameters of the raw material fuel refer to the components and amount used of the raw material fuel, and include at least one such as the components and amount used of coke, or the components and amount used of coal powder. Here, the components of the raw material fuel mean the ratio of substances in the raw material fuel to the total amount of the raw material fuel. For example, the components of coke refer to the ratio of C (carbon), H (hydrogen), O (oxygen), N (nitrogen), S (sulfur), volatile matter, ash, etc. in the coke, and the components of coal powder refer to the ratio of C, H, O, N, S, volatile matter, ash, etc. in the coal powder.

[0028] The tumbling parameters include at least one of the tumbling volume, tumbling temperature, and tumbling components. The tumbling components include at least one of the tumbling humidity and oxygen richness.

[0029] The parameters for gas injection include at least one of the following: type of injection medium, injection gas composition, injection gas volume, and injection gas temperature. The type of injection medium may include coke gas, converter gas, decarbonized blast furnace gas, natural gas, pure hydrogen, chemical waste gas, shale gas, or mixtures thereof. The injection gas composition refers to the proportion of substances contained in the injection gas. For example, it indicates the proportion of components such as H2 (hydrogen), CO (carbon monoxide), CO2 (carbon dioxide), CH4 (methane), N2 (nitrogen), and O2 (oxygen) contained in the injection gas.

[0030] The furnace top gas parameters include at least one of the furnace top gas components and furnace top gas volume. Here, the furnace top gas components refer to the proportions of substances contained in the furnace top gas. For example, the furnace top gas components may include the proportions of H2, CO, CO2, N2, etc.

[0031] The slag iron parameter includes at least one of the following: slag iron components, slag iron quantity, or slag production amount (slag quantity). Here, slag iron components refer to the proportion of substances contained in the slag iron. For example, slag iron components include the proportion of substances such as Fe (iron), C (carbon), Si (silicon), Mn (manganese), P (phosphorus), S (sulfur), and Ti (titanium) in the slag iron.

[0032] The raw fuel parameters, drum wind parameters, gas injection parameters, top gas parameters, and slag iron parameters are real-time data from the blast furnace smelting process and directly reflect the smelting conditions inside the blast furnace in real time. Therefore, it is possible to accurately predict the iron-water temperature based on these parameters.

[0033] In step S120, the total heat, Bosch gas volume, and Bosch gas composition in the nozzle rotation area are calculated based on the raw fuel parameters, drum air parameters, and gas injection parameters. Then, the theoretical combustion temperature of the gas in the nozzle rotation area is determined using this data.

[0034] In the embodiment of this application, the blast furnace is composed of five regions from top to bottom: a block zone, a soft molten zone, a drip zone, a nozzle rotation area, and a slag zone, which are located at different heights inside the blast furnace. In the block zone, moisture evaporates and thermal decomposition occurs, as well as reduction of iron ore and heat exchange between the molten material and gas. In the soft molten zone, the molten material softens, and molten slag drips from its lower end. This dripping slag undergoes a direct reduction reaction in the blast furnace, generating the first slag, so the lower end of the soft molten zone becomes a direct reduction location. In the drip zone, the dripping liquid slag iron undergoes multiple chemical reactions with gas and solid carbon. In the nozzle rotation area, the injected fuel undergoes a combustion reaction with hot air, generating high-temperature gas. In the slag zone, reactions occur at the interlayer interfaces of the slag and as the molten material passes through the slag layer.

[0035] The slag in the nozzle rotation area is liquid, and this liquid slag is called "iron water." Therefore, iron water temperature refers to the temperature of the liquid slag in the nozzle rotation area. Since heat exchange occurs between iron water and gas, the iron water temperature is affected by the theoretical combustion temperature of the gas in the nozzle rotation area. For this reason, it is necessary to determine the theoretical combustion temperature of the gas. Based on the raw fuel parameters, drum air parameters, and gas injection parameters, the total heat amount, Bosch gas amount, and Bosch gas components in the nozzle rotation area are calculated, and the theoretical combustion temperature of the gas is determined accordingly.

[0036] In the embodiment of the present application, step S120 calculates the volume of gas participating in the chemical reaction, the volume of gas not reacting, and the volume of gas generated by the chemical reaction in the tuyere rotation area based on the raw fuel parameters, the blast parameters, and the gas injection parameters. From the volume of gas participating in the chemical reaction, the heat release amount due to the chemical reaction in the tuyere rotation area is calculated. Furthermore, based on the coke heat release, the blast heat release, the gas heat release, and the heat release amount due to the chemical reaction in the tuyere rotation area, the total heat amount is calculated. The coke heat release is calculated based on the raw fuel parameters, the blast heat release is calculated based on the blast parameters, and the gas heat release is calculated based on the gas injection parameters respectively. Using the volume of gas generated by the chemical reaction and the volume of gas not reacting, the Bosch gas amount and the Bosch gas components are calculated. Based on the Bosch gas amount, the Bosch gas components, and the total heat amount input, the theoretical combustion temperature of the gas is iteratively calculated and obtained. Continue until the second convergence condition is satisfied, and calculate the theoretical combustion temperature.

[0037] In this embodiment, please refer to Table 1. Table 1 is a table of chemical reactions and heat effects in the tuyere rotation area in a specific example of the present application. As shown in Table 1, in the tuyere rotation area, the blowing gas, pulverized coal, and elemental carbon or CO2, H2O (water), CH4, or chemical substance C in the coke C4 , CH4 , C3 , C1 , , C2 , , , ,

[0039] H y O m N n come into contact with oxygen or other substances and undergo combustion or other chemical reactions, and are all converted to CO, H2, and N2. Note that different chemical reactions result in different heat effects.

[0038]

Table 1

[0039] Therefore, the calculation method of the heat release due to the chemical reaction in the tuyere rotation area is as follows. Q2 = aΔH C1 + bΔH C2 + cΔH CH4 + dΔH C3 + eΔH C4 Equation (1)

[0040] In this context, Q2 represents the amount of heat released due to chemical reactions in the nozzle rotation area. a, b, c, d, and e are the reaction participation amounts corresponding to reactions 1-5 shown in Table 1. ΔH C1 ΔH C2 ΔH CH4 ΔH C3 ΔH C4 These correspond to the thermal effects of reactions 1-5 in Table 1. The values ​​of a, b, and c depend on the volume amounts of CO2, H2O, and CH4 in the blown gas. The values ​​of d and e depend on the amount of oxygen supplied to the blast furnace. Note that when calculating the amount of heat released due to chemical reactions in the nozzle rotation area, O2 is first considered as CH4 and C x H y O m N n It reacts with gases such as [list of gases], and then reacts with solid carbon (C). The combustion priority of gas, coal dust, coke, and oxygen is gas > coal dust > coke, and the combustion completion rate of coal dust is 70-84%.

[0041] Therefore, when calculating the heat release due to chemical reactions in the nozzle rotation area, it is first necessary to identify the volume of gases participating in the chemical reaction in this area. These include CO2, H2O, CH4, and C x H y O m N n This includes the volumes of O2, CO2, H2O, CH4, and C contained in the components of the blown-out gas. x H y O m N n Based on the proportions and amount of discharged gas, CO2, H2O, CH4, C in the discharged gas x H y O m N nThe volume is calculated. Here, the parameters of the blown gas include the components and blown volume of the blown gas. Based on the O2 content and blown volume of the blown gas, the volume of O2 in the blown gas is calculated. Also, based on the O2 content and blown volume of the blast vent, the volume of O2 in the blast vent is calculated. Here, the blast vent parameters include the blast vent components and blast vent volume. Furthermore, the volume of O2 in the coke is calculated based on the O2 content and coke usage, and the volume of O2 in the coal powder is calculated based on the O2 content and coal powder usage. Here, the raw fuel parameters include the coke components and coke usage, the coal powder components and coal powder usage. Using the volume of O2 in the blown gas, the volume of O2 in the blast vent, the volume of O2 in the coke, and the volume of O2 in the coal powder, the amount of oxygen supplied to the blast furnace is calculated using the following formula. Vt=V O blast+V O Gas+V O coke+V O coal expression(2)

[0042] In this context, Vt represents the total amount of oxygen entering the blast furnace. O The blast is the volume of O2 in the tympanic air. O Gas is the volume of O2 in the blown-out gas. O coke is the volume of O2 in coke. O "Coal" refers to the volume of O2 in coal powder.

[0043] Considering the heat generated by chemical reactions in the nozzle rotation area, the total heat in the nozzle rotation area is calculated by summing the calorific value of the coke, the calorific value of the blast air, the calorific value of the gas, and the calorific value of the chemical reactions in the nozzle rotation area. The calculation method is as follows. Q=Q1+Q2+Q3+Q4 Formula (3)

[0044] In this system, Q represents the total heat of the blow-out rotating area, Q1 represents the heat indicated by the blast, Q2 represents the heat generated by the chemical reaction in the blow-out rotating area, Q3 represents the heat indicated by the gas, and Q4 represents the heat indicated by the coke. The heat indicated by the blast is determined based on the blast parameters, the heat indicated by the gas is determined based on the gas injection parameters, and the heat indicated by the coke is determined based on the parameters of the raw materials and fuel.

[0045] The Bosch gas in the nozzle rotation area contains gases generated by chemical reactions and gases that do not participate in chemical reactions. The volume of gases participating in chemical reactions in this area can be calculated based on the reaction equations shown in Table 1, including the volume of CO and H2. Soot, blown gas, and drum blast contain N2. Table 1 shows that N2 is not included in the gases participating in chemical reactions. Therefore, the volume of N2 in soot, blown gas, and drum blast can be treated as the volume of gases that do not participate in chemical reactions. Specifically, the volume of N2 in the soot is calculated from the proportion of N2 in the soot components and the amount of soot used. The volume of N2 in the blown gas is calculated from the proportion of N2 in the blown gas components and the blown gas volume. The volume of N2 in the drum blast is calculated from the proportion of N2 in the drum blast components and the drum blast volume. Next, the Bosch gas volume is calculated based on the volume of gases generated by chemical reactions and the volume of gases that do not participate in chemical reactions. The calculation method is as follows. V G =V CO coke+V CO coal+V CO Gas+V CO blast+V H2 coal+V H2 Gas+V H2 blast+V N2 coal+V N2 Gas+V N2 blast expression (4)

[0046] Among them, V G represents the Bosch gas volume, V CO Coke is the volume of CO produced by the reaction of coke in the rotating area of ​​the nozzle. Also, V COCoal represents the volume of CO produced by the reaction of coal powder in the same area. CO Gas is the volume of CO produced by the reaction of the blown gas in the same region. CO blast is the volume of CO produced by the reaction of water in the blown gas in this area. H2 coal is the volume of H2 produced by the reaction of water and hydrogen in the volatile components of coal pulverized soot in this area. H2 The blast is the volume of H2 produced by the reaction of water in the blown gas within the rotating area. H2 Gas is the volume of H2 produced by the reaction of water and hydrogen-containing gases (methane, ethane, ethylene) in the blown gas in the rotating area. N2 coal is the volume of N2 in coal powder. N2 Gas is the volume of N2 in the blown gas. N2 blast is the volume of N2 in the tympano. CO Coal is the volume of CO produced by the reaction of fixed carbon, volatile carbon, and water in coal powder. N2 Coal refers to the volume of volatilized coal dust and N2 in the coal dust carrier gas.

[0047] As can be seen from equation (4), Bosch gas contains CO, H2, and N2. The volume of each gas can be calculated from the volume of gas produced by the chemical reaction and the volume of gas that did not participate in the reaction. The proportion of CO is calculated from the volume of CO and the amount of Bosch gas, the proportion of H2 from the volume of H2 and the amount of Bosch gas, and the proportion of N2 from the volume of N2 and the amount of Bosch gas. By combining these proportions and volumes, the components of the Bosch gas are determined.

[0048] After obtaining the total heat quantity, Bosch gas quantity, and Bosch gas components, the theoretical combustion temperature of the gas is recalculated using these values, and this process continues until a second convergence condition is met, thereby calculating the theoretical combustion temperature. The second convergence condition may be that the number of recalculations reaches a second preset number, the temperature difference during iteration falls below a second preset temperature difference threshold, or other convergence conditions. No restrictions are placed on these conditions here. Furthermore, by adopting the sum of the heat of coke, the heat of the drum, the heat of the gas, and the heat generated by chemical reactions as the total heat quantity, the calorific value is comprehensively considered, thereby improving the accuracy of the calculation of the theoretical combustion temperature of the gas.

[0049] In the embodiments of this application, the following processing is performed before calculating the total heat amount based on the heat generated by coke, drum blast, gas, and chemical reactions in the nozzle rotation area. First, the specific heat of coke is calculated based on a preset coke temperature and coke components, and the heat generated by coke is calculated using this specific heat, the amount of coke used, and the coke temperature. Here, the raw fuel parameters include the coke components and the amount of coke used. Next, the specific heat of the drum blast is calculated based on the drum blast temperature and drum blast components, and the heat generated by the drum blast is calculated using this specific heat, the drum blast volume, and the drum blast temperature. Here, the drum blast parameters include the drum blast components, drum blast temperature, and drum blast volume. The specific heat of the injected gas is determined based on a preset temperature and components of the injected gas. Then, the indicated heat of the gas is calculated using the preset temperature, specific heat, and injection volume of the injected gas. The gas injection parameters include the components and injection volume of the injected gas.

[0050] In this embodiment, the drum blast, coke, and blown gas are composed of different substances, and these substances have different specific heats. Furthermore, even for the same substance, the specific heat changes with temperature, so the relationship between the specific heat of each substance and temperature can be determined in advance.

[0051] When calculating the specific heat of the drum wind, first, the specific heat of each substance at the drum wind temperature is calculated based on the predetermined relationship between the specific heat and temperature of various substances, and the drum wind temperature included in the drum wind parameters. Next, the specific heat of the drum wind is determined using these specific heats and the proportions of each substance in the drum wind component as described in the drum wind parameters. Finally, the specific heat of the drum wind is calculated using this specific heat, the drum wind temperature, and the drum wind amount indicated in the drum wind parameters. The calculation method is as follows. Q1=CbVbTb Formula (5)

[0052] In this equation, Q1 is the heat of the drum airflow, Cb is the specific heat of the drum airflow, Vb is the drum airflow rate, and Tb is the drum airflow temperature.

[0053] When calculating the calorific value of gas, first, the specific heat of each substance in the blown gas is calculated based on the predetermined relationship between the specific heat and temperature of various substances, and the temperature of the blown gas. Next, the specific heat of the injecting gas is calculated using the specific heat of each substance in the blown gas and the proportion of each substance in the components of the injecting gas. Finally, the calorific value of the coal is calculated using this specific heat, the predetermined temperature of the injecting gas, and the amount of injecting gas. The calculation method is as follows. Q3 = CgiVgiTgi Equation (6)

[0054] In this context, Q3 is the specific heat of the gas, Cgi is the specific heat of the blown gas, Vgi is the gas blowing rate, and Tgi is the preset temperature of the blown gas.

[0055] When calculating the heat of coke, first, the specific heat of each substance is calculated using the predetermined relationship between the specific heat and temperature of various substances and the temperature of the coke. Next, the specific heat of the coke is calculated by combining these specific heat values ​​with the ratio of the content of each substance in the coke components listed in the raw fuel parameters. Finally, the specific heat of the coke is calculated using this specific heat value, the predetermined coke temperature, and the amount of coke used as listed in the raw fuel parameters. The calculation method is as follows. Q4 = Ccoke·mcoke·Tcoke Equation (7)

[0056] In this case, Q4 is the indicated heat of the coke, Ccoke is the specific heat of the coke, mcoke is the amount of coke used, and Tcoke is the set coke temperature. Suggestively, the pre-set coke temperature may be any temperature value between 1400 and 1500°C, or any other temperature value. There are no restrictions here.

[0057] In this embodiment, the influence of temperature and the ratio of each substance on the specific heat of the drum breeze, gas, and coke was considered, and the accuracy of the specific heat was improved by calculating these specific heats based on temperature and the ratio of each substance, thereby improving the calculation accuracy of the specific heat of the drum breeze, gas, and coke.

[0058] In this embodiment, the theoretical combustion temperature of the gas is determined repeatedly until the second convergence condition is met, based on the Bosch gas quantity, Bosch gas components, and total heat income. This gives the theoretical combustion temperature of the gas. Specifically, the initial Bosch gas specific heat in the nozzle rotation area is calculated based on the Bosch gas components and a preset theoretical combustion temperature of the gas. Next, the initial theoretical combustion temperature of the gas is calculated using the total heat, the amount of Bosch gas, and the initial specific heat of the Bosch gas. This initial theoretical combustion temperature of the gas is used as the theoretical combustion temperature of the gas before replacement, and the specific heat of the replacement Bosch gas in the nozzle rotation area is determined based on the Bosch gas components and the theoretical combustion temperature of the gas before iteration. Then, the theoretical combustion temperature of the gas after replacement is calculated using the total heat, the amount of Bosch gas, and the specific heat of the replacement Bosch gas. The difference between the theoretical combustion temperature of the gas before replacement and the theoretical combustion temperature of the gas after replacement is calculated to determine the replacement difference in theoretical combustion temperature of the gas. If this replacement difference is less than or equal to the second preset temperature difference threshold, the second convergence condition is met, and the gas theoretical combustion temperature after replacement is adopted as the gas theoretical combustion temperature. If the replacement difference exceeds the second preset temperature difference threshold, the replacement calculation of the gas theoretical combustion temperature is performed using the Bosch gas amount, Bosch gas components, total heat amount, and the gas theoretical combustion temperature after iteration, and this is repeated until the second convergence condition is met. This gives the gas theoretical combustion temperature.

[0059] In this embodiment, the formula for calculating the theoretical combustion temperature of the gas is as follows:

[0060]

number

[0061] In this context, Tf is the theoretical combustion temperature of the gas, Q is the total heat energy, and V is the total heat energy. G This is the Bosch gas volume, C G This is the specific heat of Bosch gas.

[0062] Therefore, the calculation procedure for changing the gas theory combustion temperature is as follows.

[0063] 1. A temperature value is set in advance to determine the theoretical combustion temperature of the combustion gas. The specific heat of each substance in the Bosch gas at the predetermined theoretical combustion temperature of the combustion gas is calculated from the relationship between the specific heat and temperature of each substance. Next, the specific heat of the initial Bosch gas is calculated using the specific heat of each substance in the Bosch gas and the composition ratio of the Bosch gas. Then, the total heat amount, the amount of Bosch gas, and the specific heat of the initial Bosch gas are substituted into equation (8) to calculate the theoretical combustion temperature of the initial combustion gas. This theoretical combustion temperature of the initial combustion gas is used as the combustion temperature before recalculation.

[0064] 2. Based on the predetermined relationship between the specific heat and temperature of various substances, the specific heat of each substance is calculated using the theoretical combustion temperature of Bosch gas. Then, the specific heat of Bosch gas is iteratively calculated using the specific heat of each substance in Bosch gas and the proportion of each substance in the Bosch gas components. Next, the total heat amount, the amount of Bosch gas, and the Bosch gas specific heat after the replacement calculation are substituted into equation (8) to determine the theoretical combustion temperature.

[0065] 3. Calculate the difference between the theoretical gas combustion temperature before the replacement calculation and the theoretical gas combustion temperature after the iterative calculation, and use this as the replacement difference for the theoretical gas combustion temperature. Next, compare this replacement difference for the theoretical gas combustion temperature with a second preset temperature difference threshold.

[0066] If the temperature difference in the calculation of the replacement of the theoretical gas combustion temperature is less than or equal to the second predetermined temperature difference threshold, it is determined that the second convergence condition is met, and the replacement theoretical gas combustion temperature is taken as the theoretical gas combustion temperature. Conversely, the replacement theoretical gas combustion temperature is taken as the new theoretical gas combustion temperature before the replacement, and steps 2 and 3 are repeated. This replacement is continued until the second convergence condition is met, and the final theoretical gas combustion temperature obtained by the replacement calculation is taken as the theoretical gas combustion temperature.

[0067] By determining the theoretical combustion temperature of the gas through recalculations and improving its accuracy, the prediction accuracy of the iron-water temperature will be further enhanced.

[0068] In step S130, the degree of direct reduction of the iron ore is determined based on the furnace top gas parameters, slag iron parameters, the amount of Bosch gas, and the Bosch gas components.

[0069] In the embodiments of this application, heat is consumed when elements such as Fe, Si, Mn, S, and P in the iron water are directly reduced; therefore, this reduction also affects the iron water temperature. For this reason, it is necessary to calculate the degree of direct reduction of the iron ore. This can be calculated based on the furnace top gas parameters, slag iron parameters, Bosch gas amount, and Bosch gas composition.

[0070] In one example of this application, step S130 includes the following: Calculating the amount of carbon monoxide in the Bosch gas based on the amount and composition of the Bosch gas, and calculating the total amount of carbon monoxide and carbon dioxide in the top gas based on the amount and composition of the top gas. Calculating the total amount of carbon monoxide produced by direct reduction based on this total amount of carbon monoxide and carbon dioxide. The top gas parameters include the amount and composition of the top gas. Calculating the mass of trace elements and the mass of iron in the iron water based on the composition and production rate of the iron water. Furthermore, calculating the amount of carbon monoxide produced by the direct reduction of the oxides of the trace elements from the mass of the trace elements in the iron water. Calculating the amount of carbon monoxide produced by the direct reduction of iron ore based on this total amount of carbon monoxide and the amount of carbon monoxide produced by the direct reduction of the oxides of the trace elements. The slag iron parameters include the composition and production rate of the iron water. The degree of direct reduction of iron ore is calculated based on the amount of carbon monoxide produced by the direct reduction of iron ore, the mass of iron in the iron water, and the predetermined mass of iron in the hot-pressed iron mass.

[0071] In this embodiment, the volume of CO in the Bosch gas (i.e., the amount of CO) is calculated based on the proportion of CO contained in the Bosch gas components and the amount of Bosch gas. The volume of CO in the top gas is also calculated based on the proportion of CO contained in the top gas components and the amount of top gas. Furthermore, the volume of CO2 in the top gas is calculated based on the proportion of CO2 contained in the top gas components and the amount of top gas. The sum of the volumes of CO and CO2 in the top gas is taken as the total amount of CO and CO2 in the top gas. The difference between the total amount of CO and CO2 in the top gas and the amount of CO in the Bosch gas is calculated as the total amount of CO produced by direct reduction. The calculation method is as follows. V1=V CO+CO2 -V COb Formula (9)

[0072] Among these, V1 is the total amount of CO produced by direct reduction. CO+CO2 V is the total amount of CO and CO2 in the top gas of the furnace. COb This represents the amount of CO in Bosch gas.

[0073] What we learned here is that in a direct reduction reaction, iron ore is directly reduced to produce Fe reduction products, and oxides of trace elements are also directly reduced to produce trace element reduction products. Trace elements contained in iron water include Si, Mn, P, Ti, and S, and the oxides of these trace elements include Si, Mn, P, Ti, and S oxides, and the reduction products of trace elements include Si, Mn, P, Ti, and S reduction products. Therefore, based on the ratio of trace elements in iron water (Si, Mn, P, Ti, S) and the amount of iron water produced, the mass of these trace elements (Si, Mn, P, Ti, S) can be calculated. This makes it possible to calculate the amount of CO produced by directly reducing their oxides from the mass of trace elements such as Si, Mn, P, Ti, and S in iron water. The calculation method is as follows.

[0074]

number

[0075] In this calculation, V2 represents the amount of CO produced by the direct reduction of oxides of trace elements such as Si, Mn, P, Ti, and S. m[Si] is the mass of Si in the iron water. m[Nm] is the mass of Mn in the iron water. m[P] is the mass of P in the iron water. m[Ti] is the mass of Ti in the iron water. m[S] is the mass of S in the iron water.

[0076] The amount of CO produced by the direct reduction of iron ore is calculated as the difference between the total amount of CO produced by direct reduction and the amount of CO produced by the direct reduction of trace element oxides. The calculation method is as follows: V3=V1-V2 Equation (11)

[0077] In this data, V3 represents the amount of CO produced by the direct reduction of iron ore, V1 represents the total amount of CO produced by direct reduction, and V2 represents the amount of CO produced by the direct reduction of trace element oxides.

[0078] The mass of iron in the iron water is determined based on the proportion of iron in the iron water's composition and the amount of iron water produced. The degree of direct reduction of the iron ore is then calculated using the amount of CO produced by the direct reduction of the iron ore, the mass of iron in the iron water, and the predetermined mass of iron in the hot-pressed iron mass. The calculation method is as follows.

[0079]

number

[0080] In this system, Rd is the degree of direct reduction of iron ore, V3 is the amount of CO produced by the direct reduction of iron ore, m[Fe] is the mass of iron in the iron water, and ml is the iron content of the hot-pressed iron ingot used in the blast furnace, i.e., the predetermined mass of iron in the hot-pressed iron ingot.

[0081] In this example, considering the reducing properties of trace element oxides, the amount of CO produced by the direct reduction of iron ore is determined by calculating the total amount of CO produced by direct reduction and the amount of CO produced by the direct reduction of trace element oxides. The accuracy of the direct reduction of iron ore is improved by calculating the degree of direct reduction of iron ore based on this amount of CO.

[0082] In step S140, the gas-liquid heat exchange coefficient is calculated based on the theoretical combustion temperature of the gas, the amount of Bosch gas, the Bosch gas components, the slag iron parameters, and the gas components after direct reduction at the direct reduction position.

[0083] In one embodiment of this application, heat exchange occurs between the iron-water and the gas, so the accuracy of predicting the iron-water temperature also depends on the gas-liquid heat exchange coefficient. The gas-liquid heat exchange coefficient can be calculated based on the theoretical combustion temperature of the gas, the amount of Bosch gas, the Bosch gas components, the slag iron parameters, and the gas components after direct reduction at the direct reduction position. The amount of gas after direct reduction is equal to the amount of gas at the top of the furnace, and the volume of CO in the gas after direct reduction is equal to the sum of the volumes of CO and CO2 in the gas at the top of the furnace. Also, the volume of H2 in the gas after direct reduction is equal to the sum of the volumes of H2 and H2O in the gas at the top of the furnace, or the volume of H2 in the gas at the top of the furnace. Furthermore, the volume of N2 in the gas after direct reduction is equal to the volume of N2 in the gas at the top of the furnace, or the volume of N2 in the gas at the top of the furnace. Therefore, the gas components after direct reduction can be determined based on the parameters of the gas at the top of the furnace. Alternatively, the gas components after direct reduction can be determined based on the gas parameters, the amount of Bosch gas, and the components of the gas at the top of the furnace.

[0084] In the embodiments of this application, the following procedure is performed before calculating the gas-liquid heat exchange coefficient. First, 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 calculated based on the amount and composition of the top gas. Here, the parameters of the top gas include its amount and composition. Next, the amount of top gas is taken as the amount of gas after direct reduction, the total amount of carbon monoxide and carbon dioxide is taken as the amount of carbon monoxide in the gas after direct reduction, the total amount of water and hydrogen is taken as the amount of hydrogen in the gas after direct reduction, and the amount of nitrogen is taken as the amount of nitrogen in the gas after direct reduction. Based on the amount of gas after direct reduction, the amount of carbon monoxide in the gas after direct reduction, the amount of hydrogen in the gas after direct reduction, and the amount of nitrogen in the gas after direct reduction, the gas composition after direct reduction is determined.

[0085] In this embodiment, the relationship between the furnace top gas and the gas after direct reduction allows for the accurate identification of the components of the gas after direct reduction.

[0086] First, calculate the volume of H2 in the top gas from the proportion of H2 in the top gas and the amount of top gas. Next, calculate the volume of H2O in the top gas. The sum of these two volumes is the total amount of H2 and H2O in the top gas. Furthermore, calculate the volume of CO in the top gas from the proportion of CO in the top gas and the amount of top gas. Also, calculate the volume of CO2 in the top gas from the proportion of CO2 in the top gas and the amount of top gas. The sum of these two volumes is the total amount of CO and CO2 in the top gas. Finally, calculate the volume of N2 in the top gas, i.e., the amount of N2, from the proportion of N2 in the top gas and the amount of top gas.

[0087] Subsequently, the amount of top gas is treated as the amount of gas after direct reduction, the total amount of CO and CO2 in the top gas is treated as the amount of CO in the gas after direct reduction, the total amount of H2O and H2 in the top gas is treated as the amount of H2 in the gas after direct reduction, and furthermore, the amount of N2 in the top gas is treated as the amount of N2 in the gas after direct reduction.

[0088] Finally, the proportion of H2 in the gas after direct reduction is determined from the amount of H2 in the gas after direct reduction and the amount of gas after direct reduction; the proportion of CO in the gas after direct reduction is determined from the amount of CO in the gas after direct reduction and the amount of gas after direct reduction; and the proportion of N2 in the gas after direct reduction is determined from the amount of N2 in the gas after direct reduction and the amount of gas after direct reduction. The proportion of H2, the proportion of CO, and the proportion of N2 in the gas after direct reduction are defined as the components of the gas after direct reduction.

[0089] In another embodiment of this application, the following steps are performed before calculating the gas-liquid heat exchange coefficient. First, the total amount of carbon monoxide and carbon dioxide in the top gas is calculated based on the amount and composition of the top gas. Here, the parameters of the top gas include the amount and composition of the top gas. Next, the amount of hydrogen and nitrogen in the Bosch gas is calculated based on the amount and composition of the Bosch gas. The amount of top gas is taken as the amount of gas after direct reduction, the total amount of carbon monoxide and carbon dioxide in the top gas is taken as the amount of carbon monoxide in the gas after direct reduction, the amount of hydrogen in the Bosch gas is taken as the amount of hydrogen in the gas after direct reduction, and the amount of nitrogen in the Bosch gas is taken as the amount of nitrogen in the gas after direct reduction. Based on the amount of gas after direct reduction, the amount of carbon monoxide in the gas after direct reduction, the amount of hydrogen in the gas after direct reduction, and the amount of nitrogen in the gas after direct reduction, the gas components after direct reduction are determined.

[0090] In this embodiment, the relationship between the furnace top gas, the Bosch gas, and the gas after direct reduction allows for the precise identification of the components of the gas after direct reduction.

[0091] First, the volume of CO in the top gas is calculated from the proportion of CO in the top gas and the amount of top gas. Next, the volume of CO2 in the top gas is calculated from the proportion of CO2 in the top gas and the amount of top gas. The sum of the volumes of CO and CO2 in the top gas is the total amount of CO and CO2 in the top gas. Next, the volume of H2 in the Bosch gas, i.e., the amount of H2 in the Bosch gas, is calculated from the proportion of H2 in the Bosch gas and the amount of Bosch gas. Furthermore, the volume of N2 in the Bosch gas, i.e., the amount of N2 in the Bosch gas, is calculated from the proportion of N2 in the Bosch gas and the amount of Bosch gas.

[0092] Next, the amount of top gas is defined as the amount of gas after direct reduction, the total amount of CO and CO2 in the top gas is defined as the amount of CO in the gas after direct reduction, the amount of H2 in the Bosch gas is defined as the amount of H2 in the gas after direct reduction, and the amount of N2 in the Bosch gas is defined as the amount of N2 in the gas after direct reduction.

[0093] Finally, the proportion of H2 in the gas after direct reduction is determined from the amount of H2 in the gas after direct reduction and the amount of gas after direct reduction; the proportion of CO in the gas after direct reduction is determined from the amount of CO in the gas after direct reduction and the amount of gas after direct reduction; and the proportion of N2 in the gas after direct reduction is determined from the amount of N2 in the gas after direct reduction and the amount of gas after direct reduction. The proportion of H2, the proportion of CO, and the proportion of N2 in the gas after direct reduction are defined as the components of the gas after direct reduction.

[0094] As an embodiment of this application, step S140 includes performing interpolation calculations on the furnace bellows gas components and the gas components after direct reduction to obtain the gas components of the drip zone; determining the gas-liquid heat exchange coefficient of the rotating area based on the equivalent particle size of the slag iron, the gas thermal conductivity of the rotating area, and the Nussell number of the rotating area; both the gas thermal conductivity of the rotating area and the Nussell number of the rotating area are determined based on the furnace bellows gas components and the gas theoretical combustion temperature; and determining the equivalent particle size of the slag iron based on the slag iron parameters; equivalent The gas-liquid heat exchange coefficient at the direct reduction position is determined by the particle size, the gas thermal conductivity at the direct reduction position, and the Nussel level at the direct reduction position. Both the gas thermal conductivity and Nussel level at the direct reduction position are determined based on the gas components and theoretical gas combustion temperature after direct reduction. The gas-liquid heat exchange coefficient in the dropping zone is determined by the equivalent particle size of the slag iron, the gas thermal conductivity of the dropping zone, and the Nussel level of the dropping zone. Both the gas thermal conductivity and Nussel level in the dropping zone are determined based on the gas components and theoretical gas combustion temperature of the dropping zone. In this embodiment, the dropping zone is the region between the rotating area and the direct reduction position. The gas components differ depending on the height of the dropping zone between the direct reduction position and the rotating area, and the gas-liquid heat exchange coefficient also differs depending on the gas components. Therefore, in order to improve the accuracy of molten iron temperature prediction, it is necessary to determine the gas-liquid heat exchange coefficient at different heights in the dropping zone.

[0095] In general terms, the gas-liquid heat exchange coefficient can be determined by the correction factor, the gas thermal conductivity coefficient, the equivalent slag particle size, and the Nusselt number. The calculation method for the gas-liquid heat exchange coefficient is as follows. h g-1 =γ·kg·Nu / dl Equation (13)

[0096] Among them, h g-1 γ is the gas-liquid heat exchange coefficient, γ is the correction factor, kg is the thermal conductivity coefficient of the gas, Nu is the Nuscell number, and dl is the equivalent particle size of the slag iron.

[0097] The method for calculating the number of Nussels is as follows: Nu = 2.0 + 0.6 (9 Rep) 1 / 2 Pr 1 / 3 Formula (14)

[0098] In this system, Nu represents the number of Nusels, Rep represents the number of Relos, and Pr represents the number of plants.

[0099] The method for calculating the Lero number is as follows: Rep = ρg·ds·ug / μg Equation (15)

[0100] In this context, Rep is the Lero number, ρg is the gas density, ds is the characteristic length, ug is the gas flow velocity, and μg is the gas viscosity.

[0101] The method for calculating the number of plants is as follows: Pr=ug·C G / kg formula (16) Among them, Pr is the number of plants, ug is the gas flow rate, and C G is the specific heat of the gas, and kg is the thermal conductivity of the gas.

[0102] As supplementary information, the thermal conductivity, density, viscosity, and specific heat of a gas are all related to the gas's composition and temperature. In particular, the thermal conductivity of a gas has the following relationship with its composition. kg = m CO1 k CO +m H21 k H2 +m N21 k N2 Formula (17)

[0103] Among them, kg is the thermal conductivity coefficient of the gas, m CO1 This is the proportion of CO in the gas, m H21 This is the proportion of H2 in the gas, m N21 k is the proportion of N2 in the gas. COis the thermal conductivity of CO, k H2 is the thermal conductivity of H2, k N2 is the thermal conductivity of N2.

[0104] The relationship between the density of the gas and the gas components is as follows. ρg = m CO1 ρ CO + m H21 ρ H2 + m N21 ρ N2 Equation (18)

[0105] Among them, ρg is the density of the gas, m CO1 is the proportion of CO in the gas, m H21 is the proportion of H2 in the gas, m N21 is the proportion of N2 in the gas, ρ CO is the density of CO, ρ H2 is the density of H2, ρ N2 is the density of N2.

[0106] The relationship between the viscosity of the gas and the gas components is as follows. μg = m CO1 μ CO + m H21 μ H2 + m N21 μ N2 Equation (19)

[0107] Among them, μg is the viscosity of the gas, m​​​​​​​​​​​​​​​​​​​​​​​​​​​​​​​​​​ Among them is the specific heat of the gas, m CO1 This is the proportion of CO in the gas, m H21 This is the proportion of H2 in the gas, m N21 This is the proportion of N2 in the gas, C CO The specific heat of CO is C H2 The specific heat of H2 is C N2 This is the specific heat of N2.

[0110] Conceptually, the procedure for determining the gas-liquid heat exchange coefficient in the nozzle rotation area is as follows:

[0111] First, the specific heats of CO, H2, and N2 are calculated based on the theoretical combustion temperature of the gas and the predetermined relationship between the specific heat of each substance and its temperature. Next, these specific heats, along with the proportions of CO, H2, and N2 in the Bosch gas components, are substituted into equation (20) to determine the gas specific heat in the nozzle rotation area. Furthermore, the viscosity of CO, H2, and N2 is calculated based on the theoretical combustion temperature of the gas and the predetermined relationship between the viscosity of each substance and its temperature. Then, these viscosities, along with the proportions of CO, H2, and N2 in the Bosch gas components, are substituted into equation (19) to determine the gas viscosity in the nozzle rotation area. First, the densities of CO, H2, and N2 are calculated based on the theoretical combustion temperature of the gas and the predetermined relationship between the density of each substance and its temperature. Next, these densities, along with the proportions of CO, H2, and N2 in the Bosch gas components, are substituted into equation (18) to determine the gas density in the nozzle rotation area. Furthermore, the thermal conductivity of CO, H2, and N2 is calculated based on the theoretical combustion temperature of the gas and the predetermined relationship between the thermal conductivity and temperature of each substance. By substituting these, along with the proportions of CO, H2, and N2 in the Bosch gas components, into equation (17), the thermal conductivity of the gas in the nozzle rotation area is calculated. Substituting the thermal conductivity and specific heat of the gas in the nozzle rotation area into equation (16) yields the number of plants in that region. Also, substituting the density and viscosity of the gas into equation (15) yields the Lelo number. Here, the gas flow velocity is calculated by dividing the amount of gas by the blast furnace cross-sectional area at the calculation location. The cross-sectional area is determined by the furnace type structure of the blast furnace, and the characteristic length is the equivalent particle size of the slag iron. This equivalent particle size is determined based on the iron-water density, liquid slag density, blast furnace type structure, and the amount of slag included in the slag iron parameter. Furthermore, substituting the number of plants and the Lelo number in the nozzle rotation area into equation (14) yields the Nussel number. By substituting the thermal conductivity of the gas in the nozzle rotation area and the Nussell number into equation (13), the gas-liquid heat exchange coefficient in the nozzle rotation area can be obtained. Here, the correction factor may be a predetermined value, an arbitrary number within the range of 0.2 to 0.5, or any other number; there are no restrictions here.

[0112] Similarly, following the method described above, the gas-liquid heat exchange coefficient at the direct reduction site is calculated based on the combustion temperature, slag iron parameters, and gas components after direct reduction in the gas theory. Details are omitted here.

[0113] The gas components of the dripping zone were calculated by interpolation between the components of the Bosch gas and the gas components after direct reduction. This gas component includes the gas components at different heights of the dripping zone. Using a similar method, the gas-liquid heat exchange coefficient at each height of the dripping zone was calculated using the theoretical combustion temperature of the gas, the slag iron parameters, and the gas components corresponding to the height of the dripping zone. This will not be described in detail here. Identifying the gas-liquid heat exchange coefficient at each height of the dripping zone further improves the accuracy of the iron-water temperature prediction.

[0114] In step S150, the iron-water temperature and gas temperature are determined again based on the gas-liquid heat exchange coefficient, the direct reduction degree of the iron ore, the theoretical combustion temperature of the gas, and the slag iron parameters. This process is continued until the first convergence condition is met, and the prediction of the iron-water temperature by the blast furnace is completed.

[0115] In the embodiments of this application, a preset temperature value can be set as the iron-water temperature after direct reduction, relative to the iron-water temperature at the location of the direct reduction blast furnace. Using the gas-liquid heat exchange coefficient, the degree of direct reduction of the iron ore, the theoretical combustion temperature of the gas, the iron-water temperature after direct reduction, and the slag iron parameter, the iron-water temperature and gas temperature are iteratively calculated based on the energy conservation relationship between the gas phase and the iron-water phase. This calculation is repeated until a first convergence condition is met to calculate the gas temperature at the direct reduction location and the iron-water temperature in the nozzle rotation region. Suggestively, the first convergence condition is when the number of iterations of the iterative calculation of the iron-water temperature and gas temperature satisfies a first preset number of iterations, or when both the iterative temperature difference of the gas temperature and the iterative temperature difference of the iron-water temperature are below a first preset temperature difference threshold, or any other convergence condition. There are no limitations here.

[0116] In the embodiment of this application, step S150 includes the following: The amount of heat required for direct reduction is calculated based on the iron water components and the degree of direct reduction of the iron ore. The slag iron parameters include the iron water components mentioned above. Using the gas phase temperature, the iron water phase temperature, the gas-liquid heat exchange coefficient, and the amount of heat required for direct reduction, the iron water temperature and gas temperature are determined separately based on the energy conservation laws of the gas phase and the iron water phase. This provides the iron water temperature in the nozzle rotation area before replacement, the iron water temperature in the outlet rotation area after replacement, the gas temperature after direct reduction before replacement, and the gas temperature after direct reduction after replacement. The initial value of the gas phase temperature is the theoretical combustion temperature of the gas, and the initial value of the iron water phase temperature is the iron water temperature after direct reduction, which is set in advance. The difference between the iron-water temperature in the nozzle rotation area before replacement and the iron-water temperature in the nozzle rotation area after replacement is defined as the iron-water temperature replacement difference, and the difference between the gas temperature after direct reduction before replacement and the gas temperature after direct reduction after repetition is defined as the gas temperature repetition difference. If both the iron-water temperature repetition difference and the gas temperature repetition difference are less than or equal to a first predetermined temperature difference threshold, the first convergence condition is met, and the iron-water temperature in the nozzle rotation area after repetition is taken as the final prediction result of the iron-water temperature prediction.

[0117] In this embodiment, the law of conservation of energy has the following characteristics: The consumption of heat resulting from the direct reduction of iron ore and oxides of trace elements such as Si, Mn, S, P, and Ti is included in the change in gas energy. Furthermore, the law of conservation of energy is related to the flow rate, heat capacity, and density of the gas and slag iron. The calculation range for energy conservation is from the region where the iron slag begins to melt to the surface of the molten pool in the furnace, and the melting temperature of the iron slag is 1300-1400°C. Therefore, using the laws of conservation of energy for the gas phase and the iron-water phase, the iron-water temperature and gas temperature are determined separately based on the gas phase temperature, the iron-water phase temperature, the gas-liquid heat exchange coefficient, and the amount of heat required for direct reduction. In this case, the equation relating to the conservation of energy for the gas phase is as follows.

[0118]

number

[0119] In this equation, ρg is the gas density, ug is the gas flow velocity, Cg is the specific heat of the gas, Tg is the phase temperature of the gas, z is the length of the solving grid, and h g-1 is the heat exchange coefficient between gas and liquid, A is the specific surface area, Tl is the phase temperature of iron and water, Q is the specific surface area, and Q is the specific surface area. Rd is the amount of heat required for direct reduction, and Va is the volume of the solution region.

[0120] The relationship between iron and water energy conservation is as follows:

[0121]

number

[0122] In this equation, ρl is the density of iron water, ul is the flow velocity of iron water, Cl is the specific heat of iron water, Tl is the phase temperature of iron water, Tg is the temperature of the gas phase, z is the length of the solving grid, h g-1 is the heat exchange coefficient between gas and liquid, and A is the specific surface area.

[0123] I would like to add that, as the methods for calculating the gas density and specific heat are described in the aforementioned embodiment, I will not explain them again here. The specific surface area can be calculated based on the equivalent particle size of the slag iron. The volume of the decomposition area can be set in advance. The gas flow rate, slag iron flow rate, and equivalent particle size of the slag iron all depend on the furnace type of the blast furnace, and can therefore be determined in advance according to the structure of the furnace type. The amount of heat required for direct reduction can be calculated based on the degree of direct reduction of the iron ore and the iron-water component contained in the slag iron parameters.

[0124] Please refer to Table 2. Table 2 is a table of direct reduction chemical reactions and thermal effects in specific examples of this application. As shown in Table 2, oxides of elements such as Fe, Si, Mn, P, Ti, and S are converted into reduction products such as Fe, Si, Mn, P, Ti, and S by direct reduction reactions.

[0125] [Table 2]

[0126] Therefore, the method for calculating the amount of heat required for direct reduction is as follows:

[0127]

number

[0128] Among them, Q Rd ΔH is the amount of heat consumed in the direct reduction. Fe Fe is the thermal effect in the direct reduction reaction of iron, Rd is the degree of direct reduction of iron ore, m[Fe] is the mass of iron in iron water, M is the ore ratio, ω Fe ω is the mass fraction of Fe in the mixed ore. FeS ΔH is the mass fraction of FeS (ferrous sulfide) in the mixed ore. Si ΔH is the thermal effect in the direct reduction reaction of Si, m[Si] is the mass of Si in iron water, and ΔH Mn ΔH is the thermal effect in the direct reduction reaction of Mn, m[Mn] is the mass of Mn in iron water, and ΔH P ΔH is the thermal effect in the direct reduction reaction of element P, m[P] is the mass of P in iron water, and ΔH Ti ΔH is the thermal effect in the direct reduction reaction of Ti, m[Ti] is the mass of Ti in iron water, and ΔH S is the thermal effect in the direct reduction reaction of element S, and m[S] is the mass of S in iron water. The ore ratio, the mass fraction of Fe, and the mass fraction of FeS can be set in advance.

[0129] Conceptually, the dripping zone is divided into a grid in the height direction, and the theoretical combustion temperature of the gas is set as the initial value for the gas phase temperature, and the iron water temperature after direct reduction is set as the initial value for the iron water phase temperature. Replacement calculations are performed using equations (21) and (22), and the results are obtained. The obtained results include the gas temperature after direct reduction before replacement, the iron water temperature in the nozzle rotation area before replacement, the gas temperature after direct reduction after replacement, and the iron water temperature in the nozzle rotation area after replacement. The first convergence condition is satisfied if the difference between the gas temperature after direct reduction before replacement and the gas temperature after direct reduction after iteration (gas temperature iteration difference), and the difference between the iron water temperature in the nozzle rotation area before replacement and the iron water temperature in the nozzle rotation area after replacement (iron water temperature iteration difference), are both less than or equal to the first preset temperature difference threshold. The iron water temperature in the nozzle rotation area after replacement processing is taken as the final prediction result for the iron water temperature prediction. Conversely, the replacement calculation is performed again using equations (21) and (22), and this is repeated until the second convergence condition is met. The final iron-water temperature in the nozzle rotation area after the replacement is taken as the final prediction result for the iron-water temperature. Conceptually, the iron-water temperature after direct reduction is assumed to be 1350°C, or one of the temperature values ​​between 1300 and 1500°C, or some other temperature value. The second pre-set temperature difference threshold is set to 0.01°C, or one of the temperature values ​​between 0.01 and 0.05°C, or some other temperature value. There are no restrictions here.

[0130] Using the laws of conservation of energy in the gas phase and the iron-water phase, the iron-water temperature and gas temperature are determined by recalculation based on the theoretical combustion temperature of the gas, the direct reduction degree of the iron ore, and the gas-liquid heat exchange coefficients at different altitudes. Furthermore, convergence is confirmed by comparing the errors before and after the recalculation, thereby further improving the accuracy of the iron-water temperature prediction.

[0131] As a specific example of this application, 2300m 3 As an example, the coefficient is 3.7T / (d·m 3 The proposed solution for this application will be further explained by [reference].

[0132] The following is a prediction of the iron-water temperature in a typical blast furnace without blow-up gas.

[0133] Please refer to Table 3. Table 3 is a table of raw fuel parameters in one embodiment of this application. As shown in Table 3, the raw fuel parameters include the components and amount used of coke, and the components and amount used of blown coal. Here, the components of coke refer to the proportions of C, H, O, N, S, volatile matter, and ash in the coke, and the components of blown coal refer to the proportions of C, H, O, N, S, volatile matter, and ash in the blown coal.

[0134] [Table 3]

[0135] Please refer to Table 4. Table 4 is a table of drum air parameters in a specific embodiment of this application. As shown in Table 4, the drum air parameters include drum air volume, drum air temperature, drum air humidity, and oxygen concentration.

[0136] [Table 4]

[0137] Please refer to Table 5. Table 5 is a parameter table for the furnace top gas in a specific embodiment of this application. As shown in Table 5, the parameters for the furnace top gas include the amount of furnace top gas and the proportions of CO, CO2, H2, and N2 in the furnace top gas.

[0138] [Table 5]

[0139] Please refer to Table 6. Table 6 is a table of slag iron parameters in a specific example of this application. As shown in Table 6, the slag iron parameters include the amount of slag and the proportions of Fe, C, Si, Mn, P, S, and Ti in the iron water.

[0140] [Table 6]

[0141] According to Table 4, the sensible heat Q1 injected into the blast furnace is calculated to be 2.00 GJ / t, and the amount of oxygen that can be supplied for the combustion of pulverized coal and coke within the rotating area of ​​the blast furnace is 239.20 m³. 3 The total heat Q2 released in the rotating area by the combustion of pulverized coal, coke, or other reactions was calculated to be 2.41 GJ / t. The coke temperature entering the combustion zone is approximately 1400°C, the amount of coke burned at the nozzle is 173.46 kg / t, and the sensible heat Q4 from the coke in the rotating area is 0.29 GJ / t. Therefore, the total heat Q in the nozzle rotating area is 4.70 GJ / t. Based on Tables 3 and 4, and using the law of conservation of energy in the nozzle rotating area, the CO, H2, and N2 content in the furnace belly gas is 41.67%, 6.95%, and 51.38%, respectively, and the amount of furnace belly gas is 1193.88 m³. 3 The value is / t. Therefore, the theoretical combustion temperature of the gas is calculated to be 2252°C.

[0142] Based on Tables 5 and 6, the degree of direct reduction Rd of the iron ore is obtained to be 0.451. The CO, H2, and N2 content in the gas after direct reduction is 48.92%, 6.09%, and 44.99%, respectively. Using Table 6, the theoretical combustion temperature, and the Bosch gas volume, the Reynolds number Rep of the furnace tube is calculated to be 30883, the plant number Pr is 0.362, and the Nussels number Nu is 227.54. Therefore, the gas-liquid heat exchange coefficient h between the gas and the slag iron droplets is calculated to be 0.451. g-1 It is 26.89 W / (m 2 The result is (K). By recalculating under the law of conservation of energy, the iron-water temperature in the slag nozzle rotation area is calculated to be 1521.20°C, and the measured average iron-water temperature of the blast furnace under the corresponding operating conditions is close to 1520°C. The gas temperature after direct reduction is 1897.20°C.

[0143] During the blast furnace smelting process, gas injection occurs, causing changes in the parameters of the blast furnace blast and furnace top. The following is a prediction of the iron-water temperature in the blast furnace under gas injection conditions.

[0144] Please refer to Table 7. Table 7 is a table of gas injection parameters in specific embodiments of this application. As shown in Table 7, the gas injection parameters include the gas injection amount and the proportions of H2, CO, CO2, CH4, nitrogen, and O2 in the injected gas.

[0145] [Table 7]

[0146] Please refer to Table 8. Table 8 is a table of drum airflow parameters for gas injection conditions in specific embodiments of this application. As shown in Table 8, the drum airflow parameters for gas injection conditions, namely drum airflow rate, drum airflow humidity, and oxygen-rich percentage, differ from the values ​​in Table 4.

[0147] [Table 8]

[0148] Please refer to Table 9. Table 9 is a table of furnace top gas parameters under specific gas injection conditions in the present invention. As shown in Table 9, the components and amount of furnace top gas under gas injection conditions differ from the values ​​in Table 5.

[0149] Based on Tables 3, 7, and 8, and applying the law of conservation of matter in the nozzle rotation area, the CO, H2, and N2 content in the Bosch gas is 43.71%, 9.61%, and 46.68%, respectively, and the Bosch gas volume is 1197.4 m³. 3 The result is obtained as / t. From this, the theoretical combustion temperature of the gas was calculated to be 2163°C. From Tables 9 and 6 and the composition of the Bosch gas, the degree of direct reduction of iron ore Rd was obtained to be 0.39. The CO, H2, and N2 content in the gas after direct reduction was 49.90%, 8.55%, and 41.54%, respectively. The gas-liquid heat exchange coefficient hg-l between the gas and the slag iron droplets was 28.654 W / (m 2 It is calculated as (K). Therefore, by the energy conservation calculation, it can be seen that the iron-water temperature is 1510.61°C and the gas temperature after direct reduction is 1753.63°C.

[0150] Please refer to Figure 2. Figure 2 is a diagram of the water temperature prediction system in a blast furnace ironmaking process as shown in an embodiment of this application. This system consists of a data acquisition subsystem, a physical property database, a thermal equilibrium calculation subsystem for the blowhole area, a direct reduction calculation subsystem, and an iterative calculation subsystem. The data acquisition subsystem acquires smelting data in the blast furnace smelting process. This includes raw fuel parameters, drum wind parameters, gas injection parameters, furnace top gas parameters, and slag iron parameters. The physical property database collects and stores specific heat, density, dynamic viscosity, and thermal conductivity of various gases, and specific heat, density, and thermal conductivity of various solid phase materials. The thermal equilibrium calculation subsystem for the blowhole area calculates the thermal equilibrium state of the blowhole area. The direct reduction calculation subsystem calculates the degree of direct reduction of iron ore. The iterative calculation subsystem determines the convergence of the iron-water temperature and calculates the iron-water temperature value.

[0151] Please refer to Figure 3. Figure 3 is a flow diagram of the water and iron temperature prediction system for the blast furnace ironmaking process in the embodiment shown in Figure 2. As shown in Figure 3, the water and iron temperature prediction flow for the blast furnace ironmaking process includes the following process.

[0152] 1. Acquire smelting data in real time during the blast furnace smelting process. Smelting data includes raw fuel parameters, blast pressure parameters, gas injection parameters, top gas parameters, and slag iron parameters. 2. Based on the raw fuel parameters, blower parameters, and gas injection parameters, the theoretical combustion temperature of the gas, the Bosch gas volume, and the Bosch gas components are calculated for each nozzle rotation area. 3. Based on the parameters of the furnace top gas, the slag iron parameters, and the composition of the Bosch gas, calculate the degree of direct reduction of the iron ore, the composition of the gas after direct reduction, and the amount of gas after direct reduction. 4. Based on the physical phase database, theoretical combustion temperature of the gas, Bosch gas volume, and slag-iron parameters, calculate the gas-liquid heat exchange coefficient between the gas, iron-water, and slag. 5. Based on the law of conservation of heat, perform replacement calculations to determine the iron-water temperature and the temperature of the direct reduction gas after direct reduction.

[0153] For the flowchart in Figure 3, please refer to the detailed procedures described in each of the embodiments above. A detailed explanation will not be provided here. The technical configuration of this embodiment uses smelting data acquired in real time during the blast furnace smelting process to calculate the theoretical combustion temperature of the gas in the blowhole rotation area, the degree of reduction of the iron ore, and the gas-liquid heat exchange coefficient. This allows for the separate determination of the iron-water temperature and gas temperature, enabling the prediction of the iron-water temperature in blast furnace smelting. This provides the iron-water temperature of the blast furnace smelting process under various operating conditions, which helps operators determine the thermal state inside the blast furnace and the reduction state of the ore. This mechanism provides assurance for the stable operation of conventional and low-carbon blast furnaces.

[0154] Please refer to Figure 4. Figure 4 is a flowchart of a blast furnace iron water temperature prediction device shown in an embodiment of this application. As shown in Figure 4, the blast furnace iron water temperature prediction device of this embodiment includes the following configuration.

[0155] The smelting data acquisition module 410 consists of raw fuel parameters, drum blast parameters, gas injection parameters, top gas parameters, and slag iron parameters in the blast furnace smell process. The theoretical combustion temperature determination module 420 calculates the total heat, Bosch gas volume, and Bosch gas components of the nozzle rotation area based on the raw fuel parameters, drum blast parameters, and gas injection parameters, and uses these to determine the theoretical combustion temperature of the gas in the nozzle rotation area. The direct reduction degree determination module 430 is configured to determine the direct reduction degree of iron ore based on the top gas parameters, slag iron parameters, Bosch gas volume, and Bosch gas components. The heat exchange coefficient determination module 440 is configured to calculate the gas-liquid heat exchange coefficient based on the theoretical combustion temperature of the gas, the components of the Bosch gas, the slag iron parameters, and the components of the gas after direct reduction at the direct reduction position. The components of the gas after direct reduction are determined based on the top gas parameters, or based on the top gas parameters, Bosch gas volume, and Bosch gas components. The iterative calculation module 450 uses the gas-liquid heat exchange coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of the gas, and the slag iron parameter to perform replacement calculations for the iron-water temperature and gas temperature. The calculation is repeated until the first convergence condition is met, completing the prediction of the iron-water temperature in blast furnace steelmaking.

[0156] What I would like to explain here is that the blast furnace iron water temperature prediction device and prediction method provided in the above-mentioned embodiment are based on the same concept, and the operation methods of each module and unit have already been explained in detail in the embodiment of the method, so they will not be repeated here. In actual operation, it is possible to divide these functions into different functional modules as needed, and by dividing the internal structure of the device into multiple functional modules, all or part of the above functions can be realized. There are no limitations on this point here.

[0157] This embodiment provides an electronic device equipped with one or more processors. This electronic device is provided with a storage device for storing one or more programs, and when these programs are executed by the processors, the electronic device realizes the iron water temperature prediction method for blast furnace steelmaking provided in each of the above embodiments.

[0158] Please refer to Figure 5. Figure 5 is a structural diagram of an electronic device shown as an embodiment of this application. It should be noted that the electronic device 500 shown in Figure 5 is merely an example, and there are no limitations on the function or scope of use of the embodiment of this application.

[0159] As shown in Figure 5, the electronic device 500 includes a processor 501, a memory 502, and a communication bus 503. The communication bus 503 connects the processor 501 and the memory 502, and the processor 501 executes a computer program stored in the memory 502 to implement one or more of the methods in the above embodiment.

[0160] This embodiment provides a computer-readable storage medium that stores a computer program executed by a computer processor. This program executes the iron-water temperature prediction method using a blast furnace described above. This medium may be built into the electronic device described in the previous embodiment, or it may be a separate medium not mounted on an electronic device.

[0161] This embodiment provides a computer program product or computer program that includes computer commands recorded on a computer-readable storage medium. The processor of the computer device reads the computer commands from the computer-readable storage medium and executes the blast furnace iron water temperature prediction method provided in each of the above embodiments.

[0162] The electronic device provided in this embodiment comprises a processor, memory, transceiver, and communication interface. The memory and communication interface are connected to the processor and transceiver and communicate with each other. The memory is for storing computer programs, and the communication interface is for communication. The processor and transceiver are for executing computer programs, causing the electronic device to perform each step of the above method.

[0163] In this embodiment, the storage device may include random access memory (RAM), and may also include non-volatile memory such as at least one disk storage device.

[0164] The processors mentioned above are general-purpose processors such as central processing units (CPUs) and network processors (NPs). They also include programmable logic devices such as digital signal processing devices (DSPs), application-specific integrated circuits (ASICs), and field-programmable gate arrays (FPGAs), as well as separate gates, transistor logic devices, and separate hardware components.

[0165] The computer-readable storage medium in this embodiment will be understandable to engineers in this field. All or part of the processes in each of the above method embodiments are executable by hardware associated with a computer program. This program is stored on a computer-readable storage medium. During execution, the steps included in each of the above method embodiments are performed. The storage medium includes various media capable of storing program code, such as ROM (read-only memory), RAM (random access memory), magnetic disks, and optical disks.

[0166] The embodiments described above are merely illustrative of the principles and effects of this application and do not limit it. Those familiar with the art in this field may modify or alter the embodiments as long as they do not contradict the spirit and scope of this application. Therefore, all modifications, alterations, or changes made by those with ordinary skill in the art without departing from the spirit and technical ideas disclosed herein are included in the claims of this application.

Claims

1. This is a method for predicting the iron-water temperature obtained in a single type of blast furnace smelting, and the smelting method is characterized by including the following processes. The raw fuel parameters, drumming parameters, gas injection parameters, top gas parameters, and slag iron parameters in the blast furnace smelting process are obtained. Based on the raw fuel parameters, drum air parameters, and coal gas injection parameters, the total heat received in the nozzle rotation area, the amount of Bosch gas, and the composition of the Bosch gas are calculated. Then, the theoretical combustion temperature of the gas in the nozzle rotation area is determined using the total calorific value. The degree of direct reduction of iron ore is determined based on the parameters of the furnace top gas, the slag iron parameters mentioned above, the amount of Bosch gas, and the Bosch gas components. The gas-liquid heat exchange coefficient is calculated based on the theoretical combustion temperature of the gas, the components of the Bosch gas described above, the slag iron parameters described above, and the gas components after direct reduction at the direct reduction position. The gas components after direct reduction described above are determined based on the parameters of the furnace top gas, or the gas components directly reduced described above are determined based on the furnace top gas parameters, the amount of Bosch gas, and the components of the Bosch gas. Based on the gas-liquid heat exchange coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of coal gas, and the slag iron parameters described above, the iron water temperature and coal gas temperature are repeatedly determined until the first convergence condition is met, and the iron water temperature in blast furnace steelmaking is predicted.

2. A method for predicting the temperature of iron water obtained in blast furnace smelting as described in claim 1, which involves calculating the total heat generation amount, Bosch gas amount, and Bosch gas components received by the nozzle rotation area based on raw fuel parameters, drum wind parameters, and gas injection parameters, and using these to calculate the theoretical gas combustion temperature of the nozzle rotation area, and includes the following process. Based on raw fuel parameters, blast parameters, and coal gas injection parameters, the volume of gas participating in the chemical reaction, the volume of gas not participating in the reaction, and the volume of gas produced by the chemical reaction are calculated in the nozzle rotation area. The heat generated by the chemical reaction in the blast outlet rotation area is calculated based on the volume of gas participating in the chemical reaction. The total heat generated is then calculated based on the heat generated by the coke, blast, gas, and chemical reaction in this rotation area. The heat generated by the coke is calculated based on the raw fuel parameters, the blast heat based on the blast parameters, and the gas heat based on the gas injection parameters. The amount and composition of Bosch gas are calculated based on the volume of gas produced by the chemical reaction and the volume of gas that does not participate in the chemical reaction. Based on the amount of Bosch gas, its composition, and total heat gain, the theoretical combustion temperature of the gas is repeatedly determined until the second convergence condition is met, and finally the theoretical combustion temperature is calculated.

3. The method for predicting the temperature of iron water obtained in blast furnace smelting as described in claim 2 is characterized by calculating the total amount of heat received from the heat generated by coke, the heat generated by the drum blast, the heat generated by the gas, and the heat released by chemical reactions in the aforementioned nozzle rotation region, and the method includes the following: Based on pre-set coke temperature and coke composition, the specific heat of the coke is calculated, and this specific heat and the amount of coke used are used to calculate the calorific value of the coke. Here, the raw fuel parameters include coke composition and the amount of coke used. The specific heat of the drumhead is determined based on the drumhead temperature and drumhead components, and the specific heat of the drumhead is calculated using this specific heat, drumhead volume, and drumhead temperature. Here, the drumhead parameters include drumhead components, drumhead temperature, and drumhead volume. The specific heat of the blown gas is calculated based on the pre-set temperature and composition of the blown gas. The specific heat of the blown gas is then calculated using this specific heat, the temperature of the blown gas, and the amount of blown gas injected. The injection parameters for blown gas include the components and injection volume of the blown gas.

4. A method for predicting the temperature of iron water obtained in blast furnace smelting as described in claim 2, characterized in that, based on the amount of Bosch gas, the components of the Bosch gas, and the total heat amount, the theoretical combustion temperature of the gas is repeatedly determined until a second convergence condition is met, and the theoretical combustion temperature of the gas is calculated, and includes the following process. Based on the composition of the Bosch gas and a predetermined theoretical combustion temperature, the initial specific heat of the Bosch gas in the nozzle rotation area is calculated. Then, using the total heat, the amount of Bosch gas, and the initial specific heat of the Bosch gas, the initial theoretical combustion temperature is calculated. The initial theoretical combustion temperature of the gas is used as the theoretical combustion temperature of the gas before replacement. Based on the Bosch gas components and the theoretical combustion temperature of the gas before replacement, the specific heat of the replacement Bosch gas in the nozzle rotation area is calculated. Subsequently, the theoretical combustion temperature of the gas after replacement is calculated using the total heat, the amount of Bosch gas, and the specific heat of the replacement Bosch gas. The difference between the theoretical gas combustion temperature before and after the change is calculated, and the temperature difference in the theoretical gas combustion temperature is determined. If the temperature difference between the above-mentioned theoretical gas combustion temperatures is less than or equal to a predetermined second temperature difference threshold, the second convergence condition is met, and the theoretical gas combustion temperature after the change is adopted as the theoretical gas combustion temperature. If the temperature difference of the theoretical combustion temperature exceeds a predetermined second temperature difference threshold, the theoretical combustion temperature is calculated by using the amount of Bosch gas, gas components, total heat, and the theoretical combustion temperature after the change, until the second convergence condition is met.

5. A method for predicting the iron water temperature obtained in blast furnace smelting according to any one of claims 1 to 4. Its features include determining the degree of direct reduction of iron ore based on furnace top gas parameters, slag iron parameters, Bosch gas amount, and Bosch gas components, and includes the following process. Based on the amount and components of the Bosch gas, the amount of carbon monoxide in the Bosch gas is calculated. Based on the amount and components of the top gas, the total amount of carbon monoxide and carbon dioxide in the top gas is calculated. Based on this amount of carbon monoxide in the Bosch gas and the total amount of carbon monoxide and carbon dioxide in the top gas, the total amount of carbon monoxide produced directly by reduction is calculated. The parameters for the top gas include the amount and components of the top gas. Based on the composition and production volume of the iron water, the mass of trace elements and the mass of iron in the iron water are calculated. Then, using the mass of these trace elements in the iron water, the amount of carbon monoxide produced by the direct reduction of the oxides of the trace elements is calculated. Using the total amount of carbon monoxide produced by direct reduction and the amount of carbon monoxide produced by the direct reduction of the trace element oxides mentioned above, the amount of carbon monoxide produced by the direct reduction of iron ore is calculated. In this case, the slag iron parameter includes the composition and production volume of the iron water. The degree of direct reduction of iron ore is calculated based on the amount of carbon monoxide produced by the direct reduction of iron ore, the mass of iron in the iron water, and the mass of iron in a pre-set heat-pressure block.

6. A method for predicting the temperature of iron water obtained in blast furnace smelting according to any one of claims 1 to 4, characterized in that it includes the following process before determining the gas-liquid heat exchange coefficient. Based on the amount and composition of the top gas, 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 calculated. These top gas parameters include the amount and composition of the top gas. The amount of gas at the top of the furnace is defined 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 defined 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 defined as the amount of hydrogen in the gas after direct reduction, and furthermore, the amount of nitrogen in the gas at the top of the furnace is defined as the amount of nitrogen in the gas after direct reduction. The gas composition after direct reduction is determined based on the amount of gas produced, and the amounts of carbon monoxide, hydrogen, and nitrogen contained within it.

7. A method for predicting the temperature of iron water obtained in blast furnace smelting according to any one of claims 1 to 4, characterized in that the method includes the following process before determining the gas-liquid heat exchange coefficient. The total amount of carbon monoxide and carbon dioxide in the top gas is calculated based on the amount and composition of the top gas. The parameters for the top gas here include the amount of top gas and its composition. Based on the amount of Bosch gas and its components, the amount of hydrogen and nitrogen in the Bosch gas are calculated. The amount of top gas is defined as the amount of gas after direct reduction, the total amount of carbon monoxide and carbon dioxide in the top gas is defined as the amount of carbon monoxide in the directly reduced gas, the amount of hydrogen in the Bosch gas is defined as the amount of hydrogen in the directly reduced gas, and furthermore, the amount of nitrogen in the Bosch gas is defined as the amount of nitrogen in the directly reduced gas. The directly reduced gas components are determined based on the amount of gas directly reduced and the amounts of carbon monoxide, hydrogen, and nitrogen contained within it.

8. A method for predicting the temperature of iron water obtained in blast furnace smelting according to any one of claims 1 to 4, characterized by calculating the gas-liquid heat exchange coefficient based on the theoretical combustion temperature of the gas, Bosch gas components, slag iron parameters, and the gas components after direct reduction at the direct reduction site, and includes the following process. The gas components in the drop zone are calculated by interpolating between the Bosch gas components and the gas components after direct reduction. The gas-liquid heat exchange coefficient in the rotating area is calculated based on the equivalent particle size of slag iron and iron, the thermal conductivity of the gas in the nozzle rotation area, and the Nuscell number. Here, the thermal conductivity of the gas and the Nuscell number in the nozzle rotation area are determined based on the composition of the Bosch gas and the theoretical combustion temperature of the gas. The equivalent particle size of slag iron and iron is determined based on the parameters of slag iron and iron. The thermal conductivity coefficient and Nuscell number of the gas at the direct reduction site are determined based on the gas components after direct reduction and the theoretical combustion temperature of the gas. These thermal conductivity coefficient and Nuscell number of the gas determine the gas-liquid heat exchange coefficient at the direct reduction site, based on the equivalent particle size of the slag iron at the direct reduction site, the thermal conductivity coefficient of the gas at the direct reduction site, and the Nuscell number at the direct reduction site. The gas-liquid heat exchange coefficient in the dropping zone is calculated based on the equivalent particle size of the slag iron, the thermal conductivity of the gas in the dropping zone, and the Nuscell number in the dropping zone. The thermal conductivity and Nuscell number of the gas in the dropping zone are determined based on the gas components and theoretical combustion temperature of the gas in the dropping zone.

9. The method for predicting the temperature of iron water obtained in blast furnace smelting as described in claim 8 is characterized by repeatedly determining the iron water temperature and gas temperature until a first convergence condition is met, based on the gas-liquid heat exchange coefficient, the degree of direct reduction of iron ore, the theoretical combustion temperature of the gas, and the slag iron parameter, and predicting the temperature of the iron water, and includes the following process. Based on the composition of the iron water and the degree of direct reduction of the iron ore, the amount of heat required for direct reduction is calculated, and the iron water composition is included in the slag iron parameter. Based on the gas phase temperature, iron-water phase temperature, gas-liquid heat exchange coefficient, and the amount of heat required for direct reduction, the iron-water temperature and gas temperature changes are calculated based on the principle of energy conservation in the gas and molten iron phases. This allows for the calculation of the iron-water temperature in the nozzle rotation area before the change, the iron-water temperature after the change, the gas temperature after direct reduction before the change, and the gas temperature after direct reduction after the change. The initial value of the gas phase temperature is set to the theoretical combustion temperature of the gas, and the initial value of the iron-water phase temperature is set to the iron-water temperature after direct reduction. The difference between the iron-water temperature in the nozzle rotation area before replacement and the iron-water temperature in the nozzle rotation area after replacement is defined as the iron-water temperature change temperature difference. Furthermore, the difference between the gas temperature after direct reduction before replacement and the gas temperature after direct reduction after replacement is defined as the gas temperature change temperature difference. If both the above-mentioned difference in iron-water temperature and the above-mentioned difference in gas temperature are below a predetermined first temperature difference threshold, the first convergence condition is met, and the iron-water temperature in the rotation area of ​​the nozzle after replacement is taken as the final result of the iron-water temperature prediction.

10. This is a device for predicting the water temperature of blast furnace wrought iron, and the device consists of the following components. The smelting data acquisition module is used to acquire raw fuel parameters, drum blast parameters, gas injection parameters, top gas parameters, and slag iron parameters in the blast furnace smelting process. The theoretical combustion temperature calculation module calculates the total heat, Bosch gas volume, and Bosch gas components of the nozzle rotation area based on raw fuel parameters, drum air parameters, and gas injection parameters. These data determine the theoretical combustion temperature of the gas in the nozzle rotation area. The degree of direct reduction determines the module. The degree of direct reduction of iron ore is calculated based on furnace top gas parameters, slag iron parameters, Bosch gas volume, and Bosch gas composition. The heat exchange coefficient determines the module. The heat exchange coefficient between gas and liquid is calculated based on the theoretical gas combustion temperature, Bosch gas components, slag iron parameters, and the gas components after direct reduction at the direct reduction position. The gas components after direct reduction may be determined based on the parameters of the furnace top gas, or they may be determined by the furnace top gas parameters, Bosch gas volume, and Bosch gas components. The replacement calculation module repeatedly calculates the iron-water temperature and gas temperature until a second convergence condition is met, based on the gas-liquid heat exchange coefficient, the direct reduction degree of iron ore, the theoretical combustion temperature of coal gas, and slag iron parameters, thereby enabling the prediction of the blast furnace smelting iron water temperature.

11. It is a type of electronic device and is characterized by including the following devices: One or more memory devices. The memory device stores one or more programs. When the program is executed by one or more processors, the electronic device realizes the prediction of the blast furnace wrought iron water temperature as described in any of claims 1 to 9.

12. A storage medium that can be read by one type of computer, wherein when a computer program written on it is executed by the computer's processor, the electronic device realizes the prediction of the blast furnace wrought iron water temperature as described in any of claims 1 to 9.

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