Theoretical combustion temperature prediction method and device for blast-furnace tuyere

Abstract

The invention discloses a theoretical combustion temperature prediction method and device for a blast-furnace tuyere. The method comprises the steps that input material parameters, input material types and output material types of a rotation area are obtained; determining the amount of substance of an output substance based on the input substance parameter, the output substance type, coke consumption and a plurality of chemical reaction paths; determining total chemical reaction heat based on the input material parameters and the plurality of chemical reaction paths; based on the amount of substance of the input substance, the total chemical reaction heat, the input substance parameters, the amount of substance of the output substance, the phase change latent heat, the solid crystal transition heat and a pre-established molar constant pressure heat capacity model, determining the theoretical combustion temperature of the convolution area; according to the method, accurate modeling of the thermodynamic process of the gyration area and high-precision calculation of the combustion temperature under the condition of multiple injection media can be achieved, and the accuracy and applicability of energy balance analysis of the blast-furnace tuyere gyration area are improved.

Description

Technical Field

[0001] This invention relates to the field of thermal engineering and thermal energy calculation technology in metallurgical processes, and in particular to a method and apparatus for predicting the theoretical combustion temperature of a blast furnace tuyeres. Background Technology

[0002] The steel industry is facing increasingly severe pressure to conserve energy, reduce emissions, and lower carbon emissions. Traditional blast furnaces, using coke and pulverized coal as the main heating and reducing media, have high energy consumption and large carbon emissions, making them difficult to meet the requirements of low-carbon metallurgical development. To achieve green and efficient ironmaking, the steel industry is gradually exploring hydrogen-enriched blast furnace technology, which replaces part of the carbon source with hydrogen-rich gas, and top gas recycling oxygen blast furnace (TGR-OBF) technology, which recovers decarburized top gas, mixes it with oxygen, and then injects it back into the tuyeres. Both of these new processes achieve energy conservation and carbon reduction by adjusting the injection medium and fuel structure, enabling the tuyeres to form a multi-medium injection state, thereby significantly changing the thermodynamic characteristics of the vortex zone. This makes the accurate calculation of the theoretical combustion temperature a key issue in the control of the blast furnace smelting process.

[0003] Existing methods for calculating the theoretical combustion temperature of blast furnaces mainly include empirical formula methods and adiabatic heat balance methods. Empirical formula methods typically construct empirical models based on historical operating data and simplified mechanistic parameters. While the calculation process is relatively simple, its applicability is limited, and it is difficult to accurately reflect the thermodynamic characteristics under different injection media and operating conditions. Adiabatic heat balance methods, based on the principle of energy conservation, solve for the combustion temperature through an iterative approach, exhibiting high theoretical rigor. However, during modeling, they often neglect sensible heat, latent heat, and solidification transformation heat effects, and frequently approximate the relationship between heat capacity and temperature using constant or average heat capacity. This leads to systematic biases in the calculation results, making it difficult to meet the high-precision calculation requirements under multi-media injection conditions.

[0004] Furthermore, key factors such as the proportion of unburned pulverized coal, the proportion of SiO formation, and the partial melting of ash are set as external assumptions in most existing models, failing to achieve intrinsic coupling with the temperature solution process. This limits the model's computational accuracy and versatility under multi-media injection and complex nonlinear conditions. While published patents CN112342327B, CN115858990B, and CN115216569B propose improved solutions for theoretical combustion temperature calculation and blast furnace process optimization, none of them uniformly consider sensible heat, latent heat, solidification transformation, and heat of chemical reaction within a relative enthalpy framework, nor do they incorporate the aforementioned key proportional parameters as constraints in the solution. Therefore, their applicability remains insufficient under multi-media injection conditions.

[0005] This section is intended to provide background or context for the embodiments of the invention set forth in the claims. The description herein is not an admission that it is prior art simply because it is included in this section. Summary of the Invention

[0006] This invention provides a method for predicting the theoretical combustion temperature of blast furnace tuyeres, which enables accurate modeling of the thermodynamic process in the vortex zone under multiple injection media conditions and high-precision calculation of the combustion temperature, thereby improving the accuracy and applicability of energy balance analysis in the blast furnace tuyeres vortex zone.

[0007] The theoretical combustion temperature prediction method for the blast furnace tuyeres includes:

[0008] Obtain the input material parameters, input material type, and output material type in the cyclotron region;

[0009] Based on the input material parameters, the output material type, coke consumption, and multiple chemical reaction pathways, the amount of the output material is determined; wherein, the coke consumption is determined based on the input material parameters and the input material type.

[0010] Based on the input material parameters and multiple chemical reaction pathways, the total chemical reaction heat is determined;

[0011] The theoretical combustion temperature of the cyclone zone is determined based on the amount of substance of the input substance, the total heat of chemical reaction, the parameters of the input substance, the amount of substance of the output substance, the latent heat of phase change, the heat of solidification transformation, and a pre-established molar isobaric heat capacity model.

[0012] In some embodiments, the input substance type includes: hot air, coke oven gas, pulverized coal, coke, pulverized coal ash, and coke ash; the input substance parameters include: the molar number and mass fraction of each component in each input substance; determining the coke consumption based on the input substance parameters and input substance type includes:

[0013] The number of effective oxygen moles is determined based on the number of moles of each component in the hot air and the coke oven gas.

[0014] The net carbon requirement is determined based on the molar number and mass fraction of each component in the pulverized coal, coke, pulverized coal ash, and coke ash, as well as the molar number of available oxygen.

[0015] The number of moles of net carbon supplied is determined based on the mole number and mass fraction of each component in the pulverized coal and coke.

[0016] The amount of coke consumed is determined based on the number of moles of net carbon demand and the number of moles of net carbon supply.

[0017] In some embodiments, determining the number of moles of effective oxygen based on the molar numbers of each component in the hot air and the coke oven gas includes:

[0018] The number of moles of oxygen input is determined based on the number of moles of oxygen in the hot air and the coke oven gas.

[0019] The number of oxygen consumed corresponding to the equivalent carbon in the coke oven gas is determined based on the total number of moles of hydrocarbon equivalent carbon in the coke oven gas.

[0020] The effective number of moles of oxygen is determined based on the number of moles of input oxygen and the number of moles of oxygen consumed.

[0021] In some embodiments, determining the molar number of net carbon requirements based on the molar number and mass fraction of each component in pulverized coal, coke, pulverized coal ash, and coke ash, as well as the molar number of available oxygen, includes:

[0022] The number of moles of silicon dioxide in the coke ash is determined based on the coke mass, the mass fraction of coke ash in the coke, the mass fraction of silicon dioxide in the coke ash and pulverized coal ash, and the molar mass of silicon dioxide.

[0023] The required number of moles of net carbon is determined based on the number of moles of effective oxygen, the number of moles of water vapor in the hot air and coke oven gas, the number of moles of carbon dioxide in the coke oven gas, the pulverized coal ash and the coke ash, the number of moles of silicon dioxide in the pulverized coal ash, the number of moles of silicon dioxide in the coke ash and the preset silicon dioxide generation ratio.

[0024] In some embodiments, determining the number of moles of net carbon supplied based on the molar number and mass fraction of each component in the pulverized coal and coke includes:

[0025] The number of moles of net carbon supplied is determined based on the preset proportion of unburned pulverized coal, coke mass, pulverized coal mass, fixed carbon mass fraction of pulverized coal, fixed carbon mass fraction of coke, and molar mass of carbon.

[0026] In some embodiments, determining the total enthalpy change based on the input material parameters and multiple chemical reaction pathways includes:

[0027] Based on the molar number of available oxygen, the molar number of water vapor, the molar number of carbon dioxide, the molar number of silica in the pulverized coal ash, the molar number of silica in the coke ash, and their respective corresponding chemical reaction pathways, the equivalent number of each chemical reaction pathway is determined; wherein, the chemical reaction pathways include: carbon oxidation reaction, water-gas reaction, carbon gasification reaction, methane cracking reaction, silica reduction reaction, and graphitization reaction;

[0028] The heat of chemical reaction for each chemical reaction pathway is determined based on the equivalent number and standard enthalpy of formation corresponding to each chemical reaction pathway.

[0029] The total heat of chemical reaction is determined based on the heat of chemical reaction of each of the described chemical reaction pathways and the equivalent heat of decomposition of pulverized coal.

[0030] In some embodiments, the chemical reaction pathways include: a carbon oxidation reaction pathway, a water-gas reaction pathway, a carbon gasification reaction pathway, and a silicon dioxide reduction reaction pathway; the output substance types include: carbon monoxide, hydrogen, silicon dioxide, unburned coal powder, and various ash oxides, etc.; determining the amount of output substance based on the input substance parameters, the output substance types, coke consumption, and multiple chemical reaction pathways includes:

[0031] Based on the input material parameters, the coke consumption, the preset silicon dioxide generation ratio, the carbon oxidation reaction path, the water gas reaction path, the carbon gasification reaction path, and the silicon dioxide reduction reaction path, the amount of carbon monoxide, the amount of hydrogen, and the amount of silicon dioxide are determined respectively.

[0032] Based on the input material parameters and the coke consumption, determine the amount of each ash oxide.

[0033] The amount of unburned coal powder is determined based on the coal powder quality and the preset proportion of unburned coal powder.

[0034] In some embodiments, the input material parameters further include: absolute temperature; the determination of the theoretical combustion temperature in the cyclone region based on the amount of substance of the input material, the total heat of chemical reaction, the input material parameters, the amount of substance of the output material, the latent heat of phase change, the heat of solidification transition, and a pre-established molar isobaric heat capacity model includes:

[0035] Based on the amount of substance corresponding to the input substance type, the pre-established molar isobaric heat capacity model, the absolute temperature, the latent heat of phase change, and the solid-crystal transformation heat, a first relationship function is established between the relative enthalpy on the input side and the theoretical combustion temperature of the cyclone zone; wherein, the absolute temperature of coke is a linear function established by the theoretical combustion temperature of the cyclone zone and a preset constant.

[0036] Based on the amount of substance corresponding to the type of output substance, the pre-established molar isobaric heat capacity model, the latent heat of phase change and the solidification transformation heat, a second relationship function is established between the relative enthalpy on the output side and the theoretical combustion temperature of the cyclotron region.

[0037] Based on the first relational function, the total heat of chemical reaction and the second relational function, a third relational function is established between the energy residual and the theoretical combustion temperature of the vortex zone.

[0038] Based on the preset objective function, constraints, and convergence conditions, the third relational function is solved to obtain the theoretical combustion temperature of the vortex zone.

[0039] This invention also provides a theoretical combustion temperature prediction device for blast furnace tuyeres, which enables accurate modeling of the thermodynamic process in the vortex zone under multiple injection media conditions and high-precision calculation of combustion temperature, thereby improving the accuracy and applicability of energy balance analysis in the blast furnace tuyere vortex zone.

[0040] The theoretical combustion temperature prediction device for the blast furnace tuyeres includes:

[0041] The input parameter acquisition module is used to acquire the input substance parameters, input substance type, and output substance type in the cyclotron region.

[0042] The output substance calculation module is used to determine the amount of the output substance based on the input substance parameters, the output substance type, the coke consumption, and multiple chemical reaction paths; wherein the coke consumption is determined based on the input substance parameters and the input substance type.

[0043] The total reaction heat calculation module is used to determine the total chemical reaction heat based on the input material parameters and multiple chemical reaction pathways.

[0044] The theoretical temperature calculation module is used to determine the theoretical combustion temperature of the cyclone region based on the amount of substance of the input substance, the total heat of chemical reaction, the parameters of the input substance, the amount of substance of the output substance, the latent heat of phase change, the heat of solidification transformation, and a pre-established molar isobaric heat capacity model.

[0045] This invention also provides a computer device, including a memory, a processor, and a computer program stored in the memory and executable on the processor. When the processor executes the computer program, it implements the above-mentioned method for predicting the theoretical combustion temperature of the blast furnace tuyeres.

[0046] This invention also provides a computer-readable storage medium storing a computer program that, when executed by a processor, implements the above-described method for predicting the theoretical combustion temperature of a blast furnace tuyer.

[0047] This invention also provides a computer program product, which includes a computer program that, when executed by a processor, implements the above-mentioned method for predicting the theoretical combustion temperature of a blast furnace tuyer.

[0048] The theoretical combustion temperature prediction method and apparatus for blast furnace tuyeres provided in this invention achieves high-precision prediction of the theoretical combustion temperature in the blast furnace tuyere vortex zone by introducing the coupled solution of coke consumption, chemical reaction paths, and thermodynamic parameters into the theoretical calculation framework. By acquiring input material parameters, input material types, and output material types, and establishing the material conservation relationship between input and output materials, the product composition and reactant consumption under multi-injection media conditions can be accurately calculated. The total chemical reaction heat is quantitatively determined by calculating the chemical reaction heat corresponding to each chemical reaction path. Combining the relative enthalpy balance model of the input and output sides, and comprehensively considering the latent heat of phase change, solidification transformation heat, and molar isobaric heat capacity function, the energy balance equation can reflect the actual thermodynamic changes, thereby ensuring the physical consistency and numerical stability of the combustion temperature solution. The above method is applicable to multi-media injection conditions such as hydrogen-rich gas and coke oven gas, overcoming the problems of insufficient accuracy and limited applicability of traditional empirical methods and simplified heat balance methods, and realizing accurate modeling and universal calculation of the theoretical combustion temperature in the blast furnace tuyere vortex zone. Attached Figure Description

[0049] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort. In the drawings:

[0050] Figure 1 This is a flowchart illustrating a method for predicting the theoretical combustion temperature of a blast furnace tuyeres in one embodiment of the present invention.

[0051] Figure 2 This is a flowchart illustrating a method for predicting the theoretical combustion temperature of a blast furnace tuyeres in another embodiment of the present invention.

[0052] Figure 3 This is a flowchart illustrating a method for predicting the theoretical combustion temperature of a blast furnace tuyeres in another embodiment of the present invention.

[0053] Figure 4 This is a flowchart illustrating a method for predicting the theoretical combustion temperature of a blast furnace tuyeres in another embodiment of the present invention.

[0054] Figure 5 This is a flowchart illustrating a method for predicting the theoretical combustion temperature of a blast furnace tuyeres in another embodiment of the present invention.

[0055] Figure 6 This is a schematic diagram of the method for predicting the theoretical combustion temperature of the blast furnace tuyeres in an embodiment of the present invention;

[0056] Figure 7This is a flowchart illustrating a method for predicting the theoretical combustion temperature of a blast furnace tuyeres in another embodiment of the present invention.

[0057] Figure 8 This is a flowchart illustrating a method for predicting the theoretical combustion temperature of a blast furnace tuyeres in another embodiment of the present invention.

[0058] Figure 9 This is a schematic diagram of the theoretical combustion temperature prediction device for blast furnace tuyeres in an embodiment of the present invention.

[0059] Figure 10 This is a schematic diagram of the physical structure of a computer device provided in an embodiment of the present invention. Detailed Implementation

[0060] To make the objectives, technical solutions, and advantages of the embodiments of the present invention clearer, the embodiments of the present invention will be further described in detail below with reference to the accompanying drawings. Here, the illustrative embodiments and their descriptions are used to explain the present invention, but are not intended to limit the present invention. It should be noted that, unless otherwise specified, the embodiments and features in the embodiments of this application can be arbitrarily combined with each other. The acquisition, storage, use, and processing of data in the technical solutions of this application all comply with relevant laws and regulations. The user information in the embodiments of this application is obtained through legal and compliant means, and the acquisition, storage, use, and processing of user information have been authorized and agreed upon by the customer.

[0061] To facilitate understanding of the technical solution provided in this application, the relevant content of the technical solution in this application will be explained below.

[0062] To achieve an accurate description and temperature prediction of the thermodynamic behavior of the blast furnace tuyeres under multiple injection media conditions, this application provides a method for predicting the theoretical combustion temperature of blast furnace tuyeres. This addresses the technical problem that traditional calculation methods fail to comprehensively consider sensible heat, latent heat of phase change, solid-solid phase transformation heat, and chemical reaction heat in a unified model, and struggle to account for the complex coupling relationships between multiple injection media and multiple raw materials. The method obtains multiple input material parameters, including hot blast, coke oven gas, pulverized coal, coke, and its ash content. Combining the law of conservation of mass and multiple chemical reaction pathways, it determines the mass of output substances and the amount of coke consumed. Based on the chemical reaction equivalence number and standard enthalpy of formation, the total chemical reaction heat is calculated, establishing a relative enthalpy balance model between the input and output sides. By introducing the molar isobaric heat capacity model, latent heat of phase change, and solid-solid phase transformation heat, a nonlinear constraint solution relationship between the energy residual and the theoretical combustion temperature is constructed, achieving an accurate solution for the theoretical combustion temperature of the tuyeres. The above method can adapt to different injection media and feed structure, and significantly improves the accuracy, stability and universal applicability of the theoretical combustion temperature prediction in the swirl zone.

[0063] like Figure 1 As shown, this application provides a method for predicting the theoretical combustion temperature of a blast furnace tuyeres, including steps 101 to 104.

[0064] Step 101: Obtain the input material parameters, input material type, and output material type of the cyclotron region.

[0065] Step 102: Determine the amount of the output substance based on the input material parameters, output substance type, coke consumption, and multiple chemical reaction pathways. The coke consumption is determined based on the input material parameters and the input substance type.

[0066] Step 103: Determine the total chemical reaction heat based on the input material parameters and multiple chemical reaction pathways.

[0067] Step 104: Based on the amount of substance of the input substance, total heat of chemical reaction, input substance parameters, amount of substance of the output substance, latent heat of phase change, heat of solidification transformation, and the pre-established molar isobaric heat capacity model, determine the theoretical combustion temperature of the vortex zone. The input substance is the injection medium of the vortex zone.

[0068] According to the above embodiments, by introducing the coupled solution of coke consumption, chemical reaction paths, and thermodynamic parameters into the theoretical calculation framework, high-precision prediction of the theoretical combustion temperature in the blast furnace tuyere vortex zone is achieved. By obtaining the input material parameters, input material type, and output material type, and establishing the material conservation relationship between the input and output materials, the product composition and reactant consumption under multi-injection media conditions can be accurately calculated. By calculating the heat of chemical reaction corresponding to each chemical reaction path, the total heat of chemical reaction is quantitatively determined. Combining the relative enthalpy balance model of the input and output sides, and comprehensively considering the latent heat of phase change, solidification transformation heat, and molar isobaric heat capacity function, the energy balance equation can reflect the real thermodynamic change process, thereby ensuring the physical consistency and numerical stability of the combustion temperature solution. The above method is applicable to multi-media injection conditions such as hydrogen-rich gas and coke oven gas, overcoming the problems of insufficient accuracy and limited applicability of traditional empirical methods and simplified heat balance methods, and realizing accurate modeling and generalized calculation of the theoretical combustion temperature in the blast furnace tuyere vortex zone.

[0069] In this embodiment of the invention, during the blast furnace ironmaking process, high-temperature gas is injected into the furnace body through tuyeres located on the lower sidewall or bottom of the blast furnace. Upon contact with the coke layer and burden layer within the furnace body, the injected high-temperature gas undergoes intense combustion and redox reactions. Within the region where the high-temperature gas interacts with the coke and burden layers, the airflow impacts and pushes the coke particles to form localized void channels; this void region is called the Bosh Zone.

[0070] The injection media in the swirling zone include: hot air, coke oven gas (COG), pulverized coal, coke, pulverized coal ash, and coke ash. Among them, the hot air may contain hydrogen-enriched gas, and the pulverized coal injection may carry carrier gas.

[0071] As shown in Tables 1 to 5 below, the input material parameters include: the injection rate, absolute temperature, and molar percentage and mass fraction of each component of the injection medium. The values ​​for gaseous components such as oxygen, nitrogen, water vapor, hydrogen, carbon monoxide, methane, and carbon dioxide are expressed as molar percentages, used to characterize the molar composition ratio of each gas in the mixed injection medium. The values ​​for solid components such as fixed carbon, sulfur, ash, volatile matter, moisture, amorphous carbon, and graphitic carbon are expressed as mass fractions, used to reflect the compositional characteristics of the solid materials. Calcium oxide, silicon dioxide, magnesium oxide, aluminum oxide, and iron oxide represent the mass fractions of each oxide in pulverized coal ash and coke ash, used to characterize the mineral composition of pulverized coal ash and coke ash.

[0072]

[0073] Table 1 Hot air parameters

[0074]

[0075] Table 2 Coke oven gas parameters

[0076]

[0077] Table 3 Parameters of Pulverized Coal and Carrier Gas

[0078]

[0079] Table 4 Coke Parameters

[0080]

[0081] Table 5. Ash content of pulverized coal and coke, and their volatile matter parameters.

[0082] As shown in Table 6 below, the output material types include: carbon monoxide, hydrogen, nitrogen, silicon dioxide, unburned coal powder, and ash oxides. β represents the silicon dioxide formation ratio, characterizing the degree of conversion of silicon dioxide into silicon dioxide through a reduction reaction. α represents the unburned coal powder ratio, characterizing the retention ratio of incompletely burned components in the coal powder. γ represents the ash melting ratio, characterizing the degree of melting of coal powder ash and coke ash under high-temperature conditions.

[0083] For example, in this embodiment of the invention, the silicon oxide generation ratio β is 12%, the unburned coal powder ratio α is 12%, and the ash melting ratio γ is 80%. The above parameters are set within the range of this embodiment of the invention and are used to illustrate the feasibility of the invention. The invention is not limited thereto.

[0084]

[0085] Table 6 Physical state and scale parameters of output material type

[0086] In some embodiments, as shown in Tables 1 to 5 above, the input substance types include: hot air, coke oven gas, pulverized coal, coke, pulverized coal ash, and coke ash. The input substance parameters include: the molar number and mass fraction of each component in each input substance.

[0087] like Figure 2 As shown, determining coke consumption based on input material parameters and input material type includes steps 201 to 204.

[0088] Step 201: Determine the number of moles of effective oxygen based on the molar number of each component in the hot air and coke oven gas.

[0089] Step 202: Determine the number of moles required for net carbon based on the mole number and mass fraction of each component in pulverized coal, coke, pulverized coal ash, and coke ash, as well as the number of moles of available oxygen.

[0090] Step 203: Determine the number of moles of net carbon supplied based on the molar number and mass fraction of each component in pulverized coal and coke.

[0091] Step 204: Determine the coke consumption based on the number of moles of net carbon demand and the number of moles of net carbon supply.

[0092] According to the above embodiments, the method described above enables accurate calculation of coke consumption under multiple injection media conditions, thereby improving the accuracy of energy and material conservation analysis in the blast furnace tuyeres. This method establishes a quantitative correspondence between oxygen supply and carbon consumption by combining the molar number of oxygen in hot blast and coke oven gas with parameters related to pulverized coal ash, coke ash, and their composition. This accurately reflects the coupling characteristics of different injection media participating in combustion and reduction reactions. By calculating the molar number of net carbon demand and net carbon supply separately, and deriving coke consumption based on this, the method comprehensively considers the participation effects of oxidation, reduction, and oxides in ash, and introduces a dual-parameter coupling mechanism of mass fraction and mole fraction, making the calculation process of coke consumption more consistent with the thermodynamic characteristics of actual furnace conditions. This method effectively avoids the error accumulation caused by simplification of assumptions in traditional empirical formulas, significantly improving the physical consistency and traceability of coke consumption calculation results.

[0093] In some embodiments, such as Figure 3 As shown, step 201 includes steps 301 to 303.

[0094] Step 301: Determine the number of moles of oxygen to be input based on the number of moles of oxygen in the hot air and coke oven gas.

[0095] Step 302: Determine the number of oxygen consumption corresponding to the equivalent carbon of hydrocarbons in the coke oven gas based on the total number of moles of equivalent carbon of hydrocarbons.

[0096] Step 303: Determine the effective number of moles of oxygen based on the input number of moles of oxygen and the number of moles of oxygen consumed.

[0097] In this embodiment of the invention, as shown in Table 1 above, the hot air comprises oxygen, nitrogen, and water vapor. As shown in Table 2 above, the coke oven gas comprises hydrogen, methane, carbon monoxide, carbon dioxide, oxygen, nitrogen, and water vapor.

[0098] Assuming the vortex zone is under adiabatic conditions and no water vapor or carbon dioxide is emitted, based on the law of conservation of oxygen, and using the molar amounts of oxygen in the hot air in Table 1... and the number of moles of oxygen in coke oven gas in Table 2 Substitute into the following formula (1) to calculate the number of moles of input oxygen. .

[0099]

[0100] in, This represents the number of moles of oxygen in the hot air. This represents the number of moles of oxygen in coke oven gas, expressed in mol / t.

[0101] The equivalent total carbon moles corresponding to hydrogen and methane and other hydrocarbon components in coke oven gas in Table 2 are given. The number of moles of oxygen consumed can be converted to the equivalent carbon of hydrocarbons using the following formula (2). .

[0102]

[0103] in, This represents the total number of moles of carbon equivalent to hydrocarbons, expressed in mol / t.

[0104] The calculated number of moles of input oxygen and the number of moles of oxygen consumed Substitute into the following formula (3) to calculate the number of moles of available oxygen. .

[0105]

[0106] in, To input the number of moles of oxygen, This represents the number of moles of oxygen consumed, expressed in mol / t.

[0107] According to the above embodiments, the method described above can accurately calculate the effective number of moles of oxygen in the vortex zone, achieving an accurate match between oxygen supply and carbon consumption, thereby improving the accuracy of oxygen conservation calculations in the blast furnace tuyeres vortex zone. This method calculates the effective number of moles of oxygen actually participating in the combustion reaction by summing the number of moles of oxygen in the hot blast and coke oven gas, and then subtracting the oxygen consumption corresponding to the equivalent carbon of hydrocarbons in the coke oven gas. This calculation process effectively avoids the overestimation of oxygen and calculation errors caused by the failure to distinguish hydrocarbon oxygen consumption in traditional methods, ensuring the accuracy and physical rationality of the oxygen balance calculation results.

[0108] In some embodiments, such as Figure 4 As shown, step 202 includes steps 401 to 402.

[0109] Step 401: Determine the number of moles of silicon dioxide in the coke ash based on the coke mass, the mass fraction of coke ash in the coke, the mass fraction of silicon dioxide in the coke ash and pulverized coal ash, and the molar mass of silicon dioxide.

[0110] Step 402: Determine the required number of moles of net carbon based on the number of moles of available oxygen, the number of moles of water vapor in hot air and coke oven gas, the number of moles of carbon dioxide in coke oven gas, pulverized coal ash and coke ash, the number of moles of silicon dioxide in pulverized coal ash, the number of moles of silicon dioxide in coke ash and the preset silicon dioxide generation ratio.

[0111] In this embodiment of the invention, the coke mass to be determined is... Table 4 shows the mass fraction of coke ash in coke. Table 5 shows the mass fraction of silica in coke ash and pulverized coal ash. and the molar mass of silicon dioxide Substituting into the following formula (4), the molar number of silica in the coke ash can be calculated. .

[0112]

[0113] in, The value is the mass of coke, i.e., the amount of coke consumed, expressed in kg / t. This refers to the mass fraction of coke ash. This refers to the mass fraction of silicon dioxide in coke ash and pulverized coal ash. This is the molar mass of silicon dioxide, expressed in g·m³. .

[0114] The number of moles of effective oxygen obtained from the above calculation The number of moles of water vapor in hot air and coke oven gas in Tables 1 and 2 The molar amounts of carbon dioxide in coke oven gas, pulverized coal ash, and coke ash in Tables 2 and 5. Table 5 shows the molar amounts of silica in pulverized coal ash. Table 5 shows the molar amounts of silica in the coke ash. Substituting the silicon dioxide production ratio β in Table 6 into the following formula (5), the number of moles of net carbon required can be calculated. .

[0115]

[0116] in, The number of moles of available oxygen. This refers to the number of moles of water vapor in the hot air and coke oven gas. This refers to the number of moles of carbon dioxide in coke oven gas, pulverized coal ash, and coke ash. This represents the number of moles of silicon dioxide in the ash of pulverized coal. This represents the number of moles of silicon dioxide in the coke ash. This represents the proportion of silicon dioxide produced.

[0117] According to the above embodiments, the method described above can accurately calculate the net carbon demand in the vortex zone under multiple injection media conditions, thereby achieving a precise match between oxygen supply and carbon consumption. This method comprehensively considers the influence of various oxygen-containing components, such as oxygen, water vapor, carbon dioxide, and silica, in hot air, coke oven gas, pulverized coal ash, and coke ash during the calculation process. It also introduces a silica formation ratio parameter to reflect the contribution of pulverized coal ash and coke ash reduction reactions to carbon demand. This effectively avoids the error accumulation caused by neglecting the coupling relationship between ash oxides and gas components in traditional calculation methods, significantly improving the accuracy and reliability of carbon balance and heat balance calculations.

[0118] In some embodiments, step 203 specifically includes: determining the number of moles of net carbon supplied based on preset unburned coal powder ratio, coke mass, coal powder mass, fixed carbon mass fraction of coal powder, fixed carbon mass fraction of coke, and molar mass of carbon. Wherein, coal powder mass refers to the amount of coal powder injected.

[0119] In this embodiment of the invention, the proportion of unburned coal powder α in Table 1 and the coal powder mass in Table 3 are... Substituting the fixed carbon mass fraction of pulverized coal in Table 3, the fixed carbon mass fraction of coke in Table 4, the molar mass of carbon, and the mass of coke to be determined into the following formula (6), the number of moles of net carbon supplied can be calculated. .

[0120]

[0121] Where α is the proportion of unburned pulverized coal, The coal powder quality is the amount of coal powder injected as shown in Table 3. This refers to the fixed carbon mass fraction of pulverized coal. The molar mass of carbon. This refers to the fixed carbon mass fraction of coke. The desired coke quality.

[0122] The calculated number of moles of input oxygen Moles of oxygen consumed The number of moles of water vapor in hot air and coke oven gas The number of moles of carbon dioxide in coke oven gas, pulverized coal ash, and coke ash. And the molar number of silicon dioxide calculated based on the silicon dioxide production ratio β. The results were summarized and processed to obtain Table 7 below.

[0123]

[0124] Table 7 Summary of Moles (mol)

[0125] In some embodiments, step 204 specifically includes: based on the data in Tables 1 to 7, solving the system of equations between the calculated moles of net carbon demand and net carbon supply to obtain the coke consumption. The amount of coke consumed is the same as the mass of coke. .

[0126] In some embodiments, the chemical reaction pathways include: a carbon oxidation reaction pathway, a water-gas reaction pathway, a carbon gasification reaction pathway, and a silicon dioxide reduction reaction pathway. The types of output substances include: carbon monoxide, hydrogen, silicon dioxide, unburned coal powder, and various ash oxides, etc.

[0127] like Figure 5 As shown, step 102 includes steps 501 to 503.

[0128] Step 501: Based on the input material parameters, coke consumption, preset silicon dioxide generation ratio, carbon oxidation reaction path, water gas reaction path, carbon gasification reaction path and silicon dioxide reduction reaction path, determine the amount of carbon monoxide, hydrogen and silicon dioxide respectively.

[0129] Step 502: Determine the amount of each ash oxide based on the input material parameters and coke consumption.

[0130] Step 503: Determine the amount of unburned coal powder based on the coal powder quality and the preset unburned coal powder ratio.

[0131] In embodiments of the present invention, such as Figure 6 As shown, the chemical equation for the carbon oxidation reaction is:

[0132]

[0133] Wherein, C represents amorphous graphite and graphite in the coke. For oxygen in hot air and coke oven gas, The carbon monoxide produced.

[0134] The chemical reaction equation for the water-gas reaction is:

[0135]

[0136] in, C represents water vapor from hot air and coke oven gas, and C represents amorphous graphite and graphite in coke. For the generated carbon monoxide, The generated hydrogen gas.

[0137] The chemical equation for the carbon gasification reaction is:

[0138]

[0139] in, C represents carbon dioxide from coke oven gas, pulverized coal ash, and coke ash, while C represents amorphous graphite and graphite in coke. The carbon monoxide produced.

[0140] The chemical equation for the reduction of silicon dioxide is:

[0141]

[0142] in, The carbon dioxide (C) represents silicon dioxide in pulverized coal ash and coke ash, while the carbon (C) represents amorphous graphite and graphite in coke. For the generated silicon dioxide, The carbon monoxide produced.

[0143] Based on the molar amounts of oxygen and water vapor in hot air and coke oven gas in Tables 1 to 2, the mass fractions of amorphous graphite and graphite in coke in Table 4, the molar amounts of carbon dioxide in coke oven gas, pulverized coal ash and coke ash in Tables 2 and 5, the mass fractions of silicon dioxide in pulverized coal ash and coke ash in Tables 3 to 5, the silicon dioxide formation ratio β, the amount of coke consumed, and the above chemical reaction equations (7) to (10), the amount of carbon monoxide, the amount of hydrogen and the amount of silicon dioxide can be calculated respectively by the law of conservation of mass.

[0144] Based on the mass fraction of each ash oxide in the pulverized coal ash and coke ash in Table 5, and the amount of coke consumed, the amount of substance of each ash oxide can be calculated.

[0145] For example, taking coke parameters as an example, based on the above coke consumption... = Table 5 shows the mass fraction of calcium oxide in coke ash as 0.46% and the molar mass of calcium oxide as Mco = 56 g·mol⁻¹. The calculated amount of silicon dioxide is: .

[0146] During combustion, because the pulverized coal is not completely burned, the mass of the pulverized coal is reduced. Substituting the amount of pulverized coal injected (i.e., the injection rate of pulverized coal) and the proportion of unburned pulverized coal α into the following formula (11), the amount of unburned pulverized coal can be calculated. .

[0147]

[0148] in, For the quality of pulverized coal, This represents the proportion of unburned pulverized coal.

[0149] In addition, nitrogen is an inert gas and does not participate in the above chemical reactions. Therefore, the amount of nitrogen in the output material is the sum of the amounts of nitrogen in the hot air, coke oven gas, and pulverized coal.

[0150] The amounts of the output substances calculated above are summarized to obtain Tables 8 and 9 below.

[0151]

[0152] Table 8. Amount of substance of output gas and output solid (mol / t)

[0153]

[0154] Table 9. Amount of substance of ash oxides (mol / t)

[0155] According to the above embodiments, the method described above can systematically calculate the product composition and reactant consumption of various major chemical reactions in the blast furnace tuyeres, thereby achieving an accurate description of the gas-solid reaction process under multiple injection media conditions. This method comprehensively considers multiple major thermochemical reaction pathways, including carbon oxidation, water-gas reaction, carbon gasification, and silica reduction, fully reflecting the thermochemical coupling relationship between coke, pulverized coal, ash, and the gaseous medium. By quantitatively analyzing the stoichiometric relationships and mass conservation equations of each chemical reaction, the amounts of key products such as carbon monoxide, hydrogen, and silica can be determined. This method overcomes the shortcomings of traditional models that oversimplify reaction pathways or ignore the influence of ash oxides, making the calculation results more consistent with the thermodynamic characteristics and reaction kinetics of actual furnace conditions, thus significantly improving the accuracy and reliability of the simulation of combustion behavior in the blast furnace tuyeres.

[0156] In some embodiments, such as Figure 7 As shown, step 103 includes steps 701 to 703.

[0157] Step 701: Based on the molar amounts of available oxygen, water vapor, carbon dioxide, silica in pulverized coal ash, and silica in coke ash, and their corresponding chemical reaction pathways, determine the equivalent number of each chemical reaction pathway. These chemical reaction pathways include: carbon oxidation reaction, water-gas reaction, carbon gasification reaction, silica reduction reaction, methane cracking reaction, and graphitization reaction.

[0158] Step 702: Determine the heat of chemical reaction for each chemical reaction pathway based on the equivalent number and standard enthalpy of formation corresponding to each chemical reaction pathway.

[0159] Step 703: Determine the total heat of chemical reaction based on the heat of chemical reaction of each chemical reaction pathway and the equivalent heat of decomposition of pulverized coal.

[0160] In this embodiment of the invention, based on the number of moles of available oxygen Based on the chemical equation for the carbon oxidation reaction in formula (7) above, the equivalent number V1 of the carbon oxidation reaction can be calculated. This is based on the molar number of water vapor. Based on the chemical equation for the water-gas reaction in formula (8) above, the equivalence number V4 of the water-gas reaction can be calculated. This is based on the molar number of carbon dioxide. Based on the chemical equation for the carbon gasification reaction in formula (9) above, the equivalent number V5 of the carbon gasification reaction can be calculated. (Based on the molar number of silicon dioxide) The equivalent number V6 of the silicon dioxide reduction reaction can be calculated from the above formula (10) and the chemical equation of the silicon dioxide reduction reaction.

[0161] With graphite carbon C 石墨 The thermodynamic reference state of carbon is amorphous carbon (C). 非晶 To graphite carbon C 石墨 The transformation is a crystal form transformation process.

[0162] Amorphous carbon C 非晶 Converted to graphite carbon C 石墨 The chemical reaction equation is:

[0163]

[0164] in, It is amorphous carbon. It is graphitic carbon.

[0165] Based on the law of conservation of carbon, the equivalent number of the graphitization reaction is the number of moles of amorphous carbon converted into graphitic carbon.

[0166] For example, it can be based on the coal powder quality (i.e., the amount of pulverized coal injected) and the quality of coke. (i.e., coke consumption), and the fixed carbon mass fraction of coke. Fixed carbon mass fraction of pulverized coal Molar mass M of carbon C The molar number of amorphous carbon is calculated by fixing the proportion coefficient of amorphous carbon in the carbon. Then, based on the molar number of amorphous carbon and the preset ratio of graphite carbon to amorphous carbon, the molar number of graphite carbon can be calculated, which is the equivalent number V2 of the graphitization reaction. In this embodiment of the invention, the coke graphitization ratio is 70%, i.e., C...石墨 70%, C 非晶 It accounts for 30%, but this invention is not limited thereto.

[0167] The chemical equation for the methane cracking reaction is:

[0168]

[0169] in, It is methane. It is graphitic carbon. It is hydrogen gas.

[0170] For example, based on the injection rate of coke oven gas and the molar percentage of methane in the coke oven gas in Table 2, the number of moles of methane in the coke oven gas can be calculated. Then, based on the chemical equation of the methane cracking reaction, the number of moles of methane in the coke oven gas, and the preset cracking conversion rate, the equivalent number V3 of the methane cracking reaction can be obtained through the law of conservation of mass.

[0171] Furthermore, the thermal decomposition of volatiles in pulverized coal is considered a physicochemical process. Instead of solving it using explicit chemical reaction equations, its decomposition endothermic and exothermic characteristics are calculated based on the lower heating value (LHV) of the pulverized coal. Based on Hess's Law, the lower heating value of the pulverized coal is converted into an equivalent heat of decomposition using the law of conservation of energy. It is used to characterize the heat released or absorbed by pulverized coal during heating and pyrolysis.

[0172] Using Hess's Law and 298 K as the standard reference temperature, the actual chemical reaction is decomposed into a series of elementary reactions along a virtual chemical reaction path, and the chemical reaction heat of each elementary reaction is summed to obtain the total chemical reaction heat of the overall chemical reaction.

[0173] Specifically, under the standard reference temperature of 298 K, the standard enthalpy of formation data of the input and output substances in each chemical reaction equation are obtained by consulting thermodynamic handbooks or authoritative databases. The standard enthalpy of formation includes, but is not limited to: the standard enthalpy of formation of graphite carbon, oxygen, carbon monoxide, methane, hydrogen, water vapor, carbon dioxide, silicon dioxide, and silicon oxide, etc.

[0174] After obtaining the above basic thermodynamic data, the standard enthalpy of each reaction is calculated using Hess's Law based on the stoichiometric relationships between reactants and products in each chemical reaction equation. Based on the above calculation results, the standard enthalpy of reaction for carbon oxidation, water-gas reaction, carbon gasification, silicon dioxide reduction, and methane cracking were obtained respectively, and used for subsequent calculations of total chemical reaction heat.

[0175] Based on the equivalent numbers V1 for carbon oxidation, V2 for graphitization, V3 for methane cracking, V4 for water-gas reaction, V5 for carbon gasification, and V6 for silicon dioxide reduction calculated above, as well as the standard enthalpies of reaction for carbon oxidation, water-gas reaction, carbon gasification, silicon dioxide reduction, and methane cracking, calculate the heat of reaction for each chemical reaction pathway. .

[0176] The calculated heat of chemical reaction for each chemical reaction pathway and equivalent heat of decomposition Substituting into the following formula (14), the total heat of chemical reaction is calculated. .

[0177]

[0178] in, The heat of chemical reaction for each chemical reaction pathway, This is the equivalent heat of decomposition.

[0179] The reaction heat data obtained from the above calculations are summarized and processed to obtain Table 10 below.

[0180]

[0181] Table 10 Chemical Reactions and Thermal Effects Based on Hess's Law

[0182] Based on Table 10 and the above formula (14), the total heat of chemical reaction can be calculated. ...

[0183] According to the above embodiments, the total chemical reaction heat is accurately calculated by establishing a multi-reaction coupled energy balance model. This method integrates multiple reaction pathways, such as carbon oxidation, water-gas reaction, carbon gasification, silica reduction, methane cracking, and graphitization, into the calculation framework of Hess's Law for energy conservation analysis. It comprehensively considers the contributions of the standard enthalpy of formation and their respective equivalents of different reactants, achieving quantitative calculation of complex coupled thermochemical systems. By introducing an equivalent conversion of the pulverized coal decomposition heat, the energy calculation can accurately reflect the real thermodynamic behavior under multiple injection media conditions. Compared with traditional simplified heat balance calculation methods, this invention effectively avoids systematic errors caused by neglecting secondary reaction heats or phase change heats, significantly improving the accuracy and applicability of the total chemical reaction heat calculation.

[0184] In some embodiments, the input material parameters further include: absolute temperature. For example... Figure 8 As shown, step 104 includes steps 801 to 804.

[0185] Step 801: Based on the amount of substance corresponding to the input substance type, the pre-established molar isobaric heat capacity model, absolute temperature, latent heat of phase change, and solid-crystal transformation heat, establish the first relationship function between the relative enthalpy on the input side and the theoretical combustion temperature of the cyclone zone. The absolute temperature of the coke is a linear function established by the theoretical combustion temperature of the cyclone zone and a preset constant.

[0186] Step 802: Based on the amount of substance corresponding to the type of output substance, the pre-established molar isobaric heat capacity model, the latent heat of phase change and the solidification heat of solidification, establish a second relationship function between the relative enthalpy on the output side and the theoretical combustion temperature of the cyclotron region.

[0187] Step 803: Based on the first relational function, the total heat of chemical reaction, and the second relational function, establish a third relational function between the energy residual and the theoretical combustion temperature of the cyclone zone.

[0188] Step 804: Based on the preset objective function, constraints, and convergence conditions, solve the third relational function to obtain the theoretical combustion temperature of the cyclone region. The pre-established molar isobaric heat capacity model is the molar isobaric heat capacity... The first relationship function between the input-side relative enthalpy and the theoretical combustion temperature in the vortex region is the input-side relative enthalpy. The calculation formula is as follows. The second relationship function between the output-side relative enthalpy and the theoretical combustion temperature in the vortex zone is the output-side relative enthalpy. The calculation formula.

[0189] In this embodiment of the invention, within the adiabatic system (i.e., the blast furnace tuyeres swirling zone), a balance relationship between the total enthalpy on the input side and the total enthalpy on the output side is established based on the first law of thermodynamics, as shown in formula (15):

[0190]

[0191] in, For the total enthalpy on the input side, This is the total enthalpy on the output side.

[0192] As shown in formula (16), the total enthalpy on the input side It consists of the sensible heat, latent heat of phase change, heat of solid-state crystal transformation, and total heat of chemical reaction of the input substance:

[0193]

[0194] in, The total sensible heat of the input substance. The total latent heat of phase change of the input substance. The total solid-phase transition heat of the input material. It is the total heat of chemical reaction.

[0195] As shown in the following formula (17), the total enthalpy on the output side Represented as:

[0196]

[0197] in, The total sensible heat of the output substance. To output the total latent heat of phase transition of the substance, It is the total heat of solid-state crystal transformation of the output substance.

[0198] According to the principle of conservation of thermodynamic energy, from formula (15) to formula (17), we can obtain:

[0199]

[0200] in, The total sensible heat of the input substance. The total latent heat of phase transition of the input substance, The total heat of solid-state transformation of the input substance. The total heat of chemical reaction, The total sensible heat of the output substance. To output the total latent heat of phase transition of the substance, It is the total heat of solid-state crystal transformation of the output substance.

[0201] Furthermore, for ease of calculation and unified expression, formula (18) is converted into input-side relative enthalpy. Enthalpy relative to the output side The relational form is shown in formula (19):

[0202]

[0203] in, The total relative enthalpy of the input substance when heated from a standard reference temperature to its input temperature. The total heat of chemical reaction, The total relative enthalpy of the output substance when heated from the standard reference temperature to its output temperature.

[0204] Due to the absolute temperature of coke It is not a fixed constant, but varies with the theoretical combustion temperature in the vortex zone. The absolute temperature of coke changes with the temperature of the environment, therefore the absolute temperature of coke is established. Theoretical combustion temperature of the swirl zone The linear function between them is shown in the following formula (20):

[0205]

[0206] in, 273 represents the theoretical combustion temperature of the vortex zone, and 273 is the zero-point conversion value between the Celsius and Kelvin scales.

[0207] Since pulverized coal ash and coke ash partially melt under high temperatures, to accurately reflect the impact of this phase change process on the system's energy balance, the latent heat of phase change of pulverized coal ash and coke ash are calculated separately using the ash melting ratio γ, and the latent heat of phase change of the input material is also taken into account. middle.

[0208] As shown in the following formula (21), the relative enthalpy on the input side The calculation formula is:

[0209]

[0210] in, Indicate each input substance, The amount of substance for each input substance, expressed in mol / t. Let K be the absolute temperature of each input substance, in K, where the absolute temperature of coke and the theoretical combustion temperature of the vortex zone satisfy a linear relationship. The molar isobaric heat capacity of each input substance, in kJ· · ; The latent heat of phase transition for each input substance, expressed in kJ· ; The solid-crystallization heat of each input substance is expressed in kJ·k ... The latent heat of phase transition and solid-crystal transition of each input substance can be obtained by consulting thermodynamic data handbooks or authoritative thermochemical databases.

[0211] As shown in the following formula (22), the output-side relative enthalpy The calculation formula is:

[0212]

[0213] in, Indicate each output substance, The amount of substance of each output substance, in mol / t; The absolute temperature of each output substance, i.e., the theoretical combustion temperature of the vortex zone, is expressed in K. The molar isobaric heat capacity of each output substance, in kJ· · ; The latent heat of phase transition for each output substance, expressed in kJ· ; The solid-crystallization heat of each output substance is expressed in kJ· The latent heat of phase transition and solidification heat of each output substance can be obtained by consulting thermodynamic data handbooks or authoritative thermochemical databases.

[0214] Molar heat capacity at constant pressure The function is:

[0215]

[0216] in, , , , and These are constants related to the input or output substances and can be found in thermodynamic data handbooks or standard thermodynamic databases; T represents the absolute temperature of the input or output substances.

[0217] As shown in formula (24), based on formulas (19) to (23), the energy balance equation can be established as follows:

[0218]

[0219] in, Indicate each input substance, The amount of substance for each input substance, expressed in mol / t. Let K be the absolute temperature of each input substance, in K, where the absolute temperature of coke and the theoretical combustion temperature of the vortex zone satisfy a linear relationship. The molar isobaric heat capacity of each input substance, in kJ· · ; The latent heat of phase transition for each input substance, expressed in kJ· ; The solid-crystallization heat of each input substance is expressed in kJ·k ... ; The total heat of chemical reaction, Indicate each output substance, The amount of substance of each output substance, in mol / t; The absolute temperature of each output substance, i.e., the theoretical combustion temperature of the vortex zone, is expressed in K. The molar isobaric heat capacity of each output substance, in kJ· · ; The latent heat of phase transition for each output substance, expressed in kJ· ; The solid-crystallization heat of each output substance is expressed in kJ· .

[0220] Furthermore, by transforming formula (24), the relationship function between the energy residual and the theoretical combustion temperature in the vortex zone is obtained, as shown in formula (25) below:

[0221]

[0222] in, For the input-side relative enthalpy, The total heat of chemical reaction, This refers to the relative enthalpy on the output side.

[0223] Set the objective function as The constraints are The convergence condition is .

[0224] in, The lower limit of temperature, This is the upper limit of temperature. This is the optimal solution for the theoretical combustion temperature in the swirl zone. For energy tolerance, = and , This is the equivalent total heat capacity of the output substance.

[0225] By inputting the material parameters from Tables 1 to 5 above, the amount of substance for each input substance can be calculated. .

[0226] Furthermore, the calculated amount of substance of each input substance... The amount of substance of each output substance The absolute temperatures of each input substance in Tables 1 to 5 The absolute temperature of coke Theoretical combustion temperature of the swirl zone linear function, molar isobaric heat capacity Functions, latent heat of phase transition of each input substance Heat of solidification transformation of each input substance The latent heat of phase transition of each output substance Heat of solidification transformation of each output substance The proportionality coefficients and total heat of chemical reaction in Table 6 The objective function, constraints, and convergence conditions are input into a nonlinear optimization solver for iterative optimization, yielding the desired result. .

[0227] The calculated relative enthalpy on the input side and the relative enthalpy on the output side are summarized to obtain Table 11 and Table 12.

[0228]

[0229] Table 11 Relative enthalpy on the input side

[0230]

[0231] Table 12 Relative Enthalpy on the Output Side

[0232] According to the above embodiments, the above calculation process enables high-precision calculation of the theoretical combustion temperature in the blast furnace tuyeres under adiabatic conditions. Based on the first law of thermodynamics, this method establishes a total enthalpy balance model on both the input and output sides, unifying sensible heat, latent heat of phase change, solidification transformation heat, and total chemical reaction heat into an energy conservation framework, thus achieving coupled calculation of heat transfer and reaction exothermic processes between different substances. By introducing a temperature-dependent molar isobaric heat capacity function and combining it with the linear functional relationship between coke temperature and theoretical combustion temperature, the thermodynamic behavior of coke during heating and combustion can be dynamically characterized. Weighted correction of the latent heat of phase change using the ash melting ratio makes the calculation results more consistent with actual blast furnace conditions. The iterative optimization solution mechanism using the energy residual function and the objective function ensures consistency in numerical convergence accuracy and thermodynamic rationality of the calculation results. This method overcomes the simplification assumptions of traditional empirical formulas or constant heat capacity models, significantly improving the accuracy and computational stability of theoretical combustion temperature prediction.

[0233] In some embodiments, to adapt to different operating conditions and to conduct sensitivity analysis, the following variables are set as unknowns to be optimized: .

[0234] in, The proportion of unburned pulverized coal. The proportion of silicon dioxide produced. The ash melting ratio, This is the temperature coefficient of coke.

[0235] Based on the above settings, formula (25) is parametrically extended and optimized to establish the optimized energy residual function, as shown in formula (26):

[0236]

[0237] in, For the input-side relative enthalpy, The total heat of chemical reaction, For the output-side relative enthalpy, The proportion of unburned pulverized coal. The proportion of silicon dioxide produced. The ash melting ratio, This is the temperature coefficient of coke.

[0238] The objective function is set to minimize the squared energy residual, i.e.:

[0239]

[0240] The following set of constraints is set:

[0241]

[0242] in, The lower limit of temperature, This is the upper limit of temperature. The lower limit of coke temperature, This is the upper limit of coke temperature. The proportion of unburned pulverized coal. The proportion of silicon dioxide produced. The ash melting ratio, This is the temperature coefficient of coke.

[0243] The convergence condition is set as follows:

[0244]

[0245] in, = and , This is the optimal solution for the theoretical combustion temperature in the swirl zone. For energy tolerance, This is the equivalent total heat capacity of the output substance.

[0246] Furthermore, the calculated amount of substance of each input substance... The amount of substance of each output substance The absolute temperatures of each input substance in Tables 1 to 5 The absolute temperature of coke Theoretical combustion temperature of the swirl zone linear function, molar isobaric heat capacity Functions, latent heat of phase transition of each input substance Heat of solidification transformation of each input substance The latent heat of phase transition of each output substance Heat of solidification transformation of each output substance Total chemical reaction heat The objective function, constraints, and convergence conditions are input into a nonlinear optimization solver for iterative optimization to obtain the theoretical combustion temperature of the vortex region. .

[0247] According to the above embodiments, by introducing a multivariate optimization solution mechanism, the theoretical combustion temperature of the blast furnace tuyeres can be adaptively calculated under different injection media combinations and complex operating conditions. This method integrates key influencing factors such as the proportion of unburned pulverized coal, the proportion of silica formation, the proportion of ash melting, and the coke temperature coefficient into a parameterized energy balance model, constructing a multidimensional nonlinear optimization problem to achieve dynamic matching between the energy conservation equation and actual furnace conditions. By setting the objective function as minimizing the squared energy residual, and combining multiple constraint boundaries and convergence criteria, a balance is achieved between numerical stability and physical rationality in the calculation results. This method not only improves the prediction accuracy of the theoretical combustion temperature but also flexibly adapts to changes in different injection ratios, hydrogen-rich gas proportions, and furnace charge characteristics, significantly enhancing the model's versatility and robustness under multiple operating conditions.

[0248] This application provides a device for predicting the theoretical combustion temperature of a blast furnace tuyere, applied to the aforementioned method for predicting the theoretical combustion temperature of a blast furnace tuyere. This device is based on the same inventive concept as the method for predicting the theoretical combustion temperature of a blast furnace tuyere in one embodiment of this application, and the principle of solving the problem is similar. Therefore, the implementation of this device is the same as the implementation of the method for predicting the theoretical combustion temperature of a blast furnace tuyere in one embodiment of this application, and repeated details will not be described again. The terms "unit" or "module" used below can refer to a combination of software and / or hardware that performs a predetermined function. Although the system described in the following embodiments is preferably implemented in software, hardware implementation, or a combination of software and hardware, is also possible and contemplated.

[0249] like Figure 9 As shown, the theoretical combustion temperature prediction device 900 for the blast furnace tuyeres includes:

[0250] The input parameter acquisition module 901 is used to acquire the input material parameters, input material type and output material type of the cyclotron region.

[0251] The output substance calculation module 902 is used to determine the amount of the output substance based on the input substance parameters, output substance type, coke consumption, and multiple chemical reaction paths. The coke consumption is determined based on the input substance parameters and the input substance type.

[0252] The total reaction heat calculation module 903 is used to determine the total chemical reaction heat based on input material parameters and multiple chemical reaction pathways.

[0253] The theoretical temperature solution module 904 is used to determine the theoretical combustion temperature of the cyclone region based on the amount of substance of the input substance, the total heat of chemical reaction, the input substance parameters, the amount of substance of the output substance, the latent heat of phase change, the heat of solidification transformation, and the pre-established molar isobaric heat capacity model.

[0254] In some embodiments, the input substance types include: hot air, coke oven gas, pulverized coal, coke, pulverized coal ash, and coke ash. Input substance parameters include: the molar number and mass fraction of each component in each input substance. The theoretical combustion temperature prediction device 900 further includes a coke consumption calculation module for determining coke consumption based on the input substance parameters and input substance types, including:

[0255] The effective oxygen calculation submodule is used to determine the number of moles of effective oxygen based on the molar number of each component in hot air and coke oven gas.

[0256] The net carbon demand calculation submodule is used to determine the number of moles of net carbon demand based on the mole number and mass fraction of each component in pulverized coal, coke, pulverized coal ash, and coke ash, as well as the number of moles of available oxygen.

[0257] The net carbon supply calculation submodule is used to determine the number of moles of net carbon supply based on the mole number and mass fraction of each component in pulverized coal and coke.

[0258] The coke consumption calculation submodule is used to determine the coke consumption based on the number of moles of net carbon demand and the number of moles of net carbon supply.

[0259] In some embodiments, the effective oxygen calculation submodule includes:

[0260] The input oxygen calculation unit is used to determine the number of moles of input oxygen based on the number of moles of oxygen in the hot air and coke oven gas.

[0261] The hydrocarbon oxygen consumption calculation unit is used to determine the number of moles of oxygen consumed corresponding to the equivalent carbon in the hydrocarbons based on the total number of moles of equivalent carbon in the coke oven gas.

[0262] The effective oxygen solution unit is used to determine the number of effective oxygen moles based on the number of input oxygen moles and the number of oxygen consumed moles.

[0263] In some embodiments, the net carbon demand calculation submodule includes:

[0264] The unit for calculating the molar amount of silicon dioxide in ash is used to determine the molar amount of silicon dioxide in coke ash based on the coke mass, the mass fraction of coke ash in coke, the mass fraction of silicon dioxide in coke ash and pulverized coal ash, and the molar mass of silicon dioxide.

[0265] The net carbon demand calculation unit is used to determine the number of moles of net carbon required based on the number of moles of available oxygen, the number of moles of water vapor in hot air and coke oven gas, the number of moles of carbon dioxide in coke oven gas, pulverized coal ash and coke ash, the number of moles of silicon dioxide in pulverized coal ash, the number of moles of silicon dioxide in coke ash and the preset silicon dioxide generation ratio.

[0266] In some embodiments, the net carbon supply calculation submodule is specifically used to: determine the number of moles of net carbon supply based on preset unburned coal powder ratio, coke mass, coal powder mass, fixed carbon mass fraction of coal powder, fixed carbon mass fraction of coke, and molar mass of carbon.

[0267] In some embodiments, the total reaction heat calculation module 903 includes:

[0268] The equivalence number calculation submodule is used to determine the equivalence number of each chemical reaction pathway based on the moles of available oxygen, water vapor, carbon dioxide, silica in pulverized coal ash, and silica in coke ash, and their corresponding chemical reaction pathways. These chemical reaction pathways include: carbon oxidation, water-gas reaction, carbon gasification, methane cracking, silica reduction, and graphitization.

[0269] The reaction heat calculation submodule is used to determine the chemical reaction heat of each chemical reaction path based on the equivalent number and standard enthalpy of formation corresponding to each chemical reaction path.

[0270] The total reaction heat summary submodule is used to determine the total chemical reaction heat based on the chemical reaction heat of each chemical reaction pathway and the equivalent decomposition heat of pulverized coal.

[0271] In some embodiments, the chemical reaction pathway includes: a carbon oxidation reaction pathway, a water-gas reaction pathway, a carbon gasification reaction pathway, and a silicon dioxide reduction reaction pathway. Output substance types include: carbon monoxide, hydrogen, silicon dioxide, unburned coal powder, and various ash oxides, etc. The output substance calculation module 902 includes:

[0272] The gaseous product calculation submodule is used to determine the amount of carbon monoxide, hydrogen, and silicon dioxide based on input material parameters, coke consumption, preset silicon dioxide generation ratio, carbon oxidation reaction path, water-gas reaction path, carbon gasification reaction path, and silicon dioxide reduction reaction path.

[0273] The ash oxide calculation submodule is used to determine the amount of each ash oxide based on the input material parameters and coke consumption.

[0274] The unburned coal powder calculation submodule is used to determine the amount of unburned coal powder based on the coal powder quality and the preset unburned coal powder ratio.

[0275] In some embodiments, the input material parameters further include: absolute temperature. The theoretical temperature solution module 904 includes:

[0276] The input-side enthalpy function establishment submodule is used to establish the first relationship function between the input-side relative enthalpy and the theoretical combustion temperature of the cyclone zone, based on the amount of substance corresponding to the input substance type, the pre-established molar isobaric heat capacity model, the absolute temperature, the latent heat of phase transition, and the solid-crystallization heat of transition. The absolute temperature of the coke is a linear function established by the theoretical combustion temperature of the cyclone zone and a preset constant.

[0277] The output-side enthalpy function establishment submodule is used to establish a second relationship function between the output-side relative enthalpy and the theoretical combustion temperature of the cyclotron region based on the amount of substance corresponding to the output substance type, the pre-established molar isobaric heat capacity model, the latent heat of phase change and the solid-crystallization heat of change.

[0278] The energy residual function establishment submodule is used to establish a third relationship function between the energy residual and the theoretical combustion temperature of the cyclone zone based on the first relationship function, the total heat of chemical reaction, and the second relationship function.

[0279] The temperature optimization solution submodule is used to solve the third relation function based on the preset objective function, constraints and convergence conditions to obtain the theoretical combustion temperature of the vortex zone.

[0280] Figure 10 This is a schematic diagram of the physical structure of a computer device provided in an embodiment of the present invention, such as... Figure 10 As shown, the computer device 1000 includes: a processor 1001, a memory 1002, and a bus 1003.

[0281] The processor 1001 and the memory 1002 communicate with each other via the bus 1003.

[0282] The processor 1001 is used to call program instructions in the memory 1002 to execute the methods provided in the above-described method embodiments.

[0283] This invention also provides a computer-readable storage medium storing a computer program that, when executed by a processor, implements the above-described method for predicting the theoretical combustion temperature of a blast furnace tuyer.

[0284] This invention also provides a computer program product, which includes a computer program that, when executed by a processor, implements the above-mentioned method for predicting the theoretical combustion temperature of a blast furnace tuyer.

[0285] Those skilled in the art will understand that embodiments of the present invention can be provided as methods, systems, or computer program products. Therefore, the present invention can take the form of a completely hardware embodiment, a completely software embodiment, or an embodiment combining software and hardware aspects. Furthermore, the present invention can take the form of a computer program product embodied on one or more computer-usable storage media (including, but not limited to, disk storage, CD-ROM, optical storage, etc.) containing computer-usable program code.

[0286] This invention is described with reference to flowchart illustrations and / or block diagrams of methods, apparatus (systems), and computer program products according to embodiments of the invention. It will be understood that each block of the flowchart illustrations and / or block diagrams, and combinations of blocks in the flowchart illustrations and / or block diagrams, can be implemented by computer program instructions. These computer program instructions can be provided to a processor of a general-purpose computer, special-purpose computer, embedded processor, or other programmable data processing apparatus to produce a machine, such that the instructions, which execute via the processor of the computer or other programmable data processing apparatus, generate instructions for implementing the flowchart illustrations and / or block diagrams. Figure 1 One or more processes and / or boxes Figure 1 A device that provides the functions specified in one or more boxes.

[0287] These computer program instructions may also be stored in a computer-readable storage medium that can direct a computer or other programmable data processing device to function in a particular manner, such that the instructions stored in the computer-readable storage medium produce an article of manufacture including instruction means, which are implemented in a process Figure 1 One or more processes and / or boxes Figure 1 The function specified in one or more boxes.

[0288] These computer program instructions may also be loaded onto a computer or other programmable data processing equipment to cause a series of operational steps to be performed on the computer or other programmable equipment to produce a computer-implemented process, thereby providing instructions that execute on the computer or other programmable equipment for implementing the process. Figure 1 One or more processes and / or boxes Figure 1 The steps of the function specified in one or more boxes.

[0289] In the description of this specification, the references to terms such as "an embodiment," "a specific embodiment," "some embodiments," "for example," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples.

[0290] The specific embodiments described above further illustrate the purpose, technical solution, and beneficial effects of the present invention. It should be understood that the above descriptions are merely specific embodiments of the present invention and are not intended to limit the scope of protection of the present invention. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present invention should be included within the scope of protection of the present invention.

Claims

1. A method for predicting the theoretical combustion temperature of a blast furnace tuyeres, characterized in that, include: Obtain the input material parameters, input material type, and output material type in the cyclotron region; Based on the input material parameters, the output material type, coke consumption, and multiple chemical reaction pathways, the amount of the output material is determined; wherein, the coke consumption is determined based on the input material parameters and the input material type. Based on the input material parameters and multiple chemical reaction pathways, the total chemical reaction heat is determined; The theoretical combustion temperature of the cyclone zone is determined based on the amount of substance of the input substance, the total heat of chemical reaction, the parameters of the input substance, the amount of substance of the output substance, the latent heat of phase change, the heat of solidification transformation, and a pre-established molar isobaric heat capacity model.

2. The method according to claim 1, characterized in that, The input substance types include: hot air, coke oven gas, pulverized coal, coke, pulverized coal ash, and coke ash; the input substance parameters include: the molar number and mass fraction of each component in each input substance; determining the coke consumption based on the input substance parameters and input substance types includes: The number of effective oxygen moles is determined based on the number of moles of each component in the hot air and the coke oven gas. The net carbon requirement is determined based on the molar number and mass fraction of each component in the pulverized coal, coke, pulverized coal ash, and coke ash, as well as the molar number of available oxygen. The number of moles of net carbon supplied is determined based on the mole number and mass fraction of each component in the pulverized coal and coke. The amount of coke consumed is determined based on the number of moles of net carbon demand and the number of moles of net carbon supply.

3. The method according to claim 2, characterized in that, The step of determining the effective oxygen mole count based on the mole counts of each component in the hot air and the coke oven gas includes: The number of moles of oxygen input is determined based on the number of moles of oxygen in the hot air and the coke oven gas. The number of oxygen consumed corresponding to the equivalent carbon in the coke oven gas is determined based on the total number of moles of hydrocarbon equivalent carbon in the coke oven gas. The effective number of moles of oxygen is determined based on the number of moles of input oxygen and the number of moles of oxygen consumed.

4. The method according to claim 2 or 3, characterized in that, The determination of the net carbon requirement in moles based on the molar numbers and mass fractions of each component in pulverized coal, coke, pulverized coal ash, and coke ash, as well as the molar number of available oxygen, includes: The number of moles of silicon dioxide in the coke ash is determined based on the coke mass, the mass fraction of coke ash in the coke, the mass fraction of silicon dioxide in the coke ash and pulverized coal ash, and the molar mass of silicon dioxide. The required number of moles of net carbon is determined based on the number of moles of effective oxygen, the number of moles of water vapor in the hot air and coke oven gas, the number of moles of carbon dioxide in the coke oven gas, the pulverized coal ash and the coke ash, the number of moles of silicon dioxide in the pulverized coal ash, the number of moles of silicon dioxide in the coke ash and the preset silicon dioxide generation ratio.

5. The method according to claim 2, characterized in that, The determination of the net carbon supply moles based on the mole number and mass fraction of each component in the pulverized coal and coke includes: The number of moles of net carbon supplied is determined based on the preset proportion of unburned pulverized coal, coke mass, pulverized coal mass, fixed carbon mass fraction of pulverized coal, fixed carbon mass fraction of coke, and molar mass of carbon.

6. The method according to claim 4, characterized in that, The determination of the total chemical reaction heat based on the input material parameters and multiple chemical reaction pathways includes: Based on the molar number of available oxygen, the molar number of water vapor, the molar number of carbon dioxide, the molar number of silica in the pulverized coal ash, the molar number of silica in the coke ash, and their respective corresponding chemical reaction pathways, the equivalent number of each chemical reaction pathway is determined; wherein, the chemical reaction pathways include: carbon oxidation reaction, water-gas reaction, carbon gasification reaction, methane cracking reaction, silica reduction reaction, and graphitization reaction; The heat of chemical reaction for each chemical reaction pathway is determined based on the equivalent number and standard enthalpy of formation corresponding to each chemical reaction pathway. The total heat of chemical reaction is determined based on the heat of chemical reaction of each of the described chemical reaction pathways and the equivalent heat of decomposition of pulverized coal.

7. The method according to claim 1, characterized in that, The chemical reaction pathways include: carbon oxidation reaction pathway, water-gas reaction pathway, carbon gasification reaction pathway, and silicon dioxide reduction reaction pathway; the output substance types include: carbon monoxide, hydrogen, silicon dioxide, unburned coal powder, and various ash oxides, etc.; the determination of the amount of output substance based on the input substance parameters, the output substance types, coke consumption, and multiple chemical reaction pathways includes: Based on the input material parameters, the coke consumption, the preset silicon dioxide generation ratio, the carbon oxidation reaction path, the water gas reaction path, the carbon gasification reaction path, and the silicon dioxide reduction reaction path, the amount of carbon monoxide, the amount of hydrogen, and the amount of silicon dioxide are determined respectively. Based on the input material parameters and the coke consumption, determine the amount of each ash oxide. The amount of unburned coal powder is determined based on the coal powder quality and the preset proportion of unburned coal powder.

8. The method according to claim 1, characterized in that, The input material parameters also include: absolute temperature; the determination of the theoretical combustion temperature in the cyclone region based on the amount of substance of the input material, the total heat of chemical reaction, the input material parameters, the amount of substance of the output material, the latent heat of phase change, the heat of solidification transition, and a pre-established molar isobaric heat capacity model includes: Based on the amount of substance corresponding to the input substance type, the pre-established molar isobaric heat capacity model, the absolute temperature, the latent heat of phase change, and the solid-crystal transformation heat, a first relationship function is established between the relative enthalpy on the input side and the theoretical combustion temperature of the cyclone zone; wherein, the absolute temperature of coke is a linear function established by the theoretical combustion temperature of the cyclone zone and a preset constant. Based on the amount of substance corresponding to the type of output substance, the pre-established molar isobaric heat capacity model, the latent heat of phase change and the solidification transformation heat, a second relationship function is established between the relative enthalpy on the output side and the theoretical combustion temperature of the cyclotron region. Based on the first relational function, the total heat of chemical reaction and the second relational function, a third relational function is established between the energy residual and the theoretical combustion temperature of the vortex zone. Based on the preset objective function, constraints, and convergence conditions, the third relational function is solved to obtain the theoretical combustion temperature of the vortex zone.

9. A device for predicting the theoretical combustion temperature of a blast furnace tuyeres, characterized in that, include: The input parameter acquisition module is used to acquire the input substance parameters, input substance type, and output substance type in the cyclotron region. The output substance calculation module is used to determine the amount of the output substance based on the input substance parameters, the output substance type, the coke consumption, and multiple chemical reaction paths; wherein the coke consumption is determined based on the input substance parameters and the input substance type. The total reaction heat calculation module is used to determine the total chemical reaction heat based on the input material parameters and multiple chemical reaction pathways. The theoretical temperature calculation module is used to determine the theoretical combustion temperature of the cyclone region based on the amount of substance of the input substance, the total heat of chemical reaction, the parameters of the input substance, the amount of substance of the output substance, the latent heat of phase change, the heat of solidification transformation, and a pre-established molar isobaric heat capacity model.

10. A computer device, comprising a memory, a processor, and a computer program stored in the memory and executable on the processor, characterized in that, When the processor executes the computer program, it implements the method of any one of claims 1 to 8.

11. A computer-readable storage medium, characterized in that, The computer-readable storage medium stores a computer program that, when executed by a processor, implements the method of any one of claims 1 to 8.

12. A computer program product, characterized in that, The computer program product includes a computer program that, when executed by a processor, implements the method of any one of claims 1 to 8.

Images