Prediction method and system for blast furnace containing hydrogen fuel

Abstract

Prediction methods and systems for a blast furnace containing hydrogen fuel are provided. The method separates Fe-C-O-H system into Fe-O-H system and Fe-O-C system in the blast furnace containing hydrogen fuel, the method includes the steps of, firstly, drawing the operating line of Fe-C-O-H system in Rist diagram, and then drawing the operating line of Fe-O-H system and the operating line of Fe-O-C system, and the method can simplify the complexity of the calculation.

Description

[Technical Field]

[0001] This invention relates to a method and system for predicting blast furnaces containing hydrogen fuel, and in particular to a method and system for predicting blast furnaces containing hydrogen fuel using a blast furnace model. [Previous Technology]

[0002] The blast furnace ironmaking system is the largest single piece of equipment and energy conversion process, in which coke and coal play a crucial role in producing reducing agents (H2 and CO) for iron ore reduction. During the smelting process, the coke, pulverized coal, and hot blast entering the blast furnace react to generate carbon monoxide (CO), the gas required for reducing iron ore. The reduction of iron oxides by carbon monoxide results in the generation of large amounts of carbon dioxide (CO2), and carbon dioxide is also generated during the gasification reaction. Therefore, the blast furnace process inevitably emits a significant amount of carbon dioxide. To reduce carbon dioxide emissions, many low-carbon iron production technologies have been developed over the past few decades, such as hydrogen injection and carbon capture and storage (CCS).

[0003] It is worth noting that, if carbon capture and storage is not considered, hydrogen-rich gas (H2, methane, coke oven gas) injection technology may be an effective option for reducing carbon dioxide emissions. In this case, adding hydrogen-rich gas to replace part of the reducing agent in the blast furnace can reduce carbon dioxide emissions in the blast furnace by more than 30%. In addition, using a blast furnace model for simulation, under the optimal operating conditions of hydrogen injection rate, carbon dioxide emissions in the blast furnace can be reduced by more than 20% in another way.

[0004] Currently, blast furnace modeling methods are widely used to simulate key processes such as internal flow, chemical reactions, and heat transfer within blast furnaces. However, in the metallurgical industry, pig iron production is highly complex, and decarbonization strategies simulated using blast furnace models cannot effectively assess the potential for carbon dioxide emission reduction. This is because blast furnaces are typically considered a black box in ironmaking reactions, and their simulations cannot reveal the actual reaction processes inside, resulting in high uncertainty. Therefore, blast furnace models still cannot accurately simulate the internal material and energy flows, thus limiting carbon reduction capabilities.

[0005] Furthermore, the existing methods for calculating blast furnace operating lines are overly complex. Therefore, to overcome the shortcomings and deficiencies of the prior art, this invention needs to provide an improved method and system for predicting blast furnace operation using hydrogen-containing fuel, in order to solve the problems existing in the aforementioned prior art. [Summary of the Invention]

[0006] The main objective of this invention is to provide a method and system for predicting the effects of hydrogen fuel in blast furnaces. By decomposing the iron-carbon-oxygen-hydrogen (Fe-COH) system in the hydrogen fuel blast furnace into an iron-oxygen-hydrogen (Fe-OH) system and an iron-oxygen-carbon (Fe-OC) system, and drawing the Liss diagram operation lines of the Fe-OH system and the Fe-OC system respectively, the complexity of the calculation can be simplified.

[0007] To achieve the above objectives, the present invention provides a method for predicting the operation line of a blast furnace containing hydrogen fuel. The method includes the following steps: a Rist diagram operation line formation step for the Fe-COH system, drawing the Rist diagram operation line of the Fe-COH system of the blast furnace using blast furnace data, wherein the data includes at least one of upper blast furnace area data, heat reserve area data, lower blast furnace area data, blast diameter area data, and separation area data; a Rist diagram operation line formation step for the Fe-OH system, drawing the Rist diagram operation line of the Fe-OH system of the blast furnace by calculating the chemical balance between gas and solid in the Fe-OH system of the heat reserve area of ​​the blast furnace; and a Rist diagram operation line formation step for the Fe-OC system, drawing the Rist diagram operation line of the Fe-OC system using the reducing gas utilization rate of the Fe-OH system and the Fe-COH system... The total reducing gas utilization rate is calculated for the Fe-OC system of the blast furnace, and the Liss diagram operating line of the Fe-OC system is plotted based on the reducing gas utilization rate of the Fe-OC system and the chemical balance between gas and solid in the Fe-OC system of the thermal reserve zone. Based on the Liss diagram operating lines of the Fe-COH system, the Fe-OH system, and the Fe-OC system, at least one of the following is predicted: blast furnace iron composition, blast furnace output, blast furnace top gas composition, slag composition, blast furnace belly gas composition, blast furnace belly gas flow rate, overall blast furnace carbon emissions, and blast furnace production cost.

[0008] In some embodiments of the present invention, the Liss diagram operating line of the Fe-COH system is obtained by the chemical equilibrium between the gas and solid of the Fe-COH system in the thermal reserve and the ratio of the reducing gas mole number to the iron mole number in the molten iron.

[0009] In some embodiments of the present invention, the ratio of the reducing gas mole number to the iron mole number in the molten iron can be obtained by the following formula: where represents the mole number of carbon components fed into the iron ore; represents the mole number of carbon components fed into the coke; represents the mole number of water components supplied by the blower from the air path zone; represents the mole number of carbon components supplied by the pulverized coal from the air path zone; represents the mole number of hydrogen components supplied by the pulverized coal from the air path zone; represents the mole number of water components supplied by the pulverized coal from the air path zone; represents the mole number of iron components in the molten iron; and represents the mass fraction of carbon components in the molten iron.

[0010] In some embodiments of the present invention, the chemical equilibrium between the gas and solid in the Fe-COH system includes the theoretical equilibrium point or the actual equilibrium point of the Fe-COH system. The abscissa of the theoretical equilibrium point of the Fe-COH system is calculated by XW = 1 + (1 - xh)ωWC + xhωWH, and the ordinate YW of the theoretical equilibrium point of the Fe-COH system is 1.05, where xh is the mole fraction of H2 and H2O in the reducing gas; ωWC is the mole fraction of the equilibrium state of the Fe-OC system; and ωWH is the mole fraction of the equilibrium state of the Fe-OH system.

[0011] In some embodiments of the present invention, the horizontal coordinate of the actual equilibrium point of the Fe-COH system is XR = 1 + r(XW - 1) and the vertical coordinate of the actual equilibrium point of the Fe-COH system is YR = YA + r(YA - YW), where r represents the ratio of the oxygen actually exchanged in the blast furnace to the oxygen theoretically exchanged; YA represents the initial oxidation state of the iron oxide.

[0012] In some embodiments of the present invention, the chemical equilibrium between the gas and solid in the Fe-OH system includes the theoretical equilibrium point of the Fe-OH system. The abscissa of the theoretical equilibrium point of the Fe-OH system is calculated by XW = 1 + xhωWH, and the ordinate YW of the theoretical equilibrium point of the Fe-OH system is 1.05, where xh is the mole fraction of H2 and H2O in the reducing gas; and ωWH is the mole fraction of the equilibrium state of the Fe-OH system.

[0013] In some embodiments of the present invention, the operation line of the Liss diagram of the Fe-OH system is drawn by connecting the theoretical equilibrium point or the actual equilibrium point of the Fe-COH system with the coordinate point (1,0) on the Liss diagram.

[0014] In some embodiments of the present invention, the chemical equilibrium between the gas and solid in the Fe-OC system includes the theoretical equilibrium point or the actual equilibrium point of the Fe-OC system. The abscissa of the theoretical equilibrium point of the Fe-OC system is calculated by XW = 1 + (1 - xh)ωWC, and the ordinate YW of the theoretical equilibrium point of the Fe-OC system is 1.05, where xh is the molar fraction of H2 and H2O in the reducing gas; and ωWC is the molar fraction of the equilibrium state of the Fe-OC system.

[0015] In some embodiments of the present invention, the total reducing gas utilization rate of the Fe-COH system; the reducing gas utilization rate of the Fe-OH system; and the reducing gas utilization rate of the Fe-OC system, wherein.

[0016] Furthermore, the present invention also provides a blast furnace prediction system for hydrogen fuel, comprising: an actuator equipped with a means for performing the method described above.

Implementation Method

[0017] To make the above and other objects, features, and advantages of the present invention more apparent and understandable, embodiments of the present invention will be specifically described below in conjunction with the accompanying drawings. Furthermore, the directional terms used in this invention, such as up, down, top, bottom, front, back, left, right, inside, outside, side, surrounding, center, horizontal, transverse, vertical, longitudinal, axial, radial, uppermost, or lowermost, are merely for reference to the accompanying drawings. Therefore, the directional terms used are for illustrating and understanding the present invention, and not for limiting the present invention.

[0018] Please refer to Figures 1 and 2, which illustrate a blast furnace system according to an embodiment of the present invention. In this embodiment, the blast furnace system is constructed using simulation software (e.g., Aspen Plus) to create a steady-state model. The blast furnace system includes at least an upper blast furnace zone 2, a heat reserve zone 3, a lower blast furnace zone 4, a heating zone 5, a separation zone 6, and a blast diameter zone 7. The upper blast furnace zone 2, heat reserve zone 3, lower blast furnace zone 4, and blast diameter zone 7 are simulated using the reactor RStoic module; the separation zone 6 is simulated using the separator Sep module. The detailed structure, assembly relationship, and operating principle of each component will be described in detail below.

[0019] The hydrogen-containing fuel referred to in this invention refers to fuel and hydrogen gas containing hydrocarbon substances containing hydrogen atoms.

[0020] As shown in Figure 1, the blast furnace system of the present invention corresponds to a blast furnace 101. Its process mainly utilizes raw materials such as iron ore, coke, pulverized coal, and hot blast to produce hot metal. For example, iron ore and coke are fed from the top of the blast furnace 101, while pulverized coal and hot blast are injected into the tuyeres 7. In the tuyeres 7, coke, pulverized coal, and hot blast react to generate the required reducing gas, carbon monoxide. The remaining coke continues to react with the iron ore. Then, the carbon monoxide rises within the blast furnace 101 and reduces the descending iron ore into the required hot metal. The reducing gas eventually forms blast furnace gas, which is discharged from the top of the blast furnace 101. Finally, the hot metal and slag separate at the bottom of the blast furnace 101 to obtain the desired hot metal.

[0021] Refer to Figures 1 and 2. The upper blast furnace zone 2 includes a first reactor 21. The first reactor 21 is configured to input the iron ore and the coke. The reaction formulas of the first reactor 21 include: 3Fe2O3 + CO → 2Fe3O4 + CO2 ∆H = -52.85 kJ / mol; Fe3O4 + CO → 3FeO + CO2 ∆H = +36.46 kJ / mol; 3Fe2O3 + H2 → 2Fe3O4 + H2O ∆H = -4.86 kJ / mol; Fe3O4 + H2 → 3FeO + H2O ∆H = +84.45 kJ / mol.

[0022] Furthermore, in the upper blast furnace zone 2, the following equation 1 is used as the target specification in the blast furnace operation diagram set in the first reactor 21, and the content ratio of hematite (Fe2O3), ferromagnetite (FeO) and magnetite (Fe3O4) is estimated based on the conversion rate of magnetite (Fe3O4) as the control variable.

[0023] Specifically, hematite (Fe2O3) in iron ore will first undergo a reduction reaction with carbon monoxide (CO) and hydrogen (H2) to completely form magnetite (Fe3O4), and then some magnetite (Fe3O4) will react with carbon monoxide (CO) and hydrogen (H2) to form argumentite (FeO).

[0024] The heat reserve zone 3 is located below the upper blast furnace zone 2. The heat reserve zone 3 is configured to receive the magnetite (Fe3O4) and the aragonite (FeO) formed by the reaction in the upper blast furnace zone 2. Specifically, the heat reserve zone 3 includes a second reactor 31 connected to the first reactor 21, and the second reactor 31 is configured to receive the magnetite (Fe3O4) and the aragonite (FeO) for reaction. During this process, the aragonite (FeO) is partially reduced (indirectly reduced). The above process is exothermic for CO and endothermic for H2. Furthermore, the water-gas shift reaction reaches equilibrium in this zone. The reaction formulas of the second reactor 31 include: FeO + H2 → Fe + H2O ∆H = +30.86 kJ / mol; Fe3O4 + CO → 3FeO + CO2 ∆H = -17.13 kJ / mol; CO2 + H2 → CO + H2O ∆H = +40.45 kJ / mol.

[0025] Besides direct reduction, other related reactions also occur in the lower blast furnace zone 4. The furnace charge contains various impurities, which dissolve in the molten iron or form part of the slag. For example, Al2O3, CaO, and MgO oxides are not reduced under blast furnace conditions, so they are completely transferred to the slag. SiO2, MnO, P2O5, and TiO2 are partially reduced and dissolved in the molten iron. These impurities can be considered to be directly reduced by solid carbon. The final content of silicon, manganese, and phosphorus in the molten iron is far below the equilibrium value. When the injected fuel contains sulfur (e.g., pulverized coal), it will eventually form part of the slag. After simplification, it can be assumed that sulfur dissolves into the molten iron and then transfers to the slag. The above reactions can be represented by the following equations: Fe + S → FeS; FeS + CaO + C → Fe + CaS + CO ∆H = +143 kJ / mol; FeO + C → Fe + CO ∆H = +155.34 kJ / mol; SiO2 + 2C → Si + 2CO ∆H = +637 kJ / mol; MnO + C → Mn + CO ∆H = +286.92 kJ / mol; P2O5 + 5C → 2P + 5CO ∆H = +861.904 kJ / mol; TiO2 + 2C → Ti + 2CO ∆H = +541.242 kJ / mol.

[0026] Draw the blast furnace operation diagram (Rist diagram) for Fe-COH.

[0027] Please refer to Figure 3, which shows a schematic diagram of the operation process of a blast furnace operation diagram (Rist diagram) drawn according to an embodiment of the present invention. The blast furnace operation diagram serves as a graphical tool to analyze changes in direct and indirect reduction reactions within a specified region of the blast furnace.

[0028] The method includes the following steps: Step S11, forming the Reiss diagram operation line of the Fe-COH system, drawing the Reiss diagram operation line of the Fe-COH system of the blast furnace using data from the blast furnace, wherein the data includes at least one of the upper blast furnace area data, heat reserve area data, lower blast furnace area data, wind diameter area data, and separation area data; Step S12, forming the Reiss diagram operation line of the Fe-OH system, drawing the Reiss diagram operation line of the Fe-OH system of the blast furnace by calculating the chemical balance between the gas and solid in the Fe-OH system of the heat reserve area of ​​the blast furnace; Step S13, forming the Reiss diagram operation line of the Fe-OC system, calculating the reducing gas utilization rate of the Fe-OC system of the blast furnace using the reducing gas utilization rate of the Fe-OH system and the total reducing gas utilization rate of the Fe-COH system, and drawing the Reiss diagram operation line of the Fe-OC system using the reducing gas utilization rate of the Fe-OC system and the chemical balance between the gas and solid in the Fe-OC system of the heat reserve area.

[0029] Please refer to Figure 4, which is a schematic diagram of a blast furnace operation diagram drawn according to an embodiment of the present invention. First, the Reiss diagram operation line of the Fe-COH system of the blast furnace is drawn using blast furnace data, wherein the data includes at least one of the following: upper blast furnace zone data, heat reserve zone data, lower blast furnace zone data, blast diameter zone data, and separation zone data. This data can be provided by actual plant experience or technical data. Wherein C represents the mole number of carbon atoms; Fe represents the mole number of iron atoms; H2 represents the mole number of hydrogen molecules; O represents the mole number of oxygen atoms; X represents the coordinate, representing the composition of the gas in the blast furnace; Y represents the vertical coordinate, representing the composition of the solids in the blast furnace.

[0030] In one embodiment, the Liss diagram operating line of the Fe-COH system is obtained by the chemical equilibrium between the gas and solid of the Fe-COH system in the thermal reserve zone 3 and the ratio of the reducing gas mole number to the iron mole number in the molten iron.

[0031] The equilibrium line is determined by five points (M2, M, W2, W, and F), whose corresponding coordinates are shown in Table 1. The units of the X and Y axes are defined by X = (O + H2) / (C + H2) (where the numerator is the mole number of reducing gases from hydrogen and oxygen sources associated with a specific reaction or injection, and the denominator is the total mole number of reducing gases from hydrogen and carbon sources) and Y = (O + H2) / Fe, respectively. The operating line is described by Y = μ(X - XR) + YR. Table 1 point X Y F (iron, Fe) X F = X W Y F = 0 W (Ferrous iron ore, Fe) 0.95 O) X W = Equation 2 Y W = 1.05 W2 (Ferritin, Fe) 0.89 O) X W2 = X M Y W2 = 1.12 M (magnetite, Fe3O4) X M = Equation 3 Y M = 1.33 M2 (magnetite, Fe3O4) X M2 = 2 Y M2 = 1.33

[0032] The chemical equilibrium between the gas and solid in the Fe-COH system includes the theoretical equilibrium point or the actual equilibrium point of the Fe-COH system. The x-coordinate of the theoretical equilibrium point of the Fe-COH system is calculated using Equation 2. The y-coordinate of the theoretical equilibrium point of the Fe-COH system, YW, is 1.05, where xh is the mole fraction of H2 and H2O in the reducing gas; ωWC is the mole fraction of the equilibrium state of the Fe-OC system; and ωWH is the mole fraction of the equilibrium state of the Fe-OH system. XW = 1 + (1 - xh)ωWC + xhωWH Equation 2 XM = 1 + (1 - xh)ωMC + xhωMH Equation 3

[0033] Specifically, ωWC can be represented as nCO2 / (nCO+nCO2); ωWH can be represented as nH2O / (nH2+nH2O).

[0034] In addition, the actual equilibrium point of the Fe-COH system can be calculated from the theoretical equilibrium point of the Fe-COH system. Its horizontal axis is calculated by XR = 1 + r(XW - 1), and its vertical axis is calculated by YR = YA + r(YA - YW), where r represents the ratio of the oxygen actually exchanged in the blast furnace to the oxygen theoretically exchanged; YA represents the initial oxidation state of the iron oxide, for example, for Fe2O3, YA = 1.5.

[0035] Based on the above method, the theoretical equilibrium point of the Fe-COH system, namely the WCO-CO2-H2-H2O point, or the actual equilibrium point of the Fe-COH system, namely the RCO-CO2-H2-H2O point, can be calculated.

[0036] The ratio of the mole number of the reducing gas to the mole number of the iron in the molten iron can be obtained by the following formula: , where represents the mole number of the carbon component in the iron ore; represents the mole number of the carbon component in the coke; represents the mole number of the water component provided by the blower from the air path zone; represents the mole number of the carbon component provided by the pulverized coal from the air path zone; represents the mole number of the hydrogen component provided by the pulverized coal from the air path zone; represents the mole number of the water component provided by the pulverized coal from the air path zone; represents the mole number of the iron component in the molten iron; and represents the mass fraction of the carbon component in the molten iron.

[0037] Specifically, the ratio of the reducing gas mole number to the iron mole number in the molten iron is the slope of the operating line of the Liss diagram of the Fe-COH system. The operating line of the Liss diagram of the Fe-COH system (i.e., the black line in Figure 4) can be plotted in a point-slope manner using the WCO-CO2-H2-H2O point (or the RCO-CO2-H2-H2O point) and the slope.

[0038] It should be noted that the above-mentioned point-slope calculation method is only one embodiment of the present invention. The Rist diagram operation line of the Fe-COH system can also be drawn in any known way, such as referring to the method proposed by Bailera et al. "Revisiting the Rist diagram for predicting operating conditions in blast furnaces with multiple injections", which will not be elaborated here.

[0039] Furthermore, the operating line of the Fe-OH system of the blast furnace is plotted by calculating the chemical equilibrium between the gas and solid in the Fe-OH system of the blast furnace's heat reserve zone.

[0040] Specifically, the chemical equilibrium between the gas and solid phases of the Fe-OH system includes the theoretical equilibrium point of the Fe-OH system. The x-coordinate of this theoretical equilibrium point is calculated using XW = 1 + xhωWH, and the y-coordinate YW is 1.05. Through the above calculations, the theoretical equilibrium point of the Fe-OH system, i.e., the WH2-H2O point, can be calculated. Furthermore, the actual equilibrium point of the Fe-OH system, i.e., the RH2-H2O point, can also be calculated using the theoretical equilibrium point WH2-H2O. Utilizing the characteristics of the hydrogen reduction reaction, it only passes through the point (1,0) on the Liss diagram. The Liss diagram operation line of the Fe-OH system is plotted using the calculated WH2-H2O point (or RH2-H2O point).

[0041] In addition, the equilibrium line can be drawn using the Baur-Glaessner plot method to obtain the WH2-H2O point (or RH2-H2O point).

[0042] Next, the reducing gas utilization rate of the Fe-OC system of the blast furnace is calculated by the reducing gas utilization rate of the Fe-OH system and the total reducing gas utilization rate of the Fe-COH system, and the Riess diagram operation line of the Fe-OC system is plotted by the reducing gas utilization rate of the Fe-OC system and the chemical balance between the gas and solid in the Fe-OC system of the thermal reserve zone.

[0043] Specifically, the total reducing gas utilization rate of the Fe-COH system is , where . The reducing gas utilization rate of the Fe-OH system can be obtained from the Liss diagram operation line of the Fe-COH system and the Liss diagram operation line of the Fe-OH system. The reducing gas utilization rate of the Fe-OC system can be calculated from the total reducing gas utilization rate and the reducing gas utilization rate of the Fe-OH system, i.e., the point on Figure 4. In addition, the x-coordinate of the theoretical equilibrium point of the Fe-OC system for the chemical equilibrium between the gas and solid in this Fe-OC system is calculated using XW = 1 + (1 - xh)ωWC, and the y-coordinate YW is 1.05. Through the above calculation, the theoretical equilibrium point of the Fe-OC system, i.e., the WCO-CO2 point, can be calculated. Furthermore, the actual equilibrium point of the Fe-OC system, i.e., the RCO-CO2 point, can also be calculated from the theoretical equilibrium point WCO-CO2 of the Fe-OC system. The Liss diagram operation line of the Fe-OC system can be plotted using the point and the WCO-CO2 point (or the RCO-CO2 point).

[0044] Similarly, the balance line can be drawn using the Baur-Glaessner plot method to obtain the WCO-CO2 point (or RCO-CO2 point).

[0045] The blast furnace blasting and charging conditions are input into the blast furnace model constructed by the inventors (see the inventors' previous applications 113130578, 113130577 and the paper entitled "Development of simple blast furnace models for addressing carbon reduction strategies" published during the preferential period). The relevant parameters of the operating lines obtained from the Liskov operating lines of the Fe-COH system, Fe-OH system, and Fe-OC system plotted using the method of this invention, such as the conversion rate of ferroic ore (FeO) in the heat reserve zone and the gas composition of the upper blast furnace zone, are used as the initial settings for the upper blast furnace zone and the heat retention zone. After inputting the operating parameters and relevant initial values ​​into the model, calculations are performed to obtain the blast furnace's iron composition, iron production, blast furnace top gas composition, slag composition, and blast furnace production cost.

[0046] The parameters used in the upper blast furnace zone 2 and the heat reserve zone 3 mentioned above, such as the FeO conversion rate, are estimated using the Ries diagram of the present invention.

[0047] The present invention also provides a blast furnace prediction system for hydrogen fuel, comprising: an actuator equipped with a means for performing the method described above.

[0048] It should be noted that although some forms have been described in the context of this invention, it should be understood that these forms also represent descriptions of corresponding methods. Therefore, system or structural elements should also be understood as corresponding method steps or features of method steps. Similarly, forms already described in the context of method steps or as method steps also represent descriptions of corresponding blocks, details, or features of the corresponding device. Some or all of the method steps can be performed using hardware devices such as microcontrollers, programmable computers, or electronic circuits. In some embodiments, some or several of the most important method steps can be performed by such devices.

[0049] Depending on specific implementation requirements, embodiments of the present invention can be implemented in hardware or software. It can be implemented using digital storage media, such as floppy disk drives, DVDs, Blu-ray drives, CDs, ROMs, PROMs, EPROMs, EEPROMs, or FLASH memory, hard disks, or any other magnetic or optical memory, having electronically readable control signals stored therein, which can cooperate with a programmable computer system to execute corresponding methods. This is why digital storage media can be computer-readable. Therefore, some embodiments of the present invention include a data carrier comprising electronically readable control signals capable of cooperating with a programmable computer system to execute any of the methods described herein. Typically, embodiments of the present invention can be implemented as a computer program product having program code that, when run on a computer, can effectively execute any method. For example, the program code can also be stored on a machine-readable medium. Other embodiments include a computer program for performing any of the methods described herein, which is stored on a machine-readable medium. In other words, one embodiment of the method of the present invention is a computer program having program code for performing any of the methods described herein, when the computer program is run on a computer. Therefore, another embodiment of the method of the present invention is a data carrier (or digital storage medium or computer-readable recording medium) in which a computer program for performing any of the methods described herein is recorded. Data carriers, digital storage media, or recording media are generally tangible or non-volatile. Therefore, another embodiment of the method of the present invention is a data stream or signal sequence representing a computer program for performing any of the methods described herein. The data stream or signal sequence may be configured to be transmitted, for example, via a data communication link, such as via a network. Further embodiments include a processing unit, such as a computer or programmable logic device, configured or adapted to perform any of the methods described herein. Further embodiments include a computer on which a computer program for performing any of the methods described herein is installed.

[0050] Another embodiment of the invention includes an apparatus or system configured to transmit a computer program for performing at least one of the methods described herein to a receiver. For example, the transmission may be electrical or optical. For example, the receiver may be a computer, a mobile device, a storage device, or a similar device. For example, the apparatus or system may include a file server for transmitting the computer program to the receiver. In some embodiments, a programmable logic device (e.g., a field-programmable gate array, FPGA) may be used to perform some or all of the functions of the methods described herein. In some embodiments, the field-programmable gate array may cooperate with a micro master console to perform any of the methods described herein. Typically, in some embodiments, these methods are performed by any hardware device. The hardware device may be any general-purpose hardware such as a computer master console (CPU) or method-specific hardware such as an ASIC.

[0051] Example

[0052] Example 1: Analysis of Pulverized Coal Injection Operation

[0053] The embodiments of the present invention are based on the data of Bailera et al. regarding pulverized coal injection into blast furnaces, and the analysis and comparison are performed. The operating conditions are shown in Table 2. Table 3 shows that the model display of the embodiments of the present invention is consistent with the blast furnace operating results. In addition, good prediction results can be obtained for molten iron composition (as shown in Figure 5), slag composition (as shown in Figure 6), and blast furnace gas composition (as shown in Figure 7). Table 2, Operating conditions for pulverized coal injection into blast furnaces Comparative example Example Iron ore (kg / hr) 1558 1558 Fe2O3 73.61 73.61 FeO 12.02 12.02 SiO2 4.49 4.49 Al2O3 6.88 6.88 CaO 1.73 1.73 MgO 1.04 1.04 MnO 0.23 0.23 Coke (kg / hr) 289 289 C 88.82 88.82 Fe2O3 0.62 0.62 SiO2 6.96 6.96 Al2O3 3.22 3.22 CaO 0.28 0.28 MgO 0.1 0.1 Pulverized coal (kg / hr) 200 200 C 76.8 76.8 H 4.15 4.15 O 5.1 5.1 N 1.55 1.55 S 0.45 0.45 H2O 1.2 1.2 SiO2 6.15 6.15 Al2O3 4.45 4.45 CaO 0.15 0.15 Hot air (Nm3 / hr) 855.35 855.35 H2O (g / Nm3) 0 0 Oxygen enrichment (%) 5.8 7.9 Table 3. Comparison of Operation Results of Pulverized Coal Injection in Blast Furnace Comparative example Example Molten iron (kg / hr) 1000 1005.95 Fe 94.72 94.34 C 4.5 4.89 Si 0.53 0.52 Mn 0.25 0.24 Slag (kg / hr) 261.8 261.89 SiO2 34.76 34.76 Al2O3 47.9 47.88 CaO 10.12 10.15 MgO 6.3 6.3 CaS 0.73 0.7 Furnace top gas (kg / hr) 1966.9 2000.45 N2 42.53 41.82 CO2 34.8 32.76 CO 21.16 21.24 H2O 1.21 1.22 H2 0.3 0.29

[0054] This invention develops a novel Rist diagram calculation method. By decomposing the Fe-OC and Fe-OH systems using theoretical formulas, the calculation is relatively simple, significantly improving computational efficiency and quickly obtaining information at each point on the operating line. Combined with the Aspen model, the influence of blast furnace conditions and operating variables on the blast furnace smelting process can be analyzed, such as blast furnace top gas, slag, and molten iron composition. Furthermore, by decomposing the Fe-COH system into Fe-OC and Fe-OH systems, the impact of changes in hydrogen-containing fuels on the blast furnace can be observed more directly, thereby enabling accurate prediction and operation of blast furnaces containing hydrogen fuels.

[0055] Although the present invention has been disclosed by way of embodiments, it is not intended to limit the present invention. Any person skilled in the art can make various modifications and alterations without departing from the spirit and scope of the present invention. Therefore, the scope of protection of the present invention shall be determined by the appended claims. [Simplified Explanation of the Diagram]

[0056] Figure 1 is a schematic diagram of a blast furnace system according to an embodiment of the present invention. Figure 2 is a schematic diagram of the structural model of a blast furnace system according to an embodiment of the present invention. Figure 3 is a flowchart of drawing a blast furnace operation diagram according to an embodiment of the present invention. Figure 4 is a schematic diagram of a blast furnace operation diagram according to an embodiment of the present invention. Figure 5 is a schematic diagram of the verification results of molten iron composition under pulverized coal injection operation in the embodiments and comparative examples of the present invention. Figure 6 is a schematic diagram of the verification results of slag composition under pulverized coal injection operation in the embodiments and comparative examples of the present invention. Figure 7 is a schematic diagram of the verification results of top gas composition under pulverized coal injection operation in the embodiments and comparative examples of the present invention.

Claims

1. A method for predicting the operation of a blast furnace containing hydrogen fuel, the method comprising the following steps: a step of forming a Reiss diagram operating line of an iron-carbon-oxygen-hydrogen system, wherein the Reiss diagram operating line of the iron-carbon-oxygen-hydrogen system of the blast furnace is plotted using data from a blast furnace, wherein the data includes at least one of upper blast furnace zone data, a thermal reserve zone data, lower blast furnace zone data, a blast radius zone data, and a separation zone data; a step of forming a Reiss diagram operating line of an iron-oxygen-hydrogen system, wherein the Reiss diagram operating line of the iron-oxygen-hydrogen system of the blast furnace is plotted by calculating the chemical balance between the gas and solid components of the iron-oxygen-hydrogen system in a thermal reserve zone of the blast furnace; The steps for forming the Ries diagram operating line of an iron-oxygen-carbon system include: calculating the reducing gas utilization rate of the iron-oxygen-carbon system of the blast furnace using the reducing gas utilization rate of the iron-oxygen-hydrogen system and the total reducing gas utilization rate of the iron-carbon-oxygen-hydrogen system; and plotting the Ries diagram operating line of the iron-oxygen-carbon system using the reducing gas utilization rate of the iron-oxygen-carbon system and the chemical balance between the gas and solids of the iron-oxygen-carbon system in the thermal reserve zone. Based on the Ries diagram operating lines of the iron-carbon-oxygen-hydrogen system, the iron-oxygen-hydrogen system, and the iron-oxygen-carbon system, at least one of the following is predicted: blast furnace iron composition, iron production, blast furnace top gas composition, slag composition, blast furnace belly gas composition, blast furnace belly gas flow rate, overall blast furnace carbon emissions, and blast furnace production cost.

2. The method as claimed in claim 1, wherein the Ries diagram operating line of the iron-carbon-oxygen-hydrogen system is obtained through the chemical equilibrium between the gas and solid of the iron-carbon-oxygen-hydrogen system in the thermal reserve and the ratio of the reducing gas mole number to the iron mole number in the molten iron.

3. The method as described in claim 2, wherein the ratio of the reducing gas mole number to the iron mole number in the molten iron can be obtained by the following formula: where represents the mole number of carbon components fed into the iron ore; represents the mole number of carbon components fed into the coke; represents the mole number of water components supplied by the blast furnace from the air passage zone; represents the mole number of carbon components supplied by the pulverized coal from the air passage zone; represents the mole number of hydrogen components supplied by the pulverized coal from the air passage zone; represents the mole number of water components supplied by the pulverized coal from the air passage zone; represents the mole number of iron components in the molten iron; and represents the mass fraction of carbon components in the molten iron.

4. The method as described in claim 2, wherein the chemical equilibrium between the gas and solid in the iron-carbon-oxygen-hydrogen system comprises a theoretical equilibrium point or an actual equilibrium point of the iron-carbon-oxygen-hydrogen system, the x-coordinate of the theoretical equilibrium point of the iron-carbon-oxygen-hydrogen system is calculated by XW = 1 + (1 - xh)ωWC + xhωWH, and the y-coordinate YW of the theoretical equilibrium point of the iron-carbon-oxygen-hydrogen system is 1.05, where xh is the mole fraction of H2 and H2O in the reducing gas; ωWC is the mole fraction of the equilibrium state of the iron-oxygen-carbon system; and ωWH is the mole fraction of the equilibrium state of the iron-oxygen-hydrogen system.

5. The method as described in claim 4, wherein the x-coordinate of the actual equilibrium point of the iron-carbon-oxygen-hydrogen system is expressed by XR = 1 + r(XW - 1) and the y-coordinate of the actual equilibrium point of the iron-carbon-oxygen-hydrogen system is expressed by YR = YA + r(YA - YW), where r represents the ratio of the oxygen actually exchanged in the blast furnace to the oxygen theoretically exchanged; YA represents the initial oxidation state of the iron oxide; XW represents the x-coordinate of the theoretical equilibrium point of the iron-oxygen-hydrogen system; and YW represents the y-coordinate of the theoretical equilibrium point of the iron-oxygen-carbon system.

6. The method as described in claim 4, wherein the chemical equilibrium between the gas and solid in the iron-oxygen-hydrogen system comprises a theoretical equilibrium point of the iron-oxygen-hydrogen system, the x-coordinate of which is calculated by XW = 1 + xhωWH, and the y-coordinate YW of which is 1.05, where xh is the mole fraction of H2 and H2O in the reducing gas; and ωWH is the mole fraction of the equilibrium state of the iron-oxygen-hydrogen system.

7. The method as described in claim 4, wherein the operating line of the Ries diagram of the iron-oxygen-hydrogen system is drawn as a straight line connecting the theoretical equilibrium point of the iron-carbon-oxygen-hydrogen system or the actual equilibrium point of the iron-carbon-oxygen-hydrogen system with the coordinate point (1,0) on the Ries diagram.

8. The method as described in claim 1, wherein the chemical equilibrium between the gas and solid in the iron-oxygen-carbon system comprises a theoretical equilibrium point or an actual equilibrium point of the iron-oxygen-carbon system, the x-coordinate of which is calculated by XW = 1 + (1 - xh)ωWC, and the y-coordinate of which is 1.05, wherein xh is the mole fraction of H2 and H2O in the reducing gas; and ωWC is the mole fraction of the equilibrium state of the iron-oxygen-carbon system.

9. The method of claim 1, wherein the total reducing gas utilization rate of the iron-carbon-oxygen-hydrogen system; the reducing gas utilization rate of the iron-oxygen-hydrogen system; and the reducing gas utilization rate of the iron-oxygen-carbon system, wherein...

10. A blast furnace prediction system for hydrogen fuel, comprising: an actuator equipped with a means for performing the method as described in any one of claims 1 to 9.

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