Smelting method for accurately controlling blast furnace burden rate by quantizing and patterning

Abstract

The present application relates to a kind of quantitative mode accurate control blast furnace burden rate smelting method, belong to blast furnace smelting technical field.The method includes benchmark burdening;Burdening calculation, parameter, index check analysis;Input rich oxygen adjustment amount accurate control actual burden rate;Into furnace smelting and parameter control etc.Step.The present application is based on blast furnace basic theory, blast furnace material balance and heat balance principle, solve blast furnace routine smelting when table air volume-correction air volume-correction air volume-burden rate-theoretical index, and each smelting parameter coordination balance, smelting period and index prediction control etc.Interrelated data influence each other processing.Not only improve the degree of furnace condition smooth, also significantly reduce fuel ratio and smelting cost.Simultaneously, the method is applicable to different blast furnace, any furnace burden structure's intensification smelting process, with very strong adaptability.In a natural class blast furnace operation, after 0~3 times oxygen adjustment can reach the specified burden rate range.It has the characteristics of simple method, control fast and accurate.

Description

Technical Field

[0001] This invention belongs to the field of blast furnace smelting technology, specifically relating to a smelting method for quantitatively and systematically controlling the blast furnace charge rate. Background Technology

[0002] Achieving uniform charge rate to enhance blast furnace stability, obtaining low and stable molten iron (w([Si])) values, and maintaining stable operation of the blast furnace while continuously improving technical and economic indicators under specific conditions is a complex system engineering project. In terms of blast furnace operation techniques, this involves finding effective ways to systematically and accurately control the charge rate under different raw material conditions for blast furnaces of varying volumes, combined with the control range of molten iron (w([Si])) during the smelting process. This allows for timely and accurate reflection of the refined and precise effects of the main daily adjustment methods (oxygen enrichment, pulverized coal injection) on blast furnace operation. Furthermore, it requires quantitative and modular control of the charge rate and w([Si]) requirements under specific blast furnace smelting parameters. This ensures not only good matching of various smelting parameters but also accurate achievement of target values ​​within the effective timeframe of the adjustment factors, thereby continuously improving the stability of the blast furnace operation and temperature, and obtaining smelting results that are adapted to the conditions and have good indicators.

[0003] Essentially, the blast furnace smelting process is a process in which the relative motion of the descending furnace charge and the ascending gas flow fully carries out heat and mass transfer. In the daily intensified smelting process of the blast furnace, achieving a balanced and stable descent of the furnace charge is of great significance for the stability of the blast furnace condition, quality improvement and energy saving, and safety and long service life. The ironmaking production process is an extremely complex system engineering project. With the advancement of modern ironmaking technology and the improvement of intensification level, the requirement for the balance of the blast furnace smelting process has become even more important.

[0004] In daily blast furnace production, the quality and composition of raw materials, blast furnace type, and blast furnace condition are not static. With changes in external conditions and intensified smelting, inevitable variations occur. Furthermore, these variations are not single-factor or linear, but rather complex changes involving multiple angles and levels, with mutual influence and correlation. Therefore, precisely controlling the charge rate and the w([Si]) value (slag-iron composition) of molten iron using oxygen enrichment and pulverized coal injection methods is a complex practical operation and a constant pursuit for blast furnace operators. To a large extent, the control of charge rate and furnace temperature during blast furnace production is still based on localized, simplified calculations and experience. The shortcomings of localized calculations lie in the unsystematic and incomplete data collection, treating some calculation parameters as fixed values ​​or only taking data at the top of the hour. This fails to effectively reflect the dynamics of the specific blast furnace smelting process and the correlation of multiple factors, resulting in an inability to dynamically and in real-time consider the influence of multiple factors, and inconsistencies in the calculation process due to differences among operators on three shifts. In blast furnace production, precise control of material rate and blast furnace temperature (molten iron w([Si])) requires more timely, comprehensive, systematic, efficient and accurate calculations, and convenient data acquisition and operation. It is also necessary to quantify, standardize, real-time and comprehensively process the related calculations of this complex control process.

[0005] Currently, blast furnace equipment technology and raw material quality processing technology have made significant progress, with marked improvements in equipment reliability, instrument sensitivity, and raw material quality stability. Furthermore, the development of computer and information technology has created conditions for achieving comprehensive, systematic, and accurate dynamic joint calculations in complex blast furnace smelting processes. Therefore, overcoming the shortcomings of existing technologies is a pressing issue that needs to be addressed in the field of blast furnace smelting technology. Summary of the Invention

[0006] The purpose of this invention is to address the shortcomings of existing technologies by providing a quantitative and modular method for precisely controlling blast furnace charge rate. Based on blast furnace fundamental theory and the principles of overall material and heat balance, and following the principle of "quantitative, modular, and precise control of charge rate through oxygen adjustment," this invention forms a quantitative and modular processing mode that addresses the interrelationships between various data points in the daily intensified blast furnace smelting process, including control of coke batch quantity, hourly coal quantity, hourly oxygen enrichment, charge rate, molten iron w([Si]) value, slag-iron composition, smelting cycle and output, fuel ratio index prediction and control, verification, and coordination and balance of various direct (indirect) smelting parameters. To accurately ensure that the charge rate reaches the planned value during blast furnace smelting, significantly improve blast furnace operation, reduce fuel ratio and smelting costs, this invention provides a simple, comprehensive, widely applicable, fast, and accurate quantitative and modular method for precisely controlling blast furnace charge rate, effectively improving blast furnace operation technology and furnace stability.

[0007] To achieve the above objectives, the technical solution adopted by the present invention is as follows:

[0008] A smelting method for quantitatively and systematically controlling the blast furnace charge rate includes the following steps:

[0009] A. Standard ingredients: The smelting process is ordinary ore smelting or medium titanium slag smelting.

[0010] When smelting ordinary ore, the ordinary ore furnace charge used includes the following components by mass percentage: 65-72% sintered ore, 20-28% high-silica pellets, and 0-10% low-silica lump ore; total 100%; ore batch 53,000-55,000 kg;

[0011] When smelting medium-titanium slag, the vanadium-titanium ore furnace charge used includes the following components by mass percentage: sintered ore 60-65%, vanadium-titanium pellets 30-35%, low-silicon lump ore 0-5%, totaling 100%; ore batch 320,000-34,000 kg / batch.

[0012] In the smelting of ordinary ore or medium titanium slag, the coke batch is 7200-11000 kg / batch based on dry coke weight; the coke slag batch is 450-700 kg / batch based on dry coke weight; and the pulverized coal injection rate is 21.5-48.5 t / h.

[0013] B. Ingredient calculation, parameter and index verification analysis:

[0014] B1. Benchmark ingredient calculation, parameter and index verification analysis:

[0015] The wind pressure, air volume, wind temperature, and w([Si]) of the entire air supply remain unchanged, among which the wind temperature is the highest stable wind temperature; if the fluctuation range of factors in ordinary ore smelting or medium titanium slag smelting all meet the following conditions: clinker rate < ±1.0%, comprehensive furnace grade < ±0.20%, coke ash content < ±0.1%, and pulverized coal ash content < ±0.10%; then:

[0016] (1) Calculate the theoretical fuel ratio, utilization coefficient and smelting cycle;

[0017] (2) Calculate the theoretical composition of pig iron, theoretical composition of slag, basicity, and magnesium-aluminum ratio;

[0018] (3) Calculate the conversion factor between the corrected air volume and the surface air volume. The oxygen enrichment rate after correcting the air volume is 2.90 to 5.00%.

[0019] B2. Verification and analysis of ingredient calculations, parameters, and indicators when key verification conditions change:

[0020] The wind pressure, air volume, wind temperature, and w([Si]) of the entire air supply remain unchanged, among which the wind temperature is the highest stable wind temperature; if any one of the factors in the ordinary ore smelting or medium titanium slag smelting does not meet the following conditions: clinker rate < ±1.0%, overall furnace grade < ±0.20%, coke ash content < ±0.1%, pulverized coal ash content < ±0.10%; then:

[0021] (1) Calculate the hourly coal quantity, theoretical iron content of the batch, theoretical coal ratio, coke ratio, coke-butane ratio, coke batch, theoretical fuel ratio, utilization coefficient, smelting cycle and pulverized coal injection rate after the factors change;

[0022] (2) Calculate the theoretical composition of pig iron, theoretical composition of slag, basicity, and magnesium-aluminum ratio;

[0023] C. Input the oxygen enrichment adjustment amount to precisely control the actual material flow rate:

[0024] During blast furnace smelting, the difference between the actual material rate and the specified benchmark material rate is checked. The principle for checking whether to adjust the material rate is as follows:

[0025] (1) The absolute value of the difference between the actual material rate and the specified benchmark material rate for two consecutive hours is ≥0.5 batches / h;

[0026] (2) The difference between the actual material rate and the specified benchmark material rate in a single hour is ≥1.0 batches / h;

[0027] (3) The absolute value of the difference between the specified material rate and the actual material rate for two consecutive hours is ≥1.0 batch; (that is, the difference between the sum of the material rates for two consecutive hours exceeding (or failing to reach) the sum of the specified material rate for two hours is ≥1.0 batch);

[0028] If any one of the above three conditions is met, adjustment is required; otherwise, no adjustment is required.

[0029] The adjustment method is as follows:

[0030] (1) Collect comprehensive air supply parameters, indirect smelting parameters and fuel parameters;

[0031] (2) Based on the original oxygen enrichment, input the oxygen enrichment adjustment amount to adjust the oxygen and obtain the new oxygen enrichment; then, through the collected comprehensive air supply parameters, indirect smelting parameters and fuel parameters, calculate the oxygen enrichment rate and theoretical material rate after adjusting the oxygen correction air volume, and then judge the oxygen adjustment effect.

[0032] The judgment criteria are:

[0033] 1) The difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is defined as 0.1 to 0.3 batches.

[0034] 2) |Theoretical feed rate after oxygen adjustment - Specified feed rate| < 0.3 batches / h, and predict the batch growth rate for the shift (defined between 0.3 and 1.0 batches; the batch growth rate for the shift refers to the difference between the hourly theoretical feed rate and the actual feed rate multiplied by 8 hours);

[0035] 3) The input oxygen enrichment adjustment amount makes the theoretical material rate reach the material rate control value requirement, and the absolute value of the deviation rate between the theoretical output obtained after oxygen adjustment and the planned output requirement is <±1.50%.

[0036] If conditions 1) to 3) are met simultaneously, and the difference between the actual material rate after oxygen adjustment and the specified benchmark material rate is checked, and the result is that no adjustment is needed, then the material rate effect needs to be checked; at the same time, the theoretical combustion temperature, blast energy, permeability index and smelting cycle after oxygen adjustment are calculated.

[0037] The specific method for verifying the material flow rate effect is as follows:

[0038] The verification standard for Japanese batches is defined as follows: the absolute value error rate of the difference between any two of the three factors—actual daily material rate, specified daily material rate, and theoretical daily material rate—is <1.50%; if all three are met, the process continues.

[0039] The theoretical daily coal ratio and coke ratio are compared with the actual daily coal ratio and coke ratio. The theoretical output calculated based on the theoretical feed rate is compared with the actual daily output. If the deviation rate of the difference between the theoretical daily output and the actual daily output is <1.50%, the verification is passed and the process continues.

[0040] D. Furnace smelting and parameter control:

[0041] During the smelting process, the number of times the oxygen enrichment is adjusted in each shift should be ≤3 times, and the ratio of |Daily theoretical batch - Daily specified batch| / Daily specified batch should be <1.50%.

[0042] Smelting conditions: hot blast pressure 0.30~0.39MPa, top pressure 0.155~0.195MPa, hot blast temperature 1150℃~1250℃, and corrected furnace feed air volume 3200~5700m³. 3 / min, oxygen enrichment of 9400~15000m 3 / h, pulverized coal injection rate is 135-165 kg / t iron, pulverized coal injection rate is 22.0-35.0%; ore batch is 33.0-55.0 tons, coke batch is 7.2-11.0 tons on a dry basis; coke batch is 0.45-0.70 tons on a dry basis; w([Si]) is 0.055-0.35%, slag basicity is 1.10-1.18, and molten iron temperature is 1420-1480℃; during the smelting process, the slag ratio is 380-480 kg / t, the magnesium-aluminum ratio in the slag is 0.65-0.95, the slag basicity is 1.10-1.18, the blast temperature is controlled to be stable, the oxygen enrichment rate is 2.90%-5.0%, and the permeability index is 18000-22000 m 3 / (min.MPa), theoretical combustion temperature 2300~2400℃, actual blowing speed 255~275m / s, actual blowing kinetic energy 17000~22000kg.m / S, theoretical hourly material rate 8.5~10.0 batches.

[0043] Further, preferably, the sintered ore composition, by mass percentage, includes 52.0–54.0% TFe, 5.5–6.5% SiO2, 13.0–13.5% CaO, 1.75–2.19% Al2O3, 2.30–2.90% MgO, 0.40–1.35% TiO2, 0.045%–0.055% S, 0.165–0.150% V2O5, and 0.045%–0.055% MnO, with the balance being unavoidable impurities, and a bulk density of 1.90–2.10 t / m³. 3 ;

[0044] The vanadium-titanium pellets, by mass percentage, comprise 53.5–57.5% TFe, 4.5–5.5% SiO2, 0.55–1.35% CaO, 2.20–2.90% Al2O3, 2.35–2.90% MgO, 6.40–11.0% TiO2, 0.55–0.75% V2O5, and 0.23%–0.25% MnO, with the balance being unavoidable impurities; 2.20–2.30 t / m 3 ;

[0045] The high-silica pellets contain, by mass percentage: 58.5–60.0% TFe, 6.5–7.5% SiO2, 0.5–1.5% CaO, 1.80–2.10% Al2O3, 1.0–1.5% MgO, 2.50–3.50% TiO2, 0.165–0.150% V2O5, and 0.045%–0.055% MnO, with the balance being unavoidable impurities. The bulk density is 2.15–2.35 t / m³. 3 ;

[0046] The low-silica lump ore composition, by mass percentage, includes 64.0–66.0% TFe, 3.0–4.5% SiO2, 0.03–0.05% CaO, 1.00–1.50% Al2O3, 0.01–1.0% MgO, TiO2 <1.0%, 0.030–0.050% V2O5, and 0.110%–0.160% MnO, with the balance being unavoidable impurities. The bulk density is 2.2–2.4 t / m³. 3 .

[0047] Furthermore, preferably, the coke composition comprises 84.0–86.5% C and 13.5–14.5% ash by mass percentage, with a bulk density of 0.55–0.65 t / m³. 3 ;

[0048] The coke ash composition by mass percentage includes 53.0–56.0% SiO2, 2.20–3.0% CaO, 24.0–26.0% Al2O3, 0.15–1.0% MgO, TiO2 <2.0%, 0.35%–0.45% MnO, with the balance being unavoidable impurities.

[0049] The pulverized coal composition includes, by mass percentage, 76.0-78.0% C, 13.5-15.0% ash, and 12.5-13.5% volatile matter, with a particle size of -200 mesh accounting for 66-70%.

[0050] The ash composition of the pulverized coal, by mass percentage, includes 55.0–57.0% SiO2, 5.20–6.50% CaO, 23.0–25.0% Al2O3, 2.20–2.50% MgO, TiO2 <2.0%, and 0.35%–0.45% MnO, with the balance being unavoidable impurities.

[0051] Furthermore, preferably, the comprehensive air supply parameters include: surface air volume, humidity, air pressure, top pressure, air temperature, and tuyer area; indirect smelting parameters include corrected air volume and the oxygen enrichment rate, theoretical combustion temperature, permeability index, and blast kinetic energy after correcting the air volume; fuel parameters include the batch weight, composition, and combustion rate of coke and coke briquettes before the tuyer, as well as the hourly coal powder quantity, coal powder composition, and combustion rate before the tuyer.

[0052] Furthermore, preferably, it also includes step E, actual smelting result return correction: based on the actual smelting results obtained in step E, and based on the hourly theoretical and actual material rate, theoretical calculation control and actual w([Si]) value, theoretical slag and iron composition and actual slag and iron composition, theoretical and actual furnace output, and theoretical and actual fuel ratio, the calculation parameters are corrected according to the calculation methods in steps B to D, and smelting continues.

[0053] This invention, based on the principle of "oxygen adjustment and material control," comprehensively verifies the material (full analysis of raw materials and fuels entering the furnace) and predicts and verifies the slag and iron composition according to the baseline w([Si]) amount. It then verifies the factors influencing the material rate (corrected air volume, corrected oxygen enrichment rate, coal ratio, coke batch, etc.) and their theoretical quantitative calculations to precisely control the material rate, verify the material rate control to meet standards, and calculate the theoretical iron content and theoretical indicators. Following the definition of the material rate range after oxygen adjustment (direct input of the adjustment amount), the invention controls the material rate (specified material rate, actual material rate, and theoretically pre-controlled material rate). It combines the calculation and adjustment of the basic w([Si]) amount, actual w([Si]) amount, real-time hourly coal quantity, and the mutual influence of various factors on the material rate. Before and after adjustment (real-time oxygen enrichment rate, real-time hourly pulverized coal quantity), it precisely controls the material rate, pre-controls the slag and iron composition, balances the furnace smelting parameters, re-verifies the indicator components, and returns the actual smelting results for correction.

[0054] In this invention, the raw materials used can include 1-2 types of high-silica acid pellets, 2 types of vanadium-titanium pellets, and 2 types of dry coke. When the overall grade of the feed material, clinker rate, coke ash content, and pulverized coal ash content change, the proportions, coke batches, hourly pulverized coal injection rate, and indirect smelting parameters are checked based on the assumption that w([Si]) remains constant and the slag basicity is within a certain range. The check includes a check of the theoretical temperature; the air volume is at full capacity, the air temperature is at its highest stable temperature without adjustment, and the oxygen enrichment rate after air volume correction is 2.90-5.00%.

[0055] When changes in the overall grade of the furnace feed, clinker rate, coke ash content, and pulverized coal ash content exceed the fluctuation range (see below), the proportions, coke batches, hourly pulverized coal injection rate, and theoretical indicators must be checked based on the baseline w([Si]) remaining unchanged and the slag basicity being within the range.

[0056] This invention, under the condition of the main reference parameters of the benchmark raw materials (clinker rate, overall feed grade, coke and pulverized coal ash content), combined with the benchmark operating parameters (benchmark coal quantity, benchmark feed rate, benchmark w([Si]))), performs the following: If the benchmark operating parameters such as total air pressure, air volume, air temperature, and w([Si]) are not adjusted, and the main raw material parameters are stable (the fluctuation ranges all meet the following conditions: clinker rate < ±1.0%, overall feed grade < ±0.20%, coke < ±0.1%, and pulverized coal ash content < ±0.10%), then it directly proceeds to the benchmark index determination step.

[0057] Based on the reduction rates of elements such as [Si], [Ti], [Mn], and [V] in molten iron under a predetermined w([Si]) value (obtained by fitting the (w([Si])-Si reduction rate, w([Si])-Ti reduction rate, w([Si])-Mn reduction rate, and w([Si])-V reduction rate) under similar raw material and fuel conditions (ore and coke varieties), the following formulas are used: w([Si])-desulfurization rate fitting relationship, and [S] removal rate fitting polynomial relationship with predetermined w([Si]) → amount of corresponding element oxides and S, P, and As entering the molten iron → amount of element oxides and S, P, and As entering the slag → output slag quantity (slag ratio), alkali metals, lead, zinc, titanium, sulfur load, etc. → theoretical slag composition (including basicity, magnesium-aluminum ratio, etc.). →Theoretical pig iron composition (derived from theoretical calculations of the corresponding element oxides entering the molten iron). The calculation formulas involving the aforementioned concepts are standard formulas (Zhou Chuandian, Blast Furnace Ironmaking Process Production Technology Handbook [M], Beijing: Beijing Metallurgical Industry Press, 2008); the calculation formulas involving slag ratio, corrected blast volume, and the calculation formulas for w([Si]), w([S]), w([P]), w(Ti]), w([As]), w([V]), and w(Mn) in molten iron, and the calculation formulas for w(SiO2), w(CaO), w(MgO), w(Al2O3), w(TiO2), w(V2O5), and w(MnO) in slag are publicly available information. The calculation also involves the fitting relationship between surface blast volume and corrected blast volume (or the correction multiple of surface blast volume and corrected blast volume).

[0058] When the main reference parameters of the benchmark raw materials (clinker rate, overall grade of feed into the furnace, coke ash content, and pulverized coal ash content) change beyond the stable range, the benchmark operating parameters are adjusted according to the magnitude of the change through step B2 (including the determination of the benchmark hourly coal quantity and coke batch after the change of raw materials).

[0059] The main verification conditions for batch calculation, parameter and index verification analysis are as follows: After the factor changes, the calculation order is: determination of hourly coal quantity → theoretical iron content of batch → calculation of theoretical coal ratio → determination of coke ratio and coke-to-coke ratio → determination of new coke batch → calculation of theoretical fuel ratio, utilization coefficient, smelting cycle and pulverized coal injection rate of batch under the change of basic conditions.

[0060] The concepts and calculation formulas involved are as follows:

[0061] Hourly coal quantity after factor changes: l2 = l1 - (m h1 -m h2 )*0.015*l1

[0062] l2 represents the hourly coal quantity after the factor change, in kg / t; l1 represents the hourly coal quantity before the factor change, in kg / t; m h1 The ash content of pulverized coal before changes in factors is expressed in kg / t; mh2 The ash content of pulverized coal after changes in factors is expressed in kg / t.

[0063] Coumarin ratio after factor changes

[0064] d2=(ΣTFe1-ΣTFe2)*0.02*d1-(S1-S2) / 5*1*d1 / 100-(w([Si])1-w([Si])2)*0.01*d1-(J h1 -J h2 )*0.015*d1+d1

[0065] d2 is the theoretical coke-to-butadiene ratio after factor changes, kg / t; d1 is the coke-to-butadiene ratio before factor changes, kg / t; ΣTFe1 is the overall feed grade before factor changes, kg / t; ΣTFe2 is the overall feed grade after factor changes, %; S1 is the clinker yield before factor changes, %; S2 is the clinker yield after factor changes, %; J h1 The coke ash content before changes in factors, %; J h2 The percentage of coke ash after changes in factors.

[0066] Focal ratio after factor changes

[0067] k2=(ΣTFe1-ΣTFe2)*0.02*k1-(S1-S2) / 5*1*d1 / 100-(w([Si])1-w([Si])2)*0.01*d1-(J1-J2)*0.015*k1+k1

[0068] k2 is the theoretical coke ratio after the factor change, kg / t; k1 is the coke ratio before the factor change, kg / t; ΣTFe1 is the overall grade of the furnace feed before the factor change, kg / t; ΣTFe2 is the overall grade of the furnace feed after the factor change, %; S1 is the clinker yield before the factor change, %; S2 is the clinker yield after the factor change, %; J1 is the coke ash content before the factor change, %; J2 is the coke ash content after the factor change, %.

[0069] After the factors change, the burnt batch C2 = (k2 + d2) * t 理 / 1000-J d

[0070] C2 represents the newly determined coke batch size after the change in factors, in kg / t; J d The weight of dry coke (unchanged) is kg / t.

[0071] The formulas for calculating the theoretical fuel ratio, utilization coefficient, smelting cycle, and pulverized coal injection rate are conventional formulas.

[0072] All calculations are based on a dry basis. The baseline w([Si]) remains unchanged, and the coking batch and hourly coal quantity (with coking coal content unchanged) are automatically adjusted according to the above formula based on the raw material and fuel variables.

[0073] Then, calculate the slag ratio, various loads, theoretical pig iron composition, theoretical slag composition and basicity, magnesium-aluminum ratio, etc., in the same way as step (2) of step B1.

[0074] During blast furnace smelting, the difference between the actual material rate and the specified benchmark material rate is checked. The criteria for determining whether to adjust the material rate are: if the absolute value of the difference between the specified and actual material rates is ≥0.5 batches / h for two consecutive hours, or ≥1.0 batches / h for a single hour, or if the sum of the material rates for two consecutive hours exceeds (or does not reach) the sum of the specified batches for two hours and the difference is ≥1.0 batches (referring to the absolute value of the difference between the specified and actual material rates for two consecutive hours), then adjustment is required; otherwise, no adjustment is required. If the check result indicates that no adjustment of the oxygen enrichment is needed, proceed to step C1; if the check result indicates that the oxygen enrichment needs to be adjusted to control the material rate (increase or decrease), proceed to step C2.

[0075] C1. The difference between the specified material speed and the actual material speed is within the specified range.

[0076] Under constant air temperature and full air volume conditions, if the absolute value of the difference between the specified and actual material speed is less than 0.5 batches / h for two consecutive hours or less than 1.0 batches / h for a single hour, or if the absolute value of the difference between the specified and actual material speed is less than 1.0 batches for two consecutive hours, the cycle will proceed directly to the next cycle.

[0077] C2. Determining the amount of oxygen enrichment and accurately controlling the actual material flow rate.

[0078] Under constant air temperature and full air volume conditions, if the absolute value of the difference between the specified and actual material rate is ≥0.5 batches / h for two consecutive hours or ≥1.0 batches / h for a single hour, or if the absolute value of the difference between the total material rate and the actual material rate for two consecutive hours is ≥1.0 batches, "oxygen adjustment and material rate control" is required. The required parameters, methods, and steps are as follows:

[0079] (1) Parameters to be collected (including calculated indirect smelting parameters and fuel parameters). Directly collected comprehensive air supply parameters include: surface air volume, humidity, air pressure, top pressure, air temperature, and tuyer area; indirect smelting parameters (automatically calculated) include the corrected air volume obtained based on the table-actual air volume correction coefficient (or fitting polynomial), as well as the oxygen enrichment rate, theoretical combustion temperature, permeability index, and blast kinetic energy after the corrected air volume. Fuel parameters to be collected include: batch weight, composition, and combustion rate before the tuyer; hourly coal powder quantity, coal powder composition, and combustion rate before the tuyer.

[0080] (2) Determination of oxygen enrichment adjustment amount and precise control of actual material speed. The steps (calculation order) for determining the oxygen enrichment adjustment amount are as follows: original oxygen enrichment amount → oxygen enrichment adjustment amount (input) → new oxygen enrichment amount → oxygen enrichment rate after oxygen adjustment and correction of air volume (combined with the comprehensive blast parameters and fuel parameters in step (1)) → (obtained by combining the air volume per ton of coal consumption, air volume per hour of coal consumption, air volume per ton of coke consumption, and residual air volume after coal burning obtained from the parameters in step (1)) theoretical material speed after oxygen adjustment → judgment of oxygen adjustment effect. Compare the material speed control effect after oxygen adjustment (1 hour) (Zhou Chuandian, Blast Furnace Ironmaking Process Production Technology Manual [M], Beijing: Beijing Metallurgical Industry Press, 2008): if the material speed control effect is achieved, then proceed to step C3 and enter the next cycle. If the effect is not achieved, conduct cause analysis and error analysis. If the cause is resolved, enter the next cycle; if the cause cannot be resolved, the process stops.

[0081] The concepts and formulas involved are:

[0082] Corrected air volume V 校 =((J) 实 *1000*J C实 / 100*φ C / 100+J d实 *1000*J dC实 / 100*φ JDC )+(M 实 *1000*M C实

[0083] / 100*φ MC ))*0.9333 / (0.21+0.29*f h2O / 8 / 100+0.79*f O2 / 100) / 24 / 60

[0084] V 校 The air volume after correcting the surface air volume value, in m 3 / min; J 实 The daily dry basis consumption of coke used in the current period, in tons (t); J C实 The carbon content (%) of the coke used in the current period; Φ C The combustion rate of coke before the tuyeres, %; J d实 The daily dry basis consumption of coking coal used in the current period, in tons (t); J dC实 The carbon content of the coking coal used in the current period, in %; Φ JDC The combustion rate of coke before the air vent, %; M 实 The daily dry basis consumption of pulverized coal used in the current period, in tons (t); M C实 The carbon content (%) of the pulverized coal used in the current period; Φ MC The combustion rate of pulverized coal before the tuyeres, expressed as %; f h2O Atmospheric humidity, g / m 3 ;fO2 Oxygen enrichment rate, expressed as a percentage, is calculated based on surface air volume. Note: Coke quantity (daily consumption) is based on actual values ​​from a past period under similar raw material conditions.

[0085] Oxygen enrichment rate F after adjusting air volume O2 =0.785*V O2 / 60 / (V 校 +V O2 / 60)*100

[0086] F O2 The oxygen enrichment rate (%) was calculated after correcting the surface air volume value; V O2 The current oxygen enrichment level, m 3 / h. The rest is the same as above. Air consumption per ton of coal V after correction. m =1000*M C实

[0087] / 100 / 24*22.4 / (0.21+0.29*f h2O / 100+0.79*F O2 / 100)*Φ MC

[0088] V m To correct the air volume, the air consumption per ton of coal is calculated in m. 3 / t; the rest are the same as above;

[0089] Hourly coal consumption and air volume V after adjusting for oxygen enrichment rate mh =V m *m h / 1000

[0090] V mh To correct for the hourly coal consumption air volume after adjusting for oxygen enrichment rate, m 3 / h;m h The amount is the hourly coal quantity, kg / t; the rest is the same as above.

[0091] Air consumption per ton of coke after correction V C =1000*J C实

[0092] / 100 / 24*22.4 / (0.21+0.29*f h2O / 100+0.79*F O2 / 100)*φ C

[0093] V C To correct the air volume, the air consumption per ton of coke is calculated in m. 3 / t; the rest is the same as above.

[0094] Theoretical feed rate L before oxygen adjustment 前 =(V校 *60-V mh前 )*f 风 / V C前 / (J 批 +J d批 )*1000

[0095] L 前 The theoretical feed rate, calculated based on the oxygen enrichment level before adjustment, is given in batches per hour (V). mh前 To correct for the hourly coal consumption air volume after adjusting the oxygen enrichment rate (which is calculated using the oxygen enrichment amount before adjustment), m 3 / h;f 风 For the specific blast furnace air utilization rate, %; V C前 To correct the air volume, the air consumption per ton of coke is calculated using the oxygen enrichment rate after adjusting the oxygen enrichment rate, m 3 / t;J 批 The dry weight of each batch of coke is kg / batch; J d批 The dry weight of each batch of charcoal is expressed in kg / batch, %.

[0096] Theoretical feed rate L after oxygen adjustment 后 =(V 校 *60-V mh前后 )*f 风 / V C后 / (J 批 +J d批 )*1000

[0097] L 后 The theoretical feed rate, calculated based on the adjusted oxygen enrichment, is given in batches per hour (V). mh前 To correct for the oxygen enrichment rate (which is calculated using the adjusted oxygen enrichment amount) in terms of hourly coal consumption and air volume, m 3 / h;f 风 For the specific blast furnace air utilization rate, %; V C前 To correct the air volume, the air consumption per ton of coke is calculated using the adjusted oxygen enrichment rate. 3 / t;J 批 The dry weight of each batch of coke is kg / batch; J d批 The dry weight of each batch of charcoal is expressed in kg / batch, %.

[0098] Note: The formula for calculating the theoretical feed rate is the same before and after oxygen adjustment; the only difference is the input oxygen enrichment rate.

[0099] Similarly, the theoretical combustion temperature, blast kinetic energy, permeability index, and smelting cycle are obtained after correcting the air volume and oxygen enrichment rate (using the corrected air volume into the conventional calculation formula).

[0100] Repeatedly input the oxygen enrichment adjustment amount until the theoretical material rate output value meets the requirements. Oxygen enrichment reaction time (1 hour) (Zhou Chuandian, Blast Furnace Ironmaking Process Production Technology Manual [M], Beijing: Beijing Metallurgical Industry Press, 2008), after which the pre-control target is reached, the next cycle begins.

[0101] C3. Verification of the effect of precise oxygen regulation and material rate control

[0102] The verification standard for Japanese feed batches is defined as follows: the absolute error rate of the difference between any two of the three factors—actual daily feed rate, specified daily feed rate, and theoretical daily feed rate—is <1.50%. Parameters such as theoretical combustion temperature and kinetic energy can be used for verification. If the standard is met, continue the process; if not, find the cause and adjust the parameters.

[0103] During the blast furnace smelting process, the difference between the actual material rate and the specified benchmark material rate is within a certain range (±1.0 batches / h, and the absolute value of the difference between the daily theoretical material batch and the actual material batch is <1.50%). The actual w([Si]) achieved after the adjustment reaction is checked and analyzed in conjunction with the control method that the smelting should achieve the specified w([Si]).

[0104] Furthermore, the theoretical coal ratio and coke ratio for each day are compared and verified with the actual daily coal ratio and coke ratio, based on the theoretical daily feed rate. The concepts, calculation methods, and formulas for the theoretical output and theoretical indicators involved are as follows:

[0105] Theoretical output (calculated based on tapping time and interval) t 出铁理 =Σ(ROUND((time) 本炉终了 -time 上炉终了 )*24,3)*L 实时 *O 料批 / 1000*ΣTFe / 100*0.99 / 0.94)

[0106] t 出铁理 The cumulative theoretical iron production (t / d) calculated based on the end-of-tapping interval of each furnace within a natural day; time 本炉终了 h represents the calendar time for the completion of this furnace operation; h: min; time. 上炉终了 The calendar operation time at the end of the previous furnace run, h:min; L 实时 The theoretical material velocity, calculated based on real-time oxygen enrichment and corrected air volume, is expressed in batches per hour. 料批 ΣTFe represents the batch weight of ore, kg / h; ΣTFe represents the overall grade of the furnace feed, %.

[0107] Theoretical output (theoretical iron output based on hourly feed rate) t 下料理 =AVERAGE(L 实时 *24*O料批 / 1000*ΣTFe / 100*0.99 / 0.94)

[0108] t 出铁理 The daily output is the average value (t / d) obtained from the hourly theoretical iron output based on the hourly corrected air volume and oxygen enrichment rate; the rest is the same as above. The daily theoretical iron output is obtained by accumulating the hourly output to the daily output.

[0109] Theoretical fuel ratio (based on theoretical iron output per hour) calculated K 下料理 =C 干焦批 *L 实时 *24 / t 下料理 +M 小时喷煤 *24 / t 下 Cuisine

[0110] K 下料理 The hourly theoretical fuel ratio, measured in kg / t, is derived from the hourly theoretical iron content obtained by correcting the hourly air volume and oxygen enrichment rate. 小时喷煤 The value is the real-time hourly pulverized coal injection rate, in kg / h; the rest is the same as above.

[0111] The results of the operation show that the theoretical fuel ratio fluctuates within ±5 kg / t.

[0112] D. Following the previous steps (preliminary verification of blast furnace condition, coke batch adjustment (including coke briquettes), oxygen adjustment and material control, coal adjustment and temperature control), the raw materials and smelting parameters are adjusted and fed into the furnace. Smelting parameters are adjusted as follows: precise control of material rate, accurate control of furnace temperature (molten iron w([Si]) value), slag and iron composition control calculation, and real-time theoretical prediction and pre-control of indicators. Each step's process definition conditions meet the requirements and are within the error range. Materials are fed into the furnace in sequence for smelting. During the process, adjustments are made based on the main parameter changes of the raw materials and fuel conditions, smelting parameter adjustments, and the time of action, involving key operational parameters such as coke (including coke briquettes) batch weight, oxygen enrichment, and hourly coal quantity. The system also includes real-time theoretical material rate calculation, molten iron w([Si]) and slag and iron composition, output, and indicator prediction and pre-control, as well as comparison and verification with actual smelting output, slag and iron composition, coking coal ratio, and iron quantity, and a return and correction calculation template.

[0113] Furnace smelting and parameter control steps:

[0114] D1. The total amount of the four types of ore mentioned in A is 100% (the ore includes vanadium-titanium ore and common ore), and coke with high ash and sulfur content (including coke briquettes) is fed into the blast furnace in the usual amount. After checking the blast furnace condition, under constant blast temperature and full blast conditions, "quantitative oxygen adjustment and precise control of material rate" is adopted. The oxygen enrichment is adjusted ≤3 times per shift to achieve control of |daily theoretical batch - daily specified batch| / daily specified batch < 1.50%.

[0115] D2. Smelting shall be carried out under the following conditions:

[0116] This equipment is suitable for blast furnace smelting of titanium slag from vanadium-titanium ore and ordinary ore. The smelting parameters are as follows: hot blast pressure 0.30–0.39 MPa, top pressure 0.155–0.195 MPa, hot blast temperature 1150℃–1250℃, and furnace feed air volume (corrected) 3200–5700 m³ / h. 3 / min, oxygen enrichment of 9400~15000m 3 / h, pulverized coal injection rate is 135-165 kg / t iron (pulverized coal injection rate 22.0-35.0%); ore batch 33.0-55.0 tons, coke batch (dry basis) 7.2-11.0 tons; coke batch (dry basis) 0.45-0.70 tons; w([Si]) 0.055-0.35% (lower limit for vanadium-titanium ore smelting), slag basicity 1.10-1.18, molten iron temperature 1420-1480℃.

[0117] Coke batch adjustment: When the input (collection) raw material conditions (4 main components) reach the required adjustment range (definition requirements are defined in step A), calculations are performed according to the aforementioned rules, formulas, and methods (easy to automate). The effect of this adjustment is reflected within one smelting cycle.

[0118] (Controlling the material rate) Adjustment of oxygen enrichment: When the difference between the actual material rate and the specified material rate reaches the required adjustment range (definition requirements are defined in step A), calculation is performed according to the aforementioned rules, formulas, and methods (easy to automate). Blast furnace temperature control is achieved in conjunction with the adjustment of the hourly pulverized coal injection rate.

[0119] The adjustment effect reflects the landing time, which is resolved by the automatic search function.

[0120] The completion times for the above-mentioned influencing factors are as follows: furnace feed grade, slag basicity, clinker rate, and top pressure are all within one smelting cycle (4.5–5.5 hours, automatically calculated); pulverized coal injection is 3.5 hours; and air volume, air temperature, and humidity are 1 hour. The adjustment point is determined by the time it takes for the corresponding influencing factor to change and for the adjustment factor to take effect, based on maintaining a relatively stable overall fuel ratio (absolute deviation < 5 kg / t).

[0121] D3. Smelting shall be carried out under the following conditions:

[0122] During the smelting process, the slag ratio is 380–480 kg / t, the magnesium-aluminum ratio in the slag is 0.65–0.95, the slag basicity is 1.10–1.18, the controlled blast temperature is stable (any value within the range of 1180℃–1250℃), the oxygen enrichment rate (after adjusting for blast volume) is 2.90–5.0%, and the permeability index is 18000–22000 m³ / s. 3 / (min.MPa), theoretical combustion temperature 2300~2400℃, actual blower speed 255~275m / s, actual blower kinetic energy (after air volume correction) 17000~22000kg.m / s, theoretical hourly material rate 8.5~10.0 batches.

[0123] When oxygen is used to regulate the feed and coal is used to regulate the temperature, in addition to the deviation values ​​obtained meeting the aforementioned requirements for feed rate and silicon deviation, direct smelting parameters such as air volume, air pressure, and top pressure, as well as indirect smelting parameters such as permeability index, theoretical combustion temperature, and blast kinetic energy obtained through automatic calculation, are all within this range. For vanadium-titanium ore smelting blast furnaces, the lower limit of w([Si]) value and the upper limit of w(MgO) / w(Al2O3) value are taken.

[0124] The actual smelting results are returned for correction. According to the conventional slag and iron tapping (the number of iron tapping times in blast furnace is 2 to 3 times / day more than that in ordinary ore smelting), the corrected calculation parameters are returned based on the hourly theoretical and actual material rate, theoretical calculation control and actual w([Si]) value, theoretical slag and iron composition and actual slag and iron composition, theoretical and actual furnace output (day), theoretical and actual fuel ratio, etc.

[0125] In step B (B1) of this invention, the main raw material parameters fluctuation ranges meet the following requirements: clinker rate < ±1.0%, overall furnace grade < ±0.20%, coke < ±0.1%, and pulverized coal ash content < ±0.10%. The slag and iron composition is directly output according to the calculation sequence of step B1. Specifically, based on the benchmark smelting parameters (w([Si]), air volume, air pressure, hourly coal quantity, hourly actual material rate, etc.), and according to the smelting type of ordinary ore and vanadium-titanium ore, the iron ore furnace charge ratio (3 bins for sintered ore, vanadium-titanium pellets) is input to meet the following targets: maintaining theoretical basicity fluctuation <0.01 (±), w(TiO2) <17.0%, w(Al2O3) <13.0%, and magnesium-aluminum ratio 0.65~0.95 (upper limit for vanadium-titanium ore smelting). Based on two bins for ore and one bin for lump ore, theoretical calculations and verifications were performed on the furnace charge grade, theoretical iron content, smelting cycle, slag content, fuel ratio, pulverized coal injection rate, and slag-iron composition. The slag-iron composition, slag ratio, and potassium, sodium, zinc, and titanium loads were output. Specifically, under similar raw material and fuel conditions (ore and coke varieties) for titanium slag smelting in vanadium-titanium ore (w(TiO2) range 10.0%~17.0%), the reduction rates were: Si reduction rate <3.0%, Ti reduction rate <5.5%; Mn reduction rate <55%, V reduction rate <70%, and desulfurization rate >85%; for ordinary ore smelting, the reduction rates were: Si reduction rate <5.0%, Ti reduction rate <20.0%; Mn reduction rate <80%, V reduction rate <80%, and desulfurization rate >93.0%).

[0126] In step B (B2), if the main raw material parameters exceed the stable range (any one of the four parameters is satisfied: clinker rate > ±1.0%, overall feed grade > ±0.20%, coke > ±0.1%, and pulverized coal ash content > ±0.10%), the baseline operating parameters need to be adjusted according to the magnitude of the change (including the determination of the baseline hourly coal quantity and coke batch after the change in raw materials). Based on the baseline ore batch, coke batch (dry basis), w([Si]) quantity, constant blast temperature, and slag basicity within the range, the indirect smelting parameters such as the proportion, coke batch, hourly pulverized coal injection rate, and smelting cycle are checked. The steps and calculation order are as follows: after the factor change, determine the hourly coal quantity → theoretical iron content of the batch → calculate the theoretical coal ratio → determine the coke ratio and coke-to-coke ratio → determine the new coke batch → calculate the theoretical fuel ratio, utilization coefficient, smelting cycle, pulverized coal injection rate, etc. of the batch under the change of basic conditions. The calculation formulas for the hourly coal quantity after the change of factors, the coke-to-coke ratio after the change of factors, the coke ratio after the change of factors, and the coke batch after the change of factors (the coke-to-coke batch remains unchanged) are as follows (see the above for details; the calculation of the theoretical fuel ratio of the batch material, utilization coefficient, smelting cycle, and pulverized coal injection rate are conventional formulas). Then, step (2) of step B1 is entered to calculate the slag ratio, various loads, slag and iron composition, etc. The principle is: the coke batch is only adjusted according to the changes in the comprehensive furnace grade, clinker ratio, and coke pulverized coal ash content; the change of w([Si]) value does not adjust the coke batch, and is mainly controlled by coal adjustment. When the coal ratio is continuously lower than the specified value for 2 furnaces during the smelting process, the coke batch is adjusted after the difference between the original coal ratio (and the current coal ratio) is converted. In particular: when the changing factors improve (clinker rate and comprehensive furnace grade increase, coke ash content and pulverized coal ash content decrease), the direction of the change obtained by input calculation is: maintain the smelting parameters such as total air volume, oxygen content, and constant air temperature, the hourly pulverized coal injection quantity decreases, the coal ratio decreases; the coke batch increases, and the coke ratio decreases. The smelting cycle is extended. Conversely, the changing factors worsen (clinker rate and overall furnace grade decrease, while coke ash content and pulverized coal ash content increase).

[0127] To maintain the clinker rate, furnace grade, coke ash content, and pulverized coal ash content within the theoretical slag alkalinity range, online data acquisition and automatic calculation (real-time and cumulative) are achieved. The material rate is calculated automatically based on the changes in ore batch, coke batch, and the analysis and quantity of each component, combined with smelting parameters such as air volume, oxygen content, and air temperature.

[0128] In step C, when the reference material rate changes during the smelting process, the blast furnace charging speed is precisely controlled using the "oxygen-controlled material" method. In step C, the difference between the actual material rate and the specified reference material rate is checked during the blast furnace smelting process. The definition of the material to be checked and adjusted is: whether the absolute value of the difference between the specified and actual material rates is >0.5 batches for two consecutive hours, or whether the absolute value of the difference between the specified and actual material rates is >1.0 batches for a single hour, or whether the total material rate for two consecutive hours reaches an absolute value ≥1.0 batches of the difference between the specified and actual material rates. If it reaches this, adjustment is required; otherwise, no adjustment is required. If the check result is that no adjustment of the oxygen enrichment is needed, proceed to step C1; if the check result is that adjustment is needed, proceed to step C2. Step C2 involves the determination of the oxygen enrichment adjustment amount and the precise control of the actual material rate. The steps include: (1) parameter data acquisition (including the calculated indirect smelting parameters and fuel parameters); (2) determination of the oxygen enrichment adjustment amount and precise control of the actual material rate. The steps for determining the oxygen enrichment adjustment amount (calculation order) are as follows: original oxygen enrichment amount → oxygen enrichment adjustment amount (input) → new oxygen enrichment amount → oxygen enrichment rate after adjusting and correcting the air volume (combined with the comprehensive blower parameters and fuel parameters in step (1)) → (obtained by combining the air volume per ton of coal consumption, air volume per hour of coal consumption, air volume per ton of coke consumption, and the remaining air volume after coal burning) after adjusting the oxygen volume → judgment of the oxygen adjustment effect. Among them: the definition standard for adjusting the oxygen enrichment amount is: by arbitrarily inputting (an integer multiple of 100, the adjustment amount is not greater than 10% of the total oxygen enrichment amount) oxygen enrichment adjustment amount (m 3 / h), until the theoretical material rate output results obtained simultaneously reach (the judgment principle of oxygen adjustment effect): (1) the difference between the theoretical material rate after oxygen adjustment and the theoretical material rate before oxygen adjustment is defined as 0.1 to 0.3 batches (increase or decrease); (2) |theoretical material rate after oxygen adjustment - specified material rate| < 0.3 batches / h, and predict the batch growth amount for the shift (defined as 0.3 to 1.0 batches); (3) the input oxygen enrichment adjustment amount meets the requirements, and the absolute value of the deviation rate between the theoretical output obtained after oxygen adjustment and the planned required output is < ±1.50%. Among them: (oxygen enrichment data) is calculated based on the relevant data collected every hour (cumulative amount of data per minute).

[0129] Comparison of the effect of material rate control after oxygen adjustment (1 hour) (Zhou Chuandian, Blast Furnace Ironmaking Process Production Technology Manual [M], Beijing: Beijing Metallurgical Industry Press, 2008): If the effect is achieved, proceed to the next cycle; if the effect is not achieved, conduct cause analysis and error analysis, and if the cause is resolved, proceed to the next cycle; if the cause cannot be resolved, the process stops.

[0130] Involving: calculation formulas for corrected air volume, oxygen enrichment rate after corrected air volume, air volume per ton of coal after corrected air volume, air volume per hour of coal after corrected oxygen enrichment rate, air volume per ton of coke after corrected air volume, theoretical material velocity before (and after) oxygen adjustment (see above for details; the corrected air volume and theoretical combustion temperature, blower kinetic energy, permeability index, etc. involved are conventional formulas).

[0131] Step C (C3) involves verifying the daily feed rate, defined by the absolute error rate of the difference between any two of the actual daily feed rate, the specified daily feed rate, and the theoretical daily feed rate < 1.50%. The comparison of actual daily iron production involves concepts and formulas including: theoretical output (calculated theoretically based on tapping time duration and interval) t 出铁理 Theoretical output (calculated based on theoretical iron output per hour) t 下料理 Theoretical fuel ratio (based on theoretical iron output per hour) K calculated theoretically 下料理 .

[0132] Step E involves feeding 100% of the four types of ore mentioned in A (including vanadium-titanium ore and common ore), along with coke (containing coke briquettes) with higher ash and sulfur content, into the blast furnace in conventional quantities. After verifying the blast furnace condition, under constant blast temperature and full blast temperature conditions, "quantitative oxygen adjustment and precise control of material rate" is adopted. The oxygen enrichment is adjusted ≤3 times per shift, achieving a control ratio of |daily theoretical batch - daily specified batch| / daily specified batch < 1.50%. Specifically, coke batch adjustment: when the input (collection) of raw material conditions reaches the required adjustment range (definition requirements are defined in step A), calculations are performed according to the aforementioned rules, formulas, and methods (easy to automate). The effect of this adjustment is reflected within one smelting cycle.

[0133] (Controlling material flow rate) Adjustment of oxygen enrichment: When the difference between the actual material flow rate and the specified material flow rate reaches the required adjustment range (see step C for definition requirements), calculation is performed according to the aforementioned rules, formulas, and methods (easy to automate). The hourly adjustment of oxygen enrichment should be less than 10% of the original total. The effect of this adjustment is reflected within 1 hour.

[0134] The landing time reflected by the adjustment effect is automatically found by the reaction cycle based on the adjustment time and the specific adjustment factors.

[0135] During the smelting process, when oxygen controls the feed and coal controls the temperature, in addition to the deviation values ​​meeting the aforementioned requirements for feed rate and silicon deviation, direct smelting parameters such as air volume, air pressure, and top pressure, as well as indirect smelting parameters such as permeability index, theoretical combustion temperature, and blast kinetic energy obtained through automatic calculation, all fall within this range. For vanadium-titanium ore smelting blast furnaces, the lower limit of w([Si]) and the upper limit of w(MgO) / w(Al2O3) are taken.

[0136] In steps D1 to D3 and E, based on the constant blast temperature and full blast volume, combined with the blast furnace tip w([Si]) value and slag-iron composition control, blast furnace smelting is carried out by "inputting oxygen enrichment adjustment amount to precisely control the material rate". The smelting is completed by comparing and correcting the theoretical control and actual material rate, theoretical slag-iron composition and actual slag-iron composition, theoretical and actual output (daily), theoretical and actual fuel ratio, etc.

[0137] This invention is based on the fundamental principles of material and heat balance in a blast furnace. Under certain smelting intensity and technical specifications, when the material rate and furnace temperature (molten iron w([Si]) value) deviate from the specified values ​​during normal smelting (including ordinary ore and vanadium-titanium ore smelting) in a blast furnace, this invention, based on fundamental theory and the principle of "quantitative modular control of oxygen adjustment for precise material rate control + coal adjustment for w([Si]) value control," forms a quantitative and modular processing mode that effectively solves the complex interrelationships between various direct and indirect smelting parameters during daily intensified smelting in a blast furnace. This mode addresses the control of coke batch quantity, hourly coal quantity, hourly oxygen enrichment, material rate, molten iron w([Si]) value, and slag-iron composition (basicity, magnesium-aluminum ratio), as well as the prediction, control, and verification of smelting cycle and output, fuel ratio indicators, and the coordination and balance of various related data. It accurately ensures that the material rate and w([Si]) value during the smelting process reach the planned predetermined values ​​and has a continuous correction function.

[0138] This invention relates to a smelting method for quantitatively and modularly controlling the hourly feed rate during blast furnace smelting to improve blast furnace stability, reduce the w([Si]) value of molten iron, improve furnace temperature stability, and continuously improve stable technical and economic indicators. Specifically, it relates to a method for quantitatively and modularly controlling the feed rate and furnace temperature (w([Si]) value of molten iron) when they deviate from predetermined values ​​during normal intensified blast furnace smelting. Based on blast furnace fundamental theory and the principle of "quantitative, modular, and precise control of feed rate through oxygen adjustment," this method addresses the interrelationships between various data points during daily intensified blast furnace smelting, including control of coke batch quantity, hourly coal quantity, hourly oxygen enrichment, feed rate, w([Si]) value of molten iron, slag-iron composition (basicity, magnesium-aluminum ratio), smelting cycle and output, fuel ratio prediction and control, verification, and coordination and balance of various direct (indirect) smelting parameters. Accurately ensuring the feed rate reaches the planned value during smelting not only improves the smoothness of blast furnace operation but also significantly reduces fuel ratio and smelting costs. Furthermore, the implementation process of this method can be automated based on data acquisition and calculation, featuring simplicity, rapid control, and accuracy. Simultaneously, this method is applicable to blast furnaces of any volume and with any charge structure (including vanadium-titanium ore smelting and conventional smelting), achieving the specified charge rate range with only 0-3 oxygen adjustments per shift. It is an effective smelting method for improving the systematization and precision of blast furnace operation, enhancing furnace stability, and continuously improving technical indicators. It possesses broad applicability and adaptability.

[0139] Following the aforementioned benchmark verification of the burden ratio, coke batch, hourly coal blending, smelting indicators, and indirect smelting parameters after changes in the overall charge grade, clinker rate, coke ash content, and pulverized coal ash content, benchmark batching calculations, parameter and index verification analysis were conducted. The main verification conditions (clinker rate, overall charge grade, coke ash content, and pulverized coal ash content) were changed, and the batching calculations, parameters, and index verification analysis were performed. Combined with w([Si]) control and slag-iron composition and effect verification, the oxygen enrichment adjustment amount was input to precisely control the actual material rate. This was done according to the previous steps (preliminary verification of blast furnace conditions, coke batch adjustment (including coke briquettes), combined with control... The process of adjusting raw materials and smelting parameters (temperature-controlled oxygen and feed) and returning the adjusted smelting parameters for correction and verification, employs a "quantitative oxygen-controlled precise feed rate" method that allows for easy automatic data collection and comprehensive calculation. Within the control range of w([Si]) and slag-iron composition, the feed rate can be accurately and stably controlled by adjusting the oxygen enrichment 0-3 times per shift during daily smelting operations. This ensures that the feed rate difference is within the specified range (±1.0 batch / shift, and the difference between the specified and actual daily feed rate <1.50%), eliminating the possibility of reverse operation. Furthermore, it features real-time prediction and daily-actual value comparison and verification functions for the adjustment effect, including theoretical and actual output and theoretical and actual fuel ratios, as well as smelting parameter verification functions, all of which facilitate automatic data collection, calculation, and analysis.

[0140] This invention, based on the principle of "quantitative oxygen adjustment and precise control of feeding speed," comprehensively verifies the material (full analysis of raw materials and fuels entering the furnace) and predicts and verifies the slag and iron composition according to the baseline w([Si]) amount. It then verifies the factors affecting the feeding speed (corrected air volume, corrected oxygen enrichment rate, coal ratio, coke batch, slag and iron composition, etc.) and their theoretical quantitative calculations to precisely control the feeding speed, verify the feeding speed control to meet the standards, and calculate the theoretical iron content and theoretical indicators. Next, it defines the feeding speed range after oxygen adjustment (direct input of the adjustment amount) – feeding speed control (specified feeding speed, actual feeding speed, theoretical pre-controlled feeding speed), combines the baseline w([Si]) amount, and the adjustment (oxygen enrichment, hourly pulverized coal quantity) before and after to precisely control the feeding speed, control the molten iron w([Si]) value within the range, verify the slag and iron composition, balance the furnace smelting parameters, re-verify the indicator composition, and return the actual smelting results for correction.

[0141] This invention is based on fundamental metallurgical theories and combined with practical operational experience. It systematically understands the characteristics of raw materials and fuels, the production characteristics of blast furnace smelting, and the influence of various smelting parameters on the smelting process, as well as the matching and process control relationships of related smelting parameters. It develops a quantitative and modular processing method to address the interrelationships between various data points in the daily intensified smelting process of blast furnaces, including control of coke batch quantity, hourly coal quantity, hourly oxygen enrichment, material rate, molten iron w([Si]) value, and slag-iron composition (basicity, magnesium-aluminum ratio), smelting cycle and output, fuel ratio index prediction, control, verification, and coordination and balance of various direct (indirect) smelting parameters. During operation, quantitative and modular adjustments to oxygen enrichment and pulverized coal injection ensure that the material rate accurately reaches the planned value within the reaction cycle, significantly improving the stability of blast furnace production, improving the smoothness of blast furnace operation, and significantly reducing fuel ratio and smelting costs. Furthermore, the method should have broad applicability and adaptability, be simple and convenient to operate, requiring only input of the adjustment quantity, and automatically calculate and output the corresponding parameter adjustment results through a real-time system and multi-factor joint calculation. This has significant practical implications for production practices.

[0142] Compared with the prior art, the beneficial effects of this invention are as follows:

[0143] This invention digitizes, quantifies, and modularizes the data involved in the complex and highly interconnected smelting operations, including furnace charge preparation and indicator prediction and verification, smelting parameter verification, precise oxygen adjustment and charge rate control (core module), coal temperature control (molten iron w([Si]) value), shift (day) charge rate pre-control and verification, molten iron w([Si]) value (adjustment factors reflect furnace batch, day) and slag-iron composition pre-control and verification, and daily output and indicator tracking and pre-control of changes. It also boasts the advantages of being comprehensive, real-time, systematic, and accurate.

[0144] This invention achieves the following: 0-3 oxygen adjustments per shift are sufficient to reach the specified material rate range (the absolute deviation between the actual daily material rate and the specified material rate is <1.50%), effectively improving the systematization and precision of blast furnace operation, enhancing blast furnace stability, and continuously improving technical indicators. Furthermore, this method is applicable to blast furnaces of any volume and with any charge structure (including vanadium-titanium ore smelting and conventional smelting).

[0145] The method of this invention is simple to apply. The entire process can automatically collect and calculate the required data (including coke batch size, hourly oxygen enrichment, hourly pulverized coal injection rate, and related direct smelting parameters), adjust the time after each factor's adjustment, and compare and verify the actual effect within the corresponding time. In practical applications, simply inputting the adjustment amount (hourly oxygen enrichment adjustment amount) according to the method specified in this invention, combined with the obtained (collected) corresponding variables (raw material composition, furnace charge structure ratio, the effect of adjustment factors and reaction cycle, direct smelting parameters, etc.), can replace the cumbersome and error-prone multivariate simultaneous equation solving, directly outputting the desired effect, and enabling real-time tracking and comparison verification of the adjustment effect prediction. The calculation process also fully reflects the influence trend, amplitude, and control requirements of various factors in the smelting process on the blast furnace charge rate, furnace temperature (molten iron w([Si])) and slag-iron composition pre-control. This system enables quantitative and modular precise control of hourly feed rate and blast furnace temperature (molten iron w([Si]) value) during blast furnace smelting. This aims to improve blast furnace stability, reduce molten iron w([Si]) value, enhance furnace temperature stability, and continuously improve the trend, suitability, and matching requirements of smelting parameters in terms of stable technical and economic indicators. Specifically, it addresses the issue of feed rate deviation from specified values ​​during normal intensified smelting processes. Based on blast furnace fundamental theory and the principle of "quantitative and modular precise control of feed rate through oxygen adjustment + coal adjustment and temperature control," it provides a quantitative and modular processing mode to resolve the interrelationships between coke batch quantity, hourly coal quantity, hourly oxygen enrichment, feed rate, molten iron w([Si]) value, slag-iron composition control (basicity, magnesium-aluminum ratio), smelting cycle and output, fuel ratio index prediction, control, verification, and coordination and balance of various direct (indirect) smelting parameters during daily intensified smelting. It also features a return correction function and boasts advantages of simplicity and accurate control.

[0146] This invention is used in blast furnaces during normal intensified smelting (smelting of ordinary ore and vanadium-titanium ore) when the material rate deviates from the specified value during the smelting process, or when it is necessary to further reduce material rate and furnace temperature fluctuations, and precisely control the hourly material rate to improve blast furnace stability and reduce consumption. It is particularly suited to meet the need to continuously improve the operational skills of blast furnace operators under different raw material and equipment conditions, replacing the traditional method of relying on blast furnace operators' experience or simple local calculations for approximate adjustments. By establishing a quantitative and modular adjustment method based on the principle of "quantitative and modular precise control of material rate through oxygen adjustment + coal adjustment and temperature control," it achieves dynamic and real-time consideration of the influence of multiple related factors, overcoming the inconsistency in calculation due to differences in the abilities and skills of operators across three shifts. Furthermore, it utilizes computer technology to quantify, standardize, real-time, and comprehensively process the complex control process's related calculations, achieving: 0-3 oxygen adjustments per shift are sufficient to reach the specified material rate range, effectively improving the systematic and precise operation level of the blast furnace, enhancing blast furnace stability, and continuously improving technical indicators. Furthermore, this method is applicable to blast furnaces of any volume and any charge structure (including vanadium-titanium ore smelting and conventional smelting).

[0147] Compared with traditional approaches and models that rely on operational experience, on-site estimation, simplified local calculations, or calculations using multiple simultaneous equations, and existing methods for material and temperature control, this invention systematically addresses the interrelationships of raw material and fuel composition characteristics, blast furnace smelting production characteristics, and the combined influence of various smelting parameters on the smelting process and results. It also addresses the matching and process control relationships of relevant smelting parameters. This invention develops a quantitative and modular adjustment method for coke batches during daily intensified smelting in blast furnaces. This method addresses the quantitative and modular adjustment of hourly oxygen enrichment, material rate (specified material rate, theoretically calculated material rate based on the adjusted oxygen enrichment and corrected blast volume oxygen enrichment rate, and actual material rate), slag-iron composition control (basicity, magnesium-aluminum ratio), smelting cycle and output (theoretical output based on theoretical material rate, theoretical output based on material rate during tapping time, and actual output), fuel ratio (theoretical and actual) index prediction, control, verification, and coordination and balance of various direct (indirect) smelting parameters. During operation, the oxygen enrichment and pulverized coal injection are used for quantitative and modular adjustments to ensure that the material rate in the smelting process accurately reaches the planned value within the reaction cycle. It also has the function of comparing and verifying the adjustment effect (theoretical and calculated values ​​of material rate, molten iron w([Si]) value and slag iron composition) and indicators such as output and fuel ratio by hour, furnace, and day, and returning for correction. During operation, only the actual raw material composition and smelting parameters are needed to accurately determine indicators such as material rate, w([Si]) value, slag-iron composition, and production-fuel ratio. This solves the problems of incomplete information, unsystematic consideration, and large errors in local calculations in traditional methods. It also solves the problem that operators often rely on personal skill and experience to make rough adjustments when adjusting material rate, which easily leads to inconsistent adjustment standards and calculation methods across three shifts. Furthermore, it addresses the shortcomings of traditional methods, such as insufficient consideration of variables and lack of real-time performance. It also solves the problem that the impact of adjusting oxygen enrichment on material rate cannot be combined with actual changes in smelting parameters, resulting in insufficient accuracy of calculation results. In addition, it addresses the problem that traditional methods are too time-consuming to calculate and that parameter adjustments (coke batch, oxygen enrichment, pulverized coal injection) cannot take into account the systematic nature of smelting. The new method combines actual changes to achieve real-time calculation, realizing comprehensive, systematic, dynamic, and accurate joint calculation of complex control processes in complex blast furnace smelting. Operationally, it achieves quantification, standardization, and instant output results. This method enables automatic data acquisition and calculation, real-time correlation of direct (indirect) smelting parameters, and is easily automated, intelligent, and visualized. It is not limited by blast furnace volume or type of ore (common ore, titanium slag smelting in vanadium-titanium ore), making it a widely applicable new blast furnace smelting technology. Simply inputting the hourly oxygen enrichment dosage provides blast furnace operators with comprehensive and real-time operational support, improving furnace operation and significantly reducing fuel ratios and smelting costs. Furthermore, this method is applicable to intensified smelting processes with different blast furnaces and arbitrary charge structures, demonstrating strong adaptability.This method enables precise achievement of the specified feed rate range within a single shift of blast furnace operation, requiring only 0 to 3 oxygen adjustments. It is characterized by its simplicity, rapid control, and accuracy. Attached Figure Description

[0148] Figure 1 This is the process for verifying the composition of raw materials, fuels, slag, and iron in the method of this invention;

[0149] Figure 2 This is the process for precise control and index verification of theoretical material rate in the method of this invention;

[0150] Figure 3 The fitting relationship between w([Si]) value and [Si] reduction rate;

[0151] Figure 4 The fitting relationship between w([Si]) value and [Ti] reduction rate;

[0152] Figure 5 The fitting relationship between w([Si]) value and [Mn] reduction rate;

[0153] Figure 6 The fitting relationship between w([Si]) value and [V] reduction rate;

[0154] Figure 7 The fitting relationship between w([Si]) value and desulfurization rate;

[0155] Figure 8 The fitting relationship between w([Si]) value and [Si] reduction rate;

[0156] Figure 9 The fitting relationship between w([Si]) value and [Ti] reduction rate;

[0157] Figure 10 The fitting relationship between w([Si]) value and [Mn] reduction rate;

[0158] Figure 11 The fitting relationship between w([Si]) value and [V] reduction rate;

[0159] Figure 12 The relationship between w([Si]) value and desulfurization rate is shown. Detailed Implementation

[0160] The present invention will now be described in further detail with reference to the embodiments.

[0161] Those skilled in the art will understand that the following embodiments are for illustrative purposes only and should not be construed as limiting the scope of the invention. Where specific techniques or conditions are not specified in the embodiments, they are performed in accordance with the techniques or conditions described in the literature in the field or according to the product instructions. Materials or equipment whose manufacturers are not specified are all conventional products that can be obtained by purchase.

[0162] Example 1

[0163] A smelting method for quantitatively and systematically controlling the blast furnace charge rate includes the following steps:

[0164] A. Standard ingredients: The smelting process is ordinary ore smelting or medium titanium slag smelting.

[0165] When smelting ordinary ore, the ordinary ore furnace charge used includes the following components by mass percentage: 72% sinter, 28% high-silica pellets, and 0% low-silica lump ore; total 100%; ore batch 53,000 kg;

[0166] When smelting medium-titanium slag, the vanadium-titanium ore furnace charge used includes the following components by mass percentage: 62% sintered ore, 33% vanadium-titanium pellets, and 5% low-silicon lump ore, totaling 100%; ore batches are 320,000 kg / batch.

[0167] In the smelting of ordinary ore or medium titanium slag, the coke batch is 7200 kg / batch based on dry coke weight; the coke slag batch is 450 kg / batch based on dry coke weight; the pulverized coal injection rate is 21.5–48.5 t / h.

[0168] B. Ingredient calculation, parameter and index verification analysis:

[0169] B1. Benchmark ingredient calculation, parameter and index verification analysis:

[0170] The wind pressure, air volume, wind temperature, and w([Si]) of the entire air supply remain unchanged, among which the wind temperature is the highest stable wind temperature; if the fluctuation range of factors in ordinary ore smelting or medium titanium slag smelting all meet the following conditions: clinker rate < ±1.0%, comprehensive furnace grade < ±0.20%, coke ash content < ±0.1%, and pulverized coal ash content < ±0.10%; then:

[0171] (1) Calculate the theoretical fuel ratio, utilization coefficient and smelting cycle;

[0172] (2) Calculate the theoretical composition of pig iron, theoretical composition of slag, basicity, and magnesium-aluminum ratio;

[0173] (3) Calculate the conversion factor between the corrected air volume and the surface air volume. The oxygen enrichment rate after correcting the air volume is 2.90 to 5.00%.

[0174] B2. Verification and analysis of ingredient calculations, parameters, and indicators when key verification conditions change:

[0175] The wind pressure, air volume, wind temperature, and w([Si]) of the entire air supply remain unchanged, among which the wind temperature is the highest stable wind temperature; if any one of the factors in the ordinary ore smelting or medium titanium slag smelting does not meet the following conditions: clinker rate < ±1.0%, overall furnace grade < ±0.20%, coke ash content < ±0.1%, pulverized coal ash content < ±0.10%; then:

[0176] (1) Calculate the hourly coal quantity, theoretical iron content of the batch, theoretical coal ratio, coke ratio, coke-butane ratio, coke batch, theoretical fuel ratio, utilization coefficient, smelting cycle and pulverized coal injection rate after the factors change;

[0177] (2) Calculate the theoretical composition of pig iron, theoretical composition of slag, basicity, and magnesium-aluminum ratio;

[0178] C. Input the oxygen enrichment adjustment amount to precisely control the actual material flow rate:

[0179] During blast furnace smelting, the difference between the actual material rate and the specified benchmark material rate is checked. The principle for checking whether to adjust the material rate is as follows:

[0180] (1) The absolute value of the difference between the actual material rate and the specified benchmark material rate for two consecutive hours is ≥0.5 batches / h;

[0181] (2) The difference between the actual material rate and the specified benchmark material rate in a single hour is ≥1.0 batches / h;

[0182] (3) The absolute value of the difference between the specified material rate and the actual material rate for two consecutive hours is ≥1.0 batch; (that is, the difference between the sum of the material rates for two consecutive hours exceeding (or failing to reach) the sum of the specified material rate for two hours is ≥1.0 batch);

[0183] If any one of the above three conditions is met, adjustment is required; otherwise, no adjustment is required.

[0184] The adjustment method is as follows:

[0185] (1) Collect comprehensive air supply parameters, indirect smelting parameters and fuel parameters;

[0186] (2) Based on the original oxygen enrichment, input the oxygen enrichment adjustment amount to adjust the oxygen and obtain the new oxygen enrichment; then, through the collected comprehensive air supply parameters, indirect smelting parameters and fuel parameters, calculate the oxygen enrichment rate and theoretical material rate after adjusting the oxygen correction air volume, and then judge the oxygen adjustment effect.

[0187] The judgment criteria are:

[0188] 1) The difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is defined as 0.1 to 0.3 batches.

[0189] 2) |Theoretical feed rate after oxygen adjustment - Specified feed rate| < 0.3 batches / h, and predict the batch growth rate for the shift (defined between 0.3 and 1.0 batches; the batch growth rate for the shift refers to the difference between the hourly theoretical feed rate and the actual feed rate multiplied by 8 hours);

[0190] 3) The input oxygen enrichment adjustment amount makes the theoretical material rate reach the material rate control value requirement, and the absolute value of the deviation rate between the theoretical output obtained after oxygen adjustment and the planned output requirement is <±1.50%.

[0191] If conditions 1) to 3) are met simultaneously, and the difference between the actual material rate after oxygen adjustment and the specified benchmark material rate is checked, and the result is that no adjustment is needed, then the material rate effect needs to be checked; at the same time, the theoretical combustion temperature, blast energy, permeability index and smelting cycle after oxygen adjustment are calculated.

[0192] The specific method for verifying the material flow rate effect is as follows:

[0193] The verification standard for Japanese batches is defined as follows: the absolute value error rate of the difference between any two of the three factors—actual daily material rate, specified daily material rate, and theoretical daily material rate—is <1.50%; if all three are met, the process continues.

[0194] The theoretical daily coal ratio and coke ratio are compared with the actual daily coal ratio and coke ratio. The theoretical output calculated based on the theoretical feed rate is compared with the actual daily output. If the deviation rate of the difference between the theoretical daily output and the actual daily output is <1.50%, the verification is passed and the process continues.

[0195] D. Furnace smelting and parameter control:

[0196] During the smelting process, the number of times the oxygen enrichment is adjusted in each shift should be ≤3 times, and the ratio of |Daily theoretical batch - Daily specified batch| / Daily specified batch should be <1.50%.

[0197] Smelting conditions: hot blast pressure 0.30~0.39MPa, top pressure 0.155~0.195MPa, hot blast temperature 1150℃~1250℃, and corrected furnace feed air volume 3200~5700m³. 3 / min, oxygen enrichment of 9400~15000m 3 / h, pulverized coal injection rate is 135-165 kg / t iron, pulverized coal injection rate is 22.0-35.0%; ore batch is 33.0-55.0 tons, coke batch is 7.2-11.0 tons on a dry basis; coke batch is 0.45-0.70 tons on a dry basis; w([Si]) is 0.055-0.35%, slag basicity is 1.10-1.18, and molten iron temperature is 1420-1480℃; during the smelting process, the slag ratio is 380-480 kg / t, the magnesium-aluminum ratio in the slag is 0.65-0.95, the slag basicity is 1.10-1.18, the blast temperature is controlled to be stable, the oxygen enrichment rate is 2.90%-5.0%, and the permeability index is 18000-22000 m 3 / (min.MPa), theoretical combustion temperature 2300~2400℃, actual blowing speed 255~275m / s, actual blowing kinetic energy 17000~22000kg.m / S, theoretical hourly material rate 8.5~10.0 batches.

[0198] The sintered ore composition, by mass percentage, includes 52.0–54.0% TFe, 5.5–6.5% SiO2, 13.0–13.5% CaO, 1.75–2.19% Al2O3, 2.30–2.90% MgO, 0.40–1.35% TiO2, 0.045%–0.055% S, 0.165–0.150% V2O5, and 0.045%–0.055% MnO, with the balance being unavoidable impurities. The bulk density is 1.90–2.10 t / m³. 3 ;

[0199] The vanadium-titanium ore pellets, by mass percentage, comprise 53.5–57.5% TFe, 4.5–5.5% SiO2, 0.55–1.35% CaO, 2.20–2.90% Al2O3, 2.35–2.90% MgO, 6.40–11.0% TiO2, 0.55–0.75% V2O5, and 0.23%–0.25% MnO, with the balance being unavoidable impurities; the bulk density is 2.20–2.30 t / m³. 3 ;

[0200] The high-silica pellets contain, by mass percentage: 58.5–60.0% TFe, 6.5–7.5% SiO2, 0.5–1.5% CaO, 1.80–2.10% Al2O3, 1.0–1.5% MgO, 2.50–3.50% TiO2, 0.165–0.150% V2O5, and 0.045%–0.055% MnO, with the balance being unavoidable impurities. The bulk density is 2.15–2.35 t / m³. 3 ;

[0201] The low-silica lump ore composition, by mass percentage, includes 64.0–66.0% TFe, 3.0–4.5% SiO2, 0.03–0.05% CaO, 1.00–1.50% Al2O3, 0.01–1.0% MgO, TiO2 <1.0%, 0.030–0.050% V2O5, and 0.110%–0.160% MnO, with the balance being unavoidable impurities. The bulk density is 2.2–2.4 t / m³. 3 .

[0202] The coke composition, by mass percentage, includes 84.0–86.5% C and 13.5–14.5% ash, with a bulk density of 0.55–0.65 t / m³. 3 ;

[0203] The coke ash composition by mass percentage includes 53.0–56.0% SiO2, 2.20–3.0% CaO, 24.0–26.0% Al2O3, 0.15–1.0% MgO, TiO2 <2.0%, 0.35%–0.45% MnO, with the balance being unavoidable impurities.

[0204] The pulverized coal composition includes, by mass percentage, 76.0-78.0% C, 13.5-15.0% ash, and 12.5-13.5% volatile matter, with a particle size of -200 mesh accounting for 66-70%.

[0205] The ash composition of the pulverized coal, by mass percentage, includes 55.0–57.0% SiO2, 5.20–6.50% CaO, 23.0–25.0% Al2O3, 2.20–2.50% MgO, TiO2 <2.0%, and 0.35%–0.45% MnO, with the balance being unavoidable impurities.

[0206] The comprehensive air supply parameters include: surface air volume, humidity, air pressure, top pressure, air temperature, and tuyer area; indirect smelting parameters include corrected air volume and the oxygen enrichment rate, theoretical combustion temperature, permeability index, and blast energy after correcting the air volume; fuel parameters include the batch weight, composition, and combustion rate of coke and coke briquettes before the tuyer, as well as the hourly coal powder quantity, coal powder composition, and combustion rate before the tuyer.

[0207] It also includes step E, actual smelting result return correction: based on the actual smelting results obtained in step E, based on the hourly theoretical and actual material rate, theoretical calculation control and actual w([Si]) value, theoretical slag and iron composition and actual slag and iron composition, theoretical and actual furnace output, theoretical and actual fuel ratio, according to the calculation methods in steps B to D, the calculation parameters are corrected and smelting continues.

[0208] Example 2

[0209] A smelting method for quantitatively and systematically controlling the blast furnace charge rate includes the following steps:

[0210] A. Standard ingredients: The smelting process is ordinary ore smelting or medium titanium slag smelting.

[0211] When smelting ordinary ore, the ordinary ore furnace charge used includes the following components by mass percentage: 65% sinter, 25% high-silica pellets, and 10% low-silica lump ore; total 100%; ore batch 55,000 kg;

[0212] When smelting medium-titanium slag, the vanadium-titanium ore charge used includes the following components by mass percentage: 65% sintered ore, 35% vanadium-titanium pellets, 0% low-silicon lump ore, totaling 100%; ore batch 34,000 kg / batch.

[0213] In the smelting of ordinary ore or medium titanium slag, the coke batch is 11,000 kg / batch based on dry coke weight; the coke slag batch is 700 kg / batch based on dry coke weight; the pulverized coal injection rate is 21.5–48.5 t / h.

[0214] B. Ingredient calculation, parameter and index verification analysis:

[0215] B1. Benchmark ingredient calculation, parameter and index verification analysis:

[0216] The wind pressure, air volume, wind temperature, and w([Si]) of the entire air supply remain unchanged, among which the wind temperature is the highest stable wind temperature; if the fluctuation range of factors in ordinary ore smelting or medium titanium slag smelting all meet the following conditions: clinker rate < ±1.0%, comprehensive furnace grade < ±0.20%, coke ash content < ±0.1%, and pulverized coal ash content < ±0.10%; then:

[0217] (1) Calculate the theoretical fuel ratio, utilization coefficient and smelting cycle;

[0218] (2) Calculate the theoretical composition of pig iron, theoretical composition of slag, basicity, and magnesium-aluminum ratio;

[0219] (3) Calculate the conversion factor between the corrected air volume and the surface air volume. The oxygen enrichment rate after correcting the air volume is 2.90 to 5.00%.

[0220] B2. Verification and analysis of ingredient calculations, parameters, and indicators when key verification conditions change:

[0221] The wind pressure, air volume, wind temperature, and w([Si]) of the entire air supply remain unchanged, among which the wind temperature is the highest stable wind temperature; if any one of the factors in the ordinary ore smelting or medium titanium slag smelting does not meet the following conditions: clinker rate < ±1.0%, overall furnace grade < ±0.20%, coke ash content < ±0.1%, pulverized coal ash content < ±0.10%; then:

[0222] (1) Calculate the hourly coal quantity, theoretical iron content of the batch, theoretical coal ratio, coke ratio, coke-butane ratio, coke batch, theoretical fuel ratio, utilization coefficient, smelting cycle and pulverized coal injection rate after the factors change;

[0223] (2) Calculate the theoretical composition of pig iron, theoretical composition of slag, basicity, and magnesium-aluminum ratio;

[0224] C. Input the oxygen enrichment adjustment amount to precisely control the actual material flow rate:

[0225] During blast furnace smelting, the difference between the actual material rate and the specified benchmark material rate is checked. The principle for checking whether to adjust the material rate is as follows:

[0226] (1) The absolute value of the difference between the actual material rate and the specified benchmark material rate for two consecutive hours is ≥0.5 batches / h;

[0227] (2) The difference between the actual material rate and the specified benchmark material rate in a single hour is ≥1.0 batches / h;

[0228] (3) The absolute value of the difference between the specified material rate and the actual material rate for two consecutive hours is ≥1.0 batch; (that is, the difference between the sum of the material rates for two consecutive hours exceeding (or failing to reach) the sum of the specified material rate for two hours is ≥1.0 batch);

[0229] If any one of the above three conditions is met, adjustment is required; otherwise, no adjustment is required.

[0230] The adjustment method is as follows:

[0231] (1) Collect comprehensive air supply parameters, indirect smelting parameters and fuel parameters;

[0232] (2) Based on the original oxygen enrichment, input the oxygen enrichment adjustment amount to adjust the oxygen and obtain the new oxygen enrichment; then, through the collected comprehensive air supply parameters, indirect smelting parameters and fuel parameters, calculate the oxygen enrichment rate and theoretical material rate after adjusting the oxygen correction air volume, and then judge the oxygen adjustment effect.

[0233] The judgment criteria are:

[0234] 1) The difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is defined as 0.1 to 0.3 batches.

[0235] 2) |Theoretical feed rate after oxygen adjustment - Specified feed rate| < 0.3 batches / h, and predict the batch growth rate for the shift (defined between 0.3 and 1.0 batches; the batch growth rate for the shift refers to the difference between the hourly theoretical feed rate and the actual feed rate multiplied by 8 hours);

[0236] 3) The input oxygen enrichment adjustment amount makes the theoretical material rate reach the material rate control value requirement, and the absolute value of the deviation rate between the theoretical output obtained after oxygen adjustment and the planned output requirement is <±1.50%.

[0237] If conditions 1) to 3) are met simultaneously, and the difference between the actual material rate after oxygen adjustment and the specified benchmark material rate is checked, and the result is that no adjustment is needed, then the material rate effect needs to be checked; at the same time, the theoretical combustion temperature, blast energy, permeability index and smelting cycle after oxygen adjustment are calculated.

[0238] The specific method for verifying the material flow rate effect is as follows:

[0239] The verification standard for Japanese batches is defined as follows: the absolute value error rate of the difference between any two of the three factors—actual daily material rate, specified daily material rate, and theoretical daily material rate—is <1.50%; if all three are met, the process continues.

[0240] The theoretical daily coal ratio and coke ratio are compared with the actual daily coal ratio and coke ratio. The theoretical output calculated based on the theoretical feed rate is compared with the actual daily output. If the deviation rate of the difference between the theoretical daily output and the actual daily output is <1.50%, the verification is passed and the process continues.

[0241] D. Furnace smelting and parameter control:

[0242] During the smelting process, the number of times the oxygen enrichment is adjusted in each shift should be ≤3 times, and the ratio of |Daily theoretical batch - Daily specified batch| / Daily specified batch should be <1.50%.

[0243] Smelting conditions: hot blast pressure 0.30~0.39MPa, top pressure 0.155~0.195MPa, hot blast temperature 1150℃~1250℃, and corrected furnace feed air volume 3200~5700m³. 3 / min, oxygen enrichment of 9400~15000m 3 / h, pulverized coal injection rate is 135-165 kg / t iron, pulverized coal injection rate is 22.0-35.0%; ore batch is 33.0-55.0 tons, coke batch is 7.2-11.0 tons on a dry basis; coke batch is 0.45-0.70 tons on a dry basis; w([Si]) is 0.055-0.35%, slag basicity is 1.10-1.18, and molten iron temperature is 1420-1480℃; during the smelting process, the slag ratio is 380-480 kg / t, the magnesium-aluminum ratio in the slag is 0.65-0.95, the slag basicity is 1.10-1.18, the blast temperature is controlled to be stable, the oxygen enrichment rate is 2.90%-5.0%, and the permeability index is 18000-22000 m 3 / (min.MPa), theoretical combustion temperature 2300~2400℃, actual blowing speed 255~275m / s, actual blowing kinetic energy 17000~22000kg.m / S, theoretical hourly material rate 8.5~10.0 batches.

[0244] The sintered ore composition, by mass percentage, includes 52.0–54.0% TFe, 5.5–6.5% SiO2, 13.0–13.5% CaO, 1.75–2.19% Al2O3, 2.30–2.90% MgO, 0.40–1.35% TiO2, 0.045%–0.055% S, 0.165–0.150% V2O5, and 0.045%–0.055% MnO, with the balance being unavoidable impurities. The bulk density is 1.90–2.10 t / m³. 3 ;

[0245] The vanadium-titanium ore pellets, by mass percentage, comprise 53.5–57.5% TFe, 4.5–5.5% SiO2, 0.55–1.35% CaO, 2.20–2.90% Al2O3, 2.35–2.90% MgO, 6.40–11.0% TiO2, 0.55–0.75% V2O5, and 0.23%–0.25% MnO, with the balance being unavoidable impurities; the bulk density is 2.20–2.30 t / m³. 3 ;

[0246] The high-silica pellets contain, by mass percentage: 58.5–60.0% TFe, 6.5–7.5% SiO2, 0.5–1.5% CaO, 1.80–2.10% Al2O3, 1.0–1.5% MgO, 2.50–3.50% TiO2, 0.165–0.150% V2O5, and 0.045%–0.055% MnO, with the balance being unavoidable impurities. The bulk density is 2.15–2.35 t / m³. 3 ;

[0247] The low-silica lump ore composition, by mass percentage, includes 64.0–66.0% TFe, 3.0–4.5% SiO2, 0.03–0.05% CaO, 1.00–1.50% Al2O3, 0.01–1.0% MgO, TiO2 <1.0%, 0.030–0.050% V2O5, and 0.110%–0.160% MnO, with the balance being unavoidable impurities. The bulk density is 2.2–2.4 t / m³. 3 .

[0248] The coke composition, by mass percentage, includes 84.0–86.5% C and 13.5–14.5% ash, with a bulk density of 0.55–0.65 t / m³. 3 ;

[0249] The coke ash composition by mass percentage includes 53.0–56.0% SiO2, 2.20–3.0% CaO, 24.0–26.0% Al2O3, 0.15–1.0% MgO, TiO2 <2.0%, 0.35%–0.45% MnO, with the balance being unavoidable impurities.

[0250] The pulverized coal composition includes, by mass percentage, 76.0-78.0% C, 13.5-15.0% ash, and 12.5-13.5% volatile matter, with a particle size of -200 mesh accounting for 66-70%.

[0251] The ash composition of the pulverized coal, by mass percentage, includes 55.0–57.0% SiO2, 5.20–6.50% CaO, 23.0–25.0% Al2O3, 2.20–2.50% MgO, TiO2 <2.0%, and 0.35%–0.45% MnO, with the balance being unavoidable impurities.

[0252] The comprehensive air supply parameters include: surface air volume, humidity, air pressure, top pressure, air temperature, and tuyer area; indirect smelting parameters include corrected air volume and the oxygen enrichment rate, theoretical combustion temperature, permeability index, and blast energy after correcting the air volume; fuel parameters include the batch weight, composition, and combustion rate of coke and coke briquettes before the tuyer, as well as the hourly coal powder quantity, coal powder composition, and combustion rate before the tuyer.

[0253] It also includes step E, actual smelting result return correction: based on the actual smelting results obtained in step E, based on the hourly theoretical and actual material rate, theoretical calculation control and actual w([Si]) value, theoretical slag and iron composition and actual slag and iron composition, theoretical and actual furnace output, theoretical and actual fuel ratio, according to the calculation methods in steps B to D, the calculation parameters are corrected and smelting continues.

[0254] Example 3

[0255] A smelting method for quantitatively and systematically controlling the blast furnace charge rate includes the following steps:

[0256] A. Standard ingredients: The smelting process is ordinary ore smelting or medium titanium slag smelting.

[0257] When smelting ordinary ore, the ordinary ore furnace charge used includes the following components by mass percentage: 71% sinter, 20% high-silica pellets, and 9% low-silica lump ore; total 100%; ore batch 54,000 kg;

[0258] When smelting medium-titanium slag, the vanadium-titanium ore charge used includes the following components by mass percentage: 60% sinter, 35% vanadium-titanium pellets, and 0% low-silicon lump ore, totaling 100%; ore batches are 33,000 kg / batch.

[0259] In the smelting of ordinary ore or medium titanium slag, the coke batch is 10,000 kg / batch based on dry coke weight; the coke slag batch is 600 kg / batch based on dry coke weight; the pulverized coal injection rate is 21.5–48.5 t / h.

[0260] B. Ingredient calculation, parameter and index verification analysis:

[0261] B1. Benchmark ingredient calculation, parameter and index verification analysis:

[0262] The wind pressure, air volume, wind temperature, and w([Si]) of the entire air supply remain unchanged, among which the wind temperature is the highest stable wind temperature; if the fluctuation range of factors in ordinary ore smelting or medium titanium slag smelting all meet the following conditions: clinker rate < ±1.0%, comprehensive furnace grade < ±0.20%, coke ash content < ±0.1%, and pulverized coal ash content < ±0.10%; then:

[0263] (1) Calculate the theoretical fuel ratio, utilization coefficient and smelting cycle;

[0264] (2) Calculate the theoretical composition of pig iron, theoretical composition of slag, basicity, and magnesium-aluminum ratio;

[0265] (3) Calculate the conversion factor between the corrected air volume and the surface air volume. The oxygen enrichment rate after correcting the air volume is 2.90 to 5.00%.

[0266] B2. Verification and analysis of ingredient calculations, parameters, and indicators when key verification conditions change:

[0267] The wind pressure, air volume, wind temperature, and w([Si]) of the entire air supply remain unchanged, among which the wind temperature is the highest stable wind temperature; if any one of the factors in the ordinary ore smelting or medium titanium slag smelting does not meet the following conditions: clinker rate < ±1.0%, overall furnace grade < ±0.20%, coke ash content < ±0.1%, pulverized coal ash content < ±0.10%; then:

[0268] (1) Calculate the hourly coal quantity, theoretical iron content of the batch, theoretical coal ratio, coke ratio, coke-butane ratio, coke batch, theoretical fuel ratio, utilization coefficient, smelting cycle and pulverized coal injection rate after the factors change;

[0269] (2) Calculate the theoretical composition of pig iron, theoretical composition of slag, basicity, and magnesium-aluminum ratio;

[0270] C. Input the oxygen enrichment adjustment amount to precisely control the actual material flow rate:

[0271] During blast furnace smelting, the difference between the actual material rate and the specified benchmark material rate is checked. The principle for checking whether to adjust the material rate is as follows:

[0272] (1) The absolute value of the difference between the actual material rate and the specified benchmark material rate for two consecutive hours is ≥0.5 batches / h;

[0273] (2) The difference between the actual material rate and the specified benchmark material rate in a single hour is ≥1.0 batches / h;

[0274] (3) The absolute value of the difference between the specified material rate and the actual material rate for two consecutive hours is ≥1.0 batch; (that is, the difference between the sum of the material rates for two consecutive hours exceeding (or failing to reach) the sum of the specified material rate for two hours is ≥1.0 batch);

[0275] If any one of the above three conditions is met, adjustment is required; otherwise, no adjustment is required.

[0276] The adjustment method is as follows:

[0277] (1) Collect comprehensive air supply parameters, indirect smelting parameters and fuel parameters;

[0278] (2) Based on the original oxygen enrichment, input the oxygen enrichment adjustment amount to adjust the oxygen and obtain the new oxygen enrichment; then, through the collected comprehensive air supply parameters, indirect smelting parameters and fuel parameters, calculate the oxygen enrichment rate and theoretical material rate after adjusting the oxygen correction air volume, and then judge the oxygen adjustment effect.

[0279] The judgment criteria are:

[0280] 1) The difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is defined as 0.1 to 0.3 batches.

[0281] 2) |Theoretical feed rate after oxygen adjustment - Specified feed rate| < 0.3 batches / h, and predict the batch growth rate for the shift (defined between 0.3 and 1.0 batches; the batch growth rate for the shift refers to the difference between the hourly theoretical feed rate and the actual feed rate multiplied by 8 hours);

[0282] 3) The input oxygen enrichment adjustment amount makes the theoretical material rate reach the material rate control value requirement, and the absolute value of the deviation rate between the theoretical output obtained after oxygen adjustment and the planned output requirement is <±1.50%.

[0283] If conditions 1) to 3) are met simultaneously, and the difference between the actual material rate after oxygen adjustment and the specified benchmark material rate is checked, and the result is that no adjustment is needed, then the material rate effect needs to be checked; at the same time, the theoretical combustion temperature, blast energy, permeability index and smelting cycle after oxygen adjustment are calculated.

[0284] The specific method for verifying the material flow rate effect is as follows:

[0285] The verification standard for Japanese batches is defined as follows: the absolute value error rate of the difference between any two of the three factors—actual daily material rate, specified daily material rate, and theoretical daily material rate—is <1.50%; if all three are met, the process continues.

[0286] The theoretical daily coal ratio and coke ratio are compared with the actual daily coal ratio and coke ratio. The theoretical output calculated based on the theoretical feed rate is compared with the actual daily output. If the deviation rate of the difference between the theoretical daily output and the actual daily output is <1.50%, the verification is passed and the process continues.

[0287] D. Furnace smelting and parameter control:

[0288] During the smelting process, the number of times the oxygen enrichment is adjusted in each shift should be ≤3 times, and the ratio of |Daily theoretical batch - Daily specified batch| / Daily specified batch should be <1.50%.

[0289] Smelting conditions: hot blast pressure 0.30~0.39MPa, top pressure 0.155~0.195MPa, hot blast temperature 1150℃~1250℃, and corrected furnace feed air volume 3200~5700m³. 3 / min, oxygen enrichment of 9400~15000m 3 / h, pulverized coal injection rate is 135-165 kg / t iron, pulverized coal injection rate is 22.0-35.0%; ore batch is 33.0-55.0 tons, coke batch is 7.2-11.0 tons on a dry basis; coke batch is 0.45-0.70 tons on a dry basis; w([Si]) is 0.055-0.35%, slag basicity is 1.10-1.18, and molten iron temperature is 1420-1480℃; during the smelting process, the slag ratio is 380-480 kg / t, the magnesium-aluminum ratio in the slag is 0.65-0.95, the slag basicity is 1.10-1.18, the blast temperature is controlled to be stable, the oxygen enrichment rate is 2.90%-5.0%, and the permeability index is 18000-22000 m 3 / (min.MPa), theoretical combustion temperature 2300~2400℃, actual blowing speed 255~275m / s, actual blowing kinetic energy 17000~22000kg.m / S, theoretical hourly material rate 8.5~10.0 batches.

[0290] The sintered ore composition, by mass percentage, includes 52.0–54.0% TFe, 5.5–6.5% SiO2, 13.0–13.5% CaO, 1.75–2.19% Al2O3, 2.30–2.90% MgO, 0.40–1.35% TiO2, 0.045%–0.055% S, 0.165–0.150% V2O5, and 0.045%–0.055% MnO, with the balance being unavoidable impurities. The bulk density is 1.90–2.10 t / m³. 3 ;

[0291] The vanadium-titanium ore pellets, by mass percentage, comprise 53.5–57.5% TFe, 4.5–5.5% SiO2, 0.55–1.35% CaO, 2.20–2.90% Al2O3, 2.35–2.90% MgO, 6.40–11.0% TiO2, 0.55–0.75% V2O5, and 0.23%–0.25% MnO, with the balance being unavoidable impurities; the bulk density is 2.20–2.30 t / m³. 3 ;

[0292] The high-silica pellets contain, by mass percentage: 58.5–60.0% TFe, 6.5–7.5% SiO2, 0.5–1.5% CaO, 1.80–2.10% Al2O3, 1.0–1.5% MgO, 2.50–3.50% TiO2, 0.165–0.150% V2O5, and 0.045%–0.055% MnO, with the balance being unavoidable impurities. The bulk density is 2.15–2.35 t / m³. 3 ;

[0293] The low-silica lump ore composition, by mass percentage, includes 64.0–66.0% TFe, 3.0–4.5% SiO2, 0.03–0.05% CaO, 1.00–1.50% Al2O3, 0.01–1.0% MgO, TiO2 <1.0%, 0.030–0.050% V2O5, and 0.110%–0.160% MnO, with the balance being unavoidable impurities. The bulk density is 2.2–2.4 t / m³. 3 .

[0294] The coke composition, by mass percentage, includes 84.0–86.5% C and 13.5–14.5% ash, with a bulk density of 0.55–0.65 t / m³. 3 ;

[0295] The coke ash composition by mass percentage includes 53.0–56.0% SiO2, 2.20–3.0% CaO, 24.0–26.0% Al2O3, 0.15–1.0% MgO, TiO2 <2.0%, 0.35%–0.45% MnO, with the balance being unavoidable impurities.

[0296] The pulverized coal composition includes, by mass percentage, 76.0-78.0% C, 13.5-15.0% ash, and 12.5-13.5% volatile matter, with a particle size of -200 mesh accounting for 66-70%.

[0297] The ash composition of the pulverized coal, by mass percentage, includes 55.0–57.0% SiO2, 5.20–6.50% CaO, 23.0–25.0% Al2O3, 2.20–2.50% MgO, TiO2 <2.0%, and 0.35%–0.45% MnO, with the balance being unavoidable impurities.

[0298] The comprehensive air supply parameters include: surface air volume, humidity, air pressure, top pressure, air temperature, and tuyer area; indirect smelting parameters include corrected air volume and the oxygen enrichment rate, theoretical combustion temperature, permeability index, and blast energy after correcting the air volume; fuel parameters include the batch weight, composition, and combustion rate of coke and coke briquettes before the tuyer, as well as the hourly coal powder quantity, coal powder composition, and combustion rate before the tuyer.

[0299] It also includes step E, actual smelting result return correction: based on the actual smelting results obtained in step E, based on the hourly theoretical and actual material rate, theoretical calculation control and actual w([Si]) value, theoretical slag and iron composition and actual slag and iron composition, theoretical and actual furnace output, theoretical and actual fuel ratio, according to the calculation methods in steps B to D, the calculation parameters are corrected and smelting continues.

[0300] Example 4

[0301] A smelting method for quantitatively and systematically controlling the blast furnace charge rate includes the following steps:

[0302] A. Standard ingredients: The smelting process is ordinary ore smelting or medium titanium slag smelting.

[0303] When smelting ordinary ore, the ordinary ore furnace charge used includes the following components by mass percentage: 71% sinter, 20% high-silica pellets, and 9% low-silica lump ore; total 100%; ore batch 54,000 kg;

[0304] When smelting medium-titanium slag, the vanadium-titanium ore charge used includes the following components by mass percentage: 65% sintered ore, 30% vanadium-titanium pellets, and 5% low-silicon lump ore, totaling 100%; ore batches are 33,000 kg / batch.

[0305] In the smelting of ordinary ore or medium titanium slag, the coke batch is 10,000 kg / batch based on dry coke weight; the coke slag batch is 600 kg / batch based on dry coke weight; the pulverized coal injection rate is 21.5–48.5 t / h.

[0306] B. Ingredient calculation, parameter and index verification analysis:

[0307] B1. Benchmark ingredient calculation, parameter and index verification analysis:

[0308] The wind pressure, air volume, wind temperature, and w([Si]) of the entire air supply remain unchanged, among which the wind temperature is the highest stable wind temperature; if the fluctuation range of factors in ordinary ore smelting or medium titanium slag smelting all meet the following conditions: clinker rate < ±1.0%, comprehensive furnace grade < ±0.20%, coke ash content < ±0.1%, and pulverized coal ash content < ±0.10%; then:

[0309] (1) Calculate the theoretical fuel ratio, utilization coefficient and smelting cycle;

[0310] (2) Calculate the theoretical composition of pig iron, theoretical composition of slag, basicity, and magnesium-aluminum ratio;

[0311] (3) Calculate the conversion factor between the corrected air volume and the surface air volume. The oxygen enrichment rate after correcting the air volume is 2.90 to 5.00%.

[0312] B2. Verification and analysis of ingredient calculations, parameters, and indicators when key verification conditions change:

[0313] The wind pressure, air volume, wind temperature, and w([Si]) of the entire air supply remain unchanged, among which the wind temperature is the highest stable wind temperature; if any one of the factors in the ordinary ore smelting or medium titanium slag smelting does not meet the following conditions: clinker rate < ±1.0%, overall furnace grade < ±0.20%, coke ash content < ±0.1%, pulverized coal ash content < ±0.10%; then:

[0314] (1) Calculate the hourly coal quantity, theoretical iron content of the batch, theoretical coal ratio, coke ratio, coke-butane ratio, coke batch, theoretical fuel ratio, utilization coefficient, smelting cycle and pulverized coal injection rate after the factors change;

[0315] (2) Calculate the theoretical composition of pig iron, theoretical composition of slag, basicity, and magnesium-aluminum ratio;

[0316] C. Input the oxygen enrichment adjustment amount to precisely control the actual material flow rate:

[0317] During blast furnace smelting, the difference between the actual material rate and the specified benchmark material rate is checked. The principle for checking whether to adjust the material rate is as follows:

[0318] (1) The absolute value of the difference between the actual material rate and the specified benchmark material rate for two consecutive hours is ≥0.5 batches / h;

[0319] (2) The difference between the actual material rate and the specified benchmark material rate in a single hour is ≥1.0 batches / h;

[0320] (3) The absolute value of the difference between the specified material rate and the actual material rate for two consecutive hours is ≥1.0 batch; (that is, the difference between the sum of the material rates for two consecutive hours exceeding (or failing to reach) the sum of the specified material rate for two hours is ≥1.0 batch);

[0321] If any one of the above three conditions is met, adjustment is required; otherwise, no adjustment is required.

[0322] The adjustment method is as follows:

[0323] (1) Collect comprehensive air supply parameters, indirect smelting parameters and fuel parameters;

[0324] (2) Based on the original oxygen enrichment, input the oxygen enrichment adjustment amount to adjust the oxygen and obtain the new oxygen enrichment; then, through the collected comprehensive air supply parameters, indirect smelting parameters and fuel parameters, calculate the oxygen enrichment rate and theoretical material rate after adjusting the oxygen correction air volume, and then judge the oxygen adjustment effect.

[0325] The judgment criteria are:

[0326] 1) The difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is defined as 0.1 to 0.3 batches.

[0327] 2) |Theoretical feed rate after oxygen adjustment - Specified feed rate| < 0.3 batches / h, and predict the batch growth rate for the shift (defined between 0.3 and 1.0 batches; the batch growth rate for the shift refers to the difference between the hourly theoretical feed rate and the actual feed rate multiplied by 8 hours);

[0328] 3) The input oxygen enrichment adjustment amount makes the theoretical material rate reach the material rate control value requirement, and the absolute value of the deviation rate between the theoretical output obtained after oxygen adjustment and the planned output requirement is <±1.50%.

[0329] If conditions 1) to 3) are met simultaneously, and the difference between the actual material rate after oxygen adjustment and the specified benchmark material rate is checked, and the result is that no adjustment is needed, then the material rate effect needs to be checked; at the same time, the theoretical combustion temperature, blast energy, permeability index and smelting cycle after oxygen adjustment are calculated.

[0330] The specific method for verifying the material flow rate effect is as follows:

[0331] The verification standard for Japanese batches is defined as follows: the absolute value error rate of the difference between any two of the three factors—actual daily material rate, specified daily material rate, and theoretical daily material rate—is <1.50%; if all three are met, the process continues.

[0332] The theoretical daily coal ratio and coke ratio are compared with the actual daily coal ratio and coke ratio. The theoretical output calculated based on the theoretical feed rate is compared with the actual daily output. If the deviation rate of the difference between the theoretical daily output and the actual daily output is <1.50%, the verification is passed and the process continues.

[0333] D. Furnace smelting and parameter control:

[0334] During the smelting process, the number of times the oxygen enrichment is adjusted in each shift should be ≤3 times, and the ratio of |Daily theoretical batch - Daily specified batch| / Daily specified batch should be <1.50%.

[0335] Smelting conditions: hot blast pressure 0.30~0.39MPa, top pressure 0.155~0.195MPa, hot blast temperature 1150℃~1250℃, and corrected furnace feed air volume 3200~5700m³. 3 / min, oxygen enrichment of 9400~15000m 3 / h, pulverized coal injection rate is 135-165 kg / t iron, pulverized coal injection rate is 22.0-35.0%; ore batch is 33.0-55.0 tons, coke batch is 7.2-11.0 tons on a dry basis; coke batch is 0.45-0.70 tons on a dry basis; w([Si]) is 0.055-0.35%, slag basicity is 1.10-1.18, and molten iron temperature is 1420-1480℃; during the smelting process, the slag ratio is 380-480 kg / t, the magnesium-aluminum ratio in the slag is 0.65-0.95, the slag basicity is 1.10-1.18, the blast temperature is controlled to be stable, the oxygen enrichment rate is 2.90%-5.0%, and the permeability index is 18000-22000 m 3 / (min.MPa), theoretical combustion temperature 2300~2400℃, actual blowing speed 255~275m / s, actual blowing kinetic energy 17000~22000kg.m / S, theoretical hourly material rate 8.5~10.0 batches.

[0336] The sintered ore composition, by mass percentage, includes 52.0–54.0% TFe, 5.5–6.5% SiO2, 13.0–13.5% CaO, 1.75–2.19% Al2O3, 2.30–2.90% MgO, 0.40–1.35% TiO2, 0.045%–0.055% S, 0.165–0.150% V2O5, and 0.045%–0.055% MnO, with the balance being unavoidable impurities. The bulk density is 1.90–2.10 t / m³. 3 ;

[0337] The vanadium-titanium ore pellets, by mass percentage, comprise 53.5–57.5% TFe, 4.5–5.5% SiO2, 0.55–1.35% CaO, 2.20–2.90% Al2O3, 2.35–2.90% MgO, 6.40–11.0% TiO2, 0.55–0.75% V2O5, and 0.23%–0.25% MnO, with the balance being unavoidable impurities; the bulk density is 2.20–2.30 t / m³. 3 ;

[0338] The high-silica pellets contain, by mass percentage: 58.5–60.0% TFe, 6.5–7.5% SiO2, 0.5–1.5% CaO, 1.80–2.10% Al2O3, 1.0–1.5% MgO, 2.50–3.50% TiO2, 0.165–0.150% V2O5, and 0.045%–0.055% MnO, with the balance being unavoidable impurities. The bulk density is 2.15–2.35 t / m³. 3 ;

[0339] The low-silica lump ore composition, by mass percentage, includes 64.0–66.0% TFe, 3.0–4.5% SiO2, 0.03–0.05% CaO, 1.00–1.50% Al2O3, 0.01–1.0% MgO, TiO2 <1.0%, 0.030–0.050% V2O5, and 0.110%–0.160% MnO, with the balance being unavoidable impurities. The bulk density is 2.2–2.4 t / m³. 3 .

[0340] The coke composition, by mass percentage, includes 84.0–86.5% C and 13.5–14.5% ash, with a bulk density of 0.55–0.65 t / m³. 3 ;

[0341] The coke ash composition by mass percentage includes 53.0–56.0% SiO2, 2.20–3.0% CaO, 24.0–26.0% Al2O3, 0.15–1.0% MgO, TiO2 <2.0%, 0.35%–0.45% MnO, with the balance being unavoidable impurities.

[0342] The pulverized coal composition includes, by mass percentage, 76.0-78.0% C, 13.5-15.0% ash, and 12.5-13.5% volatile matter, with a particle size of -200 mesh accounting for 66-70%.

[0343] The ash composition of the pulverized coal, by mass percentage, includes 55.0–57.0% SiO2, 5.20–6.50% CaO, 23.0–25.0% Al2O3, 2.20–2.50% MgO, TiO2 <2.0%, and 0.35%–0.45% MnO, with the balance being unavoidable impurities.

[0344] The comprehensive air supply parameters include: surface air volume, humidity, air pressure, top pressure, air temperature, and tuyer area; indirect smelting parameters include corrected air volume and the oxygen enrichment rate, theoretical combustion temperature, permeability index, and blast energy after correcting the air volume; fuel parameters include the batch weight, composition, and combustion rate of coke and coke briquettes before the tuyer, as well as the hourly coal powder quantity, coal powder composition, and combustion rate before the tuyer.

[0345] It also includes step E, actual smelting result return correction: based on the actual smelting results obtained in step E, based on the hourly theoretical and actual material rate, theoretical calculation control and actual w([Si]) value, theoretical slag and iron composition and actual slag and iron composition, theoretical and actual furnace output, theoretical and actual fuel ratio, according to the calculation methods in steps B to D, the calculation parameters are corrected and smelting continues.

[0346] Application Example 1

[0347] A. Intensive smelting of titanium slag in blast furnace vanadium-titanium ore, using a vanadium-titanium ore charge structure, including sintered ore, high-titanium pellets, and low-silicon lump ore. A baseline batching is performed as follows:

[0348] The chemical composition of the sinter is: TFe 52.096%, SiO 26.14%, CaO 13.14%, Al 2O 32.19%, MgO 2.85%, TiO 21.337%, S 0.045%, V 2O 50.142%, MnO 0.241%, with a bulk density of 1.97 t / m³. 3 The composition of the vanadium-titanium pellets (1) is: TFe 57.32%, SiO2 4.53%, CaO 0.56%, Al2O3 2.89%, MgO 2.36%, TiO2 6.46%, V2O5 0.737%, MnO 0.23%; bulk density 2.28 t / m³ 3 The composition of the vanadium-titanium pellets (2) is as follows: TF: 53.58%, SiO2: 5.14%, CaO: 1.23%, Al2O3: 2.52%, MgO: 2.71%, TiO2: 10.14%, V2O5: 0.546%, MnO: 0.270%, with a bulk density of 2.16 t / m³. 3 The composition of the low-silica lump ore is: TFe 65.34%, SiO2 3.83%, CaO 0.030%, Al2O3 1.08%, MgO 0.010%, TiO2 0.010%, V2O5 0.030%, MnO 0.199%, with a bulk density of 2.30 t / m³. 3 .

[0349] The chemical composition of the coke is: C 85.63%, ash content 13.6%, and bulk density 0.65 t / m³. 3The complete analysis of coke ash composition is as follows: SiO2 54.352%, CaO 2.636%, Al2O3 24.897%, MgO 0.463%, TiO2 1.55%, MnO 0.39%; the chemical composition of pulverized coal is as follows: C 77.58%, ash 10.51%, volatile matter 13.31%, fineness (-200 mesh) 67%; the complete analysis of pulverized coal ash composition is as follows: SiO2 47.245%, CaO 5.475%, Al2O3 23.85%, MgO 2.38%, TiO2 1.284%, MnO 0.370%.

[0350] Baseline conditions and material verification results:

[0351] Ore batch: 33,000 kg, coke batch (wet weight): 7,600 kg (dry weight): 7,296 kg, coke briquettes (wet weight): 500 kg (dry weight): 480 kg. Batching basis: Baseline: w([Si]) value: 0.160%; slag basicity: 1.14. Baseline material rate: 8.96 batches / h; Baseline coal quantity: 21,615 kg / h.

[0352] Ingredient verification results:

[0353] Sintered ore 60% (20%+20%+20%) + sintered small particles 2%, vanadium-titanium pellets (1) 15.0%, vanadium-titanium pellets (2) 19.0%, low-silicon lump ore 4.0%. Total furnace feed grade TFe: 53.69%.

[0354] B. Ingredient calculation, parameter and index verification analysis:

[0355] B1. Benchmark ingredient calculation, parameter and index verification analysis:

[0356] For conventional blast furnace ore and coke batches, the chemical composition (full analysis) of various materials is as described in step A. Under the main reference parameters of the baseline raw materials (clinker rate, overall charge grade, coke and pulverized coal ash content), combined with the baseline operating parameters of step A (baseline coal quantity, baseline material rate, baseline w([Si])), the baseline operating parameters such as total air (air pressure, air volume), air temperature, and w([Si]) are not adjusted.

[0357] Under the baseline conditions in step A (assuming that the main raw material parameters are stable (the fluctuation ranges all meet the following conditions: clinker rate < ±1.0%, overall furnace feed grade < ±0.20%, coke < ±0.1%, and pulverized coal ash content < ±0.10%)), proceed directly to the baseline index determination step, following the steps below. The calculation order and results are as follows:

[0358] (1) Calculate the theoretical fuel ratio, utilization coefficient, smelting cycle, etc. under the basic conditions.

[0359] The calculated theoretical fuel ratio is 549.8 kg / t (dry basis); the utilization factor is 3.696 t / (m³). 3 .d); The smelting cycle is 42.4 batches, as shown in Table 1 and Table 2.

[0360] Table 1

[0361]

[0362] Table 2

[0363] project Batch volume cycle Wet fuel ratio Moisture Dry fuel ratio Theoretical utilization coefficient Coal injection rate Clinker ratio Grade of furnace ash content coal ash unit <![CDATA[m 3 / pi]]> pi Kg / t ％ Kg / t <![CDATA[t / (m 3 .d)]]> ％ ％ ％ ％ ％ numerical values 24.3 42.4 567.3 4.00％ 549.80 3.696 24.38 96.00 53.69132 13.6 10.51

[0364] (2) Output the slag and iron composition and related intermediate process results according to the baseline conditions (assuming that the changes in raw materials and fuels are all within the required range).

[0365] Taking each batch of material as a unit, the following are the fitting formulas for the reduction rates of elements such as [Si], [Ti], [Mn], and [V] in molten iron under the predetermined w([Si]) value: (w([Si])-Si reduction rate, w([Si])-Ti reduction rate, w([Si])-Mn reduction rate, w([Si])-V reduction rate), w([Si])-desulfurization rate fitting formula, and [S] removal rate fitting polynomial formula with predetermined w([Si]) value: Figures 3-7 ):

[0366] Based on the reduction rates of the above elements (desulfurization rate, and 100% reduction rates of [P] and [As], etc.), combined with material balance, the amounts of corresponding element oxides and S, P, and As entering the molten iron are calculated. Further calculations are made of the amounts of each element oxide and S, P, and As entering the slag, the output slag quantity (slag ratio), alkali metals, lead, zinc, titanium, sulfur load, etc., as well as the theoretical slag composition (including basicity, magnesium-aluminum ratio, etc.) and theoretical pig iron composition (theoretically calculated from the corresponding element oxides entering the molten iron) (Tables 3 to 6).

[0367] Table 3 shows the reduction rate corresponding to the baseline w([Si]) based on the fitting formula between the w([Si]) value and the reduction rate of each element.

[0368]

[0369] Note: The baseline w([Si]) is the input, and the others are automatically calculated outputs.

[0370] Table 4 Output baseline mix ratio, slag quantity (slag ratio), alkali metals, lead-zinc and titanium, sulfur load under baseline w([Si])

[0371]

[0372]

[0373] Table 5 Theoretical pig iron composition under output baseline w([Si])

[0374] project Si S P Ti As V Mn unit ％ ％ ％ ％ ％ ％ ％ numerical values 0.16 0.056 0.072 0.205 0.018 0.19 0.227

[0375] Table 6 Theoretical slag composition under output baseline w([Si])

[0376] project <![CDATA[SiO2]]> CaO MgO S <![CDATA[Al2O3]]> <![CDATA[TiO2]]> <![CDATA[V2O5]]> MnO magnesium-aluminum ratio alkalinity unit ％ ％ ％ ％ ％ ％ ％ ％ numerical values 28.73 32.63 10.66 0.72 12.51 13.65 0.43 0.64 0.852 1.14

[0377] In this example, the corrected air volume calculation is based on the air volume corrected for actual fuel consumption (the cumulative average value of the samples is 3289.0 m³). 3 / min) and the corresponding metered air volume (the cumulative average value of the samples is 2669.42m). 3 The multiple of ( / min) is relatively stable, with a value between 1.22 and 1.24 times. Here, the conversion factor of the multiple of the corrected air volume and the surface air volume is used = 3289.0 / 2669.42 = 1.23 times.

[0378] When the main reference parameters of the benchmark raw materials (clinker rate, overall furnace grade, coke ash content, and pulverized coal ash content) change beyond the stable range, the process proceeds to step B2.

[0379] B2. Analysis of batching calculations, parameters, and index verification when key verification conditions (clinker rate, overall furnace grade, coke and pulverized coal ash content) change:

[0380] Changes in the composition of the raw materials were detected. Specifically:

[0381] The chemical composition of the sinter is: TFe 52.26%, SiO 26.07%, CaO 12.76%, Al 2O 32.19%, MgO 2.89%, TiO 21.283%, S 0.043%, V 2O 50.14%, MnO 0.24%, with a bulk density of 1.99 t / m³. 3 The composition of the vanadium-titanium pellets (1) is: TFe 57.32%, SiO2 4.53%, CaO 0.56%, Al2O3 2.89%, MgO 2.36%, TiO2 6.46%, V2O5 0.737%, MnO 0.23%; bulk density 2.28 t / m³ 3 The composition of the vanadium-titanium pellets (2) is as follows: TF: 53.58%, SiO2: 5.14%, CaO: 1.23%, Al2O3: 2.52%, MgO: 2.71%, TiO2: 10.14%, V2O5: 0.546%, MnO: 0.270%, with a bulk density of 2.16 t / m³. 3The composition of the low-silica lump ore is: TFe 65.34%, SiO2 3.83%, CaO 0.030%, Al2O3 1.08%, MgO 0.010%, TiO2 0.010%, V2O5 0.030%, MnO 0.199%, with a bulk density of 2.30 t / m³. 3 .

[0382] The chemical composition of the coke is: C 85.54%, ash content 13.63%, and bulk density 0.65 t / m³. 3 The complete analysis of coke ash composition is as follows: SiO2 54.836%, CaO 2.936%, Al2O3 24.538%, MgO 0.753%, TiO2 1.55%, MnO 0.39%; the chemical composition of pulverized coal is as follows: C 77.98%, ash 10.56%, volatile matter 13.35%, fineness (-200 mesh) 66%; the complete analysis of pulverized coal ash composition is as follows: SiO2 47.245%, CaO 5.475%, Al2O3 23.85%, MgO 2.38%, TiO2 1.284%, MnO 0.370%.

[0383] In this example, the grade of sintered ore and the ash content of coke and pulverized coal vary. The initial batching and verification are performed according to step A. The verification data is as follows: Ore batch: 33000 kg, Coke batch (wet weight): 7600 kg (dry basis weight): 7296 kg, Coke slag batch (wet weight): 500 kg (dry basis weight): 480 kg (Note: The coke batch needs adjustment based on the raw material composition and the grade and clinker ratio after the initial batching). Batching baseline: w([Si]) value: 0.160%; slag basicity: 1.14. Baseline material rate: 8.96 batches / h, base coal quantity: 21615 kg / h (Note: Adjustments need to be made based on changes in pulverized coal ash content). After adjusting the coke batch and hourly coal quantity, the batching results will be verified and adjusted again (based on the target slag basicity).

[0384] Ingredient verification results:

[0385] Sintered ore 60% (21%+21%+21%) + sintered small particles 2%, vanadium-titanium pellets (1) 15.0%, vanadium-titanium pellets (2) 19.0%, low-silicon lump ore 1.0%. Total furnace feed grade TFe: 53.40%.

[0386] In this example, the main parameters of the raw materials and fuels exceeded the stable range (clinker rate increased by 3.0% > ±1.0%, overall feed grade decreased by 0.29% > ±0.20%, coke ash content increased by 0.03%, and pulverized coal ash content increased by 0.05%). The baseline operating parameters were adjusted according to the magnitude of the changes (including the determination of the baseline hourly coal quantity and coke batch after the change in raw materials and fuels).

[0387] The following steps are calculated in sequence: determination of hourly coal quantity after factor changes, theoretical iron content of batch, calculation of theoretical coal ratio, new coke ratio and coke-to-coke ratio, determination of new coke batch, theoretical fuel ratio of batch under changing conditions, utilization coefficient, smelting cycle, pulverized coal injection rate, etc. (see Tables 7-8 for details).

[0388] The concepts and formulas involved in the calculation process are as follows:

[0389] Hourly coal quantity after factor changes: l2 = l1 - (m h1 -m h2 )*0.015*l1

[0390] l2 represents the hourly coal quantity after the factor change, in kg / t; l1 represents the hourly coal quantity before the factor change, in kg / t; m h1 The ash content of pulverized coal before changes in factors is expressed in kg / t; m h2 The ash content of pulverized coal after changes in factors is expressed in kg / t.

[0391] The J / T ratio after factor changes is d2 = (ΣTFe1 - ΣTFe2) * 0.02 * d1 - (S1 - S2) / 5 * 1 * d1 / 100 - (w([Si])1 - w([Si])2) * 0.01 * d1 - (J / T) h1 -J h2 )*0.015*d1+d1

[0392] d2 is the theoretical coke-to-butadiene ratio after factor changes, kg / t; d1 is the coke-to-butadiene ratio before factor changes, kg / t; ΣTFe1 is the overall feed grade before factor changes, kg / t; ΣTFe2 is the overall feed grade after factor changes, %; S1 is the clinker yield before factor changes, %; S2 is the clinker yield after factor changes, %; J h1 The coke ash content before changes in factors, %; J h2 The percentage of coke ash after changes in factors.

[0393] The focal ratio k2 after factor changes is: k2 = (ΣTFe1 - ΣTFe2) * 0.02 * k1 - (S1 - S2) / 5 * 1 * d1 / 100 - (w([Si])1 - w([Si])2) * 0.01 * d1 - (J1 - J2) * 0.015 * k1 + k1

[0394] k2 is the theoretical coke ratio after the factor change, kg / t; k1 is the coke ratio before the factor change, kg / t; ΣTFe1 is the overall grade of the furnace feed before the factor change, kg / t; ΣTFe2 is the overall grade of the furnace feed after the factor change, %; S1 is the clinker yield before the factor change, %; S2 is the clinker yield after the factor change, %; J1 is the coke ash content before the factor change, %; J2 is the coke ash content after the factor change, %.

[0395] After the factors change, the burnt batch C2 = (k2 + d2) * t 理 / 1000-J d

[0396] C2 represents the newly determined coke batch size after the change in factors, in kg / t; J d The weight of dry coke (unchanged) is kg / t.

[0397] The formulas for calculating the theoretical fuel ratio, utilization coefficient, smelting cycle, and pulverized coal injection rate are conventional formulas.

[0398] All calculations are based on a dry basis. The baseline w([Si]) is set unchanged, and adjustments are made to the coke batch and hourly coal quantity (coke yield remains unchanged) based on the original fuel variables.

[0399] (1) Calculate the theoretical fuel ratio, utilization coefficient, smelting cycle, etc. after the change of calculation conditions.

[0400] Following the calculation method and steps of B2, based on the fundamental parameters, the dry coke batch weight after changes in raw material and fuel conditions is obtained as 7369 kg / batch, and the hourly coal consumption is 21632 kg / h. The corresponding theoretical changes are: the calculated theoretical fuel ratio is 555.8 kg / t (dry basis); the utilization coefficient is 3.68 t / (m³). 3 .d); The smelting cycle is 42.1 batches (Tables 7 and 8).

[0401] Table 7 shows the calculation results after changes in raw materials and fuels (compared to baseline conditions) and the verification of their indicators.

[0402]

[0403] Table 8

[0404]

[0405]

[0406] Note: In this example, after adjusting the coke batch and hourly coal quantity, the verification target (alkalinity) has been achieved, and the aforementioned furnace charge structure and proportioning are maintained.

[0407] (2) Slag and iron composition and related intermediate process results after adjusting the furnace charge structure ratio, coke batch, and hourly coal quantity according to changes in raw material and fuel conditions.

[0408] Taking each batch of material as a unit, the reduction rates of elements such as [Si], [Ti], [Mn], and [V] obtained under the predetermined w([Si]) value in the molten iron are obtained by fitting (w([Si])-Si reduction rate, w([Si])-Ti reduction rate, w([Si])-Mn reduction rate, and w([Si])-V reduction rate), the fitting relationship of w([Si])-desulfurization rate, and the fitting polynomial relationship between [S] removal rate and predetermined w([Si]) are mentioned above. Figures 1-5 ).

[0409] In the same step B1, output the slag quantity (slag ratio), alkali metals, zinc and titanium, sulfur load, etc. after the change of raw materials and fuels, as well as the theoretical slag composition (including basicity, magnesium-aluminum ratio, etc.) and theoretical pig iron composition (Tables 9 to 12).

[0410] Table 9 shows the reduction rates corresponding to the baseline w([Si]) based on the fitting formula between the w([Si]) value and the reduction rates of each element.

[0411]

[0412] Note: The baseline w([Si]) is the input, and the others are automatically calculated outputs.

[0413] Table 10 Output variation ratio, slag quantity (slag ratio), alkali metal, zinc and titanium, sulfur load under baseline w([Si])

[0414]

[0415] Table 11 Theoretical pig iron composition under the baseline w([Si]) after changes in output raw materials.

[0416] project Si S P Ti As V Mn unit ％ ％ ％ ％ ％ ％ ％ Baseline conditions 0.16 0.056 0.072 0.205 0.018 0.19 0.227 Raw material changes 0.16 0.057 0.071 0.204 0.032 0.165 0.366

[0417] Table 12 Theoretical slag composition under the baseline w([Si]) after outputting raw material changes.

[0418]

[0419]

[0420] The conversion factor for calculating the corrected air volume to the surface air volume is the same as in step B1 (1.23 times).

[0421] During the smelting process, the reference feed rate often changes, and it is controlled in conjunction with "oxygen-regulated feed" to proceed to step C.

[0422] C. Input the oxygen enrichment adjustment amount to precisely control the actual material flow rate:

[0423] Data collection and calculation output should be performed according to the following steps and methods (the determination and adjustment of whether adjustments are needed should be made according to the definition principles of step C (C1~C2).

[0424] C2. Determining the amount of oxygen enrichment and accurately controlling the actual material flow rate.

[0425] (1) Parameters to be collected (including calculated indirect smelting parameters and fuel parameters). Directly collected comprehensive air supply parameters include: surface air volume, humidity, air pressure, top pressure, air temperature, and tuyer area; indirect smelting parameters (automatically calculated) include the corrected air volume obtained based on the actual air volume correction coefficient (or fitting polynomial) and the oxygen enrichment rate, theoretical combustion temperature, permeability index, and blast kinetic energy after the corrected air volume. Fuel parameters to be collected include: batch weight, composition, and combustion rate before the tuyer; hourly pulverized coal quantity, pulverized coal composition, and combustion rate before the tuyer (Tables 13 and 14). Note: Calculated based on hourly cumulative quantities (hourly cumulative quantities are automatically collected by the computer at certain time intervals).

[0426] (2) Determination of oxygen enrichment adjustment amount and precise control of actual material speed. Input, calculate and output the results of precise control of material speed and intermediate process data of oxygen enrichment according to the steps. The steps for determining the oxygen enrichment adjustment amount (calculation order) are: original oxygen enrichment amount → oxygen enrichment adjustment amount (input) → new oxygen enrichment amount → oxygen enrichment rate after oxygen adjustment and correction of air volume (combined with the comprehensive blower parameters and fuel parameters in step (1)) → (obtained by combining the air volume per ton of coal consumption, air volume per hour of coal consumption, air volume per ton of coke consumption, and residual air volume after coal burning obtained from the parameters in step (1)) theoretical material speed after oxygen adjustment → judgment of oxygen adjustment effect.

[0427] The concepts and formulas involved are:

[0428] Corrected air volume V 校 =((J) 实 *1000*J C实 / 100*Φ C / 100+J d实 *1000*J dC实 / 100*φ JDC )+(M 实 *1000*M C实 / 100*Φ MC ))*0.9333 / (0.21+0.29*f h2O / 8 / 100+0.79*f O2 / 100) / 24 / 60

[0429] V 校 The air volume after correcting the surface air volume value, in m 3 / min; J 实 The daily dry basis consumption of coke used in the current period, in tons (t); J C实 The carbon content (%) of the coke used in the current period; Φ C The combustion rate of coke before the tuyeres, %; Jd实 The daily dry basis consumption of coking coal used in the current period, in tons (t); J dC实 The carbon content (%) of the coking coal used in the current period; φ JDC The combustion rate of coke before the air vent, %; M 实 The daily dry basis consumption of pulverized coal used in the current period, in tons (t); M C实 The carbon content (%) of the pulverized coal used in the current period; φ MC The combustion rate of pulverized coal before the tuyeres, expressed as %; f h2O Atmospheric humidity, g / m 3 ;f O2 Oxygen enrichment rate, expressed as a percentage, calculated based on surface air volume. Note: Coke quantity (daily consumption) is based on actual values ​​from a past period (within two months) under similar raw material conditions.

[0430] Oxygen enrichment rate F after adjusting air volume O2 =0.785*V O2 / 60 / (V 校 +V O2 / 60)*100

[0431] F O2 The oxygen enrichment rate (%) was calculated after correcting the surface air volume value; V O2 The current oxygen enrichment level, m 3 / h. The rest is the same as above.

[0432] Corrected air volume per ton of coal consumption V m =1000*M C实 / 100 / 24*22.4 / (0.21+0.29*f h2O / 100+0.79*F O2 / 100)*φ MC

[0433] V m To correct the air volume, the air consumption per ton of coal is calculated in m. 3 / t; the rest are the same as above;

[0434] Hourly coal consumption and air volume V after adjusting for oxygen enrichment rate mh =V m *m h / 1000

[0435] V mh To correct for the hourly coal consumption air volume after adjusting for oxygen enrichment rate, m 3 / h;m h The amount is the hourly coal quantity, kg / t; the rest is the same as above.

[0436] Air consumption per ton of coke after correction V C =1000*J C实 / 100 / 24*22.4 / (0.21+0.29*f h2O / 100+0.79*F O2 / 100)*φC

[0437] V C To correct the air volume, the air consumption per ton of coke is calculated in m. 3 / t; the rest is the same as above.

[0438] Theoretical feed rate L before oxygen adjustment 前 =(V 校 *60-V mh前 )*f 风 / V C前 / (J 批 +J d批 )*1000

[0439] L 前 The theoretical feed rate, calculated based on the oxygen enrichment level before adjustment, is given in batches per hour (V). mh前 To correct for the hourly coal consumption air volume after adjusting the oxygen enrichment rate (which is calculated using the oxygen enrichment amount before adjustment), m 3 / h;f 风 For the specific blast furnace air utilization rate, %; V C前 To correct the air volume, the air consumption per ton of coke is calculated using the oxygen enrichment rate after adjusting the oxygen enrichment rate, m 3 / t;J 批 The dry weight of each batch of coke is kg / batch; J d批 The dry weight of each batch of charcoal is expressed in kg / batch, %.

[0440] Theoretical feed rate L after oxygen adjustment 后 =(V 校 *60-V mh前后 )*f 风 / V C后 / (J 批 +J d批 )*1000

[0441] L 后 The theoretical feed rate, calculated based on the adjusted oxygen enrichment, is given in batches per hour (V). mh前 To correct for the oxygen enrichment rate (which is calculated using the adjusted oxygen enrichment amount) in terms of hourly coal consumption and air volume, m 3 / h;f 风 For the specific blast furnace air utilization rate, %; V C前 To correct the air volume, the air consumption per ton of coke is calculated using the adjusted oxygen enrichment rate. 3 / t;J 批 The dry weight of each batch of coke is kg / batch; J d批The dry weight of each batch of charcoal is expressed in kg / batch, %.

[0442] Note: The formula for calculating the theoretical feed rate is the same before and after oxygen adjustment; the only difference is the input oxygen enrichment rate.

[0443] Similarly, the theoretical combustion temperature, blast energy, permeability index, and smelting cycle are obtained after correcting the air volume and oxygen enrichment rate (using the corrected air volume into the conventional calculation formula).

[0444] Repeatedly input the oxygen enrichment adjustment amount until the theoretical material rate output value meets the requirements.

[0445] The results and process parameters obtained in this example are shown in Tables 13 and 14 (based on data and operations from two natural classes).

[0446] Table 13 Data Acquisition (Calculation), Process, and Effects of Precise Oxygen Control of Material Rate

[0447]

[0448]

[0449] Table 14

[0450]

[0451]

[0452] In this example: Based on the principle of precise control of material flow rate during oxygen adjustment, oxygen was adjusted three times during the first shift (0:00 to 7:00), specifically at 2:00, 3:00, and 5:00. Based on the adjusted oxygen level, the post-adjustment oxygen enrichment was obtained. Following the aforementioned calculation method, the system automatically combined relevant parameters such as the corrected air volume and air consumption per ton of coke and coal to calculate and output the post-adjustment material flow rate control effect (oxygen adjustment reaction time 1 hour). The results after the three oxygen enrichment adjustments were obtained: the first oxygen adjustment was +800m³. 3 / h, the difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment was +0.12 batches / h. After the reaction, the feed rate increased to 8.93 batches / h, which was 0.07 batches / h different from the specified feed rate (9 batches / h). The actual feed rate still did not meet the standard (8.5 batches / h), so the agent was adjusted again. The second oxygen adjustment was +700m 3 / h, the difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is +0.11 batches / h, and the feed rate after reaction is 8.93 batches / h, which is 0.07 batches / h different from the specified feed rate (9 batches / h); the oxygen adjustment amount reaches the specified feed rate (9 batches / h) after the reaction; the third oxygen adjustment amount is -400m 3 / h (actual material rate for the current period is 10 batches / h), the difference between the theoretical material rate after oxygen adjustment and the theoretical material rate before oxygen adjustment is -0.05 batches / h, the material rate after reflection is 8.90 batches / h, the difference between the specified material rate (9 batches / h) is 0.10 batches / h, which meets the specified oxygen adjustment definition standard (until the theoretical material rate output result obtained simultaneously reaches (the principle of oxygen adjustment effect judgment): (1) the difference between the theoretical material rate after oxygen adjustment and the theoretical material rate before oxygen adjustment is defined as 0.1 to 0.3 batches (increase or decrease); (2) |theoretical material rate after oxygen adjustment - specified material rate| < 0.3 batches / h, the predicted growth of batches per shift is -0.96 batches / shift (defined as (±) 0.3 to 1.5 batches)). Similarly, the second shift (8:00 AM to 3:00 PM) will have oxygen adjusted once, at 11:00 AM. Because the total material rate over the past two hours is 1.0 batch below the specified rate, the oxygen adjustment will be +800 m³ / min. 3 / h, the difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is +0.05 batches / h. The expected feed rate after reaction is 8.97 batches / h, which is 0.03 batches / h different from the specified feed rate (9 batches / h). The actual feed rate after reaction reaches the standard (9.0 batches / h), and the predicted increase in batches per shift is 0.40 batches / shift (defined between (±) 0.3 and 1.5 batches). After that, the feed rate reaches the range that does not need to be adjusted and continues.

[0453] The input oxygen enrichment adjustment amount meets the requirements, and based on the theoretical output obtained after oxygen adjustment (the utilization coefficient is calculated to be 3.67 t / (m²) based on the hourly average theoretical material rate), the yield is as follows: 3 .d)) and the planned output (planned 3.68t / (m 3 The absolute value of the deviation rate of .d) is used for verification. In this example, it is 0.27% < ±1.50%, and the theoretical fuel ratio is < 5 kg / t under the same raw material conditions. Once the material rate control effect is achieved, the process proceeds to step C3 and then to the next cycle, continuing the process.

[0454] C3. Verification of the effect of precise oxygen regulation and material rate control

[0455] The verification standard for daily feed batches is defined as follows: the absolute value of the error rate between any two of the three daily actual feed rate, daily specified feed rate, and daily theoretical feed rate is <1.50% (Table 15). Theoretical combustion temperature, kinetic energy, and other parameters are all within the specified range of smelting parameters. Satisfied, proceed with the process.

[0456] Table 15 Verification of the Effect of Precise Oxygen Regulation on Material Rate Control

[0457]

[0458] Verification of the average w([Si]) and theoretical indicators in this example:

[0459] The average w([Si]) value, daily theoretical coal ratio, coke ratio, and daily actual coal ratio and coke ratio in this example were compared and verified with the daily theoretical output calculated based on the theoretical feed rate (Table 16). All met the required range. The concepts, calculation methods, and formulas of the theoretical output and theoretical indicators involved are as follows:

[0460] Theoretical output (calculated based on tapping time and interval) t 出铁理 =Σ(ROUND((time) 本炉终了 -time 上炉终了 )*24,3)*L 实时 *O 料批 / 1000*ΣTFe / 100*0.99 / 0.94)

[0461] t 出铁理 The cumulative theoretical iron production (t / d) calculated based on the end-of-tapping interval of each furnace within a natural day; time 本炉终了 h represents the calendar time for the completion of this furnace operation; h: min; time. 上炉终了 The calendar operation time at the end of the previous furnace run, h:min; L 实时 The theoretical material velocity, calculated based on real-time oxygen enrichment and corrected air volume, is expressed in batches per hour. 料批 ΣTFe represents the batch weight of ore, kg / h; ΣTFe represents the overall grade of the furnace feed, %.

[0462] Theoretical output (theoretical iron output based on hourly feed rate) t 下料理 =AVERAGE(L 实时 *24*O 料批 / 1000*ΣTFe / 100*0.99 / 0.94)

[0463] t 出铁理 The daily output is the average value (t / d) obtained from the hourly theoretical iron output based on the hourly corrected air volume and oxygen enrichment rate; the rest is the same as above. The daily theoretical iron output is obtained by accumulating the hourly output to the daily output.

[0464] Theoretical fuel ratio (based on theoretical iron output per hour) calculated K 下料理 =C 干焦批 *L 实时 *24 / t 下料理 +M 小时喷煤 *24 / t 下 Cuisine

[0465] K 下料理 The hourly theoretical fuel ratio, measured in kg / t, is derived from the hourly theoretical iron content obtained by correcting the hourly air volume and oxygen enrichment rate. 小时喷煤 The value is the real-time hourly pulverized coal injection rate, in kg / h; the rest is the same as above.

[0466] Table 16 Comparison and verification of average theoretical and actual values ​​in this example (production, fuel ratio)

[0467]

[0468] D. Following the previous steps (preliminary verification of blast furnace condition, adjustment of coke batch (including coke briquettes), adjustment of oxygen and control of materials, adjustment of coal and control of temperature), the raw materials and smelting parameters are fed into the furnace, and the smelting parameters are adjusted: precise control of material rate, accurate control of furnace temperature (w([Si]) value of molten iron), control and calculation of slag and iron composition, and real-time theoretical prediction and pre-control of indicators). In this example, the process definition conditions of each step meet the requirements and are within the error range, and the materials are fed into the furnace for smelting according to the material sequence.

[0469] Furnace smelting and parameter control steps:

[0470] D1. The total amount of the four types of ore mentioned in A is 100% (in this example, titanium slag smelting in vanadium-titanium ore), and coke with high ash and sulfur content (including coke briquettes) is fed into the blast furnace in the usual amount. After checking the blast furnace condition, under constant blast temperature and full blast conditions, "quantitative oxygen adjustment and precise control of material rate" is adopted. The oxygen enrichment is adjusted ≤3 times per shift (3 times in the first shift and 1 time in the second shift in this example), so as to control |daily theoretical batch - daily specified batch| / daily specified batch < 1.50% (0.66% in this example).

[0471] D2. Smelting shall be carried out under the following conditions:

[0472] This example illustrates the smelting of titanium slag from vanadium-titanium ore. The smelting parameters are as follows: hot blast pressure 0.319–0.344 MPa (full blast), top pressure 0.154–0.166 MPa, hot blast temperature 1170℃ (top blast temperature), and furnace feed air volume (corrected) 3250–3354 m³ / h. 3 / min, oxygen enrichment rate is 9408~11308m 3 / h, pulverized coal injection rate is 136-143 kg / t iron (raw material analysis exceeded the specified change once, pulverized coal injection rate 24.2-26.1%); ore batch 33.0 tons, coke batch (dry basis) 7.296-7.369 tons; coke slag batch (dry basis) 0.48 tons; w([Si]) 0.102-0.153% (vanadium-titanium ore smelting), slag basicity 1.12-1.15, molten iron temperature 1432-1452℃. All are within the specified range.

[0473] This example demonstrates adjustments made to the coke batch according to defined principles and methods. The effects of these adjustments are reflected within one smelting cycle.

[0474] In this example, the hourly oxygen enrichment (precisely adjusted feed rate) was adjusted four times within two natural shifts: the adjustment amount of the hourly oxygen enrichment was less than 10.0% of the original total oxygen enrichment. The effect of this adjustment took one hour to take effect.

[0475] The adjustment effect reflects the landing time, which is resolved by the automatic search function.

[0476] The completion times for the above-mentioned influencing factors are as follows: furnace grade, slag basicity, clinker rate, and top pressure are all within one smelting cycle (4.5–5.5 hours, automatically calculated); pulverized coal injection is 3.5 hours; and air volume, air temperature, and humidity are 1 hour. The adjustment point is when the change in the corresponding influencing factor coincides with the time it takes for the adjustment factor to take effect, based on maintaining a relatively stable overall fuel ratio (the absolute value of the raw material composition deviation under the same raw material conditions (when no coke batch adjustment is required) <5 kg / t).

[0477] D3. Smelting shall be carried out under the following conditions:

[0478] In actual smelting processes, the slag ratio is 468–475 kg / t, the magnesium-aluminum ratio in the slag is 0.842–0.867, the slag basicity is 1.12–1.15, the constant blast temperature is 1170℃, the oxygen enrichment rate (after adjusting for blast volume) is 3.90–4.24%, and the permeability index is 18336–20039 m³ / t. 3 / (min.MPa), theoretical combustion temperature 2352~2374℃, actual blower velocity 261~269m / s, actual blower kinetic energy (after air volume correction) 15965~18106kg.m / s, theoretical hourly material rate 8.62~8.87 batches / h.

[0479] In this example of oxygen-controlled material handling, in addition to the deviation values ​​meeting the aforementioned requirements for material rate and silicon deviation, direct smelting parameters such as air volume, air pressure, and top pressure, as well as indirect smelting parameters such as permeability index, theoretical combustion temperature, and blast kinetic energy obtained through automatic calculation, are all within the specified range. For vanadium-titanium ore smelting blast furnaces, the lower limit of w([Si]) and the upper limit of w(MgO) / w(Al2O3) are used.

[0480] The actual smelting results in this example have been corrected. The hourly theoretical and actual material rate, the theoretical calculated control and actual w([Si]) value, the theoretical and actual slag-iron composition, the theoretical and actual furnace output (day), and the theoretical and actual fuel ratio comparison and verification all meet the control requirements. No changes or corrections to the relevant parameters are needed.

[0481] The calculation process in step A is as follows: Knowing the full composition of the raw materials (sintered ore, pellets, lump ore, coke, pulverized coal), the furnace charge ratio is determined based on the basic w([Si]) value, the specified slag basicity, and the magnesium-aluminum ratio range.

[0482] The calculation process in step B (B1~B2) is as follows: Knowing the complete analysis of raw materials and fuels, when the fluctuation range is within the required range (step B1), the baseline operating parameters such as total air pressure, air volume, air temperature, and w([Si]) are not adjusted. The theoretical indicators, smelting cycle, reduction rates of various elements in molten iron, alkali metal and lead-zinc-titanium-sulfur loads, and slag-iron composition are calculated in conjunction with the baseline operating parameters (baseline coal quantity, base material rate, and base w([Si])). Knowing the complete analysis of raw materials and fuels, if any of the main parameters exceeds the required fluctuation range (step B2), then… The baseline operating parameters need to be adjusted according to the magnitude of changes (including the determination of the baseline hourly coal quantity and coke batch after changes in raw materials and fuels). Based on the baseline ore batch, coke-butane batch (dry basis), w([Si]) quantity, constant blast temperature, and slag basicity within the range, the indirect smelting parameters such as the proportion, coke batch, hourly pulverized coal injection rate, and smelting cycle are checked. The hourly coal quantity, theoretical iron content of the batch, theoretical coal ratio, coke ratio, coke-butane ratio, new coke batch, theoretical fuel ratio of the batch under changed basic conditions, utilization coefficient, smelting cycle, and pulverized coal injection rate are calculated in the following order after the factor changes. The concepts and calculations involved include: hourly coal quantity l2 after factor changes, coke-butane ratio d2 after factor changes, coke ratio k2 after factor changes, and coke batch C2 after factor changes. All calculations are based on a dry basis. The baseline w([Si]) is set unchanged, and the coke batch and hourly coal quantity (coke-butane unchanged) are adjusted according to the raw material and fuel variables. Other calculations include: theoretical fuel ratio of the batch, utilization coefficient, smelting cycle, and pulverized coal injection rate.

[0483] The computer verification process in step C (including steps C1 to C3) is as follows: It is determined based on the principle of whether the material rate needs adjustment during the smelting process. If no adjustment is needed, the process proceeds directly to the next cycle; if adjustment is required, theoretical calculations and verification are performed based on the method of precisely controlling the actual material rate. Knowing (directly acquiring) the comprehensive air supply parameters (including surface air volume, humidity, air pressure, top pressure, air temperature, tuyer area, etc.) and fuel composition and related parameters (including batch weight, composition, and combustion rate before the tuyer, hourly coal powder quantity, coal powder composition, and combustion rate before the tuyer), the indirect smelting parameters are automatically calculated (including the corrected air volume obtained based on the surface-actual air volume correction coefficient (or fitting polynomial), as well as the oxygen enrichment rate, theoretical combustion temperature, permeability index, and blast kinetic energy after the corrected air volume). The smelting control range for each parameter is as described in step E. Knowing the above relevant parameters (collection or calculation results), the calculation order and process are as follows: original oxygen enrichment amount → oxygen enrichment adjustment amount (input) → new oxygen enrichment amount → oxygen enrichment rate after oxygen adjustment and correction air volume (combined with the comprehensive blower parameters and fuel parameters in step (1)) → (obtained by combining the air volume per ton of coal consumption, air volume per hour of coal consumption, air volume per ton of coke consumption, and residual air volume after coal burning obtained from the parameters in step (1)) theoretical material speed after oxygen adjustment → judgment of oxygen adjustment effect. And check the material speed control effect after oxygen adjustment (input adjustment amount) (for daily batches of material, the definition standard is: the absolute value error rate of any two of the differences between the daily actual material speed, the daily specified material speed, and the daily theoretical material speed is <1.50%). In this step, the correction air volume is substituted into the conventional calculation formula to obtain the theoretical combustion temperature, blower kinetic energy, permeability index, smelting cycle, etc. after correction air volume and correction oxygen enrichment rate.

[0484] The method involves repeatedly inputting the oxygen enrichment adjustment amount until the theoretical material flow rate output value meets the requirements (all calculations are automatic). The calculation concepts and formulas involved in the process are: Corrected air volume V 校 Oxygen enrichment rate F after correcting air volume O2 , Air consumption per ton of coal after correction V m Hourly coal consumption and air volume V after adjusting for oxygen enrichment rate mh , Air consumption per ton of coke after correction V C Theoretical feed rate L before oxygen adjustment 前 Theoretical feed rate L after oxygen adjustment 后 .

[0485] Step C also involves verifying the output and fuel ratio. During blast furnace smelting, the difference between the actual material rate and the specified benchmark material rate is within a certain range (±1.0 batches / h, the absolute value of the difference between the daily theoretical material rate and the actual material rate <1.50%). This is combined with the control method focusing on achieving the specified w([Si]) in smelting, and with the actual w([Si]) achieved after the adjustment reaction, for verification and analysis. Furthermore, the daily theoretical coal ratio and coke ratio are compared and verified with the daily actual coal ratio and coke ratio, and the daily theoretical output calculated based on the theoretical material rate is compared with the daily actual output. The concepts, calculation methods, and formulas of the theoretical output and theoretical indicators involved are as follows:

[0486] Theoretical output (calculated based on tapping time and interval) t 出铁理 =Σ(ROUND((time) 本炉终了 -time 上炉终了 )*24,3)*L 实时 *O 料批 / 1000*ΣTFe / 100*0.99 / 0.94)

[0487] t 出铁理 The cumulative theoretical iron production (t / d) calculated based on the end-of-tapping interval of each furnace within a natural day; time 本炉终了 h represents the calendar time for the completion of this furnace operation; h: min; time. 上炉终了 The calendar operation time at the end of the previous furnace run, h:min; L 实时 The theoretical material velocity, calculated based on real-time oxygen enrichment and corrected air volume, is expressed in batches per hour. 料批 ΣTFe represents the batch weight of ore, kg / h; ΣTFe represents the overall grade of the furnace feed, %.

[0488] Theoretical output (theoretical iron output based on hourly feed rate) t 下料理 =AVERAGE(L 实时 *24*O 料批 / 1000*ΣTFe / 100*0.99 / 0.94)

[0489] t 出铁理 The daily output is the average value (t / d) obtained from the hourly theoretical iron output based on the hourly corrected air volume and oxygen enrichment rate; the rest is the same as above. The daily theoretical iron output is obtained by accumulating the hourly output to the daily output.

[0490] Theoretical fuel ratio (based on theoretical iron output per hour) calculated K 下料理 =C 干焦批 *L 实时 *24 / t 下料理 +M 小时喷煤 *24 / t 下 Cuisine

[0491] K 下料理 The hourly theoretical fuel ratio, measured in kg / t, is derived from the hourly theoretical iron content obtained by correcting the hourly air volume and oxygen enrichment rate. 小时喷煤 The value is the real-time hourly pulverized coal injection rate, in kg / h; the rest is the same as above.

[0492] The results of the operation show that the theoretical fuel ratio fluctuates within ±5 kg / t.

[0493] The verification process in step E is as follows: based on the actual smelting results obtained in step E, the calculation parameters are corrected according to the calculation methods in steps B to D to form a closed loop.

[0494] Application Example 2

[0495] A. Intensive smelting of titanium slag in blast furnace vanadium-titanium ore, using a vanadium-titanium ore charge structure, including sintered ore, high-titanium pellets, and low-silicon lump ore. A baseline batching is performed as follows:

[0496] The chemical composition of the sinter is: TFe 52.26%, SiO 26.07%, CaO 12.76%, Al 2O 32.19%, MgO 2.89%, TiO 21.283%, S 0.043%, V 2O 50.14%, MnO 0.24%, with a bulk density of 1.99 t / m³. 3 The composition of the vanadium-titanium pellets (1) is: TFe 57.32%, SiO2 4.53%, CaO 0.56%, Al2O3 2.89%, MgO 2.36%, TiO2 6.46%, V2O5 0.737%, MnO 0.23%; bulk density 2.28 t / m³ 3 The composition of the vanadium-titanium pellets (2) is as follows: TF: 53.58%, SiO2: 5.14%, CaO: 1.23%, Al2O3: 2.52%, MgO: 2.71%, TiO2: 10.14%, V2O5: 0.546%, MnO: 0.270%, with a bulk density of 2.16 t / m³. 3 The composition of the low-silica lump ore is: TFe 65.34%, SiO2 3.83%, CaO 0.030%, Al2O3 1.08%, MgO 0.010%, TiO2 0.010%, V2O5 0.030%, MnO 0.199%, with a bulk density of 2.30 t / m³. 3 .

[0497] The chemical composition of the coke is: C 85.54%, ash content 13.63%, and bulk density 0.65 t / m³. 3The complete analysis of coke ash composition is as follows: SiO2 54.836%, CaO 2.936%, Al2O3 24.538%, MgO 0.753%, TiO2 1.55%, MnO 0.39%; the chemical composition of pulverized coal is as follows: C 77.98%, ash 10.56%, volatile matter 13.35%, fineness (-200 mesh) 66%; the complete analysis of pulverized coal ash composition is as follows: SiO2 47.245%, CaO 5.475%, Al2O3 23.85%, MgO 2.38%, TiO2 1.284%, MnO 0.370%.

[0498] Baseline conditions and material verification results:

[0499] Ore batch: 33,000 kg, coke batch (wet weight): 7,676 kg (dry weight): 7,369 kg, coke briquettes (wet weight): 500 kg (dry weight): 480 kg. Batching basis: Baseline: w([Si]) value: 0.160%; slag basicity: 1.14. Baseline material rate: 8.96 batches / h; Baseline coal quantity: 21,632 kg / h.

[0500] Ingredient verification results:

[0501] Sintered ore 63% (21%+21%+21%) + sintered small particles 3%, vanadium-titanium pellets (1) 15.0%, vanadium-titanium pellets (2) 19.0%, low-silicon lump ore 1.0%. Total furnace feed grade TFe: 53.40%.

[0502] B. Ingredient calculation, parameter and index verification analysis:

[0503] B1. Benchmark ingredient calculation, parameter and index verification analysis:

[0504] For conventional blast furnace ore and coke batches, the chemical composition (full analysis) of various materials is as described in step A. Under the main reference parameters of the baseline raw materials (clinker rate, overall charge grade, coke and pulverized coal ash content), combined with the baseline operating parameters of step A (baseline coal quantity, baseline material rate, baseline w([Si])), the baseline operating parameters such as total air (air pressure, air volume), air temperature, and w([Si]) are not adjusted.

[0505] Under the baseline conditions in step A (assuming that the main raw material parameters are stable (the fluctuation ranges all meet the following conditions: clinker rate < ±1.0%, overall furnace feed grade < ±0.20%, coke < ±0.1%, and pulverized coal ash content < ±0.10%)), proceed directly to the baseline index determination step, following the steps below. The calculation order and results are as follows:

[0506] (1) Calculate the theoretical fuel ratio, utilization coefficient, smelting cycle, etc. under the basic conditions.

[0507] The calculated theoretical fuel ratio is 555.80 kg / t (dry basis); the utilization factor is 3.676 t / (m³). 3 .d); The smelting cycle is 42.1 batches (Tables 17-18).

[0508] Table 17 Calculation Basis Conditions and Verification of Basic Indicators

[0509]

[0510] Table 18

[0511]

[0512] (2) Output the slag and iron composition and related intermediate process results according to the baseline conditions (assuming that the changes in raw materials and fuels are all within the required range).

[0513] The calculation process, method, and results are the same as in Example 1.

[0514] Based on the reduction rates of the obtained elements (desulfurization rate, and 100% reduction rates of [P] and [As], etc.), combined with the material balance, the amounts of corresponding element oxides and S, P, and As entering the molten iron are calculated. Further calculations are made of the amounts of each element oxide and S, P, and As entering the slag. The output slag quantity (slag ratio), alkali metals, lead, zinc, titanium, sulfur load, etc., as well as the theoretical slag composition (including basicity, magnesium-aluminum ratio, etc.) and theoretical pig iron composition (theoretically calculated from the corresponding element oxides entering the molten iron) are obtained (Tables 19 to 22).

[0515] Table 19 shows the reduction rate corresponding to the baseline w([Si]) based on the fitting formula between w([Si]) value and the reduction rate of each element.

[0516]

[0517] Note: The baseline w([Si]) is the input, and the others are automatically calculated outputs.

[0518] Table 20 Output baseline mix ratio, slag quantity (slag ratio), alkali metals, lead-zinc and titanium, sulfur load under baseline w([Si])

[0519]

[0520] Table 21 Theoretical pig iron composition under output reference w([Si])

[0521] project Si S P Ti As V Mn unit ％ ％ ％ ％ ％ ％ ％ numerical values 0.16 0.057 0.071 0.204 0.032 0.165 0.236

[0522] Table 22 Theoretical slag composition under output baseline w([Si])

[0523] project <![CDATA[SiO2]]> CaO MgO S <![CDATA[Al2O3]]> <![CDATA[TiO2]]> <![CDATA[V2O5]]> MnO magnesium-aluminum ratio alkalinity unit ％ ％ ％ ％ ％ ％ ％ ％ times times numerical values 28.85 32.91 10.90 0.71 12.55 13.41 0.43 0.69 0.868 1.14

[0524] In this example, the corrected air volume calculation is based on the air volume corrected for actual fuel consumption (the cumulative average value of the samples is 3289.0 m³). 3 / min) and the corresponding metered air volume (the cumulative average value of the samples is 2669.42m). 3 The multiple of ( / min) is relatively stable, with a value between 1.22 and 1.24 times. Here, the conversion factor of the multiple of the corrected air volume and the surface air volume is used = 3289.0 / 2669.42 = 1.23 times.

[0525] When the main reference parameters of the benchmark raw materials (clinker rate, overall furnace grade, coke ash content, and pulverized coal ash content) change beyond the stable range, the process proceeds to step B2.

[0526] B2. Analysis of batching calculations, parameters, and index verification when key verification conditions (clinker rate, overall furnace grade, coke and pulverized coal ash content) change:

[0527] Changes in the composition of the raw materials were detected. Specifically:

[0528] The chemical composition of the sinter is: TFe 51.76%, SiO 26.25%, CaO 12.96%, Al 2O 32.11%, MgO 2.77%, TiO 21.253%, S 0.041%, V 2O 50.141%, MnO 0.22%, with a bulk density of 1.93 t / m³. 3 The composition of the vanadium-titanium pellets (1) is: TFe 57.32%, SiO2 4.53%, CaO 0.56%, Al2O3 2.89%, MgO 2.36%, TiO2 6.46%, V2O5 0.737%, MnO 0.23%; bulk density 2.28 t / m³ 3 The composition of the vanadium-titanium pellets (2) is as follows: TF: 53.58%, SiO2: 5.14%, CaO: 1.23%, Al2O3: 2.52%, MgO: 2.71%, TiO2: 10.14%, V2O5: 0.546%, MnO: 0.270%, with a bulk density of 2.16 t / m³. 3 The composition of the low-silica lump ore is: TFe 65.34%, SiO2 3.83%, CaO 0.030%, Al2O3 1.08%, MgO 0.010%, TiO2 0.010%, V2O5 0.030%, MnO 0.199%, with a bulk density of 2.30 t / m³. 3 .

[0529] The chemical composition of the coke is: C 85.32%, ash content 13.76%, and bulk density 0.63 t / m³. 3The complete analysis of coke ash composition is as follows: SiO2 53.868%, CaO 2.985%, Al2O3 24.538%, MgO 0.175%, TiO2 1.53%, MnO 0.39%; the chemical composition of pulverized coal is as follows: C 77.75%, ash 10.51%, volatile matter 13.40%, fineness (-200 mesh) 69%; the complete analysis of pulverized coal ash composition is as follows: SiO2 47.739%, CaO 5.365%, Al2O3 22.88%, MgO 2.31%, TiO2 1.39%, MnO 0.390%.

[0530] In this example, the grade of sintered ore and the ash content of coke and pulverized coal vary. The initial batching and verification are performed according to step A. The verification data is as follows: Ore batch: 33000 kg, Coke batch (wet weight): 7676 kg (dry weight): 7369 kg, Coke slag batch (wet weight): 500 kg (dry weight): 480 kg (Note: The coke batch needs adjustment based on the raw material composition and the grade and clinker ratio after the initial batching). Batching baseline: w([Si]) value: 0.160%; slag basicity: 1.14. Baseline material rate: 8.96 batches / h, base coal quantity: 21648 kg / h (Note: Adjustments need to be made based on changes in pulverized coal ash content). After adjusting the coke batch and hourly coal quantity, further verification and adjustments will be made based on the batching results (according to the target slag basicity).

[0531] Ingredient verification results:

[0532] Sintered ore 61.50% (20.5% + 20.5% + 20.5%) + sintered small particles 3.0%, vanadium-titanium pellets (1) 15.0%, vanadium-titanium pellets (2) 19.0%, low-silica lump ore 1.50%. Total furnace feed grade TFe: 53.14%.

[0533] In this example, key parameters of the raw materials exceeded the stable range (clinker rate decreased by 0.50%; overall feed grade decreased by 0.26% > ±0.20%; coke ash content increased by 0.13%; and pulverized coal ash content increased by 0.05%). The baseline operating parameters were adjusted based on the magnitude of the changes (including the baseline hourly coal quantity and coke batch determination after the change in raw materials):

[0534] The following steps are calculated in sequence: determination of hourly coal quantity after factor changes, theoretical iron content of batch, calculation of theoretical coal ratio, new coke ratio and coke-to-coke ratio, determination of new coke batch, theoretical fuel ratio of batch under changing conditions, utilization coefficient, smelting cycle, pulverized coal injection rate, etc. (see Tables 23 to 28 for details).

[0535] The concepts and formulas involved in the calculation process are the same as in Example 1.

[0536] (1) Calculate the theoretical fuel ratio, utilization coefficient, smelting cycle, etc. after the change of calculation conditions.

[0537] Following the calculation method and steps of B2, based on the fundamental parameters, the dry coke batch weight after changes in raw material and fuel conditions is obtained as 7378 kg / batch, and the hourly coal consumption is 21648 kg / h. The corresponding theoretical changes are: the calculated theoretical fuel ratio is 559.11 kg / t (dry basis); the utilization coefficient is 3.66 t / (m³). 3 .d); The smelting cycle is 42.1 batches.

[0538] Table 23 shows the calculation results after changes in raw materials and fuels (compared to baseline conditions) and the verification of their indicators.

[0539]

[0540] Table 24

[0541]

[0542] Note: In this example, after adjusting the coke batch and hourly coal quantity, the verification target (alkalinity) has been achieved, and the aforementioned furnace charge structure and proportioning are maintained.

[0543] (2) Slag and iron composition and related intermediate process results after adjusting the furnace charge structure ratio, coke batch, and hourly coal quantity according to changes in raw material and fuel conditions.

[0544] Taking each batch of material as a unit, the reduction rates of elements such as [Si], [Ti], [Mn], and [V] obtained under the predetermined w([Si]) value in the molten iron are obtained by fitting (w([Si])-Si reduction rate, w([Si])-Ti reduction rate, w([Si])-Mn reduction rate, and w([Si])-V reduction rate), the fitting relationship of w([Si])-desulfurization rate, and the fitting polynomial relationship between [S] removal rate and predetermined w([Si]) are mentioned above. Figures 1-5 ).

[0545] In the same step B1, output the slag quantity (slag ratio), alkali metals, zinc and titanium, sulfur load, etc. after the change of raw materials and fuels, as well as the theoretical slag composition (including basicity, magnesium-aluminum ratio, etc.) and theoretical pig iron composition (Tables 25 to 28).

[0546] Table 25 shows the reduction rate corresponding to the baseline w([Si]) based on the fitting formula between w([Si]) value and the reduction rate of each element.

[0547]

[0548] Note: The baseline w([Si]) is the input, and the others are automatically calculated outputs.

[0549] Table 26 Output variation ratio, slag quantity (slag ratio), alkali metal, zinc and titanium, sulfur load under baseline w([Si])

[0550]

[0551] Table 27 Theoretical pig iron composition under the baseline w([Si]) after changes in output raw materials and fuels.

[0552] project Si S P Ti As V Mn unit ％ ％ ％ ％ ％ ％ ％ Baseline conditions 0.16 0.057 0.071 0.204 0.032 0.165 0.236 Raw material changes 0.16 0.055 0.072 0.207 0.018 0.165 0.196

[0553] Table 28 Theoretical slag composition under the baseline w([Si]) after output of raw material changes.

[0554] project <![CDATA[SiO2]]> CaO MgO S <![CDATA[Al2O3]]> <![CDATA[TiO2]]> <![CDATA[V2O5]]> MnO magnesium-aluminum ratio alkalinity unit ％ ％ ％ ％ ％ ％ ％ ％ times times Baseline conditions 28.85 32.91 10.90 0.71 12.55 13.41 0.43 0.69 0.868 1.14 Raw material changes 28.75 32.73 10.97 0.71 12.61 13.56 0.45 0.64 0.870 1.14

[0555] The corrected air volume ratio is the same as in step B1 (1.23 times).

[0556] During the smelting process, the reference feed rate often changes, and it is controlled in conjunction with "oxygen-regulated feed" to proceed to step C.

[0557] C. Input the oxygen enrichment adjustment amount to precisely control the actual material flow rate:

[0558] Data collection and calculation output should be performed according to the following steps and methods (the determination and adjustment of whether adjustments are needed should be made according to the definition principles of step C (C1~C2).

[0559] C2. Determining the amount of oxygen enrichment and accurately controlling the actual material flow rate.

[0560] (2) Parameters to be collected (including calculated indirect smelting parameters and fuel parameters). Directly collected comprehensive air supply parameters include: surface air volume, humidity, air pressure, top pressure, air temperature, tuyer area, etc.; indirect smelting parameters (automatically calculated) include corrected air volume obtained based on the table-actual air volume correction coefficient (or fitting polynomial), as well as the oxygen enrichment rate, theoretical combustion temperature, permeability index, and blast kinetic energy after correcting the air volume. Fuel parameters to be collected include: batch weight, composition, and combustion rate before the tuyer; hourly pulverized coal quantity, pulverized coal composition, and combustion rate before the tuyer. Note: Calculated based on hourly cumulative quantity (hourly cumulative quantity is automatically collected by computer at certain time intervals).

[0561] (2) Determination of oxygen enrichment adjustment amount and precise control of actual material speed. Input, calculate and output the results of precise control of material speed and intermediate process data of oxygen enrichment according to the steps. The steps for determining the oxygen enrichment adjustment amount (calculation order) are: original oxygen enrichment amount → oxygen enrichment adjustment amount (input) → new oxygen enrichment amount → oxygen enrichment rate after oxygen adjustment and correction of air volume (combined with the comprehensive blower parameters and fuel parameters in step (1)) → (obtained by combining the air volume per ton of coal consumption, air volume per hour of coal consumption, air volume per ton of coke consumption, and residual air volume after coal burning obtained from the parameters in step (1)) theoretical material speed after oxygen adjustment → judgment of oxygen adjustment effect.

[0562] The concepts, calculation methods, and formulas involved are the same as in Example 1.

[0563] Repeatedly input the oxygen enrichment adjustment amount until the theoretical material rate output value meets the requirements.

[0564] The results and process parameters obtained in this example are shown in Table 29 (based on data and operations from two natural classes).

[0565] Table 29 Data Acquisition (Calculation) and Process / Effects of Precise Oxygen Control of Material Rate

[0566]

[0567]

[0568] Table 30

[0569]

[0570]

[0571] In this example: Based on the principle of precise control of material rate during oxygen adjustment, the first shift (8:00 AM to 3:00 PM) will have its oxygen adjustment at 11:00 AM. Based on the adjusted oxygen amount, the post-adjustment oxygen enrichment will be obtained. Following the aforementioned calculation method, the system automatically combines relevant parameters such as the corrected air volume and air consumption per ton of coke and coal to calculate and output the post-adjustment material rate control effect (oxygen adjustment reaction time 1 hour). The effect after one adjustment of the oxygen enrichment is: because the total material rate difference over two consecutive hours is 1.0 batch, the adjusted oxygen amount is +800m³. 3 / h, the difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is +0.05 batches / h, the expected feed rate after reaction is 8.97 batches / h, the difference between the specified feed rate (9 batches / h) is 0.03 batches / h; the actual feed rate after reaction meets the standard (9.0 batches / h), which meets the specified oxygen adjustment criteria (until the theoretical feed rate output result is simultaneously met (the principle of judging the oxygen adjustment effect): (1) the difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is defined as 0.1 to 0.3 batches (increase or decrease); (2) |theoretical feed rate after oxygen adjustment - specified feed rate| < 0.3 batches / h, the predicted increase in batches per shift is 0.40 batches / shift (defined as (±) 0.3 to 1.5 batches)). Similarly, the second shift (15:00-23:00) required oxygen adjustment once, at 17:00, because the total material rate exceeded the specified rate by 1.0 batch over two consecutive hours, and the oxygen adjustment was -400m³. 3 / h, the difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is -0.16 batches / h. After the reaction, the expected feed rate is reduced to 8.85 batches / h, which is 0.15 batches / h different from the specified feed rate (9 batches / h). The actual feed rate after the reaction meets the standard (8.5 batches / h), and the predicted increase in batches per shift is -1.28 batches / shift (defined between ±0.3 and 1.5 batches). Thereafter, the feed rate reaches the range where no adjustment is needed, and the process continues.

[0572] The input oxygen enrichment adjustment amount meets the requirements, and based on the theoretical output obtained after oxygen adjustment (the utilization coefficient is calculated to be 3.67 t / (m²) based on the hourly average theoretical material rate), the yield is as follows: 3 .d)) and the planned output (planned 3.66t / (m 3 The absolute value of the deviation rate of .d) is used for verification. In this example, it is 0.27% < ±1.50%, and the theoretical fuel ratio is < 5 kg / t under the same raw material conditions. Once the material rate control effect is achieved, the process proceeds to step C3 and then to the next cycle, continuing the process.

[0573] C3. Verification of the effect of precise oxygen regulation and material rate control

[0574] The verification standard for the daily feed batch is defined as follows: the absolute value of the error rate between any two of the actual daily feed rate, the specified daily feed rate, and the theoretical daily feed rate is <1.50% (Table 31). The theoretical combustion temperature, kinetic energy, and other parameters are all within the specified range of smelting parameters. Satisfied, proceed with the process.

[0575] Table 31 Verification of the effect of precise oxygenation control on material flow rate

[0576]

[0577] The daily theoretical indicators for this example were verified by comparing the theoretical output calculated based on the theoretical feed rate with the actual daily output (Table 32). Both met the required range. The concepts, calculation methods, and formulas for theoretical output and theoretical indicators are the same as in Example 1, as follows:

[0578] Table 32 Comparison and verification of the average theoretical value and the actual value in this example.

[0579]

[0580] D. Following the previous steps (preliminary verification of blast furnace condition, adjustment of coke batch (including coke briquettes), adjustment of oxygen and control of materials, adjustment of coal and control of temperature), the raw materials and smelting parameters are fed into the furnace, and the smelting parameters are adjusted: precise control of material rate, accurate control of furnace temperature (w([Si]) value of molten iron), control and calculation of slag and iron composition, and real-time theoretical prediction and pre-control of indicators). In this example, the process definition conditions of each step meet the requirements and are within the error range, and the materials are fed into the furnace for smelting according to the material sequence.

[0581] Furnace smelting and parameter control steps:

[0582] D1. The total amount of the four types of ore mentioned in A is 100% (in this example, titanium slag smelting in vanadium-titanium ore), and coke with high ash and sulfur content (including coke briquettes) is fed into the blast furnace in the usual amount. After checking the blast furnace condition, under constant blast temperature and full blast conditions, "quantitative oxygen adjustment and precise control of material rate" is adopted. The oxygen enrichment is adjusted ≤3 times per shift (1 time in the first shift and 1 time in the second shift in this example), so as to control |daily theoretical batch - daily specified batch| / daily specified batch < 1.50% (0.97% in this example).

[0583] D2. Smelting shall be carried out under the following conditions:

[0584] This example illustrates the smelting of titanium slag from vanadium-titanium ore. The smelting parameters are as follows: hot blast pressure 0.331–0.344 MPa (full blast), top pressure 0.159–0.170 MPa, hot blast temperature 1170℃ (top blast temperature), and furnace feed air volume (corrected) 3275–3342 m³ / h. 3 / min, oxygen enrichment is 10508~11308m 3 / h, pulverized coal injection rate is 138-142 kg / t iron (raw material analysis exceeded the specified change once, pulverized coal injection rate 24.0-26.0%); ore batch 33.0 tons, coke batch (dry basis) 7.369-7.378 tons; coke slag batch (dry basis) 0.48 tons; w([Si]) 0.117-0.214% (vanadium-titanium ore smelting), slag basicity 1.13-1.15, molten iron temperature 1441-1460℃. All are within the specified range.

[0585] This example demonstrates adjustments made to the coke batch according to defined principles and methods. The effects of these adjustments are reflected within one smelting cycle.

[0586] In this example, the hourly oxygen enrichment (precisely adjusted feed rate) was adjusted twice within two shifts: the adjustment amount of the hourly oxygen enrichment was less than 10.0% of the original total oxygen enrichment. The effect of this adjustment took one hour to take effect.

[0587] The adjustment effect reflects the landing time, which is resolved by the automatic search function.

[0588] The completion times for the above-mentioned influencing factors are as follows: furnace grade, slag basicity, clinker rate, and top pressure are all within one smelting cycle (4.5–5.5 hours, automatically calculated); pulverized coal injection is 3.5 hours; and air volume, air temperature, and humidity are 1 hour. The adjustment point is when the change in the corresponding influencing factor coincides with the time it takes for the adjustment factor to take effect, based on maintaining a relatively stable overall fuel ratio (the absolute value of the deviation under the same raw material conditions (when no coke batch adjustment is required) <5 kg / t).

[0589] D3. Smelting shall be carried out under the following conditions:

[0590] In actual smelting processes, the slag ratio is 475–476 kg / t, the magnesium-aluminum ratio in the slag is 0.859–0.870, the slag basicity is 1.13–1.15, the constant blast temperature is 1170℃, the oxygen enrichment rate (after adjusting for blast volume) is 3.90–4.25%, and the permeability index is 18529–19096 m³ / t. 3 / (min.MPa), theoretical combustion temperature 2360~2375℃, actual blower velocity 261~269m / s, actual blower kinetic energy (after air volume correction) 16321~17551kg.m / s, theoretical hourly material rate 8.71~8.96 batches / h.

[0591] In this example, when oxygen is used to regulate the feed and coal to regulate the temperature, in addition to the deviation values ​​meeting the aforementioned requirements for feed rate and silicon deviation, the direct smelting parameters such as air volume, air pressure, and top pressure, as well as the indirect smelting parameters such as permeability index, theoretical combustion temperature, and blast kinetic energy obtained through automatic calculation, are all within the specified range. For vanadium-titanium ore smelting blast furnaces, the lower limit of w([Si]) and the upper limit of w(MgO) / w(Al2O3) are used.

[0592] The actual smelting results in this example have been corrected. The hourly theoretical and actual material rate, the theoretical calculated control and actual w([Si]) value, the theoretical and actual slag-iron composition, the theoretical and actual furnace output (average, daily average), and the theoretical and actual fuel ratio comparison and verification all meet the control requirements. No changes or corrections to the relevant parameters are needed.

[0593] The concepts, calculation steps, and methods of each step are the same as in Example 1.

[0594] Application Example 3

[0595] A. Intensified smelting of ordinary ore in blast furnaces, using a common ore burden structure, including sinter, high-silica magnesia pellets, and low-silica lump ore. A standard batching process is performed:

[0596] The chemical composition of the sinter is: TFe 53.66%, SiO 25.85%, CaO 13.31%, Al 2O 31.77%, MgO 2.32%, TiO 20.46%, S 0.045%, V 2O 50.142%, MnO 0.129%, with a bulk density of 2.03 t / m³. 3 The composition of the acidic magnesium oxide pellets is: TFe 59.14%, SiO2 6.87%, CaO 0.073%, Al2O3 1.84%, MgO 1.02%, TiO2 2.88%, V2O5 0.145%, MnO 0.097%; bulk density 2.29 t / m³ 3The composition of the low-silica lump ore is: TFe 65.98%, SiO2 6.62%, CaO 0.20%, Al2O3 1.336%, MgO 0.05%, TiO2 0.093%, V2O5 0.030%, MnO 0.129%, with a bulk density of 2.30 t / m³. 3 .

[0597] The chemical composition of the coke is: C 84.24%, ash content 14.49%, and bulk density 0.65 t / m³. 3 The complete analysis of coke ash composition is as follows: SiO2 56.836%, CaO 2.284%, Al2O3 25.256%, MgO 0.75%, TiO2 1.55%, MnO 0.39%; the chemical composition of pulverized coal is as follows: C 76.58%, ash 11.52%, volatile matter 13.44%, fineness (-200 mesh) 71%; the complete analysis of pulverized coal ash composition is as follows: SiO2 57.245%, CaO 5.334%, Al2O3 24.17%, MgO 2.307%, TiO2 1.553%, MnO 0.390%.

[0598] Baseline conditions and material verification results:

[0599] Ore batch: 54,000 kg, coke batch (wet weight): 10,800 kg (dry weight): 10,470 kg, coke briquettes (wet weight): 700 kg (dry weight): 680 kg. Batching standards: Standard: w([Si]) value: 0.280%; slag basicity: 1.17. Standard material rate: 9.09 batches / h; Standard coal quantity: 46,915 kg / h.

[0600] Ingredient verification results:

[0601] Sintered ore 69% (23%+23%+23%), acidic magnesia pellets 24.2% (12.1%+12.1%), low-silica lump ore 6.80%. Overall furnace feed grade TFe: 55.69%.

[0602] B. Ingredient calculation, parameter and index verification analysis:

[0603] B1. Benchmark ingredient calculation, parameter and index verification analysis:

[0604] For conventional blast furnace ore and coke batches, the chemical composition (full analysis) of various materials is as described in step A. Under the main reference parameters of the baseline raw materials (clinker rate, overall charge grade, coke and pulverized coal ash content), combined with the baseline operating parameters of step A (baseline coal quantity, baseline material rate, baseline w([Si])), the baseline operating parameters such as total air (air pressure, air volume), air temperature, and w([Si]) are not adjusted.

[0605] Under the baseline conditions in step A (assuming that the main raw material parameters are stable (the fluctuation ranges all meet the following conditions: clinker rate < ±1.0%, overall furnace feed grade < ±0.20%, coke < ±0.1%, and pulverized coal ash content < ±0.10%)), proceed directly to the baseline index determination step, following the steps below. The calculation order and results are as follows:

[0606] (1) Calculate the theoretical fuel ratio, utilization coefficient, smelting cycle, etc. under the basic conditions.

[0607] The calculated theoretical fuel ratio is 515.71 kg / t (dry basis); the utilization factor is 2.763 t / (m³). 3 .d); The smelting cycle is 58.6 batches (Tables 33-34).

[0608] Table 33 Calculation Basis Conditions and Verification of Basic Indicators

[0609]

[0610] Table 34

[0611]

[0612]

[0613] (2) Output the slag and iron composition and related intermediate process results according to the baseline conditions (assuming that the changes in raw materials and fuels are all within the required range).

[0614] Taking each batch of material as a unit, the following are the fitting formulas for the reduction rates of elements such as [Si], [Ti], [Mn], and [V] in molten iron under the predetermined w([Si]) value: (w([Si])-Si reduction rate, w([Si])-Ti reduction rate, w([Si])-Mn reduction rate, w([Si])-V reduction rate), w([Si])-desulfurization rate fitting formula, and [S] removal rate fitting polynomial formula with predetermined w([Si]) value: Figures 3-5 ):

[0615] Based on the reduction rates of the above elements (desulfurization rate, and 100% reduction rates of [P] and [As], etc.), combined with material balance, the amounts of corresponding element oxides and S, P, and As entering the molten iron are calculated. Further, the amounts of each element oxide and S, P, and As entering the slag are calculated, as well as the output slag quantity (slag ratio), alkali metals, lead, zinc, titanium, sulfur load, etc., and the theoretical slag composition (including basicity, magnesium-aluminum ratio, etc.) and theoretical pig iron composition (theoretically calculated from the corresponding element oxides entering the molten iron) are calculated (Tables 35 to 38).

[0616] Table 35 shows the reduction rate corresponding to the baseline w([Si]) based on the fitting formula between the w([Si]) value and the reduction rate of each element.

[0617]

[0618] Note: The baseline w([Si]) is the input, and the others are automatically calculated outputs.

[0619] Table 36 Output baseline mix ratio, slag quantity (slag ratio), alkali metals, lead, zinc and titanium, sulfur load under baseline w([Si])

[0620]

[0621] Table 37 Theoretical pig iron composition under output benchmark w([Si])

[0622] project Si S P Ti As V Mn unit ％ ％ ％ ％ ％ ％ ％ numerical values 0.28 0.028 0.093 0.165 0.056 0.051 0.29

[0623] Table 38 Theoretical slag composition under output baseline w([Si])

[0624] project <![CDATA[SiO2]]> CaO MgO S <![CDATA[Al2O3]]> <![CDATA[TiO2]]> <![CDATA[V2O5]]> MnO magnesium-aluminum ratio alkalinity unit ％ ％ ％ ％ ％ ％ ％ ％ times times numerical values 34.30 40.26 7.98 0.77 11.68 3.90 0.34 0.37 0.683 1.17

[0625] In this example, the corrected air volume calculation is based on the air volume corrected for actual fuel consumption (the cumulative average value of the samples is 5606.18 m³). 3 / min) and the corresponding metered air volume (the cumulative average value of the samples is 4523.11m). 3 The multiple of ( / min) is relatively stable, with a value between 1.23 and 1.25 times. Here, the conversion factor between the corrected air volume and the surface air volume is used: 5606.18 / 4523.11 = 1.24 times.

[0626] When the main reference parameters of the benchmark raw materials (clinker rate, overall furnace grade, coke ash content, and pulverized coal ash content) change beyond the stable range, the process proceeds to step B2.

[0627] B2. Analysis of batching calculations, parameters, and index verification when key verification conditions (clinker rate, overall furnace grade, coke and pulverized coal ash content) change:

[0628] Changes in the composition of the raw materials were detected. Specifically:

[0629] First change of materials:

[0630] The chemical composition of the sinter is: TFe 53.36%, SiO 25.73%, CaO 13.13%, Al 2O 31.75%, MgO 2.177%, TiO 20.526%, S 0.042%, V 2O 50.029%, MnO 0.115%, with a bulk density of 2.02 t / m³. 3The composition of the acidic magnesium oxide pellets is: TFe 59.37%, SiO2 6.756%, CaO 0.77%, Al2O3 1.785%, MgO 0.925%, TiO2 2.75%, V2O5 0.137%, MnO 0.053%; bulk density 2.30 t / m³ 3 The composition of the low-silica lump ore is: TFe 65.34%, SiO2 3.83%, CaO 0.030%, Al2O3 1.08%, MgO 0.010%, TiO2 0.010%, V2O5 0.030%, MnO 0.199%, with a bulk density of 2.30 t / m³. 3 .

[0631] The chemical composition of the coke is: C 85.05%, ash content 14.31%, and bulk density 0.63 t / m³. 3 The complete analysis of coke ash composition is as follows: SiO2 55.868%, CaO 2.985%, Al2O3 24.538%, MgO 0.553%, TiO2 390%, MnO 0.39%; the chemical composition of pulverized coal is as follows: C 77.62%, ash 11.27%, volatile matter 13.22%, fineness (-200 mesh) 72%; the complete analysis of pulverized coal ash composition is as follows: SiO2 57.245%, CaO 5.475%, Al2O3 23.85%, MgO 2.38%, TiO2 1.55%, MnO 0.390%.

[0632] Second change of materials:

[0633] The chemical composition of the sinter is: TFe 53.80%, SiO 25.73%, CaO 13.13%, Al 2O 31.75%, MgO 2.21%, TiO 20.533%, S 0.04%, V 2O 50.021%, MnO 0.104%, with a bulk density of 2.05 t / m³. 3 The composition of the acidic magnesium oxide pellets is: TFe 59.61%, SiO2 6.536%, CaO 0.70%, Al2O3 1.755%, MgO 0.859%, TiO2 2.684%, V2O5 0.143%, MnO 0.049%; bulk density 2.30 t / m³ 3 The composition of the low-silica lump ore is: TFe 65.34%, SiO2 3.83%, CaO 0.030%, Al2O3 1.08%, MgO 0.010%, TiO2 0.010%, V2O5 0.030%, MnO 0.199%, with a bulk density of 2.30 t / m³. 3 .

[0634] The chemical composition of the coke is: C 85.33%, ash content 14.23%, and bulk density 0.64 t / m³. 3The complete analysis of coke ash composition is as follows: SiO2 56.83%, CaO 2.286%, Al2O3 25.256%, MgO 0.786%, TiO2 1.55%, MnO 0.39%; the chemical composition of pulverized coal is as follows: C 77.07%, ash 11.38%, volatile matter 13.31%, fineness (-200 mesh) 71%; the complete analysis of pulverized coal ash composition is as follows: SiO2 57.24%, CaO 5.48%, Al2O3 23.85%, MgO 2.38%, TiO2 1.55%, MnO 0.370%.

[0635] In this example, the grade of sintered ore and the ash content of coke and pulverized coal are subject to change. The batching and material verification should be carried out according to step A. The verification data is as follows: Ore batch: 54,000 kg, Coke batch (wet weight): 10,800 kg (dry weight): 10,470 kg, Coke briquettes batch (wet weight): 700 kg (dry weight): 680 kg (Note: The coke batch needs to be adjusted based on the composition of the raw materials and the grade and clinker ratio after the initial batching).

[0636] Batching baseline: w([Si]) value: 0.280%; slag basicity: 1.14. Baseline material rate: 9.09 batches / h; baseline coal quantity: 46915 kg / h (Note: Adjustments are required based on changes in pulverized coal ash content). Further adjustments will be made based on the batching results (according to the target slag basicity) after adjustments to coke batch and hourly coal quantity.

[0637] Ingredient verification results:

[0638] Variable feedstock 1: 67.5% sinter (22.5% + 22.5% + 22.5%), 24.10% acidic magnesia pellets, and 8.4% low-silica lump ore. Overall furnace feed grade TFe: 55.70%.

[0639] Variable feedstock 2: 68.1% sinter (22.7% + 22.7% + 22.7%), 24.20% acidic magnesia pellets, and 7.7% low-silica lump ore. Overall furnace feed grade TFe: 55.99%.

[0640] In this example, for feedstock change 1: the main parameters of the raw materials exceed the stable range (clinker rate decreases by 1.6% > ±1.0%, overall feed grade increases by 0.001%, coke ash content decreases by 0.18% > ±0.1%, pulverized coal ash content decreases by 0.25% > ±0.1%); for feedstock change 2: the main parameters of the raw materials exceed the stable range (clinker rate increases by 0.70%, overall feed grade increases by 0.29% > ±0.20%, coke ash content decreases by 0.08%, pulverized coal ash content increases by 0.11% > ±0.1%). The baseline operating parameters are adjusted according to the magnitude of the changes (including the determination of the baseline hourly coal quantity and coke batch after the change in raw materials):

[0641] The following parameters were calculated in sequence (for two material changes): the hourly coal quantity after factor changes, the theoretical iron content of the batch, the theoretical coal ratio, the new coke ratio and coke-to-coke ratio, the determination of the new coke batch, the theoretical fuel ratio of the batch under changing conditions, the utilization coefficient, the smelting cycle, and the pulverized coal injection rate (see Tables 39 to 44 for details).

[0642] The concepts, calculation methods, and formulas involved in the calculation process are the same as in Example 1.

[0643] (1) Calculate the theoretical fuel ratio, utilization coefficient, smelting cycle, etc. after the change of calculation conditions.

[0644] The results obtained from changing material 1 and changing material 2 are shown in Table 39.

[0645] Table 39 shows the calculation results after changes in raw materials and fuels (compared to baseline conditions) and the verification of their indicators.

[0646]

[0647] Table 40

[0648]

[0649] Note: In this example, after adjusting the coke batch and hourly coal quantity, the verification target (alkalinity) has been achieved, and the aforementioned furnace charge structure and proportioning are maintained.

[0650] (2) Slag and iron composition and related intermediate process results after adjusting the furnace charge structure ratio, coke batch, and hourly coal quantity according to changes in raw material and fuel conditions.

[0651] After the material change (each time), taking each batch of material as a unit, the reduction rates of elements such as [Si], [Ti], [Mn], and [V] obtained under the predetermined w([Si]) value in the molten iron are fitted with (w([Si])-Si reduction rate, w([Si])-Ti reduction rate, w([Si])-Mn reduction rate, and w([Si])-V reduction rate), w([Si])-desulfurization rate fitting relationship, and [S] removal rate fitting polynomial relationship with predetermined w([Si]) are mentioned above. Figures 8-12 ).

[0652] In the same step B1, output the slag quantity (slag ratio), alkali metals, zinc and titanium, sulfur load, etc. after the change of raw materials and fuels, as well as the theoretical slag composition (including basicity, magnesium-aluminum ratio, etc.) and theoretical pig iron composition (Tables 41 to 44).

[0653] Table 41 shows the reduction rate corresponding to the baseline w([Si]) based on the fitting formula between the w([Si]) value and the reduction rate of each element.

[0654]

[0655] Note: The baseline w([Si]) is the input, and the others are automatically calculated outputs.

[0656] Table 42 Output variation ratio, slag quantity (slag ratio), alkali metal, zinc and titanium, sulfur load under baseline w([Si])

[0657] project Slag volume scumbag K load Na loading Zn load S load Ti load Slag alkalinity unit Kg / pi Kg / t Kg / t Kg / t Kg / t Kg / t Kg / t times Baseline conditions 12780 404 2.65 1.09 0.79 3.41 11.08 1.17 Raw material changes 1 12666 400 2.63 1.06 0.77 3.37 10.77 1.17 Raw material changes 2 12392 389 2.62 1.16 0.75 3.35 10.95 1.17

[0658] Table 43 Theoretical pig iron composition under the baseline w([Si]) after changes in output raw materials and fuels.

[0659] project Si S P Ti As V Mn unit ％ ％ ％ ％ ％ ％ ％ Baseline conditions 0.28 0.028 0.093 0.165 0.056 0.051 0.29 Raw material changes 1 0.28 0.028 0.096 0.160 0.053 0.46 0.31 Raw material changes 2 0.28 0.027 0.096 0.158 0.059 0.039 0.30

[0660] Table 44 Theoretical slag composition under the baseline w([Si]) after outputting changes in raw materials.

[0661] project <![CDATA[SiO2]]> CaO MgO S <![CDATA[Al2O3]]> <![CDATA[TiO2]]> <![CDATA[V2O5]]> MnO magnesium-aluminum ratio alkalinity unit ％ ％ ％ ％ ％ ％ ％ ％ times times Baseline conditions 34.30 40.26 7.98 0.77 11.68 3.90 0.34 0.37 0.683 1.17 Raw material changes 1 34.84 40.72 7.93 0.76 11.79 3.83 0.43 0.36 0.673 1.17 Raw material changes 2 34.47 40.36 7.65 0.79 11.70 4.00 0.40 0.39 0.649 1.17

[0662] The corrected air volume ratio is the same as in step B1 (both are 1.24 times).

[0663] During the smelting process, the reference feed rate often changes, and it is controlled in conjunction with "oxygen-regulated feed" to proceed to step C.

[0664] C. Input the oxygen enrichment adjustment amount to precisely control the actual material flow rate:

[0665] Data collection and calculation output should be performed according to the following steps and methods (the determination and adjustment of whether adjustments are needed should be made according to the definition principles of step C (C1~C2).

[0666] C2. Determining the amount of oxygen enrichment and accurately controlling the actual material flow rate.

[0667] (3) Parameters to be collected (including calculated indirect smelting parameters and fuel parameters). Directly collected comprehensive air supply parameters include: surface air volume, humidity, air pressure, top pressure, air temperature, tuyer area, etc.; indirect smelting parameters (automatically calculated) include corrected air volume obtained based on the table-actual air volume correction coefficient (or fitting polynomial), as well as the oxygen enrichment rate, theoretical combustion temperature, permeability index, and blast kinetic energy after correcting the air volume, etc. Fuel parameters to be collected include: batch weight, composition, and combustion rate before tuyer; hourly coal powder quantity, coal powder composition, and combustion rate before tuyer. Note: Calculated based on hourly cumulative quantity (hourly cumulative quantity is automatically collected by computer at certain time intervals).

[0668] (2) Determination of oxygen enrichment adjustment amount and precise control of actual material speed. Input, calculate and output the results of precise control of material speed and intermediate process data of oxygen enrichment according to the steps. The steps for determining the oxygen enrichment adjustment amount (calculation order) are: original oxygen enrichment amount → oxygen enrichment adjustment amount (input) → new oxygen enrichment amount → oxygen enrichment rate after oxygen adjustment and correction of air volume (combined with the comprehensive blower parameters and fuel parameters in step (1)) → (obtained by combining the air volume per ton of coal consumption, air volume per hour of coal consumption, air volume per ton of coke consumption, and residual air volume after coal burning obtained from the parameters in step (1)) theoretical material speed after oxygen adjustment → judgment of oxygen adjustment effect.

[0669] The concepts, calculation methods, and formulas involved are the same as in Example 1. Repeatedly input the oxygen enrichment adjustment amount until the theoretical feed rate output value meets the requirements.

[0670] The results and process parameters obtained in this example are shown in Table 45 (based on data and operations from 3 natural shifts (including two material changes)).

[0671] Table 45 Data Acquisition (Calculation) and Process / Effects of Precise Oxygen Control of Material Rate

[0672]

[0673]

[0674] Table 46

[0675]

[0676]

[0677] In this example: Based on the principle of precise control of material flow rate during oxygen adjustment, the first shift (0:00 to 7:00) involves oxygen adjustment at 3:00. Based on the adjusted oxygen level, the post-adjustment oxygen enrichment is obtained. Following the aforementioned calculation method, the system automatically combines relevant parameters such as the corrected air volume and air consumption per ton of coke and coal to calculate and output the post-adjustment material flow rate control effect (oxygen adjustment reaction time 1 hour). The result after one oxygen enrichment adjustment is: the batch size exceeds the limit by one batch for two consecutive hours; the first oxygen adjustment was -700m³. 3 / h, the difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is -0.12 batches / h (the batches per shift are reduced by 1.00 batches), the feed rate after reaction is reduced to 8.98 batches / h, the difference from the specified feed rate (9 batches / h) is 0.02 batches / h; the actual feed rate is 9.0 batches / h, which meets the specified oxygen adjustment criteria (until the theoretical feed rate output results obtained simultaneously reach (the principle for judging the effect of oxygen adjustment): (1) the difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is defined as 0.1 to 0.3 batches (increase or decrease); (2) |theoretical feed rate after oxygen adjustment - specified feed rate| < 0.3 batches / h, the predicted reduction in batches per shift is 1.00 batches / shift (defined as (±) 0.3 to 1.5 batches)). No situation requiring adjustment of oxygen enrichment occurred in the second shift. Similarly, oxygen was adjusted once during the third shift (16:00-23:00), at 17:00. Because the total material rate for the past two hours was 1.0 batch below the specified rate, the oxygen adjustment was +600m³. 3 / h, the difference between the theoretical feed rate after oxygen adjustment and the theoretical feed rate before oxygen adjustment is +0.06 batches / h. The expected feed rate after reaction is 8.93 batches / h, which is 0.07 batches / h different from the specified feed rate (9 batches / h). The actual feed rate after reaction reaches the standard (9.0 batches / h). The predicted increase in batches per shift is 0.50 batches / shift (defined between (±) 0.3 and 1.5 batches). After that, the feed rate reaches the range that does not need to be adjusted and continues.

[0678] The input oxygen enrichment adjustment amount meets the requirements, and based on the theoretical output obtained after oxygen adjustment (the utilization coefficient is calculated to be 3.75 t / (m²) based on the hourly average theoretical material rate), the yield is as follows: 3 .d)) and the planned output (planned 3.77t / (m 3 The absolute value of the deviation rate of .d) is used for verification. In this example, it is 0.72% < ±1.50%, and the theoretical fuel ratio is <5kg / t under the same raw material conditions. Once the material rate control effect is achieved, the process proceeds to step C3 and then to the next cycle, continuing the process.

[0679] C3. Verification of the effect of precise oxygen regulation and material rate control

[0680] The verification standard for the daily feed batch is defined as follows: the absolute value of the error rate between any two of the actual daily feed rate, the specified daily feed rate, and the theoretical daily feed rate is <1.50% (Table 47). The theoretical combustion temperature, kinetic energy, and other parameters are all within the specified range of smelting parameters. Satisfied, proceed with the process.

[0681] Table 47 Verification of the Effect of Precise Oxygen Regulation on Material Rate Control

[0682]

[0683]

[0684] The theoretical output calculated based on the theoretical feed rate was compared with the actual daily output on the verification day for this example (Table 48), and both met the required range. The concepts, calculation methods, and formulas of theoretical output and theoretical indicators are the same as in Example 1.

[0685] During operation, it was found that the theoretical fuel ratio fluctuated within ±5 kg / t under the same raw material conditions.

[0686] Table 48 Comparison and Verification of Average Theoretical Value and Actual Value in This Example

[0687]

[0688] D. Following the previous steps (preliminary verification of blast furnace condition, adjustment of coke batch (including coke briquettes), adjustment of oxygen and control of materials, adjustment of coal and control of temperature), the raw materials and smelting parameters are fed into the furnace, and the smelting parameters are adjusted: precise control of material rate, accurate control of furnace temperature (w([Si]) value of molten iron), control and calculation of slag and iron composition, and real-time theoretical prediction and pre-control of indicators). In this example, the process definition conditions of each step meet the requirements and are within the error range, and the materials are fed into the furnace for smelting according to the material sequence.

[0689] Furnace smelting and parameter control steps:

[0690] E1. The total amount of the four types of ore mentioned in A is 100% (in this example, titanium slag smelting in vanadium-titanium ore), and coke with high ash and sulfur content (including coke briquettes) is fed into the blast furnace in the usual amount. After checking the blast furnace condition, under constant blast temperature and full blast conditions, "quantitative oxygen adjustment and precise control of material rate" is adopted. The number of times the oxygen enrichment is adjusted in each shift is ≤3 times (in this example, it is adjusted once in the first shift, 0 times in the second shift, and 1 time in the third shift), so as to control |daily theoretical batch - daily specified batch| / daily specified batch <1.50% (0.23% in this example).

[0691] D2. Smelting shall be carried out under the following conditions:

[0692] This example illustrates the intensified smelting of a large blast furnace in a conventional mine. The smelting parameters are as follows: hot blast pressure 0.376–0.385 MPa (all blast), top pressure 0.184–0.192 MPa, hot blast temperature 1220℃ (top blast temperature), and furnace feed air volume (corrected) 5550–5640 m³ / h. 3 / min, oxygen enrichment is 13300~14000m 3 / h, pulverized coal injection rate is 157-170 kg / t iron (raw material analysis exceeded the specified changes twice, pulverized coal injection rate is 30.98%-31.97%); ore batch 54.0 tons, coke batch (dry basis) 10.399-10.470 tons; coke slag batch (dry basis) 0.68 tons; w([Si]) 0.21-0.31% (ordinary ore smelting), slag basicity 1.16-1.18, molten iron temperature 1440-1480℃. All are within the specified range.

[0693] This example demonstrates adjustments made to the coke batch according to defined principles and methods. The effects of these adjustments are reflected within one smelting cycle.

[0694] In this example, the hourly oxygen enrichment (precisely adjusted feed rate) was adjusted twice within three shifts: the adjustment amount of the hourly oxygen enrichment was less than 10.0% of the original total oxygen enrichment. The effect of this adjustment took one hour to take effect.

[0695] The completion times for the above-mentioned influencing factors are as follows: furnace grade, slag basicity, clinker rate, and top pressure are all within one smelting cycle (4.5–5.5 hours, automatically calculated); pulverized coal injection is 3.5 hours; and air volume, air temperature, and humidity are 1 hour. The adjustment point is when the change in the corresponding influencing factor coincides with the time it takes for the adjustment factor to take effect, based on maintaining a relatively stable overall fuel ratio (the absolute value of the raw material composition deviation under the same raw material conditions (when no coke batch adjustment is required) <5 kg / t).

[0696] D3. Smelting shall be carried out under the following conditions:

[0697] In actual smelting processes, the slag ratio is 380–410 kg / t, the magnesium-aluminum ratio in the slag is 0.65–0.69, the slag basicity is 1.16–1.18, the constant blast temperature is 12500℃, the oxygen enrichment rate (after adjusting for blast volume) is 2.97–3.15%, and the permeability index is 28000–3500 m³ / s. 3 / (min.MPa), theoretical combustion temperature 2321~2331℃, actual blower velocity 273~278m / s, actual blower kinetic energy (after air volume correction) 20000~21500kg.m / s, theoretical hourly material rate 8.86~9.27 batches / h.

[0698] In this example, when oxygen is used to regulate the feed and coal to regulate the temperature, in addition to the deviation values ​​meeting the aforementioned requirements for feed rate and silicon deviation, the direct smelting parameters such as air volume, air pressure, and top pressure, as well as the indirect smelting parameters such as permeability index, theoretical combustion temperature, and blast kinetic energy obtained through automatic calculation, are all within the specified range. For vanadium-titanium ore smelting blast furnaces, the lower limit of w([Si]) and the upper limit of w(MgO) / w(Al2O3) are used.

[0699] The actual smelting results in this example have been corrected. The hourly theoretical and actual material rate, the theoretical calculated control and actual w([Si]) value, the theoretical and actual slag-iron composition, the theoretical and actual furnace output (day), and the theoretical and actual fuel ratio comparison and verification all meet the control requirements. No changes or corrections to the relevant parameters are needed.

[0700] The foregoing has shown and described the basic principles, main features, and advantages of the present invention. Those skilled in the art should understand that the present invention is not limited to the above embodiments. The embodiments and descriptions in the specification are merely illustrative of the principles of the invention. Various changes and modifications can be made to the invention without departing from its spirit and scope, and all such changes and modifications fall within the scope of the present invention as claimed. The scope of protection of this invention is defined by the appended claims and their equivalents.

Claims

1. A smelting method for quantitatively and precisely controlling the burden rate of a blast furnace by patterning, characterized by, It comprises the following steps: A, reference burden: the smelting is ordinary ore smelting or medium titanium slag smelting; When it is ordinary ore smelting, the ordinary ore furnace burden used comprises the following components in terms of mass percentage: sinter 65~72%, high-silicon acid pellet 20~28%, low-silicon lump ore 0~10%; total 100%; ore batch 53000~55000kg; When it is medium titanium slag smelting, the vanadium-titanium ore burden used comprises the following components in terms of mass percentage: sinter 60~65%, vanadium-titanium pellet 30~35%, low-silicon lump ore 0~5%, total 100%; ore batch 320000~34000kg; When it is ordinary ore smelting or medium titanium slag smelting, the coke batch is 7200~11000kg / batch of dry basis of coke; the coke nut batch is 450~700kg / batch of dry basis of coke; the pulverized coal injection amount is 21.5~48.5t / h; B, burden calculation, parameter, index checking analysis: B1, reference burden calculation, parameter, index checking analysis: The wind pressure, wind volume, wind temperature and w [Si] is constant, wherein the wind temperature is the highest stable wind temperature; if the factor fluctuation range of ordinary mineral smelting or medium titanium slag smelting meets: clinker rate < ±1.0%, comprehensive charging grade < ±0.20%, coke ash < ±0.1%, and coal ash < ±0.10%; then: (1) calculate the theoretical fuel ratio, utilization coefficient and smelting period; (2) calculate the theoretical pig iron composition, theoretical slag composition and basicity, magnesium-aluminum ratio; (3) calculate the multiple conversion coefficient of corrected air volume and table air volume, and the oxygen enrichment rate after correction is 2.90~5.00%; B2, burden calculation, parameter, index checking analysis when the main checking conditions change: The wind pressure, wind volume, wind temperature and w ([Si] is constant, wherein the highest stable wind temperature is the wind temperature; if any one of the factor fluctuation ranges of ordinary mineral smelting or medium titanium slag smelting does not satisfy the following conditions: clinker rate < ±1.0%, comprehensive charging grade < ±0.20%, coke ash < ±0.1%, and coal ash < ±0.10%, then: (1) calculate the hourly coal amount, batch theoretical iron amount, theoretical coal ratio, coke ratio, coke nut ratio, coke batch, theoretical fuel ratio, utilization coefficient, smelting period and coal injection rate after the factor change; (2) calculate the theoretical pig iron composition, theoretical slag composition and basicity, magnesium-aluminum ratio; C, input oxygen adjustment amount precise control of actual material speed: In the blast furnace smelting process, the material speed difference between the actual material speed and the specified reference material speed is checked, and the principle of whether to adjust the material speed is: (1) the absolute value of the difference between the actual material speed and the specified reference material speed for two consecutive hours ≥0.5 batch / h; (2) the difference between the actual material speed and the specified reference material speed for a single hour ≥1.0 batch / h; (3) the absolute value of the difference between the specified material speed and the actual material speed for two consecutive hours ≥1.0 batch; Any one of the above three conditions needs to be adjusted, otherwise it does not need to be adjusted; The adjustment method is: (1) collect comprehensive air supply parameters, indirect smelting parameters and fuel parameters; (2) input oxygen adjustment amount on the basis of the original oxygen amount to adjust the oxygen, obtain the new oxygen amount; then calculate the oxygen adjustment correction air volume and the theoretical material speed through the collected comprehensive air supply parameters, indirect smelting parameters and fuel parameters, and then determine the oxygen adjustment effect; The determination conditions are: 1) the difference between the theoretical material speed after oxygen adjustment and the theoretical material speed before oxygen adjustment is within the range of 0.1~0.3 batches; 2) |theoretical material speed after oxygen adjustment-specification material speed|<0.3 batch / h, and the batch growth amount is predicted; 3) the input oxygen adjustment amount makes the theoretical material speed meet the material speed control value requirement, and the absolute value of the deviation rate of the theoretical output obtained after oxygen adjustment from the planned required output is <±1.50%; If the three conditions 1) ~ 3) are met at the same time, and the judgment result is that adjustment is not needed after checking the difference between the actual stock rate after oxygen adjustment and the specified reference stock rate, then stock rate effect checking is needed; the theoretical combustion temperature, blast kinetic energy, permeability index and smelting period after oxygen adjustment are calculated at the same time; The specific method of stock rate effect checking is: For daily stock checking, the standard is defined as: the absolute value error rate of the difference between any two of the daily actual stock rate, the daily specified stock rate and the daily theoretical stock rate < 1.50%; if all are met, continue the process; The daily theoretical coal ratio and coke ratio are compared and checked with the daily actual coal ratio and coke ratio, and the theoretical daily output calculated according to the theoretical stock rate is compared and checked with the daily actual output; if the deviation rate of the difference between the theoretical daily output and the daily actual output < 1.50%, then the checking is passed, and the process continues; D. Charging smelting and parameter control: During the charging smelting process, the number of times of adjusting the oxygen enrichment amount in each shift is controlled to be ≤ 3, and the control | daily theoretical stock batch - daily specified stock batch | / daily specified stock batch < 1.50%; Smelting conditions: hot blast pressure is 0.30~0.39MPa, top pressure is 0.155~0.195Mpa, hot blast temperature is 1150℃~1250℃, corrected into the furnace air volume is 3200~5700m 3 / min, oxygen enrichment is 9400~15000m 3 / h, coal injection amount is 135~165kg / t iron, coal injection rate is 22.0~35.0%; ore batch is 33.0~55.0 tons, coke batch is 7.2~11.0 tons in dry basis, coke briquette batch is 0.45~0.70 tons in dry basis; w [Si]0.055~0.35%, slag basicity is 1.10~1.18, molten iron temperature is 1420~1480℃; during smelting, slag ratio is 380~480kg / t, magnesium-aluminum ratio in slag is 0.65~0.95, slag basicity is 1.10~1.18, control wind temperature is stable, oxygen enrichment rate is 2.90%~5.0%, permeability index is 18000~22000m 3 / (min.MPa), theoretical combustion temperature is 2300~2400℃, actual blast speed is 255~275m / s, actual blast kinetic energy is 17000~22000kg.m / S, theoretical hourly material speed is 8.5~10.0 batches.

2. The smelting method of claim 1, wherein, The sinter composition comprises, by mass percentage, 52.0-54.0% of TFe, 5.5-6.5% of SiO2, 13.0-13.5% of CaO, 1.75-2.19% of Al2O3, 2.30-2.90% of MgO, 0.40-1.35% of TiO2, 0.045%-0.055% of S, 0.165-0.150% of V2O5, 0.045%-0.055% of MnO, and the balance of inevitable impurities, and the bulk specific gravity is 1.90-2.10 t / m 3 ; The vanadium-titanium pellet composition comprises, in percentage by mass, 53.5-57.5% of TFe, 4.5-5.5% of SiO2, 0.55-1.35% of CaO, 2.20-2.90% of Al2O3, 2.35-2.90% of MgO, 6.40-11.0% of TiO2, 0.55-0.75% of V2O5, 0.23-0.25% of MnO, and the balance is inevitable impurities; the bulk specific gravity is 2.20-2.30 t / m 3 ; The high-silicon acid pellet composition comprises, by mass percentage, 58.5-60.0% of TFe, 6.5-7.5% of SiO2, 0.5-1.5% of CaO, 1.80-2.10% of Al2O3, 1.0-1.5% of MgO, 2.50-3.50% of TiO2, 0.165-0.150% of V2O5, 0.045-0.055% of MnO, and the balance is inevitable impurities, and the bulk specific gravity is 2.15-2.35 t / m 3 ; The low-silicon lump ore composition comprises, by mass percentage, 64.0-66.0% of TFe, 3.0-4.5% of SiO2, 0.03-0.05% of CaO, 1.00-1.50% of Al2O3, 0.01-1.0% of MgO, TiO2<1.0%, 0.030-0.050% of V2O5, 0.110-0.160% of MnO, and the balance is inevitable impurities, and the bulk specific gravity is 2.2-2.4 t / m 3 .

3. The smelting method for quantitatively and systematically controlling the blast furnace charge rate according to claim 1, characterized in that, The comprehensive blast parameters include: table air volume, humidity, air pressure, top pressure, air temperature and tuyere area; the indirect smelting parameters include corrected air volume and oxygen enrichment rate after correction, theoretical combustion temperature, permeability index and blast kinetic energy; the fuel parameters include batch weight, composition of coke and coke butter, and pre-tuyere combustion rate, as well as hourly coal powder volume, coal powder composition and pre-tuyere combustion rate.

4. The smelting method for quantitatively and systematically controlling the blast furnace charge rate according to claim 1, characterized in that, Also included is step E, actual smelting result return correction: according to the actual smelting result obtained in step E, according to the hourly theory and actual material speed, theoretical calculation control and actual w [Si] value, theoretical and actual slag iron composition, theoretical and actual tapping output, theoretical and actual fuel ratio, continue smelting after correction of calculation parameters according to step B~D calculation method.

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