WO2021237946A1 - 一种底吹O2-CO2-CaO转炉炼钢过程动态控制方法 - Google Patents

一种底吹O2-CO2-CaO转炉炼钢过程动态控制方法 Download PDF

Info

Publication number
WO2021237946A1
WO2021237946A1 PCT/CN2020/108455 CN2020108455W WO2021237946A1 WO 2021237946 A1 WO2021237946 A1 WO 2021237946A1 CN 2020108455 W CN2020108455 W CN 2020108455W WO 2021237946 A1 WO2021237946 A1 WO 2021237946A1
Authority
WO
WIPO (PCT)
Prior art keywords
blowing
gas
converter
cao
flow rate
Prior art date
Application number
PCT/CN2020/108455
Other languages
English (en)
French (fr)
Inventor
朱荣
李伟峰
魏光升
冯超
董凯
刘润藻
周赟
阮强
魏国立
王德勇
朱青德
韩志国
Original Assignee
北京科技大学
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 北京科技大学 filed Critical 北京科技大学
Priority to US17/440,648 priority Critical patent/US20220325368A1/en
Publication of WO2021237946A1 publication Critical patent/WO2021237946A1/zh

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
    • C21C5/00—Manufacture of carbon-steel, e.g. plain mild steel, medium carbon steel or cast steel or stainless steel
    • C21C5/28—Manufacture of steel in the converter
    • C21C5/30—Regulating or controlling the blowing
    • C21C5/35—Blowing from above and through the bath
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B7/00—Blast furnaces
    • C21B7/16—Tuyéres
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
    • C21C5/00—Manufacture of carbon-steel, e.g. plain mild steel, medium carbon steel or cast steel or stainless steel
    • C21C5/28—Manufacture of steel in the converter
    • C21C5/42—Constructional features of converters
    • C21C5/46—Details or accessories
    • C21C5/48—Bottoms or tuyéres of converters
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
    • C21C7/00—Treating molten ferrous alloys, e.g. steel, not covered by groups C21C1/00 - C21C5/00
    • C21C7/0037—Treating molten ferrous alloys, e.g. steel, not covered by groups C21C1/00 - C21C5/00 by injecting powdered material
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
    • C21C2300/00—Process aspects
    • C21C2300/06—Modeling of the process, e.g. for control purposes; CII
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/25—Process efficiency

Definitions

  • the present disclosure relates to the technical field of steelmaking technology, in particular to a method for dynamic control of a bottom-blowing O 2 -CO 2 -CaO converter steelmaking process.
  • the converter steelmaking process can process various components of molten iron and steel scrap.
  • the charging material can be adjusted flexibly, and the blowing cycle is short, and the production capacity is strong. Therefore, it has become the most widely used steelmaking method in the world.
  • the converter steelmaking process uses top-blowing oxygen as a means of heating and stirring the molten pool, combined with bottom-blowing to strengthen the molten pool stirring, to provide better kinetic conditions for the metallurgical reaction, and to produce qualified end-point carbon content, phosphorus content and temperature Molten steel.
  • the melting pool stirring in the conventional converter smelting process is not strong enough, and there is still a large room for improvement in the metallurgical effect and steelmaking cost.
  • the bottom-blown O 2 -CaO converter steelmaking process has enhanced molten pool stirring and good dephosphorization effect, but there are a series of problems: 1) The bottom blowing O 2 reacts with the silico-manganese elements in the molten pool to generate oxides into the slag in the early stage of blowing. The amount of floating gas is greatly reduced and the molten pool agitation is weak; 2) The dephosphorization effect is good, but the injection rate of CaO powder is not accurate, and the effective utilization rate still needs to be improved; 3) The proportion of bottom blowing CO 2 can reduce the bottom blowing fire point area Temperature, but the mixing ratio is not accurate. If the ratio of bottom blowing CO 2 is too large, the end temperature will be low. If the ratio of bottom blowing CO 2 is too small, the effect of protecting the bottom blowing gun and enhancing the stirring of the molten pool will not be achieved.
  • Patent Application No. 201810013096.3 discloses a converter steelmaking process. This method introduces a converter steelmaking method with a combination of feeding and top-blowing oxygen lances in the conventional converter steelmaking process, which reduces the metal during constant pressure and variable lance position oxygen supply. The problem of loss. In the actual blowing, this method has higher requirements for process operation, limited mixing in the molten pool, and unstable end-point molten steel composition and temperature.
  • the present disclosure proposes a bottom-blowing O 2 -CO 2 -CaO converter steelmaking process dynamic control method, which solves the existing conventional converter steelmaking process with large end-point composition fluctuations, molten steel peroxidation, long blowing time, etc. technical challenge.
  • the bottom blowing gun of the bottom blowing O 2 +CO 2 +CaO converter process is a concentric ring seam tube.
  • O 2 +CO 2 +CaO is blown into the molten pool from the center hole of the bottom blowing gun, and the bottom blowing gun is circularly seamed.
  • CH 4 is blown into the molten pool, and the top blowing oxygen lance blows high-speed O 2 into the molten pool.
  • the converter steelmaking is based on the conservation of materials.
  • the composition of molten steel in the process is predicted.
  • the blowing process is divided into three stages: the early stage and the middle stage by the decarburization speed, and the top blowing oxygen amount, bottom blowing gas ratio and lime powder are dynamically adjusted in stages according to the target composition requirements of the blowing end point.
  • the converter bath On the basis of strengthening the stirring effect of the converter bath, it promotes the balance of the slag-gold reaction; at the same time, it avoids the over-oxidation at the end of the converter, reduces the consumption of deoxidized alloys, reduces the number of inclusions in the steel, improves the quality of the molten steel, and improves Based on the efficiency of the slag-gold reaction, the converter smelting cycle is shortened, and the cost is again reduced.
  • a method for dynamic control of bottom-blowing O 2 -CO 2 -CaO converter steelmaking process which is characterized in that the bottom-blowing O 2 -CO 2 -CaO converter conversion process is divided into early stage, middle stage, and late stage according to the decarburization rate v C three stages; data calculation module based on the total amount charged into the furnace m total, the molten iron into the furnace temperature T 0-1, carbon content [% C] 0-1, the silicon content [% Si] 0-1, scrap ratio ⁇ , The carbon content in scrap steel [%C] 0-2 , silicon content [%Si] 0-2 , target carbon content [%C] f and target temperature T f parameters to calculate the oxygen consumption, CO 2 ratio and The amount of lime powder injected; according to the charge structure, the temperature rise rate of the molten pool v T and the decarburization rate v C , the central control system is used to formulate the blowing operation process in the early stage of the blowing; the blowing process is calculated by the de
  • the CO 2 calculation module calculates the CO 2 mixing ratio through the bottom blowing fire point temperature calculation model and the dephosphorization model, and then formulates the middle and later stages of the blowing operation Process, reduce the temperature of the fire zone, strengthen the stirring of the molten pool, and promote the reaction balance of the slag metal in the molten pool.
  • the end point of blowing is determined by the decarburization rate v C , and the bottom blowing gas parameters are adjusted, and then the steel is poured out of the furnace.
  • the temperature of the fire point area can be reduced, the life of the bottom blowing gun can be extended, and the stirring of the molten pool can be enhanced according to different blowing stages, which can achieve rapid decarburization, high efficiency dephosphorization and avoid molten steel over-oxidation, shorten the blowing time, The purpose of stabilizing the composition of the molten steel at the end of the blowing and reducing production costs.
  • the bottom blowing gun is a concentric ring-slit pipe, and the center tube uses O 2 + CO 2 mixed gas as the carrier gas to blow lime powder directly into the bottom of the converter In the molten pool, the annular slot is sprayed with cooling shielding gas.
  • the gas can be CH 4 , CO 2 , N 2 , and Ar. Combining the converter charge composition and flue gas composition, predict the composition and temperature of the molten steel during the blowing process.
  • the target steel composition and temperature requirements calculate the CO 2 mixing amount through the bottom blowing fire point temperature calculation model and dephosphorization model , Based on the decarburization rate of the molten pool, and dynamically adjust the proportion of CO 2 in the bottom blowing gas in stages.
  • control steps of the method described above are as follows:
  • Step 1 Obtain the converter charge structure, key component data and target parameters through the data acquisition system, and transmit them to the data calculation module, and use the central control system to formulate and control the early-stage operation process of the converter;
  • Step 2 In the early stage of blowing, according to the operating process established in Step 1, the top blowing oxygen lance is lowered into the furnace to blow oxygen, and the center tube of the bottom blowing lance uses O 2 + CO 2 mixed gas as the carrier gas to blow lime powder into the melting In the tank, the bottom blowing gun is blown into the ring seam of CH 4 as a protective gas, and the decarburization rate obtained by the flue gas composition data and the decarburization rate calculation module Determine the end node of the early stage of blowing,
  • Step 3 In the middle of blowing, the decarburization rate obtained through step 2 Determine the start time of the mid-term blowing, and then formulate the mid-term operation plan,
  • Step 4 In the late stage of blowing, pass the decarburization speed Determine the starting node of the later stage of blowing, use the CO 2 calculation module to calculate the amount of CO 2 mixed in the later stage according to the heating rate v T , and then formulate the later stage operation plan;
  • Step 5 The end of blowing, according to the decarburization rate Determine the time node for the end of blowing
  • Step 6 Switch bottom blowing center hole gas to Ar, flow rate 2500-18400Nm 3 /h, bottom blowing ring seam gas switch to Ar, flow rate 200-1790Nm 3 /h, reduce bath agitation, accelerate slag-iron separation, and pour The furnace is tapped.
  • the specific operation scheme of the early stage of blowing in step (2) is as follows: the bottom lime powder blowing speed is 300-900kg/min; the top blowing oxygen flow rate is 10000-63000Nm 3 /h, the bottom blowing center hole O 2 + The total flow of CO 2 is 3000-18900Nm 3 /h, of which the proportion of CO 2 is 0-100%, the flow of CH 4 in the bottom blowing ring seam is 300-1890Nm 3 /h, and the end time of blowing is 3-6min.
  • the specific operation plan of the middle stage of the blowing in step (3) is as follows: the bottom lime powder injection speed is 300-900kg/min, and the powder injection is stopped for 8-10min; the top blowing oxygen flow rate is 9000-62000Nm 3 /h, the bottom The flow rate of O 2 in the center hole of blowing is 3000-18900Nm 3 /h, the ratio of CO 2 is 0, the flow rate of CH 4 in the bottom blowing ring seam is 300-1890Nm 3 /h, and the end time of middle blowing is 9-13min.
  • the specific operation plan of the later stage of blowing in step (4) is as follows: the bottom lime powder injection speed is 0kg/min; the top blowing oxygen flow rate is 9000-62000Nm 3 /h, the bottom blowing center hole O 2 +CO 2 total The flow rate is 3000-18900Nm 3 /h, of which the CO 2 ratio is 50-100%, the bottom blowing ring seam CH 4 flow rate is 300-1890Nm 3 /h, and the end of the blowing period is 13-18min.
  • the present disclosure is applicable to the smelting process of 30-300t bottom blowing O 2 -CO 2 -CaO converter.
  • the life of the bottom blowing lance is prolonged, and at the same time, the stirring effect of the molten pool in the converter blowing process is strengthened, the metallurgical reaction balance is further promoted, the carbon and phosphorus content in the molten steel is reduced, the quality of the molten steel is improved, and the terminal steel of the converter blowing is avoided at the same time
  • Liquid peroxidation reduces the consumption of deoxidizing alloys and ferromanganese alloys, reduces production costs, and shortens the converter smelting cycle.
  • the final carbon content is reduced by 0.01-0.03%, the oxygen content is reduced by 200-400PPm, the alloy consumption is reduced by 3-8%, the phosphorus content is reduced by 0.005%-0.010%, the converter production cycle is shortened by 0.5-2min, and the steel material consumption is reduced by 10 -80kg/t, which improves the quality of molten steel and reduces costs.
  • Figure 1 is a dynamic control logic block diagram of a disclosed method for dynamic control of a bottom-blowing O 2 -CO 2 -CaO converter steelmaking process.
  • Example 1 The present disclosure is applied in the 120t bottom blowing O 2 -CO 2 -CaO converter steelmaking process, the top blowing gas is O 2 , the bottom blowing center gas includes O 2 + CO 2 , and the bottom blowing ring seam protection gas is CH 4 . Specific steps are as follows:
  • the temperature is 1635°C, which is transmitted to the injection parameter calculation module, and the operation process of the early stage of blowing is formulated through the central control system.
  • step 2 In the early stage of blowing, according to the operation process established in step 1, oxygen is blown from the top, and the central tube of the bottom blowing gun uses the mixed gas O 2 + CO 2 as the carrier gas, and sprays CaO powder into the molten pool to enhance the stirring of the molten pool and promote After slagging, the bottom blowing gun blows CH 4 circumferentially, cools and protects the central tube, calculates the decarburization rate of the molten pool according to the decarburization rate calculation module, and determines the end time of the early stage of blowing.
  • the specific operation plan is as follows: the oxygen flow rate of the top blowing lance is 19500Nm 3 /h, the total flow rate of the mixed gas O 2 +CO 2 in the center pipe of the bottom blowing lance is 7600Nm 3 /h, in which the CO 2 mixing ratio is 50%, and the lime powder injection speed It is 300kg/min, the flow rate of bottom blowing gun annular seam gas CH 4 is 760Nm 3 /h, and the initial blowing time is 0-5min;
  • the specific operation plan is as follows: the oxygen flow rate of the top blowing oxygen lance is 17600Nm 3 /h, the flow rate of pure O 2 blowing from the center tube of the bottom blowing lance is 7600Nm 3 /h, the lime powder injection speed is 300kg/min, and the blowing time reaches 10min, stop For powder spraying, the flow rate of the bottom blowing gun annular seam gas CH 4 is 760Nm 3 /h, and the middle period of blowing is 5-13min;
  • the measured temperature is 1635°C
  • the carbon content of the molten pool is 0.02%
  • the oxygen content is 800PPm
  • the temperature and composition are qualified.
  • the bottom blowing center hole gas is switched to pure Ar with a flow rate of 7000Nm 3 /h
  • the bottom blowing ring seam gas is switched to pure Ar with a flow rate of 600Nm 3 /h.
  • the stirring of the molten pool is reduced, and the separation of slag and iron is accelerated.
  • Example 2 The present disclosure is applied to the 300t bottom blowing O 2 -CO 2 -CaO converter steelmaking process, the top blowing gas is O 2 , the bottom blowing center gas includes O 2 + CO 2 , and the bottom blowing ring seam protection gas is CH 4 . Specific steps are as follows:
  • the temperature is 1635°C, which is transmitted to the injection parameter calculation module, and the operation process of the early stage of blowing is formulated through the central control system.
  • step 2 In the early stage of blowing, according to the operation process established in step 1, oxygen is blown from the top, and the central tube of the bottom blowing gun uses the mixed gas O 2 + CO 2 as the carrier gas, and sprays CaO powder into the molten pool to enhance the stirring of the molten pool and promote After slagging, the bottom blowing gun blows CH 4 circumferentially, cools and protects the central tube, calculates the decarburization rate of the molten pool according to the decarburization rate calculation module, and determines the end time of the early stage of blowing.
  • the specific operation plan is as follows: the oxygen flow rate of the top blowing oxygen gun is 47800Nm 3 /h, the total flow rate of the mixed gas O 2 +CO 2 in the center pipe of the bottom blowing gun is 19000Nm 3 /h, in which the mixing ratio of CO 2 is 40%, and the lime powder injection speed It is 700kg/min, the flow rate of the bottom blowing gun annular seam gas CH 4 is 1900Nm 3 /h, and the blowing time is 0-6min;
  • the specific operation plan is as follows: the oxygen flow rate of the top blowing lance is 44000Nm 3 /h, the flow rate of pure O 2 blowing from the center tube of the bottom blowing lance is 19000Nm 3 /h, the lime powder injection speed is 700kg/min, and the blowing time is 9min, stop For powder spraying, the flow rate of the bottom blowing gun annular seam gas CH 4 is 1900Nm 3 /h, and the middle period of blowing is 6-14min;
  • the specific operation plan is as follows: the oxygen flow rate of the top blowing lance is 50600Nm 3 /h, the total flow rate of the mixed gas O 2 +CO 2 in the center pipe of the bottom blowing gun is 19000Nm 3 /h, and the mixing ratio of CO 2 is 70%, and the bottom blowing gun is circular seam
  • the gas CH 4 flow rate is 1900Nm 3 /h, and the post-conversion time is 14-17min;
  • the measured temperature is 1637°C
  • the carbon content of the molten pool is 0.02%
  • the oxygen content is 750PPm.
  • the bottom blowing center hole gas is switched to pure Ar with a flow rate of 49000Nm 3 /h
  • the bottom blowing ring seam gas is switched to pure Ar with a flow rate of 1300Nm 3 /h.
  • the stirring of the molten pool is reduced, and the separation of slag and iron is accelerated.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacturing & Machinery (AREA)
  • Carbon Steel Or Casting Steel Manufacturing (AREA)

Abstract

一种底吹O2-CO2-CaO转炉炼钢过程动态控制方法，属于炼钢技术领域，适用于30-300t底吹O2-CO2-CaO转炉炼钢过程。底吹O2-CO2-CaO转炉炼钢工艺，采用O2作为顶吹气体，O2+CO2混合气作为底吹载气，将石灰粉从底吹喷枪喷入炉内，结合入炉铁水及废钢成分数据、转炉吹炼过程炉气成分数据及底吹设备工作条件，基于物料守恒对转炉炼钢过程钢液成分进行预测，并根据吹炼终点目标成分要求分阶段动态调整顶吹氧气量、底吹气配比及石灰粉流量，在降低底吹火点区温度的同时，强化转炉熔池搅拌效果，促进渣金反应平衡的进行，降低钢液的碳含量、磷含量；同时避免转炉吹炼终点的过氧化，降低脱氧合金消耗，减少钢中夹杂物数量，改善钢液质量；在高效冶金反应的基础上，再次增加金属收得率、降低生产成本、缩短冶炼周期。

Description

一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法 技术领域
本公开涉及炼钢工艺技术领域，尤其涉及一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法。
背景技术
转炉炼钢工艺能够处理各种成分的铁水及废钢，入炉料可灵活调整，且吹炼周期短，生产能力强，因而成为全球最为广泛的炼钢方法。转炉炼钢工艺以顶吹氧气作为熔池升温及搅拌的手段，配合底吹加强熔池搅拌，为冶金反应提供更好的动力学条件，用以生产达到终点碳含量、磷含量及温度合格的钢水。然而常规转炉冶炼过程熔池搅拌不够强，冶金效果及炼钢成本仍有较大的改善空间。底吹O 2-CaO转炉炼钢工艺熔池搅拌增强，脱磷效果好，但是存在一系列的问题：1)吹炼前期底吹O 2与熔池硅锰元素反应生成氧化物进入渣中，上浮气体量大大降低，熔池搅拌弱；2)脱磷效果较好，但是CaO粉剂喷吹量不精准，有效利用率仍有待提升；3)底吹混入CO 2比例可降低底吹火点区温度，但是混入比例不精准，底吹CO 2比例混入过大则造成终点温度低，底吹CO 2比例混入过小，则起不到保护底吹枪、增强熔池搅拌的效果。
专利申请号201810013096.3公开了一种转炉炼钢工艺，该法介绍了常规转炉炼钢工艺的一种加料及顶吹氧枪相配合的转炉炼钢方式，降低了恒压变枪位供氧时金属损失的问题。该法在实际吹炼中对过程操作要求较高，熔池搅拌有限，终点钢水成分及温度不稳定。
因此，如何实现底吹O 2-CO 2-CaO转炉炼钢过程的精准控制，延长底吹喷嘴寿命、强化熔池搅拌强度、防止钢水过氧化、减少钢种夹杂物、降低终点磷含量、缩短吹炼周期、降低生产成本，充分发挥该方法的技术优势是亟待解决的问题。
公开内容
针对上述问题，本公开提出一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法，解决了现有常规转炉炼钢过程终点成分波动大、钢液过氧化、吹炼时间长等技术难题。底吹O 2+CO 2+CaO转炉工艺的底吹枪为同心环缝管，吹炼过程，由底吹枪中心孔向熔池吹入O 2+CO 2+CaO，由底吹枪环缝向熔池吹入CH 4，顶吹氧枪向熔池吹入高速O 2，结合入炉铁水成分数据、转炉吹炼过程炉气成分数据及底吹设备工作条件，基于物料守恒对转炉炼钢过程钢液成分进行预测，通过脱碳速度将吹炼过程划分为前期、中期后期三个阶段，并根据吹炼 终点目标成分要求分阶段动态调整顶吹氧气量、底吹气配比及石灰粉流量，在强化转炉熔池搅拌效果的基础上，促进渣金反应平衡的进行；同时避免转炉吹炼终点的过氧化，降低脱氧合金消耗，减少钢中夹杂物数量，改善钢液质量，在提升渣金反应效率的基础上，缩短转炉冶炼周期，再次降低成本。
本公开是通过以下技术方案实现的：
一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法，其特征在于，根据脱碳速率v C将底吹O 2-CO 2-CaO转炉吹炼过程划分为前期、中期、后期3个阶段；数据计算模块根据入炉总装入量m 总、入炉铁水温度T 0-1、碳含量[％C] 0-1、硅含量[％Si] 0-1、废钢比为γ，废钢中碳含量[％C] 0-2、硅含量[％Si] 0-2、目标碳含量[％C] f及目标温度T f参数计算出吹炼耗氧量、CO 2配比及石灰粉喷入量；根据入炉料结构、熔池升温速度v T及脱碳速率v C，进而通过中心控制系统制定吹炼前期的吹炼操作工艺；吹炼过程通过脱碳速率计算模块计算出脱碳速率v C，并确定吹炼中期、后期的开始时间节点，CO 2计算模块通过底吹火点区温度计算模型、脱磷模型计算CO 2混入比例，进而制定中期、后期的吹炼操作工艺，降低火点区温度，加强熔池搅拌，促进熔池炉渣金属的反应平衡。
通过脱碳速率v C确定吹炼终点，并调整底吹气体参数，然后倒炉出钢。通过该动态控制方法，可降低火点区温度、延长底吹枪寿命，根据不同吹炼阶段增强熔池搅拌，可达到快速脱碳、高效脱磷及避免钢液过氧化、缩短吹炼时间、稳定吹炼终点钢液成分、降低生产成本的目的。
进一步地，在底吹O 2-CO 2-CaO转炉炼钢过程，底吹枪为同心环缝管，中心管采用O 2+CO 2混合气作为载气，将石灰粉从转炉底部直接吹入熔池，环缝喷吹冷却保护气，气体可以是CH 4、CO 2、N 2、Ar。结合转炉入炉料成分和烟气成分，对吹炼过程钢液的成分及温度进行预测，根据目标钢种成分、温度要求，通过底吹火点区温度计算模型、脱磷模型计算CO 2混入量，基于熔池脱碳速度，并分阶段动态调控底吹气中的CO 2比例。
进一步地，如上所述方法控制步骤如下：
根据入炉料总量m 总、硅含量[％Si]及碱度R要求，由粉剂计算模块计算石灰粉喷入速度，通过公式v CaO·t＝{[％Si] 0-1·(1-γ)+[％Si] 0-2·γ}·m 总·R计算并调整喷吹石灰粉速度；根据顶底吹设备工作反馈参数计算转炉炉气瞬时产生量S o-gas，同时根据炉气成分数据，计算出转炉吹炼过程脱碳速度变化，进而确定转炉的吹炼阶段及对应的钢液成分；炉气中CO 2、CO、O 2、H 2的瞬时含量分别为P 0-CO2、P 0-CO、P 0-O2、P 0-H2；顶吹氧气流量为Q U-O2，底吹中心气为O 2+CO 2混合气，底吹环缝为CH 4，底吹总流量、CO 2及CH 4比例分别为Q b、ε b-CO2、 ε b-CH4；根据公式2Q b(ε b-CH4)＝S o-gas·P o-H2及底吹工作参数计算及核定炉气流量S o-gas，由脱碳速率计算模块计算脱碳速度，通过公式
Figure PCTCN2020108455-appb-000001
Figure PCTCN2020108455-appb-000002
计算转炉吹炼过程的脱碳速度。
进一步地，如上所述方法具体控制步骤如下：
步骤1：通过数据采集系统获取转炉入炉料结构、关键成分数据及目标参数，将之传输至数据计算模块，并通过中心控制系统制定并控制转炉吹炼前期的操作工艺；
步骤2：吹炼前期，根据步骤1制定的操作工艺，顶吹氧枪降至炉内进行吹氧，底吹枪中心管以O 2+CO 2混合气作为载气，将石灰粉吹入熔池，底吹枪环缝吹入CH 4作为保护气，通过烟气成分数据及脱碳速率计算模块得出的脱碳速度
Figure PCTCN2020108455-appb-000003
确定吹炼前期的结束节点，
步骤3：吹炼中期，通过步骤2得到的脱碳速度
Figure PCTCN2020108455-appb-000004
确定吹炼中期的开始时间，进而制定中期操作方案，
步骤4：吹炼后期，通过脱碳速度
Figure PCTCN2020108455-appb-000005
确定吹炼后期的开始节点，根据升温速率v T，利用CO 2计算模块计算后期混入CO 2量，进而制定后期操作方案；
步骤5：吹炼终点，根据脱碳速率
Figure PCTCN2020108455-appb-000006
确定吹炼结束的时间节点；
步骤6：底吹中心孔气体切换为Ar，流量为2500-18400Nm 3/h，底吹环缝气体切换为Ar，流量为200-1790Nm 3/h，降低熔池搅拌，加速渣铁分离，倒炉出钢。
进一步地，步骤(2)所述吹炼前期的具体操作方案如下：底部石灰粉喷吹速度为300-900kg/min；顶吹氧气流量为10000-63000Nm 3/h，底吹中心孔O 2+CO 2总流量为3000-18900Nm 3/h，其中CO 2比例为0-100％，底吹环缝CH 4流量为300-1890Nm 3/h，吹炼结束时间为3-6min。
进一步地，步骤(3)所述吹炼中期具体操作方案如下：底部石灰粉喷吹速度为300-900kg/min，8-10min停止喷粉；顶吹氧气流量为9000-62000Nm 3/h，底吹中心孔O 2流量为3000-18900Nm 3/h，CO 2比例为0，底吹环缝CH 4流量为300-1890Nm 3/h，吹炼中期结束时间为9-13min。
进一步地，步骤(4)所述吹炼后期具体操作方案如下：底部石灰粉喷吹速度为0kg/min；顶吹氧气流量为9000-62000Nm 3/h，底吹中心孔O 2+CO 2总流量为3000-18900Nm 3/h，其中CO 2比例为50-100％，底吹环缝CH 4流量为300-1890Nm 3/h，吹炼后期结束时间为13-18min。
本公开适用于30-300t底吹O 2-CO 2-CaO转炉冶炼过程。通过本公开延长了底吹枪寿命，同时强化转炉吹炼过程的熔池搅拌效果，进一步地促进冶金反应平衡，降低钢液中碳、磷含量，改善钢液质量，同时避免转炉吹炼终点钢液过氧化，减少脱氧合金及锰铁合金的消耗，降低生产成本，缩短转炉冶炼周期。使得终点碳含量降低0.01-0.03％，氧含量降低了 200-400PPm，合金消耗量减少3～8％，磷含量降低0.005％-0.010％，转炉生产周期缩短0.5～2min，钢铁料消耗降低了10-80kg/t，提高了钢液质量，降低了成本。
附图说明
图1为本公开一底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法的动态控制逻辑框图。
具体实施方式
为了使本公开的目的、技术方案及优点更加清楚明白，以下结合实施例，对本公开进行进一步详细描述。应当理解，此处所描述的具体实施例仅仅用于解释本公开，并不用于限定本公开。
本公开涵盖任何由权利要求定义的在本公开的精髓和范围上做的替代、修改、等效方法以及方案。进一步，为了使公众对本公开有更好的了解，在下文对本公开的细节描述中，详尽描述了一些特定的细节部分。对本领域技术人员来说没有这些细节部分的描述也可以完全理解本公开。
实施例1：本公开应用在120t底吹O 2-CO 2-CaO转炉炼钢工序，顶吹气体为O 2，底吹中心气体包括O 2+CO 2，底吹环缝保护气为CH 4。具体步骤如下：
1)：通过原料参数采集系统采集铁水温度为1300℃，铁水碳含量[％C] 0＝4.0％、硅含量[％Si] 0＝0.60％、磷含量为[％P] 0＝0.109％，废钢碳含量为[％C] 0＝0.10％、硅含量[％Si] 0＝0.25％、磷含量为[％P] 0＝0.020％，废钢比为15％，目标碳含量为0.02％，目标温度为1635℃，将之传输至喷吹参数计算模块，通过中心控制系统制定吹炼前期的操作工艺。
2)：吹炼前期，根据步骤1制定的操作工艺，顶吹氧气，底吹枪中心管以混合气O 2+CO 2为载气，将CaO粉剂喷入熔池，增强熔池搅拌，促进化渣，底吹枪环缝吹CH 4，冷却保护中心管，根据脱碳速率计算模块计算出熔池脱碳速度，确定吹炼前期的结束时间。具体操作方案如下：顶吹氧枪氧气流量为19500Nm 3/h，底吹枪中心管混合气O 2+CO 2总流量7600Nm 3/h，其中CO 2混入比例为50％，石灰粉喷吹速度为300kg/min，底吹枪环缝气体CH 4流量为760Nm 3/h，吹炼前期时间为0-5min；
3)：吹炼中期，根据脱碳速度
Figure PCTCN2020108455-appb-000007
确定吹炼中期的开始时间为5min，顶吹氧气，底吹枪中心管以纯氧气为载气，将CaO粉剂喷入熔池，加速脱碳反应，增强熔池搅拌，环缝吹CH 4，冷却保护中心管。具体操作方案如下：顶吹氧枪氧气流量为17600Nm 3/h，底吹枪中心管纯吹O 2流量7600Nm 3/h，石灰粉喷吹速度为300kg/min，吹炼时间至10min时，停止喷粉， 底吹枪环缝气体CH 4流量为760Nm 3/h，吹炼中期时间为5-13min；
4)：吹炼后期，根据脱碳速度
Figure PCTCN2020108455-appb-000008
确定吹炼后期的开始时间为13min，项吹氧气，底吹枪中心管喷吹混合气O 2+CO 2，降低底吹火点区温度，增强熔池搅拌，促进冶金反应平衡，环缝吹CH 4，冷却保护中心管。具体操作方案如下：项吹氧枪氧气流量为20600Nm 3/h，底吹枪中心管混合气O 2+CO 2总流量7600Nm 3/h，其中CO 2混入比例为80％，底吹枪环缝气体CH 4流量为760Nm 3/h，吹炼后期时间为13-15min；
5)：吹炼终点，测得温度为1635℃，熔池碳含量为0.02％，氧含量为800PPm，温度及成分合格。底吹中心孔气体切换为纯Ar，流量为7000Nm 3/h，底吹环缝气体切换为纯Ar，流量为600Nm 3/h，降低熔池搅拌，加速渣铁分离，然后倒炉出钢。
实施例2：本公开应用在300t底吹O 2-CO 2-CaO转炉炼钢工序，顶吹气体为O 2，底吹中心气体包括O 2+CO 2，底吹环缝保护气为CH 4。具体步骤如下：
1)：通过原料参数采集系统采集铁水温度为1300℃，铁水碳含量[％C] 0＝4.0％、硅含量[％Si] 0＝0.50％、磷含量为[％P] 0＝0.100％，废钢碳含量为[％C] 0＝0.15％、硅含量[％Si] 0＝0.20％、磷含量为[％P] 0＝0.020％，废钢比为15％，目标碳含量为0.02％，目标温度为1635℃，将之传输至喷吹参数计算模块，通过中心控制系统制定吹炼前期的操作工艺。
2)：吹炼前期，根据步骤1制定的操作工艺，顶吹氧气，底吹枪中心管以混合气O 2+CO 2为载气，将CaO粉剂喷入熔池，增强熔池搅拌，促进化渣，底吹枪环缝吹CH 4，冷却保护中心管，根据脱碳速率计算模块计算出熔池脱碳速度，确定吹炼前期的结束时间。具体操作方案如下：顶吹氧枪氧气流量为47800Nm 3/h，底吹枪中心管混合气O 2+CO 2总流量19000Nm 3/h，其中CO 2混入比例为40％，石灰粉喷吹速度为700kg/min，底吹枪环缝气体CH 4流量为1900Nm 3/h，吹炼前期时间为0-6min；
3)：吹炼中期，根据脱碳速度
Figure PCTCN2020108455-appb-000009
确定吹炼中期的开始时间为6min，顶吹氧气，底吹枪中心管以纯氧气为载气，将CaO粉剂喷入熔池，加速脱碳反应，增强熔池搅拌，环缝吹CH 4，冷却保护中心管。具体操作方案如下：顶吹氧枪氧气流量为44000Nm 3/h，底吹枪中心管纯吹O 2流量19000Nm 3/h，石灰粉喷吹速度为700kg/min，吹炼时间至9min时，停止喷粉，底吹枪环缝气体CH 4流量为1900Nm 3/h，吹炼中期时间为6-14min；
4)：吹炼后期，根据脱碳速度
Figure PCTCN2020108455-appb-000010
确定吹炼后期的开始时间为14min，顶吹氧气，底吹枪中心管喷吹混合气O 2+CO 2，增强熔池搅拌，促进冶金反应平衡，环缝吹CH 4，冷却保护中心管。具体操作方案如下：顶吹氧枪氧气流量为50600Nm 3/h，底吹枪中心管混合气O 2+CO 2 总流量19000Nm 3/h，其中CO 2混入比例为70％，底吹枪环缝气体CH 4流量为1900Nm 3/h，吹炼后期时间为14-17min；
5)：吹炼终点，测得温度为1637℃，熔池碳含量为0.02％，氧含量为750PPm。底吹中心孔气体切换为纯Ar，流量为49000Nm 3/h，底吹环缝气体切换为纯Ar，流量为1300Nm 3/h，降低熔池搅拌，加速渣铁分离，然后倒炉出钢。
以上所述本公开的具体实施方式，并不构成对本公开保护范围的限定。任何根据本公开的技术构思所作出的各种其他相应的改变与变形，均应包含在本公开权利要求的保护范围内。

Claims (8)

  1. 一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法，包括：
    根据脱碳速率ν C将底吹O 2-CO 2-CaO转炉吹炼过程划分为前期、中期、后期3个阶段；数据计算模块根据入炉总装入量m 总、入炉铁水温度T 0-1、碳含量[％C] 0-1、硅含量[％Si] 0-1、废钢比为γ，废钢中碳含量[％C] 0-2、硅含量[％Si] 0-2、目标碳含量[％C] f及目标温度T f参数计算出吹炼耗氧量、CO 2配比及石灰粉喷入量；根据入炉料结构、熔池升温速度ν T及脱碳速率ν C，进而通过中心控制系统制定吹炼前期的吹炼操作工艺；吹炼过程通过脱碳速率计算模块计算出脱碳速率ν C，并确定吹炼中期、后期的开始时间节点，CO 2计算模块通过底吹火点区温度计算模型、脱磷模型计算CO 2混入比例，进而制定中期、后期的吹炼操作工艺，降低火点区温度，加强熔池搅拌，促进熔池炉渣金属的反应平衡。
  2. 根据权利要求1所述的一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法，其中，在底吹O 2-CO 2-CaO转炉炼钢过程，底吹枪包括同心环缝管，中心管采用O 2+CO 2混合气作为载气，将石灰粉从转炉底部直接吹入熔池，环缝喷吹冷却保护气，气体包括CH 4、CO 2、N 2、Ar；结合转炉入炉料成分和烟气成分，对吹炼过程钢液的成分及温度进行预测，根据目标钢种成分、温度要求，通过底吹火点区温度计算模型、脱磷模型计算CO 2混入量，基于熔池脱碳速度，并分阶段动态调控底吹气中的CO 2比例。
  3. 根据权利要求1所述的一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法，其中，控制步骤如下：
    根据入炉料总量m 总、硅含量[％Si]及碱度R要求，由粉剂计算模块计算石灰粉喷入速度，通过公式u CaO·t＝{[％Si] 0-1·(1-γ)+[％Si] 0-2·γ}·m 总·R计算并调整喷吹石灰粉速度；根据顶底吹设备工作反馈参数计算转炉炉气瞬时产生量S o-gas，同时根据炉气成分数据，计算出转炉吹炼过程脱碳速度变化，进而确定转炉的吹炼阶段及对应的钢液成分；炉气中CO 2、CO、O 2、H 2的瞬时含量分别为P 0-CO2、P 0-CO、P 0-O2、P 0-H2；顶吹氧气流量为Q U-O2，底吹中心气为O 2+CO 2混合气，底吹环缝为CH 4，底吹总流量、CO 2及CH 4比例分别为Q b、ε b-CO2、ε b-CH4；根据公式2Q b(ε b-CH4)＝S o-gas·P o-H2及底吹工作参数计算及核定炉气流量S o-gas，由脱碳速率计算模块计算脱碳速度。
  4. 根据权利要求3所述的一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法，通过公式
    Figure PCTCN2020108455-appb-100001
    计算转炉吹炼过程的脱碳速度。
  5. 根据权利要求1或4所述的一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法，其中， 具体控制步骤如下：
    步骤1：通过数据采集系统获取转炉入炉料结构、关键成分数据及目标参数，将之传输至数据计算模块，并通过中心控制系统制定并控制转炉吹炼前期的操作工艺；
    步骤2：吹炼前期，根据步骤1制定的操作工艺，顶吹氧枪降至炉内进行吹氧，底吹枪中心管以O 2+CO 2混合气作为载气，将石灰粉吹入熔池，底吹枪环缝吹入CH 4作为保护气，通过烟气成分数据及脱碳速率计算模块得出的脱碳速度
    Figure PCTCN2020108455-appb-100002
    确定吹炼前期的结束节点；
    步骤3：吹炼中期，通过步骤2得到的脱碳速度
    Figure PCTCN2020108455-appb-100003
    确定吹炼中期的开始时间，进而制定中期操作方案；
    步骤4：吹炼后期，通过脱碳速度
    Figure PCTCN2020108455-appb-100004
    确定吹炼后期的开始节点，根据升温速率ν T，利用CO 2计算模块计算后期混入CO 2量，进而制定后期操作方案；
    步骤5：吹炼终点，根据脱碳速率
    Figure PCTCN2020108455-appb-100005
    确定吹炼结束的时间节点；
    步骤6：底吹中心孔气体切换为Ar，流量为2500-18400Nm 3/h，底吹环缝气体切换为Ar，流量为200-1790Nm 3/h，降低熔池搅拌，加速渣铁分离，倒炉出钢。
  6. 根据权利要求5所述的一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法，其中，步骤(2)所述吹炼前期的具体操作方案如下：底部石灰粉喷吹速度为300-900kg/min；顶吹氧气流量为10000-63000Nm 3/h，底吹中心孔O 2+CO 2总流量为3000-18900Nm 3/h，其中CO 2比例为0-100％，底吹环缝CH 4流量为300-1890Nm 3/h，吹炼结束时间为3-6min。
  7. 根据权利要求4所述的一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法，其中，步骤(3)所述吹炼中期具体操作方案如下：底部石灰粉喷吹速度为300-900kg/min，8-10min停止喷粉；顶吹氧气流量为9000-62000Nm 3/h，底吹中心孔O 2流量为3000-18900Nm 3/h，CO 2比例为0，底吹环缝CH 4流量为300-1890Nm 3/h，吹炼中期结束时间为9-13min。
  8. 根据权利要求5所述的一种底吹O 2-CO 2-CaO转炉炼钢过程动态控制方法，其中，步骤(4)所述吹炼后期具体操作方案如下：底部石灰粉喷吹速度为0kg/min；顶吹氧气流量为9000-62000Nm 3/h，底吹中心孔O 2+CO 2总流量为3000-18900Nm 3/h，其中CO 2比例为50-100％，底吹环缝CH 4流量为300-1890Nm 3/h，吹炼后期结束时间为13-18min。
PCT/CN2020/108455 2020-05-28 2020-08-11 一种底吹O2-CO2-CaO转炉炼钢过程动态控制方法 WO2021237946A1 (zh)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US17/440,648 US20220325368A1 (en) 2020-05-28 2020-08-11 METHOD OF DYNAMIC CONTROL FOR BOTTOM BLOWING O2-CO2-CaO CONVERTER STEELMAKING PROCESS

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN202010469302.9A CN111500815B (zh) 2020-05-28 2020-05-28 一种底吹O2-CO2-CaO转炉炼钢过程动态控制方法
CN202010469302.9 2020-05-28

Publications (1)

Publication Number Publication Date
WO2021237946A1 true WO2021237946A1 (zh) 2021-12-02

Family

ID=71870408

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2020/108455 WO2021237946A1 (zh) 2020-05-28 2020-08-11 一种底吹O2-CO2-CaO转炉炼钢过程动态控制方法

Country Status (3)

Country Link
US (1) US20220325368A1 (zh)
CN (1) CN111500815B (zh)
WO (1) WO2021237946A1 (zh)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114410877A (zh) * 2021-12-30 2022-04-29 钢铁研究总院 一种转炉冶炼过程中顶吹氧枪供氧工艺的自动控制方法

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111500815B (zh) * 2020-05-28 2021-06-11 北京科技大学 一种底吹O2-CO2-CaO转炉炼钢过程动态控制方法
CN113234883B (zh) * 2021-04-23 2022-03-15 甘肃酒钢集团宏兴钢铁股份有限公司 一种转炉底吹喷粉的冶炼工艺
CN113215349B (zh) * 2021-04-23 2022-08-26 甘肃酒钢集团宏兴钢铁股份有限公司 一种降低转炉终点钢水自由氧含量的方法
CN113355477B (zh) * 2021-05-18 2022-07-05 北京科技大学 一种底吹氢气实现转炉高废钢比冶炼的方法
CN114317869A (zh) * 2021-12-07 2022-04-12 河北敬业高品钢科技有限公司 一种转炉底吹富氧炼钢的方法
CN114807497A (zh) * 2022-03-28 2022-07-29 邯郸钢铁集团有限责任公司 利用底吹氧、石灰粉复吹转炉冶炼高硅铁水的方法
CN114854929B (zh) * 2022-05-07 2023-03-17 北京科技大学 一种转炉喷吹co2钢液成分与温度实时动态预测的方法
CN115164610B (zh) * 2022-05-23 2024-06-11 华中科技大学 一种基于co/o2的水泥分解炉燃烧优化方法及系统
CN115044735B (zh) * 2022-06-16 2024-05-10 首钢集团有限公司 一种底吹枪、转炉和底吹方法
CN115786628B (zh) * 2022-11-12 2024-06-11 甘肃酒钢集团宏兴钢铁股份有限公司 一种利用二氧化碳与氧气混合顶吹洗炉底的方法
CN115927784B (zh) * 2022-11-30 2023-07-14 北京科技大学 一种基于co2动态混合喷吹的转炉炼钢终点控制方法
CN116434856B (zh) * 2023-03-17 2024-04-16 北京科技大学 一种基于分段式氧气脱碳效率的转炉供氧量预测方法
CN116628576B (zh) * 2023-07-26 2023-10-13 中南大学 用于热载体石灰窑的智能生产产量监测方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS59205410A (ja) * 1983-05-10 1984-11-21 Nippon Steel Corp 転炉操業方法
CN105803155A (zh) * 2016-05-12 2016-07-27 北京科技大学 一种电弧炉炼钢脱磷方法
CN105907914A (zh) * 2016-06-22 2016-08-31 北京科技大学 一种利用co2延长底吹氧气转炉寿命的炼钢方法
CN108251593A (zh) * 2018-02-08 2018-07-06 北京科技大学 一种转炉炼钢动态调节底吹co2流量改善脱氮的方法
CN108359766A (zh) * 2018-03-02 2018-08-03 北京科技大学 一种基于钢水连续测温的底吹氧气转炉冶炼过程控制方法
CN111500815A (zh) * 2020-05-28 2020-08-07 北京科技大学 一种底吹O2-CO2-CaO转炉炼钢过程动态控制方法

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4474361A (en) * 1980-07-30 1984-10-02 Nippon Steel Corporation Oxygen-blown steelmaking furnace
US4388113A (en) * 1980-09-26 1983-06-14 Nippon Steel Corporation Method of preventing damage of an immersed tuyere of a decarburization furnace in steel making
CN106048136B (zh) * 2016-07-27 2017-12-08 北京科技大学 一种炼钢出钢过程在线喷粉脱氧方法及系统
CN106086289B (zh) * 2016-08-01 2018-05-29 朱荣 一种采用顶吹氧枪喷粉冶炼不锈钢母液的炼钢方法及装置
CN109234490B (zh) * 2018-11-07 2020-06-26 北京科技大学 一种提钒-脱碳双联转炉高效长寿喷吹方法及系统
CN109957637B (zh) * 2019-03-27 2019-11-29 北京科技大学 一种rh喷吹co2精炼超低碳钢的动态控制方法
CN110804684B (zh) * 2019-10-16 2020-08-11 北京科技大学 一种转炉co2-o2混合喷吹冶炼火点区温度动态控制方法
CN110578032B (zh) * 2019-10-23 2021-06-11 辽宁科技大学 一种大型转炉喷吹工艺方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS59205410A (ja) * 1983-05-10 1984-11-21 Nippon Steel Corp 転炉操業方法
CN105803155A (zh) * 2016-05-12 2016-07-27 北京科技大学 一种电弧炉炼钢脱磷方法
CN105907914A (zh) * 2016-06-22 2016-08-31 北京科技大学 一种利用co2延长底吹氧气转炉寿命的炼钢方法
CN108251593A (zh) * 2018-02-08 2018-07-06 北京科技大学 一种转炉炼钢动态调节底吹co2流量改善脱氮的方法
CN108359766A (zh) * 2018-03-02 2018-08-03 北京科技大学 一种基于钢水连续测温的底吹氧气转炉冶炼过程控制方法
CN111500815A (zh) * 2020-05-28 2020-08-07 北京科技大学 一种底吹O2-CO2-CaO转炉炼钢过程动态控制方法

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"Introduction to Steel Production", 30 September 2017, METALLURGICAL INDUSTRY PRESS, CN, ISBN: 978-7-5024-7596-3, article SUN, BINYI ET AL.: "Chapter 2. Steelmaking production. Section 9. Oxygen converter steelmaking", pages: 90 - 91, XP009532269 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114410877A (zh) * 2021-12-30 2022-04-29 钢铁研究总院 一种转炉冶炼过程中顶吹氧枪供氧工艺的自动控制方法

Also Published As

Publication number Publication date
US20220325368A1 (en) 2022-10-13
CN111500815A (zh) 2020-08-07
CN111500815B (zh) 2021-06-11

Similar Documents

Publication Publication Date Title
WO2021237946A1 (zh) 一种底吹O2-CO2-CaO转炉炼钢过程动态控制方法
CN105063474B (zh) 一种焊丝用钢的电炉冶炼方法
CN102134628A (zh) 一种低硅含量的低碳铝镇静钢冶炼方法
CN108396097A (zh) 一种低Ca、低Al焊丝钢的冶炼方法
CN108588326B (zh) 一种含钒铁水冶炼高强焊丝钢er80-g的方法
CN103773919A (zh) 一种转炉冶炼中、高磷铁水的方法
CN113322364B (zh) 一种极地用钢的超高磷铁水低成本冶炼方法
CN105525055A (zh) 一种转炉少渣冶炼脱碳期喷溅的控制方法
CN107653358A (zh) Lf精炼炉冶炼过程快速脱氧的方法
CN104043797A (zh) 一种超低硫高铬钢的连铸方法及其制备的大方坯
CN114150100B (zh) 一种转炉冶炼高碳低磷钢的炼钢方法
CN102965465A (zh) 一种转炉渣固化的方法
CN101864508B (zh) 小渣量转炉炼钢方法
CN102634634B (zh) 采用电弧炉生产锅炉管用高合金低磷钢的方法
CN113832288A (zh) 一种全铁水冶炼控制喷溅的方法
CN110527786B (zh) 转炉锰矿直接合金化炼钢的方法
JPS63195209A (ja) 製鋼方法
CN102453786B (zh) 一种转炉冶炼钻杆接头用钢的方法及钻杆接头用钢
CN1218060C (zh) 用富氮合金和含钒合金微合金化高强度低合金钢的冶炼方法
CN110564908A (zh) 半钢转炉双渣脱磷炼钢的方法
JPS6067608A (ja) 中・低炭素フエロマンガンの製造方法
CN102140567B (zh) 一种氩氧精炼低碳铬铁合金的方法
CN110592309A (zh) 一种低磷钢的冶炼方法
JPS63290242A (ja) 低炭素低シリコンフェロマンガンの製造方法およびその実施のための転炉およびランス
JPS58147506A (ja) 溶銑予備処理方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 20937567

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 20937567

Country of ref document: EP

Kind code of ref document: A1