US3884677A - Blast furnace operating methods - Google Patents

Blast furnace operating methods Download PDF

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Publication number
US3884677A
US3884677A US417622A US41762273A US3884677A US 3884677 A US3884677 A US 3884677A US 417622 A US417622 A US 417622A US 41762273 A US41762273 A US 41762273A US 3884677 A US3884677 A US 3884677A
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United States
Prior art keywords
blast furnace
blast
furnace gas
gas
hearth
Prior art date
Legal status (The legal status 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 status listed.)
Expired - Lifetime
Application number
US417622A
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English (en)
Inventor
Werner Wenzel
Heinrich Wilhelm Gudenau
Tsutomu Fukushima
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JFE Engineering Corp
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Nippon Kokan Ltd
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Publication date
Priority claimed from DE2257922A external-priority patent/DE2257922C3/de
Priority claimed from DE2311466A external-priority patent/DE2311466C3/de
Application filed by Nippon Kokan Ltd filed Critical Nippon Kokan Ltd
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Publication of US3884677A publication Critical patent/US3884677A/en
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    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/06—Making pig-iron in the blast furnace using top gas in the blast furnace process
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
    • C21B2100/22—Increasing the gas reduction potential of recycled exhaust gases by reforming
    • 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
    • Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
    • 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

  • a further important object of the present invention is to operate a blast furnace in such a way that all of the blast furnace gas is utilized without any excess blast furnace gas being present to be wasted.
  • blast furnace gas is regenerated into a condition where it is enriched with carbon monoxide and hydrogen.
  • This regenerated blast furnace gas iis then introduced into the hearth of the blast furnace as part of the blast, and the components of the blast are such that the blast is substantially free of nitrogen while being made up at least in part of the regenerated blast furnace gas.
  • FIG. 1 is a schematic illustration of one method according to the present invention.
  • FIG. 2 is a schematic illustration of a further embodiment of a method according to the present invention.
  • This method of operation is carried out while excluding nitrogen, as encountered, for example, in normal air, from the blast.
  • the role which is performed by the nitrogen as a temperature limiting agent during burning of oxygen in the hearth and as a heat-transfer agent for transferring heat from the hearth up into the stack is taken over by the carbon monoxide and hydrogen.
  • the hot reducing gas whose temperature, in the same way as the reducing gas which is blown into the stack, can be lO0-l200C or higher, there is blown into the hearth a highly concentrated oxygen, in a concentration of, for example, 95%, so that this oxygen together with the regenerated blast furnace gas is introduced through the tuyeres into the hearth.
  • the conservation of coke resulting from blowing the regenerated blast furnace gas through the tuyeres into the hearth provides important advantages because it is possible to blow the blast furnace gas at higher temperatures, for example at temperatures of l400C and more in the same way as the remainder of the blast, because decomposition heat for the blast is not required and because the selected large excess of gas is blown with concentrated oxygen which requires only a small amount of preheating can be used, as contrasted with combustion oxygen, without requiring the amount of heat for raising the temperature of the oxygen to the hearth temperature, this latter amount of heat normally representing a loss at the hearth.
  • the blowing of the regenerated blast furnace gas into the hearth through the tuyeres is combined with blowing the regenerated gas into the stack.
  • This particularly favorable operating method involves deriving from the total regenerated gas a part thereof in the form of a reducing gas which primarily is made up of carbon monoxide and hydrogen, approximately 60% of the total regenerated gas having this latter characteristic and being introduced into the hearth of the blast furnace while the remaining 40% is blown into the stack.
  • the part of the regenerated gas which is introduced into the stack is of course effective also only at the outer wall region of the furnace, but in addition the part of the regenerated gas which is introduced through the tuyeres flows upwardly from the hearth through the central region of the furnace and has the same nitrogen-free composition so that the reducing action takes place throughout the entire cross section of the blast furnace in a uniform manner.
  • This method of combining introduction of the reducing gas into the hearth and into the stack has with respect to coke consumption and total fuel consumption optimum conditions, with achievement also of the added advantage of requiring for combustion purposes in the hearth only a particularly small amount of concentrated oxygen.
  • FIG. 1 there is schematically illustrated therein one possible method according to the invention.
  • the blast furnace gas which gas regenerated with the oil is blown only into the hearth of the blast furnace.
  • FIG. 1 illustrates schematically the blast furnace l as well as the blast furnace gas cleaning unit 2 in which, as a result of cooling, the greatest part of the steam is separated from the blast furnace gas in the form of liquid water, and in addition the dust or foreign particle content-is reduced in the usual way by known measures.
  • the blast furnace gas after passing through the cleaning unit 2 is received by the reactor or gas converter 3 in which the blast furnace gas is regenerated by means of a fossil fuel such as natural gas, oil or coal, so that the carbon dioxide of the blast furnace gas and 'the residual content of steam is converted by way of the carboncontaining material so as to form carbon monoxide and hydrogen.
  • the top end or mouth of the blast furnace 1 receives the coke charge 4 as well as the charge 5 composed of ore and flux.
  • the blast furnace gas 6 discharges from the top of the blast furnace and flows through the cleaning unit 2.
  • the cleaned blast furnace gas 7 is divided into three streams 8, 9 and 10.
  • the stream 8 is directed to the regenerator 3 so as to form the regenerated blast furnace gas, the stream 9 is used as a source of heat for the regenerator 3, and the remaining stream 10 is excess blast furnace gas which is discharged to the exterior from the blast furnace installation.
  • the regenerator 3 receives not only the streams 8 and 9 but also the fossil fuel 11 required for regenerating the blast furnace gas stream 8.
  • This fossil fuel may, for example, take the form of oil.
  • combustion air 12 is introducted to the regenerator 3.
  • the regenerated blast furnace gas 13 discharges from the regenerator 3 and flue gas 14 also is discharged from the regenerator 3.
  • the regenerated blast furnace gas 13 is blown into the blast furnace l, to be received in the hearth thereof through the tuyeres.
  • the blast introduced through the tuyeres contains not only the regenerated blast furnace gas 13 but also the oxygen 15 and if desired a liquid fuel 16 such as, for example, oil.
  • the pig iron 17 and the slag l8 flow out of the hearth at the bottom of the blast furnace.
  • additional auxiliary units such as blowers, controls, and the like are not illustrated.
  • FIG. 2 schematically illustrates an embodiment of the invention according to which the regenerated blast furnace gas which is blown into the blast furnace is divided into a pair of streams.
  • the larger of these pair of streams is blown in the manner described above into the hearth through the tuyeres while the smaller of the pair of streams is blown into the stack.
  • the stream 13a illustrates that part of the regenerated blast furnace gas which is introduced through the tuyeres
  • the stream 13b illustrates that part of the regenerated blast furnace gas which is blown into the stack, primarily directly over the melting zone of the charge.
  • the method of the invention makes possible a series of further variations which are capable of providing optimum operating conditions.
  • the reducing gas which is blown into the hearth of the blast furnace has smaller requirements with respect to the residual content of carbon dioxide and water as well as with respect to cracking carbon, than reducing gas which is blown into the stack.
  • the cracking carbon which results is burned with the oxygen which is simultaneously blown in with the blast, while the regenerated blast furnace gas which is blown into the stack does not meet the requirements essential for this purpose.
  • the reducing gas in the gas regenerating installation 3 it is possible when forming the reducing gas in the gas regenerating installation 3 to divide the total amount of reducing gas into one type of gas which has a relatively large amount of cracking carbon and/or a high content of carbon monoxide and hydrogen while another type of reducing gas is provided which has a relatively small amount of these components.
  • a division of the total regenerated blast furnace gas into these two types can be achieved in a relatively simple manner by converting the blast furnace gas in the regenerator 3 during an initial operating phase during which the regeneration is carried out at a conversion temperature which is higher than that which is present during a final operating phase of the regenerator 3.
  • a further possibility of achieving two different types of regenerated blast furnace gas resides in directing the gas product from the regenerator to a cyclone separator.
  • This gas product contains cracking carbon, and in the cyclone separator, as a result of the known cyclone action the particles of cracking carbon become situated at the outer wall region of the cyclone while at the central region thereof there is a regenerated blast furnace gas which is substantially free of the cracking carbon or has a much lower content thereof.
  • the gas fromthe central region of the cyclone is delivered to the stack while the gas product at the outer wall region of the cyclone with its high content of cracking carbon is delivered to the hearth.
  • an important feature of the invention resides in further elevating the preheating temperature for the reducing gas introduced into the hearth, such as up to l400l500C, while additionally preheating the other components of the blast which is introduced into the hearth, these other components being oxygen and oil or CH.,, the temperature of these latter components being raised to 400500C.
  • nitrogen is eliminated from the hearth gas by introducing through the tuyeres together with oxygen the reducing gas derived from regenerating the blast furnace gas with a liquid fossil fuel, with the regenerated blast furnace gas also being advantageously blown into the stack.
  • One of the most important objectives to be achieved in connection with blast furnace operation is the production of the pig iron with the smallest possible consumption of fuel. Initially it was considered satisfactory to reduce the coke consumption to a considerable extent, and in this connection an important auxiliary measure was the blowing of auxiliary fuel, particularly oil, into the hearth of the blast furnace through the tuyeres. With such known expedients, it is indeed possible to reduce the coke in the charge to approximately 350-450 kg, in accordance with the particular operating conditions, per ton of produced pig iron, while at the same time utilizing for this purpose oil in an amount of approximately 40 kgkg per ton of pig iron. However, with these measures the total heat requirement per ton of produced pig iron is not reduced, and in some cases is in fact increased. However, one of the most important objectives to be achieved in connection with the development of blast furnace operation is to provide special measures by which not only the coke consumption is reduced but also the total heatrequirement is maintained as low as possible.
  • a further important objective of blast furnace development is to achieve as large an output as possible, with the specific output in general being achieved either with respect to the hearth area of the furnace or with respect to the useful volume thereof.
  • steel mills require blast furnaces which have a daily output capacity for each individual blast furnace which is in the range of approximately 10,000 tons.
  • the required hearth diameter is approximately 13m 1 m, in accordance with, the specific charge requirements.
  • the specific installation cost of a blast furnace which is to say the amount of capital required per ton of produced pig iron, does not continuously decrease with an increase in the size of the furnace.
  • the amount of coke which is included in the charge delivered to the top mouth of the blast furnace should be approximately between 225kg and 255kg.
  • the amount of oil which is delivered to the regenerator for the blast furnace gas should be between l30kg and l45kg.
  • the amount of oil which is blown into the tuyeres so as to be burned with oxygen in the hearth or immediately before reaching the hearth should be approximately 40kg-60kg.
  • the regenerated blast furnace gas derived at the regenerator from the oil and from the part of the blast furnace gas which is delivered to the regenerator is divided between the tuyeres and the stack.
  • the amount of regenerated blast furnace gas which is blown in should be approximately 37-45% of the total amount of regenerated blast furnace gas which is produced.
  • the amount of regenerated blast furnace gas which is blown in through the tuyeres is the remainder of the total 8 amount of regenerated blast furnace gas which is produced and should be between 63 and 55%.
  • the blast furnace gas which discharges from the top of the blast furnace is utilized in the following way in accordance with the operating method of the invention:
  • the total amount of blast furnace gas flowing from the blast furnace to the regenerator 3 is approximately 4045% of the total blast furnace gas.
  • the residual amount of blast furnace gas in a range of approximately 0l0% is utilized.
  • the temperature of the regenerated blast furnace gas which is blown into the stack is approximately 1 C 1250C, while the temperature of the blast introduced into the hearth through the tuyeres has with respect to the components of the blast the following the charge by simultaneously increasing the amount of oil which is blown in with the blast.
  • the total heat consumption of the method of the invention is not substantially changed.
  • the present invention also is fully effective in the case where for commercial reasons the surlfur-free blast furnace gas is partially withdrawn from the blast furnace to be utilized for other purposes and is replaced for the purposes of the present invention with a I more economical interchangeable fuel such as oil. In general this latter possibility is available for that part of the blast furnace gas which is utilized for heating purposes in accordance with the data presented above.
  • a blast furnace operating method for producing metal comprising providing a blast furnace having an hearth, stack and top, charging said blast furnace with ore and coke, introducing a blast into the hearth of the blast furnace, introducing a reducing gas into the stack of the blast furnace, reducing the ore to form metal and simultaneously producing blast furnace gas, recovering the metal and discharging all of the blast furnace gas from the top of the blast furnace, the improvement in combination therewith comprising the steps of regenerating a first portion of blast furnace gas issuing from the top of a blast furnace by means of fossil fuel into a condition where it is enriched with carbon monoxide and hydrogen, utilizing a second portion of the blast furnace gas as at least part of a source of heat for regenerating the first portion of the blast furnace gas, introducing into the hearth of the blast furnace a blast which is substantially free of nitrogen and which is made up in part of a portion of the regenerated blast furnace gas, preheating that part of the blast which does not include the regenerated blast furnace gas at least partly with the residual
  • the amount of regenerated blast furnace gas which is included in the blast is sufficient to provide in the hearth an amount of carbon monoxide and hydrogen adequate to provide a peak combustion temperature of approximately 2,000C while also providing a sufficient excess of carbon monoxide and hydrogen at the hearth to flow from the hearth up into the stack of the blast furnace for transferring into the stack by way of the excess carbon monoxide and hydrogen heat for carrying out the required reactions in the stack.
  • the blast introduced into the hearth of the blast furnace contains oxygen and a fossil fuel, with these components of the blast being delivered to the hearth in amounts and temperatures which substantially eliminate any excess blast furnace gas in the discharge from the blast furnace.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacture Of Iron (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • Carbon And Carbon Compounds (AREA)
US417622A 1972-11-25 1973-11-20 Blast furnace operating methods Expired - Lifetime US3884677A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE2257922A DE2257922C3 (de) 1972-11-25 1972-11-25 Verfahren für den Betrieb eines Hochofens mit einem aus Gichtgas hergestellten Hilfsreduktionsgas
DE2311466A DE2311466C3 (de) 1973-03-08 1973-03-08 Verfahren zur Erzielung optimaler Brennstoffverbrauchs- und Leistungsdaten beim Hochofen

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US3884677A true US3884677A (en) 1975-05-20

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US417622A Expired - Lifetime US3884677A (en) 1972-11-25 1973-11-20 Blast furnace operating methods

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US (1) US3884677A (enrdf_load_stackoverflow)
JP (1) JPS4979910A (enrdf_load_stackoverflow)
AT (1) AT338306B (enrdf_load_stackoverflow)
BR (1) BR7309161D0 (enrdf_load_stackoverflow)
CA (1) CA1009455A (enrdf_load_stackoverflow)
FR (1) FR2207990B1 (enrdf_load_stackoverflow)
GB (1) GB1438999A (enrdf_load_stackoverflow)
IT (1) IT1001934B (enrdf_load_stackoverflow)

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4301997A (en) * 1978-06-30 1981-11-24 Southwire Company Continuous copper melting furnace
US4537626A (en) * 1980-07-02 1985-08-27 Klockner-Humboldt-Deutz Ag Method for the production of reaction gases
US6214084B1 (en) * 1997-09-03 2001-04-10 The Boc Group, Inc. Iron manufacturing process
WO2001088207A1 (de) * 2000-05-15 2001-11-22 Voest-Alpine Industrieanlagenbau Gmbh & Co Verfahren und vorrichtung zur herstellung von roheisen oder flüssigen stahlvorprodukten aus eisenerzhältigen einsatzstoffen
US20110209576A1 (en) * 2008-10-31 2011-09-01 Paul Wurth S.A. Method for operating a blast furnace and blast furnace installation
US20130344450A1 (en) * 2012-06-21 2013-12-26 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Syngas generator for blast furnace
KR20140027099A (ko) * 2011-01-28 2014-03-06 에너지 인디펜던스 오브 아메리카 코포레이션 액체 철 및 철강 제조 방법과 장치
WO2014198635A1 (de) * 2013-06-14 2014-12-18 CCP Technology GmbH Hochofen und verfahren zum betrieb eines hochofens
US8992664B2 (en) 2009-03-17 2015-03-31 ArcelorMittal Investigación y Desarrollo, S.L. Blast furnace top gas recycling process and corresponding recycling equipment
WO2015078962A1 (en) * 2013-11-28 2015-06-04 Ccp Technology Blast furnace and method for operating a blast furnace
EP2886666A1 (en) 2013-12-20 2015-06-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for operating a top gas recycling blast furnace installation
CN106702052A (zh) * 2015-11-17 2017-05-24 鞍钢股份有限公司 一种高炉炉顶均压煤气回收系统及方法
WO2019057930A1 (en) 2017-09-25 2019-03-28 Paul Wurth S.A. PROCESS FOR PRODUCING HOT SYNTHESIS GAS, ESPECIALLY FOR USE IN OPERATING A HIGH-STOVE
US11377700B2 (en) * 2017-07-03 2022-07-05 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Method for operating an iron- or steelmaking- plant

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DE2710106B2 (de) * 1977-03-08 1980-08-14 Eisenwerk-Gesellschaft Maximilianshuette Mbh, 8458 Sulzbach-Rosenberg Verfahren zur Erzeugung von flüssigem Roheisen
BE1000776A6 (fr) * 1987-07-31 1989-04-04 Centre Rech Metallurgique Procede de conduite d'un haut fourneau.
GB2281311B (en) * 1993-03-29 1996-09-04 Boc Group Plc Metallurgical processes and apparatus
FR2847659B1 (fr) * 2002-11-25 2005-12-16 Air Liquide Procede d'optimisation en energie d'un site industriel, par enrichissement en oxygene d'air de combustion
JP2006315651A (ja) * 2005-05-16 2006-11-24 Makoto Nozaki 鉄道車両の二種軌間兼用台車
JP5770124B2 (ja) * 2012-03-06 2015-08-26 新日鐵住金株式会社 高炉操業方法
EP2719778A1 (en) * 2012-10-12 2014-04-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Blast-furnace process with CO2-lean blast furnace gas recycle and production plant for same
EP2719779A1 (en) * 2012-10-12 2014-04-16 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Blast-furnace process with recycle of a CO-fraction of the blast furnace gas and production plant for same
GB2513185A (en) * 2013-04-19 2014-10-22 Siemens Vai Metals Tech Gmbh Blast furnace plant
JP6463626B2 (ja) * 2014-12-16 2019-02-06 新日鐵住金株式会社 高炉の操業方法
TW202500764A (zh) * 2023-06-21 2025-01-01 日商日本製鐵股份有限公司 高爐的作業方法

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US2790711A (en) * 1957-04-30 Molten
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GB369393A (en) * 1930-03-21 1932-03-24 Linde Eismasch Ag Improvements in or relating to blast furnaces
US2837419A (en) * 1957-02-15 1958-06-03 Texaco Development Corp Reduction of metal oxides
FR1337277A (fr) * 1962-06-14 1963-09-13 Perfectionnements au procédé de production de fonte dans un haut fourneau
FR2040708A5 (en) * 1969-04-10 1971-01-22 Fink Ferdinand Treating iron minerals in a blast furnace
JPS5232323B2 (enrdf_load_stackoverflow) * 1970-07-29 1977-08-20

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US2790711A (en) * 1957-04-30 Molten
US3151974A (en) * 1961-04-26 1964-10-06 Huttenwerk Salzgitter Ag Process for the operation of blast furnaces
US3594154A (en) * 1967-05-20 1971-07-20 Sumitomo Metal Ind Iron making process and its arrangement thereof

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4301997A (en) * 1978-06-30 1981-11-24 Southwire Company Continuous copper melting furnace
US4537626A (en) * 1980-07-02 1985-08-27 Klockner-Humboldt-Deutz Ag Method for the production of reaction gases
US6214084B1 (en) * 1997-09-03 2001-04-10 The Boc Group, Inc. Iron manufacturing process
WO2001088207A1 (de) * 2000-05-15 2001-11-22 Voest-Alpine Industrieanlagenbau Gmbh & Co Verfahren und vorrichtung zur herstellung von roheisen oder flüssigen stahlvorprodukten aus eisenerzhältigen einsatzstoffen
US6858061B2 (en) 2000-05-15 2005-02-22 Voest-Alpine Industrieanlagenbau Gmbh & Co. Method and device for producing pig iron or liquid steel pre-products from charge materials containing iron ore
RU2263714C2 (ru) * 2000-05-15 2005-11-10 Фоест-Альпине Индустрианлагенбау Гмбх Унд Ко Способ и устройство для получения чугуна или жидких стальных продуктов из шихты, содержащей железную руду
KR100769794B1 (ko) 2000-05-15 2007-10-25 지멘스 브이에이아이 메탈스 테크놀로지스 게엠베하 앤드 컴퍼니 고로에서 선철 또는 액상의 1차 강 제품을 생산하기 위한 방법 및 플랜트
US20110209576A1 (en) * 2008-10-31 2011-09-01 Paul Wurth S.A. Method for operating a blast furnace and blast furnace installation
US8545597B2 (en) 2008-10-31 2013-10-01 Paul Wurth S.A. Method for operating a blast furnace and blast furnace installation
US8992664B2 (en) 2009-03-17 2015-03-31 ArcelorMittal Investigación y Desarrollo, S.L. Blast furnace top gas recycling process and corresponding recycling equipment
EP2668301A4 (en) * 2011-01-28 2017-07-05 Energy Independence Of America Corp. Method and apparatus for making liquid iron and steel
KR20140027099A (ko) * 2011-01-28 2014-03-06 에너지 인디펜던스 오브 아메리카 코포레이션 액체 철 및 철강 제조 방법과 장치
US20130344450A1 (en) * 2012-06-21 2013-12-26 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Syngas generator for blast furnace
WO2014198635A1 (de) * 2013-06-14 2014-12-18 CCP Technology GmbH Hochofen und verfahren zum betrieb eines hochofens
US10526670B2 (en) * 2013-06-14 2020-01-07 CCP Technology GmbH Blast furnace and method for operating a blast furnace
EA029710B1 (ru) * 2013-06-14 2018-05-31 Ссп Текнолоджи Гмбх Доменная печь и способ работы доменной печи
WO2015078962A1 (en) * 2013-11-28 2015-06-04 Ccp Technology Blast furnace and method for operating a blast furnace
CN105793442B (zh) * 2013-11-28 2018-02-27 Ccp技术有限公司 处理金属矿石的方法和金属生产用的高炉
CN105793442A (zh) * 2013-11-28 2016-07-20 Ccp技术有限公司 高炉以及操作高炉的方法
US10287643B2 (en) 2013-11-28 2019-05-14 CCP Technology GmbH Blast furnace and method for operating a blast furnace
US10072312B2 (en) 2013-12-20 2018-09-11 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for operating a top gas recycling blast furnace installation
EP2886666A1 (en) 2013-12-20 2015-06-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method for operating a top gas recycling blast furnace installation
CN106702052A (zh) * 2015-11-17 2017-05-24 鞍钢股份有限公司 一种高炉炉顶均压煤气回收系统及方法
US11377700B2 (en) * 2017-07-03 2022-07-05 L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Method for operating an iron- or steelmaking- plant
WO2019057930A1 (en) 2017-09-25 2019-03-28 Paul Wurth S.A. PROCESS FOR PRODUCING HOT SYNTHESIS GAS, ESPECIALLY FOR USE IN OPERATING A HIGH-STOVE

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FR2207990A1 (enrdf_load_stackoverflow) 1974-06-21
GB1438999A (en) 1976-06-09
AU6251873A (en) 1975-05-29
IT1001934B (it) 1976-04-30
BR7309161D0 (pt) 1974-08-29
JPS4979910A (enrdf_load_stackoverflow) 1974-08-01
AT338306B (de) 1977-08-25
ATA986773A (de) 1976-12-15
CA1009455A (en) 1977-05-03
FR2207990B1 (enrdf_load_stackoverflow) 1977-08-12

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