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WO1988004329A1 - Procede de production de fonte brute liquide et de gaz de gueulard - Google Patents

Procede de production de fonte brute liquide et de gaz de gueulard Download PDF

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Publication number
WO1988004329A1
WO1988004329A1 PCT/SE1987/000571 SE8700571W WO8804329A1 WO 1988004329 A1 WO1988004329 A1 WO 1988004329A1 SE 8700571 W SE8700571 W SE 8700571W WO 8804329 A1 WO8804329 A1 WO 8804329A1
Authority
WO
WIPO (PCT)
Prior art keywords
blast
gas
top gas
crude iron
oxygen
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.)
Ceased
Application number
PCT/SE1987/000571
Other languages
English (en)
Inventor
Per Harald Collin
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
NONOX ENGINEERING AB
Original Assignee
NONOX ENGINEERING AB
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 NONOX ENGINEERING AB filed Critical NONOX ENGINEERING AB
Publication of WO1988004329A1 publication Critical patent/WO1988004329A1/fr
Priority to DK421688A priority Critical patent/DK421688D0/da
Priority to NO883448A priority patent/NO883448L/no
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • 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
    • C21B2100/24—Increasing the gas reduction potential of recycled exhaust gases by shift reactions
    • 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
    • C21B2100/28—Increasing the gas reduction potential of recycled exhaust gases by separation
    • C21B2100/282—Increasing the gas reduction potential of recycled exhaust gases by separation of carbon dioxide
    • 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
    • C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
    • C21B2100/44—Removing particles, e.g. by scrubbing, dedusting

Definitions

  • the present invention relates to a method of producing liquid crude iron and high-grade top gas with a molecular ratio of (CO+H 2 )/N 2 > 2.8 in a blast furnace in which normal temperatures are maintained in the hearth and top zones, and which is fed by a charge of conventional composition, at the same time as additional fuel and preheated blast, obtained by mixing air, oxygen and water, are supplied to the raceways.
  • the invention also relates to a way of making steel and ammonia by producing liquid crude iron and high- grade top gas in the way mentioned above and processing the top gas to ammonia.
  • THM/m 2 .24h tons of crude iron per m 2 of hearth area and 24 hours.
  • Raceways refers to the hot zone ranging from the tuyeres and usually penetrating 1,5-2 m towards the blast furnace centre.
  • a great number of patents, magazine articles etc. discuss the way of optimizing the blast furnace operation, especially by minimizing the costs of fuel/THM.
  • the steps suggested to obtain optimum working conditions include (1) increased blast temperature, (2) charge preparation, (3) gas injection into the stack, (4) pre-reducing the charge, (5) blast additives, (6) high top pressure, and so on. When operating modern conventional optimized furnaces, one or more of the steps (1), (2), (5) and (6) are usually applied.
  • blast furnace optimization has implied steps that reduce the costs of fuel consumption/THM, esoecially by measures reducing the coke content of the charge, but also by replacing the coke with a cheaper fuel, for instance coal dust, injected into the raceways.
  • the optimization has been very successful, and existing blast furnaces, operated in a conventional manner, usually have a fuel consumption less than 370 kgs of coke + 100 kgs of coal dust/THM.
  • the specific crude iron production usually amounts to 55 - 65 THM/m 2 .24h.
  • Such a blast furnace may be operated in a range of -20% of the optimum production, but the prime cost of crude iron will then be higher on both sides of the optimum conditions.
  • the furnace hearth diameter is 8.5 m and its optimum crude iron capacity, that is the capacity having the lowest costs of production/THM, amounts to an average of 130 THM/h at a degree of utilization of 96%.
  • the optimum capacity corresponds to a specific crude iron capacity of 57 THM/m 2 .24h.
  • Required charging of iron raw materials, slag formers, fuel and air blast are shown in Table No 1 that also shows analyses in percentage by weight of the charge components, additional fuel, slags and crude iron together with vol% in the air blast.
  • the specific slag flow in the hearth area amounts to 8.5 tons of slag/m 2 .24h.
  • the adiabatic flame temperature in the raceways is calculated to 2460°K, and the top gas has a temperature of 430°K.
  • the quality improvement of the top gas is obtained by replacing the normal air blast with oxygen enriched air and recirculated top gas, in case (2) combined with fuel injection into the raceways.
  • the first mentioned article is most interesting in relation to the present invention, since it deals with industrial ammonia production on basis of processed top gas from a blast furnace with modified operating conditions. Owing to the CO 2 -content of the recirculated top gas, the fuel consumption and the CO-content of the top gas will increase. Accordingly, see (1), by blowing through separate channels of the tuyeres, 31% of the top gas flow and oxygen enriched air with 55.1 vol% O 2 corresponding to 35.1 vol% O 2 in a total air blast a top gas was obtained that had the following analysis in vol%: 59.5% CO, 13.4% CO 2 , 3.3% H 2 , 23.6% N 2 . The molecular ratio (CO+H 2 )/N 2 then amounted to 2.66.
  • the same article (1) also outlines operation without recirculation of top gas - instead 80 kgs of heavy-oil/THM was injected into the raceway and the production capacity of crude iron was increased by about 10%; the molecular ratio (CO+H 2 )/N 2 , however, was reduced to 0.67, and therefore the suitability of the top gas for further processing to synthesis gas for ammonia production was eliminated.
  • US-A 4.529.440 also describes an operating cycle for blast furnaces in which the air blast is replaced with air enriched to > 65 vol% O 2 together with recirculated top gas containing carbonaceous material. Flow conditions are not stated.
  • the top gas is said to contain a vol% of about 50 vol% CO, and gas discharged from the stack in the upper part of the hearth area is stated to contain about 75 vol% CO.
  • the claims refer to a method of increasing the gas production without increasing the top gas temperature, by removing heat from the stack, for instance by discharging hot gas from the stack, increasing the slag production and the crude iron temperature, that is, by increasing the thermal losses on purpose.
  • US-A 4.013.454 outlines a way of operation of a blast furnace in which the air blast is replaced by carbon dioxide and oxygen, or oxygen enriched air in case ammonia is the end-product of the top gas processing. Also in this case it is a kind of recirculation, since the carbon dioxide will be extracted from the top gas or from the same after water-gas shifting.
  • US-A 2.593.957 describes a method of nitrogen-free operation of a blast furnace.
  • the blast contains solely oxygen and water vapour.
  • the specific crude iron production obtained with this method could have been high as compared with the normal specific production in 1948, but, with the knowledge of the present invention, it can, ex poste, be supposed that a specific crude iron production could not have been reached that would be considered high today.
  • a very high specific production of liquid crude iron and high grade top gas with a molecular ratio of (CO+H 2 )N 2 > 2.8 is possible in a blast furnace together with an energy consumption/THM even lower than that which is obtained in a conventional optimized blast furnace of identical dimensions.
  • the energy consumption/Nm 3 of the synthesis gas obtained from the top gas produced according to the invention is also surprisingly considerably lower than that required by industrial methods of production of such synthesis gas existing today. This is made possible fundamentally by the fact, that the charge flow, the additional fuel flow and the blast flow are controlled so that the specific crude iron production is > 75 THM/m 2 ,24h; The oxygen content in the blast is controlled within the interval 40-60 vol%, the vapour content within the interval 15-30 vol% and the ratio
  • O 2 /H 2 O is maintained > 2.0.
  • the produced top gas is not utilized for recirculation but entirely or almost entirely it can be processed into synthesis gas especially suitable for ammonia production.
  • the content of water vapour should preferably exceed 18 vol%. It can for example be 18-22 vol% and then, a specific production > 82 THM/m 2 .24h can be obtained.
  • the high molecular ratio (CO+H 2 )/N 2 of the top gas according to Example No 1 enables optimal economical exploitation of the exhaust gas from the oxygen fining of the crude iron by intermixing the exhaust gas with the top gas.
  • the gas mixture obtained in this way may be further processed to a composition suitable for ammonia synthesis as will be described below in connection with Example No. 1.
  • crude iron is obtained which, when fined in an LD converter, gives an exhaust gas which, when mixed with the top gas, results in a gas having the analysis shown in Table No 4 (dry gas).
  • the blast flow will be controlled to 575 Nm 3 /THM, and the oil supply to the raceways to 74 kgs/THM in addition to the 100 kgs of coal dust/THM of the conventional operation.
  • the total economy for a blast furnace operated according to the invention combined for instance with an LD-plant and a plant for ammonia synthesis, will be far superior to the economy of two separate plants based upon the same raw materials and producing steel and ammonia respectively, for instance a blast furnace + an LD-converter and a Texaco-gasifier + an NH 3 -synthesis unit.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Air Supply (AREA)
  • Manufacture Of Iron (AREA)

Abstract

Le haut fourneau est alimenté avec une charge d'une composition classique et la soufflerie par un mélange d'oxygène dans la proportion de 50 %, de vapeur d'eau dans la proportion de 20 % et d'azote pour le reste. Un apport supplémentaire de combustible sous forme de poussière de charbon et/ou de fuel est envoyé par les conduits d'amenée. La sole et les zones supérieures sont maintenues aux températures ordinaires. La production de fonte brute obtenue par mètre carré de sole et par 24 heures est très élevée par rapport à celle qu'on obtient par le procédé classique. Le rapport moléculaire CO+H2/N2 du gaz de gueulard est supérieur à 2,8, ce qui le rend propre à la production d'ammoniac.
PCT/SE1987/000571 1986-12-05 1987-12-02 Procede de production de fonte brute liquide et de gaz de gueulard Ceased WO1988004329A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
DK421688A DK421688D0 (da) 1986-12-05 1988-07-28 Fremgangsmaade til fremstilling af flydende raajern og en vaerdifuld topgas
NO883448A NO883448L (no) 1986-12-05 1988-08-03 Fremgangsmaate for fremstilling av flytende raajern og hoeyverdig toppgass.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
SE8605226A SE8605226L (sv) 1986-12-05 1986-12-05 Syntesgas fran masugn
SE8605226-3 1986-12-05

Publications (1)

Publication Number Publication Date
WO1988004329A1 true WO1988004329A1 (fr) 1988-06-16

Family

ID=20366530

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/SE1987/000571 Ceased WO1988004329A1 (fr) 1986-12-05 1987-12-02 Procede de production de fonte brute liquide et de gaz de gueulard

Country Status (4)

Country Link
EP (1) EP0271464A3 (fr)
DK (1) DK421688D0 (fr)
SE (1) SE8605226L (fr)
WO (1) WO1988004329A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2166546C1 (ru) * 1998-10-28 2001-05-10 Праксайр Текнолоджи, Инк. Способ объединения доменной печи и реактора прямого восстановления с использованием криогенной ректификации

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6190632B1 (en) 1999-02-25 2001-02-20 Praxair Technology, Inc. Method and apparatus for the production of ammonia utilizing cryogenic rectification
RU2147321C1 (ru) * 1999-03-12 2000-04-10 Московский государственный институт стали и сплавов (технологический университет) Способ доменной плавки
CN101978078B (zh) * 2008-03-18 2013-03-20 杰富意钢铁株式会社 高炉煤气的分离方法
CN116445671B (zh) * 2023-05-29 2024-10-01 山东钢铁集团永锋临港有限公司 一种高炉煤气高效利用方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2593257A (en) * 1948-08-26 1952-04-15 Standard Oil Dev Co Blast furnace operation
FR1091146A (fr) * 1953-01-06 1955-04-07 Stamicarbon Procédé pour la préparation de ferro-silicium
US2824793A (en) * 1956-11-27 1958-02-25 Alan N Mann Process for producing steel by high temperature gaseous reduction of iron oxide
US3659832A (en) * 1969-06-04 1972-05-02 Mifuji Iron Works Co Ltd Cupolas
US3985520A (en) * 1973-05-30 1976-10-12 Louis Gold Gasification process and apparatus
US4052173A (en) * 1974-07-29 1977-10-04 Dynecology Incorporated Simultaneous gasification of coal and pyrolysis of organic solid waste materials

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2776885A (en) * 1953-01-06 1957-01-08 Stamicarbon Process for producing ferrosilicon
US4013454A (en) * 1975-03-04 1977-03-22 Robert Kenneth Jordan Coproduction of iron with methanol and ammonia
US4529440A (en) * 1978-07-21 1985-07-16 Jordan Robert K Chemicals from coal

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2593257A (en) * 1948-08-26 1952-04-15 Standard Oil Dev Co Blast furnace operation
FR1091146A (fr) * 1953-01-06 1955-04-07 Stamicarbon Procédé pour la préparation de ferro-silicium
US2824793A (en) * 1956-11-27 1958-02-25 Alan N Mann Process for producing steel by high temperature gaseous reduction of iron oxide
US3659832A (en) * 1969-06-04 1972-05-02 Mifuji Iron Works Co Ltd Cupolas
US3985520A (en) * 1973-05-30 1976-10-12 Louis Gold Gasification process and apparatus
US4052173A (en) * 1974-07-29 1977-10-04 Dynecology Incorporated Simultaneous gasification of coal and pyrolysis of organic solid waste materials

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2166546C1 (ru) * 1998-10-28 2001-05-10 Праксайр Текнолоджи, Инк. Способ объединения доменной печи и реактора прямого восстановления с использованием криогенной ректификации

Also Published As

Publication number Publication date
SE8605226D0 (sv) 1986-12-05
EP0271464A3 (fr) 1989-10-25
DK421688A (da) 1988-07-28
EP0271464A2 (fr) 1988-06-15
SE8605226L (sv) 1988-06-06
DK421688D0 (da) 1988-07-28

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