WO2018057025A1 - Procédés et systèmes d'augmentation de la teneur en carbone de l'éponge de fer dans un four de réduction - Google Patents

Procédés et systèmes d'augmentation de la teneur en carbone de l'éponge de fer dans un four de réduction Download PDF

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Publication number
WO2018057025A1
WO2018057025A1 PCT/US2016/053676 US2016053676W WO2018057025A1 WO 2018057025 A1 WO2018057025 A1 WO 2018057025A1 US 2016053676 W US2016053676 W US 2016053676W WO 2018057025 A1 WO2018057025 A1 WO 2018057025A1
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Prior art keywords
gas stream
carbon monoxide
rich gas
providing
rich
Prior art date
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PCT/US2016/053676
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English (en)
Inventor
Mirmohammadyousef Motamedhashemi
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Midrex Technologies, Inc.
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Publication date
Priority claimed from US15/270,692 external-priority patent/US10508314B2/en
Application filed by Midrex Technologies, Inc. filed Critical Midrex Technologies, Inc.
Priority to RU2019110105A priority Critical patent/RU2726175C1/ru
Publication of WO2018057025A1 publication Critical patent/WO2018057025A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D3/00—Charging; Discharging; Manipulation of charge
    • F27D3/16—Introducing a fluid jet or current into the charge
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0073—Selection or treatment of the reducing gases
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/02—Making spongy iron or liquid steel, by direct processes in shaft furnaces
    • 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
    • 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
    • C21B2100/26—Increasing the gas reduction potential of recycled exhaust gases by adding additional fuel in recirculation pipes
    • 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
    • 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
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen

Definitions

  • the present invention relates generally to methods and systems for increasing the carbon content of sponge iron in a direct reduction (DR) furnace.
  • DR direct reduction
  • Direct reduced iron which is also referred to as sponge iron, is typically produced by the reaction of iron ore in a reactive gas stream containing reducing agents, such as 3 ⁇ 4 and CO, in a moving bed or vertical shaft reactor.
  • reducing agents such as 3 ⁇ 4 and CO
  • the product DRI still contains unreacted iron oxide, which may be as high as 15.0 % by weight. Due to the equilibrium-limited nature of reactions (1) and (2), it is not economical to achieve complete (i.e. 100.0%) reduction within the reduction reactor. In fact, when the degree of reduction approaches 100.0 %, an excessively long residence time inside the reduction reactor is required to remove the remaining oxygen from the partially reacted material. While the rate of reduction reactions can be increased to some extent by increasing temperature, such temperature increases are limited by the fact that the operating temperature must be kept below the sintering temperature so that clusters are not formed inside the reduction reactor. Thus, the typical reduction is maintained somewhere in the 85.0 -95.0 % range at the discharge of conventional commercial reduction reactors, depending on the quality of the oxide material and plant operating conditions.
  • Such product DRJ can be used as a source of low-residual iron, in addition to ferrous scrap and pig iron in the production of steel, mainly through an electric arc furnace (EAP) in a steelmaking facility.
  • EAF electric arc furnace
  • the EAF melts that charged material by means of an electric arc, typically accompanied by the injection of oxygen in order to burn impurity carbon and Fe 3 C, if any.
  • the partial or complete combustion of the carbon with oxygen provides a uniform internal source of energy for the EAF when the oxygen is injected into the EAP.
  • the conversion of Fe 3 C into iron and carbon is an exothermic reaction, which improves the thermal efficiency of the EAF. Therefore, the carbon content of the DRI can be interpreted as an energy source, and this energy is finally utilized in the EAF when the DRI is melted.
  • carbon can be generated (i.e. physical carbon - C) or added to the DRI (i.e. chemical carbon - Fe 3 C) through the following global reactions:
  • a hydrocarbon source is normally utilized to produce the reducing agents via a catalytic or non-catalytic reforming process.
  • the required oxidants are typically 3 ⁇ 40 (i.e. steam) and C0 2 .
  • the required oxidant is typically oxygen (0 2 ).
  • very fast partial and complete combustion reactions generate 3 ⁇ 40 and C0 2 for further homogeneous and/or heterogenous reforming reactions.
  • All reforming processes convert some portion of the carbon and hydrogen contents of the hydrocarbons into CO and H 2 , respectively. For instance, in the case of CH 4 being the only hydrocarbon source, the global reaction schemes governing the homogenous and heterogenous reforming processes are:
  • the gas leaving the reforming process is therefore a mixture of CO, H 2 , and unreacted hydrocarbons and oxidants, and is called the reformed gas.
  • the reformed gas is a mixture of CO, H 2 , and unreacted hydrocarbons and oxidants.
  • the present invention makes use of industrially available technologies, i.e. membrane modules (organic/inorganic/organometallic) by which a majority of the hydrogen and or C0 2 are recovered from a reformed gas stream in a plant via the rejection (i.e. separation) of other components.
  • membrane modules organic/inorganic/organometallic
  • Such separation typically results in two different streams with distinct chemical compositions: one rich in CO and the other rich in H 2 .
  • the H 2 -rich gas stream then blends with different gas streams in the process, including, but not limited to, the feed gas stream to the reformer unit, the cooling gas stream, the reducing gas stream, the fuel gas streams, etc.
  • the CO-rich gas stream flows into the transition zone and/or the cooling zone of the reduction furnace to increase the carbon content of the sponge iron.
  • the exothermic nature of reactions (4) and (7) permits the addition of more gas into the transition zone to keep the temperature high.
  • a hydrocarbon-rich gas stream is blended with the CO-rich gas stream
  • the present invention is not limited to the use of membrane modules. All other separation/adsorption technologies (e.g. pressure/vacuum pressure/temperature swing adsorption (PSA/VPSA/TSA) units) meeting process requirements can be used to accomplish the carburization task of the present invention based on the guidelines presented.
  • PSA/VPSA/TSA pressure/vacuum pressure/temperature swing adsorption
  • the present invention provides a method for producing direct reduced iron having increased carbon content, comprising: providing a reformed gas stream from a reformer; delivering the reformed gas stream to a carbon monoxide recovery unit to form a carbon monoxide-rich gas stream and a hydrogen-rich gas stream; and delivering the carbon monoxide-rich gas stream to a direct reduction furnace and exposing partially or completely reduced iron oxide to the carbon monoxide-rich gas stream to increase the carbon content of resulting direct reduced iron.
  • the carbon monoxide-rich gas stream is delivered to one of a transition zone and a cooling zone of the direct reduction furnace.
  • the reformed gas stream generated in a tubular catalytic reformer in direct reduction plants, typically comprises 50.0 - 80.0 % 3 ⁇ 4, 20.0 - 40.0 % CO, 1.0 - 5.0 % C0 2 , 0.0 - 3.0 % C3 ⁇ 4, and 0.0 - 5.0 % N 2 , all dry bases, depending on the operating conditions of the reformer.
  • the method further comprises cooling the reformed gas stream to less than its saturation temperature, preferably ambient temperature, e.g. 20 - 50 degrees C in a cooler/chiller.
  • the method further comprises compressing the reformed gas stream to a pressure of 5.0-20.0 barg, preferably 10.0-15.0 barg, in a single or multi-stage compressor set before flowing into the CO recovery unit.
  • the carbon monoxide -rich gas stream leaving the CO recovery unit should comprise more than 60.0 % carbon monoxide, preferably between 70.0 - 90.0 %.
  • the method further comprises recycling the hydrogen-rich gas stream for use in a direct reduction plant for different potential applications, including, but not limited to, fuel for combustion applications, feed gas to the reformer, and reducing gas to the reduction furnace. In the case of using the hydrogen-rich stream as a fuel, it reduces the amount of C0 2 released to atmosphere.
  • the method further comprises mixing the carbon monoxide-rich gas stream with a hydrocarbon-rich gas stream, preferably natural gas, to form the final carburizing gas.
  • the hydrocarbon-rich gas stream should comprise more than 80.0 % hydrocarbon.
  • the method comprises one or more of a dehumidifier and a mist-eliminator/saturator for reducing the humidity of the hydrocarbon-rich gas stream to below 1.0 %, and preferably dry it.
  • the method comprises one desulfurization step to drop the sulfur content of the hydrocarbon-rich stream to less than 100 ppm, preferably to less than 10 ppm.
  • the system comprises a preheater for elevating the temperature of the final carburizing gas to a temperature of not more than 400 degrees C, preferably somewhere between 50 and 300 degrees C.
  • the method further comprises injection of the final carburizing gas onto the bulk of the already reduced materials inside the reduction reactor.
  • the present invention provides a method for producing direct reduced iron having increased carbon content, comprising: providing a carbon monoxide-rich gas stream; and delivering the carbon-monoxide- rich gas stream to a direct reduction furnace and exposing partially or completely reduced iron oxide to the carbon monoxide-rich gas stream to increase the carbon content of resulting direct reduced iron.
  • the carbon monoxide rich gas stream delivered to the direct reduction furnace comprises at least 60 % CO prior to being mixed with any other gas stream.
  • the carbon monoxide-rich gas stream is delivered to one or more of a transition zone and a cooling zone of the direct reduction furnace.
  • providing the carbon monoxide-rich gas stream comprises initially providing one of a reformed gas stream from a reformer (such as a catalytic reformer (for example, a tubular reformer), a non-catalytic reformer (for example, a partial oxidation reactor), or a combination reformer (for example, an auto-thermal reformer or a two-stage reformer) and a syngas stream from a syngas source (such as a gasifier, a coke oven gas source, or a blast furnace).
  • a reformer such as a catalytic reformer (for example, a tubular reformer), a non-catalytic reformer (for example, a partial oxidation reactor), or a combination reformer (for example, an auto
  • the carbon monoxide-rich gas stream is derived, at least in part, from a carbon monoxide recovery unit that forms the carbon monoxide-rich gas stream and an effluent gas stream.
  • the carbon monoxide rich gas stream leaving the carbon monoxide recovery unit comprises at least 60 % CO.
  • the carbon monoxide recovery unit is operated in parallel with a bypass line, the carbon monoxide recovery unit and the bypass line each providing a portion of the carbon monoxide-rich gas stream.
  • the method also includes recycling the effluent gas stream for use in a direct reduction plant.
  • the method further includes providing a hydrocarbon-rich gas stream to the direct reduction furnace with the carbon monoxide-rich gas stream.
  • the method still further includes providing a hydrocarbon-rich gas stream to one or more of a transition zone and a cooling zone of the direct reduction furnace.
  • FIG. 1 is a schematic diagram illustrating one exemplary embodiment of the process for increasing the carbon content of sponge iron by injecting a carbon monoxide-rich stream into a reduction furnace of the present invention
  • FIG. 2 is a schematic diagram illustrating another exemplary embodiment of the process for increasing the carbon content of sponge iron in a reduction furnace of the present invention, where a hydrocarbon-rich stream, with or without adjustment of its moisture and sulfur content, is blended with the carbon monoxide-rich stream of FIG. 1 ; and
  • FIG. 3 is a schematic diagram illustrating a further exemplary embodiment of the process for increasing the carbon content of sponge iron in a reduction furnace of the present invention, optionally where a carbon monoxide recovery unit bypass is utilized, optionally utilizing reformer or other syngas source, and optionally where a hydrocarbon-rich stream, with or without adjustment of its moisture and sulfur content, is blended with the carbon monoxide-rich stream of FIGS. 1 and 2 and/or delivered directly to the transition zone and/or cooling zone of the reduction furnace.
  • a carbon monoxide recovery unit bypass is utilized, optionally utilizing reformer or other syngas source, and optionally where a hydrocarbon-rich stream, with or without adjustment of its moisture and sulfur content, is blended with the carbon monoxide-rich stream of FIGS. 1 and 2 and/or delivered directly to the transition zone and/or cooling zone of the reduction furnace.
  • the present invention provides an efficient and cost effective process for increasing the carbon content of DRI in a DR plant. It provides a carbon monoxide- rich stream with limited impurities that is directly injected into the bulk of hot and partially or completely reduced materials inside the reduction furnace, or first blended with other gases (e.g. a hydrocarbon-rich gas stream). The combination of coking reactions noticeably increases the carbon content of the resulting DRI, while keeping the temperature of the bulk high.
  • gases e.g. a hydrocarbon-rich gas stream
  • the conventional method of injecting a hydrocarbon-rich stream into the reduction furnace increases the carbon content of the material by endothermic hydrocarbon cracking reactions; hence lowering the material temperature.
  • the present invention boosts the carbon content of the iron via an exothermic reaction that keeps the reduction zone hot, yielding improved plant product! vity. This is a plus for DR plants producing hot-discharged DRI.
  • the process utilizes relatively little equipment.
  • the design can be added as a supplemental plug-in package for existing DR plants.
  • the process 5 of the present invention includes cooling at least a portion of the reformed gas derived from a reformer unit 10 of any design (such as a catalytic reformer (for example, a tubular reformer), a non-catalytic reformer (for example, a partial oxidation reactor), or a combination reformer (for example, an auto-thermal reformer or a two-stage reformer), or any other reducing gas generating unit capable of producing a CO-containing gas with a relatively high CO/C0 2 ratio) to close to ambient temperature (e.g. 30 degrees C) using a cooler/chiller 14.
  • the reformed gas stream 12 contains at least 20.0 % CO.
  • the cooler/chiller 14 can utilize direct contact cooling, indirect contact cooling, refrigeration cooling, etc.
  • reformed gas will lose some of its water content, which in turn improves the carburization potential of the reformed gas.
  • the cool/dry reformed gas optionally flows through a compressor 16 that boosts its pressure (to e.g. 15 barg), as most separation/adsorption methods works best at higher pressures.
  • the gas loses even more water, resulting in further improved carburization potential.
  • the compressed gas after optional temperature adjustment, flows into a system of membrane modules 18 for CO recovery.
  • Any other kind of CO recovery mechanism can also be used for this step, like PSA/VPSA/TSA, refrigeration, etc.
  • the CO-rich gas stream 20 contains more than 60.0 % CO, while the H 2 -rich gas stream 22 may contain more than 70.0 % 3 ⁇ 4 correspondingly.
  • the CO-rich gas stream 20 coming from the CO recovery unit 18 is optionally passed through a preheater 26, which heats it to 50 - 300 degrees C.
  • the CO-rich gas stream 20 is then introduced into the DR furnace 28 below the primary reduction zone 30 (e.g. into the transition zone 32 and/or the cooling zone 34), where the CO-rich gas stream 20 comes into contact with partially or completely reduced iron oxide and deposits carbon based on the well known reactions 2CO C + C0 2 and 3Fe + 2CO Fe 3 C + C0 2 .
  • the partially or completely reduced iron oxide in the transition zone 32 and/or the cooling zone 34 contains 0.0 % - 3.0 % combined carbon before, and up to 4.5 % combined carbon after the CO-rich stream addition.
  • the rejected gas 22 from the CO recovery unit 18 can be used in different portions of the DR plant as fuel, cooling gas, syngas, or process gas, or it can be exported to another facility.
  • the process 7 of the present invention includes cooling at least a portion of the reformed gas derived from a reformer unit 10 of any design (such as a catalytic reformer (for example, a tubular reformer), a non-catalytic reformer (for example, a partial oxidation reactor), or a combination reformer (for example, an auto-thermal reformer or a two-stage reformer), or any other reducing gas generating unit capable of producing a CO- containing gas with a relatively high CO/C0 2 ratio) to close to ambient temperature (e.g. 30 degrees C) using a cooler/chiller 14.
  • the reformed gas stream 12 contains at least 20.0 % CO.
  • the cooler/chiller 14 can utilize direct contact cooling, indirect contact cooling, refrigeration cooling, etc.
  • reformed gas will lose some of its water content, which in turn improves the carburization potential of the reformed gas.
  • the cool/dry reformed gas optionally flows through a compressor 16 that boosts its pressure (to e.g. 15 barg), as most separation/adsorption methods works best at higher pressures.
  • the gas loses even more water, resulting in further improved carburization potential.
  • the compressed gas after optional temperature adjustment, flows into a system of membrane modules 18 for CO recovery.
  • Any other kind of CO recover)' mechanism can also be used for this step, like PSA/VPSA/TSA, refrigeration, etc.
  • the CO-rich gas stream 20 contains more than 60.0 % CO, while the H 2 -rich gas stream 22 may contain more than 70.0 % 3 ⁇ 4 correspondingly.
  • the rejected gas 22 from the CO recovery unit 18 can be used in different portions of the DR plant as fuel, cooling gas, syngas, or process gas, or it can be exported to another facility.
  • a hydrocarbon-rich gas stream 36 (natural gas, for example) is blended with the CO-rich gas stream 20 in a mixer 24 before both are introduced into the DR furnace 28.
  • one or more dehumidification units 38 can be used to make the gas dry for suppressing decarburization reactions.
  • one desulfurization unit 40 can be used to decrease and control the amount of total sulfur below 100 ppm, preferably, below 10 ppm, before flowing into the reduction furnace.
  • the preheater 26 can be used to preheat the hydrocarbon-rich gas stream 36 prior to mixing the hydrocarbon- rich gas stream 36 with the CO-rich gas stream 20 in the mixer 24, and at a different temperature (e.g. about 350-400 degrees C), such that soot formation is minimized as compared to preheating after the mixer 24 at a temperature of about 50-300 degrees C.
  • the preheater 26 can alternatively be disposed before or after the mixer 24 in all embodiments.
  • the present invention makes use of industrially available technologies, i.e. membrane module units (organic/organic/organometallic) by which a majority of the hydrogen and or C0 2 are recovered from a reformed gas stream in a plant via the rejection (i.e. separation) of other components.
  • membrane module units organic/organic/organometallic
  • Such separation typically results in two different streams with distinct chemical compositions: one rich in CO and the other rich in H 2 .
  • the H 2 -rich gas stream then blends with different gas streams in the process, including, but not limited to, the feed gas stream to the reformer unit, the cooling gas stream, the reducing gas stream, the fuel gas stream, etc.
  • the CO-rich gas stream flows into the transition zone and/or the cooling zone of the reduction furnace to increase the carbon content of the sponge iron.
  • the exothermic nature of reactions (4) and (7) above permits the addition of more gas into the transition zone to keep the temperature high.
  • a hydrocarbon-rich gas stream is blended with the CO-rich gas
  • the present invention is not limited to the use of membrane modules. All other separation/adsorption technologies (e.g. pressure/vacuum or pressure/temperature swing adsorption (PSA/VPSA/TSA) units) meeting process requirements can be used to accomplish the carburization task of the present invention based on the guidelines presented.
  • PSA/VPSA/TSA pressure/temperature swing adsorption
  • FIG. 3 provides further refinements to the process 9 of the present invention.
  • the CO recovery unit 18 can be bypassed, in part or in whole, via a bypass line 50.
  • a 30-60% bypass is the most likely scenario. However, lower or higher percentages are possible, anywhere from 0-100%, depending on the chemical composition of the reformed gas or syngas. If a 100% bypass is employed, then the compressor 16 can operate at about 2-7 barg, as opposed to 10-15 barg. However, if a 100% bypass is employed, then a drying unit (not illustrated) can be included along the bypass line 50.
  • the reformer 10 and reformed gas 12 (and the related components) can be replaced with gas from a coal gasifier or the like.
  • the reformer 10 can be a catalytic reformer (for example, a tubular reformer), a non-catalytic reformer (for example, a partial oxidation reformer), or a combination reformer (for example, an auto-thermal reformer or two-stage reformer).
  • the coal gasifier can be substituted with another type of gasifier, a coke oven gas source, an export gas source, a blast furnace, or the like - collectively referred to herein as a syngas source.
  • a two-stage CO recovery unit 18 or the like is preferred to achieve the desired 35-70% CO-rich stream delivery to the transition zone 32 of the DR furnace 28.
  • the hydrocarbon-rich stream 36 is blended with the CO-rich stream 20 and/or delivered directly to the transition zone 32 and/or the cooling zone 34 of the DR furnace 28.
  • all transition zone/cooling injection may be via ports disposed about the circumference of the transition zone 32 and/or cooling zone 34 of the DR furnace 28.
  • the key aspect is that it is partially or completely reduced iron oxide that is exposed to the CO-rich stream 20 and, optionally, the hydrocarbon-rich stream 36.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Manufacture Of Iron (AREA)

Abstract

Cette invention concerne un procédé de production d'éponge de fer ayant une teneur en carbone accrue, comprenant : la fourniture d'un flux de gaz riche en monoxyde de carbone ; et la distribution du flux de gaz riche en monoxyde de carbone vers un four de réduction directe et l'exposition partielle ou complète de l'oxyde de fer réduit au flux de gaz riche en monoxyde de carbone pour augmenter le taux de carbone de l'éponge de fer obtenue. Le flux gazeux riche en monoxyde de carbone est distribué à une zone de transition et/ou une zone de refroidissement du four de réduction directe. Facultativement, la fourniture du flux de gaz riche en monoxyde de carbone comprend initialement la fourniture d'un flux de gaz récupéré à partir d'un reformeur et d'un flux de gaz de synthèse provenant d'une source de gaz de synthèse. Facultativement, le flux de gaz riche en monoxyde de carbone est dérivé, au moins en partie, d'une unité de récupération de monoxyde de carbone qui forme le flux de gaz riche en monoxyde de carbone et un flux de gaz effluent.
PCT/US2016/053676 2016-09-20 2016-09-26 Procédés et systèmes d'augmentation de la teneur en carbone de l'éponge de fer dans un four de réduction WO2018057025A1 (fr)

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RU2019110105A RU2726175C1 (ru) 2016-09-20 2016-09-26 Способы и системы для повышения содержания углерода в губчатом железе в восстановительной печи

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US15/270,692 US10508314B2 (en) 2015-06-24 2016-09-20 Methods and systems for increasing the carbon content of sponge iron in a reduction furnace
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