WO2022253938A1 - Procédé de fonctionnement d'une installation de haut-fourneau - Google Patents

Procédé de fonctionnement d'une installation de haut-fourneau Download PDF

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Publication number
WO2022253938A1
WO2022253938A1 PCT/EP2022/065003 EP2022065003W WO2022253938A1 WO 2022253938 A1 WO2022253938 A1 WO 2022253938A1 EP 2022065003 W EP2022065003 W EP 2022065003W WO 2022253938 A1 WO2022253938 A1 WO 2022253938A1
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WIPO (PCT)
Prior art keywords
blast furnace
gas
stream
hydrogen
plant
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PCT/EP2022/065003
Other languages
English (en)
Inventor
Klaus Peter KINZEL
Gilles Kass
Miriam VALERIUS
Original Assignee
Paul Wurth S.A.
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Filing date
Publication date
Application filed by Paul Wurth S.A. filed Critical Paul Wurth S.A.
Priority to CN202280037764.0A priority Critical patent/CN117377778A/zh
Priority to BR112023024416A priority patent/BR112023024416A2/pt
Priority to JP2023572537A priority patent/JP2024522088A/ja
Priority to EP22731244.4A priority patent/EP4347897A1/fr
Priority to KR1020237040652A priority patent/KR20240016962A/ko
Priority to AU2022284294A priority patent/AU2022284294A1/en
Publication of WO2022253938A1 publication Critical patent/WO2022253938A1/fr

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Classifications

    • 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
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/001—Injecting additional fuel or reducing agents
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B9/00—Stoves for heating the blast in blast furnaces
    • C21B9/14—Preheating the combustion air
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B5/00—Making pig-iron in the blast furnace
    • C21B5/001—Injecting additional fuel or reducing agents
    • C21B2005/005—Selection or treatment of the reducing gases
    • 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
    • C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
    • C21B2100/42—Sulphur removal
    • 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 generally relates to a method for operating a blast furnace installation as well as to such a blast furnace installation.
  • blast furnace gas BFG
  • top gas the blast furnace gas exiting the top of the blast furnace
  • CO2 One component in the blast furnace gas
  • the blast furnace gas being combusted usually comprises besides the before mentioned CO2 considerable amounts of N2, CO, H2O and H2.
  • the N2 content however, largely depends on whether hot air or (pure) oxygen is used for the blast furnace.
  • PSA Pressure Swing Adsorption
  • VPSA Vacuum Pressure Swing Adsorption
  • the blast furnace gas is used as a reforming agent for hydrocarbons in order to obtain a synthesis gas (also referred to as syngas) that can be used for several industrial purposes.
  • a synthesis gas also referred to as syngas
  • the blast furnace gas is mixed with a carbonaceous gas that contains at least one hydrocarbon (e.g. lower alkanes).
  • the hydrocarbons of the gas react with the CO2 in the blast furnace gas to produce H2 and CO.
  • the hydrocarbons react with the H2O in the blast furnace gas also producing H2 and CO by so called steam reforming reaction.
  • the present invention proposes, in a first aspect, a method for operating a blast furnace, comprising the steps of
  • a stream of hh is added to the hydrocarbon containing gas before step (c) and/or to the stream of blast furnace gas before step (c) and/or to a mixture comprising the blast furnace gas and the hydrocarbon containing gas before step (c) and/or to the stream of syngas before step (d).
  • hh addition is performed in order to increase the amount of hh injected (i.e. fed) to the blast furnace.
  • a method according to the invention does not comprise any hh removal step.
  • the feeding of at least a portion of the stream of syngas to the blast furnace occurs at the shaft level / through the shaft of the blast furnace.
  • the feeding of at least a portion of the stream of syngas to the blast furnace occurs at the tuyere level / through a tuyere of the blast furnace or both through the shaft of the blast furnace and through the tuyere of the blast furnace.
  • a portion of the stream of syngas is fed at the shaft level and another portion of the stream of syngas is simultaneously fed through the tuyere of the blast furnace, while in other embodiments, the feeding of a portion of the stream of syngas occurs only through the shaft of the blast furnace.
  • a further stream of hydrogen and/or hydrocarbons may be added at the tuyere of the blast furnace.
  • the blast furnace is normally used for producing pig iron.
  • a syngas refers to a synthesis gas produced by a reforming process in a reformer.
  • the reforming plant comprises at least one reformer.
  • the reforming plant may comprise a plurality of reformers, the reformers being arranged in a series or in parallel with regard to each other, or the reforming plant may comprise a plurality of reformers arranged to form at least two series of reformers, the at least two series being arranged in parallel with respect to each other.
  • the reformers of the reforming plant may be of any type, such as e.g. a regenerative reformer or a catalytic dry and/or wet reformer of any type, in particular bottom fired, side fired, terrace type or top fired.
  • reformers may be identical or different from each other.
  • the reforming plant may e.g. comprise a pre-reformer and a main reformer.
  • the exact number, type and arrangement of reformers in the reforming plant could advantageously be adapted depending on the level of subsequent feeding of the produced syngas to the blast furnace in order to meet requirements for the produced syngas (such as e.g. temperature, reduction degree), or depending on the position of the addition of the hydrogen.
  • the reforming process For the reforming process to take place in the reforming plant, as carbon dioxide and steam source, e.g. the collected blast furnace gas, and a hydrocarbon containing gas must be combined (i.e. mixed) to form a gas mixture before or on entering the reaction chamber of the first reformer of the reforming plant.
  • the first reformer corresponds to this reformer.
  • the gas being reformed in the reactor is a gas mixture of the blast furnace gas and hydrocarbon containing gas and possibly also steam and which can be more or less well mixed.
  • Combining the blast furnace gas with the hydrocarbon containing gas and possibly the steam in general refers to "allowing the blast furnace gas to mix with the hydrocarbon gas and possibly the steam". This may comprise (actively) mixing the blast furnace gas with the hydrocarbon containing gas and possibly the steam, i.e. applying mechanical force to mix the gases. However, in some cases it may be sufficient e.g. to inject the gases into a pipe, so that mixing occurs more or less passively by convection and/or diffusion. It is understood, though, that the chemical reaction is enhanced by a higher degree of mixing.
  • the gases are combined and mixed in a dedicated vessel which may be referred to as a mixing vessel or mixing chamber.
  • a dedicated vessel which may be referred to as a mixing vessel or mixing chamber.
  • the present invention also proposes a method for operating a blast furnace plant by improving the efficiency of hydrogen utilization.
  • the method comprises the combination of H2 addition to the blast furnace, with a reforming reaction, wherein the part of hydrogen utilisation in a blast furnace plant comprising the blast furnace, a reform ing plant and a cowper plant is above 60% of the hydrogen fed to the blast furnace and preferably above 65% of the hydrogen fed to the blast furnace, wherein the hydrogen fed to the blast furnace is totalling a flow of minimum 200 Nm 3 /t of produced hot metal and out of which a minimum of 50Nm 3 / 1 of hot metal are fed to the blast furnace plant in form of molecular hydrogen H2.
  • the hydrogen utilisation is defined as: (hydrogen input to the blast furnace plant - hydrogen export from the blast furnace plant) / (hydrogen input to the blast furnace plant).
  • the hydrogen input to the blast furnace, or hydrogen fed to the blast furnace, or hydrogen input to the blast furnace plant is defined as the total hydrogen content of the bosh gas (i.e. gas in the cohesive zone of the blast furnace) and of the shaft gas injected to the blast furnace at shaft level.
  • This hydrogen input to the blast furnace includes in particular the hydrogen contained in the syngas, in the injected molecular hydrogen hh, in the other hydrogen containing gases, in the injected coal and/or tar, in the humidity of the injected gases and solid fuels and in the humidity of the hot blast.
  • the hydrogen export is defined as the hydrogen contained in the blast furnace gas leaving the blast furnace at its top subtracting its utilization in the cowper plant and if applicable in the reforming plant.
  • the present invention proposes a blast furnace plant comprising a blast furnace provided with a shaft, tuyeres arranged for feeding a stream of hydrogen containing gas to the blast furnace and gas inlets in the shaft of the blast furnace arranged for feeding a stream of syngas to the blast furnace, preferably a stream of hot syngas.
  • the blast furnace plant further comprises: a reforming plant comprising at least one reformer in fluidic connection with the top of the blast furnace and with a source of a hydrocarbon containing gas, said reforming plant being arranged for converting a stream of blast furnace gas and the hydrocarbon containing gas to a stream of syngas and being in fluidic downstream connection with said gas inlets in the shaft of the blast furnace; and a source of a stream of hh in fluidic connection with the at least one reformer and/or with the gas inlets in the shaft of the blast furnace and/or the tuyere of the blast furnace.
  • the reforming plant may also be in fluidic downstream connection with the tuyeres of the blast furnace.
  • the blast furnace installation is configured for being operated by implementing a method according to the first aspect and as described more in detail below.
  • the disclosure thus proposes an integrated method and a corresponding installation allowing for operating a blast furnace with a reduced coke and other carbon source rate, with a smaller CO2 footprint and with an increased efficiency of hydrogen (H2) utilization.
  • the present inventors have found that by combining hydrogen (H2) utilization, recycling of blast furnace gas with reforming of hydrocarbons, the CO2 emission of a blast furnace installation could be reduced without negatively affecting the quality of the produced metal, e.g. pig iron.
  • H2 hydrogen
  • One of the major advantages of the present method and installation is thus that by reconditioning part of the blast furnace gas for re-use, the overall CO2 production of the blast furnace operation can be substantially reduced.
  • Another major advantage is that by reconditioning part of the blast furnace gas for re-use, the overall energy efficiency of the blast furnace plant, comprising the blast furnace, the reforming plant and a cowper plant, can be increased, thereby improving the efficiency of hydrogen utilization.
  • Added H2 is generally not entirely consumed inside the blast furnace plant, so that at least a part of the added H2 exits the blast furnace plant within the export blast furnace gas.
  • Export blast furnace gas means in the present context the blast furnace gas that is left from the blast furnace gas exiting the blast furnace after its consumption within the blast furnace plant, more specifically after its consumption in the blast furnace, cowper plant and reforming plant.
  • the injection of the resulting syngas at the shaft level of the blast furnace allows for a significant reduction of the coke rate, i.e. the amount of coke and/or other carbon source per ton of pig iron produced.
  • the injection of syngas in the shaft of the blast furnace is allowing a higher tuyere injection of pulverized coal, of natural gas, and especially also of hydrogen, or of other materials.
  • extra amounts of coke can be replaced by hydrogen rich auxiliary fuels allowing to further reduce the carbon content of the blast furnace reductant and consequently the CO2 emissions.
  • the syngas injection temperature through the shaft should be about 950°C but not exceed 1050°C in order not to melt the material within the furnace,
  • H2 can advantageously be added to the stream of hot syngas downstream of the at least one reformer.
  • the stream of H2 acts thus as a coolant of the stream of syngas.
  • Hydrogen may also be added to both the hydrocarbon containing gas and/or the stream of blast furnace gas upstream of the reformer and to the stream of syngas to be injected at the shaft level. Addition of hydrogen needs to be equilibrated between its utilisation as coolant of the stream of syngas to be fed through the shaft and its addition to the hydrocarbon containing gas and/or the stream of blast furnace gas upstream of the reformer for syngas production. As already mentioned, the addition of hydrogen to the hydrocarbon containing gas and/or the stream of blast furnace gas will help to reduce the soot formation during the reforming reaction.
  • Another advantage of the present inventive methods for operating a blast furnace is that the hydrogen is injected either as cold hydrogen (i.e. non-heated stream heated only to temperature levels which are economically interesting) or as pure hot H2 (i.e. without CO2 and/or H2O content) thus preventing steel cracking.
  • cold hydrogen i.e. non-heated stream heated only to temperature levels which are economically interesting
  • pure hot H2 i.e. without CO2 and/or H2O content
  • the disclosed method for operating a blast furnace further comprises the sub-steps of: a1 ) Optionally hydrogenation and/or desulfurization of the hydrocarbon containing gas and/or blast furnace gas c1 ) feeding another portion of the blast furnace gas, on its own or in a mixture with other gases, to the burners of the reformer
  • the gas cleaning, the reforming conditions and the syngas temperature requirements could advantageously be adapted depending on the position of the addition of the hydrogen.
  • H2 may be added to the stream of blast furnace gas and/or to the hydrocarbon containing gas upstream of the hydrogenation unit (before step a1 ), upstream of the reformer (before step b) and/or downstream of the reforming plant (after step c) in case that the syngas temperature is too high for its direct injection in the blast furnace.
  • a stream of steam may also be added to the hydrocarbon containing gas before step a1 ), step c) and/or to the stream of blast furnace gas before step c) or to a mixture of blast furnace gas and hydrocarbon containing gas before step c).
  • the stream of hh and/or the stream of hydrocarbon containing gas and/or the stream of blast furnace gas might be heated, in particular any one or all of these streams may be heated prior the reforming process, preferably in a heat exchanger, the heat exchanger preferably recovering part of the energy of the flue gas coming from the reformer.
  • the stream of hydrocarbon containing gas and/or the stream of blast furnace gas are pre-heated (i.e. heated to a moderate temperature) upstream of the reformer.
  • the stream of hh may be pre-heated in a dedicated heating device prior to its addition to the stream of hydrocarbon containing gas and/or the stream of blast furnace gas.
  • the stream of hh may be pre-heated simultaneously with the stream of hydrocarbon containing gas and/or the stream of blast furnace gas after the addition.
  • the stream of H2 is added to the stream of syngas downstream of the reformer, the stream of H2 is preferably not heated or only to temperature levels which are economically interesting, i.e. for example temperature levels not requiring costly precautions against high temperature hydrogen attack, typically below 600°C or even below 400°C.
  • a non-heated stream of hydrogen or a stream of hydrogen heated only to temperature levels which are economically interesting is referred to as cold.
  • a desulfurization of the hydrocarbon containing gas may be required, depending on its composition.
  • the removal of the sulphur, for example in a zinc oxide bed requires that the sulphur is present in an inorganic form, more specifically in the form of H2S.
  • the hydrocarbon containing gas very often comprises also organic sulphur which needs to be converted in inorganic sulphur, H2S, in the presence of hydrogen and a specific catalyst. Therefore, in embodiments, it might be advantageous to add the hydrogen to the hydrocarbon gas also prior to the hydrogenation step (step a1 ) in case that a desulphurization will be required. The latter does not necessarily apply to the blast furnace gas since the blast furnace gas itself may contain sufficient hydrogen for the hydrogenation process.
  • a fuel gas comprising a portion of the blast furnace gas as well as air for its respective utilisation in the burners of the at least one reformer of the reforming plant is also heated in a heat exchanger using a part of the energy of the flue gas of the reforming process.
  • the stream of hh is produced by electrolysis in an electrolysis cell.
  • the hydrogen is renewable or “green”.
  • a renewable or “green” hydrogen means that it is preferably produced by water and/or steam electrolysis and/or that the electric power for operating the electrolysis cell is produced by a renewable source, such as wind, solar and/or hydropower.
  • hydrocarbon or “hydrocarbon containing gas” in the context of the present disclosure means any hydrocarbon which is in gaseous state at ambient temperature.
  • Such hydrocarbon gas thus comprises natural gas, i.e. a naturally occurring hydrocarbon gas mixture of fossil origin consisting primarily of methane and commonly including varying amounts of other higher alkanes, but also gases with similar hydrocarbon constituents, such as biogas, coke oven gas, etc.
  • Coke oven gas is a mixture of several gases, mainly hydrogen (i.e. having a hydrogen content of at least 50%), methane (conventionally amounting for 25% of the coke oven gas) and the rest being a mixture of various gases such as nitrogen, CO, CO2 or H2O.
  • the coke oven gas itself already contains a high amount of hydrogen.
  • the hydrocarbon containing gas comprises natural gas, coke oven gas and/or biogas.
  • the reformer can be of any kind, such as a catalytic reformer, a regenerator type reactor also called a regenerative reformer, a reformer with plasma torches, a partial oxidation reformer, a reformer with oxygen/carbon and/or hydrocarbon burners.
  • the stream of syngas results from a dry or wet reforming process.
  • the hydrocarbons of the hydrocarbon containing gas such as methane
  • the hydrocarbons react with the H2O in the blast furnace gas also to produce H2 and CO.
  • the reforming process can be performed either catalytically or non-catalytically.
  • the reforming of natural gas process may be performed either catalytically or non-catalytically while the reforming of coke oven gas is preferably performed non- catalytically.
  • a process performed catalytically is performed in the presence of a catalyst while a process performed non-catalytically is performed without a catalyst, i.e. in the absence of a catalyst.
  • the reforming process can furthermore be performed in a single reformer or also in multiple reformers, as for example in a pre-reformer and a secondary or main reformer.
  • the produced syngas needs to be of high quality for its effective utilisation in the blast furnace. This quality is normally described with its reduction potential being defined as the following molar ratio: (cC0+cH 2 )/(cH 2 0+cC0 2 ). In order to ensure a sufficient quality of the syngas, the reduction potential should be as high as possible and preferably higher than six, more preferably higher than seven and most preferably higher than seven and a half.
  • a certain degree of reduction potential of a syngas can only be achieved by applying a minimum temperature level to the reforming process.
  • the reforming process is preferably carried out at a temperature high enough for the stream of syngas to have both a desired reduction potential and a temperature allowing its feeding through the shaft of the blast furnace.
  • hydrogen addition will help to reduce the soot formation in the reformer and in the piping leading from the reformer to the blast furnace to feed the syngas through the shaft of the blast furnace.
  • the stream of blast furnace gas may advantageously be subjected to a gas cooling and/or cleaning and/or pressurization step, preferably a vapor removal step, a dust removal step, metals removal step, HCI removal step and/or sulfurous component removal step, before being fed to the reformer.
  • a second stream of the blast furnace gas may be used on its own, or in a mixture with other gases, in the burners of the reforming plant.
  • as much as possible of the blast furnace gas exiting the blast furnace is collected for its utilization in the cowper and reforming plant.
  • the export blast furnace gas that is fed to other units within the steel plant is as small as possible. Preferably it is so low that its utilization in the thermal power plant is avoided.
  • in fluidic connection means that two devices are connected by conducts or pipes such that a fluid, e.g. a gas, can flow from one device to another.
  • a fluid e.g. a gas
  • This expression includes means for changing this flow, e.g. valves or fans for regulating the mass flow, compressors for regulating the pressure, etc., as well as control elements, such as sensors, actuators, etc. necessary or desirable for an appropriate control of the blast furnace operation as a whole or the operation of each of the elements within the blast furnace installation.
  • reformer means any container in which a reforming process could be performed, such as a reformer reactor or a reformer vessel.
  • shaft feeding means the injection of a material (such as e.g. a gas) above the hot blast level, i.e. above the bosh, preferably within the gas solid reduction zone of ferrous oxide above the cohesive zone in a blast furnace.
  • a material such as e.g. a gas
  • “Feeding ... at the tuyere level”, “Feeding ... through the tuyere”, “fed at the tuyere level”, or “injected at the tuyere level” implies the injection of a material (such as e.g. a gas) through a tuyere of a blast furnace.
  • step (c) refers to reforming in general. It covers producing syngas for injection through either the shaft or the tuyere, and also producing syngas for simultaneous injection through shaft and tuyere.
  • Fig. 1 is a schematic view of an embodiment of a first variant of a blast furnace plant configured to implement the present blast furnace operating method
  • Fig. 2 is a schematic view of an embodiment of a second variant of a blast furnace plant configured to implement the present blast furnace operating method
  • Fig. 3 is a schematic view of an embodiment of a third variant of a blast furnace plant configured to implement the present blast furnace operating method
  • Fig. 4 is a graph showing the variation of C 2 FI 4 concentration in a reformer as a function of the temperature for various hydrogen content.
  • Coke is the main energy input in the blast furnace iron making. From the CO2 and often also from the economic point of view, this is the less favorable energy source. Substitution of coke by other energy sources, mostly injected at tuyere level, is widely employed. Due to cost reasons mostly pulverized coal is injected, however in countries with low natural gas price, this energy is used. Often residues like waste plastics are also injected in the blast furnace. In an ambition of reduction of greenhouse gas emissions, industrial operations start to incorporate also hydrogen in their auxiliary fuels and with the expected higher availability of hydrogen it is expected that the contribution of hydrogen as auxiliary fuel will strongly increase.
  • blast furnace gas BFG
  • BFG blast furnace gas
  • About 25% of that blast furnace gas leaving the blast furnace is normally used in the cowper plant for heating of the blast that is injected at the tuyeres of the blast furnace.
  • the remaining 75% of that blast furnace gas, containing about 30% of the energy input to the blast furnace is generally used for internal heat requirements in the steel plant, but also for electric energy production.
  • the synthesis gas production should, beside the utilization of a CO2 lean hydrocarbon, also use blast furnace gas as much as possible in order to improve the CO2 emission reduction potential from the blast furnace iron making, as well as, if available in the blast furnace plant, converter gas and/or cold basic oxygen furnace (BOF) gas.
  • blast furnace gas as much as possible in order to improve the CO2 emission reduction potential from the blast furnace iron making, as well as, if available in the blast furnace plant, converter gas and/or cold basic oxygen furnace (BOF) gas.
  • the hydrogen utilization for iron making can be divided in the direct utilization of the hydrogen in the blast furnace as well as its utilization in the auxiliary plants, specifically the cowper plant and if installed the reforming plant for the production of the syngas to be injected in the shaft of the blast furnace.
  • Eta H2 ((H2 in BF) - (H2 out BF in top gas)) / (H2 in BF).
  • BF means blast furnace, so that (H2 in BF) refers to the flow of H2 going into the blast furnace, and (H2 out BF in top gas) refers to the flow of H2 in the blast furnace top gas exiting the top of the blast furnace.
  • H2 in BF is defined as the total hydrogen content of the bosh gas (i.e. gas in the cohesive zone of the blast furnace) and of the shaft gas injected to the blast furnace at shaft level.
  • This hydrogen input to the blast furnace includes in particular the hydrogen contained in the syngas, in the injected molecular hydrogen H2, in the other hydrogen containing gases, in the injected coal and/or tar, in the humidity of the injected gases and solid fuels and the humidity of the hot blast.
  • “Fh out BF in top gas” is defined in the dry flow rate of the top gas leaving the blast furnace times the dry concentration of hydrogen in that top gas.
  • the eta Fh is normally below 50% and often below 45%.
  • the eta Fh, and thus the percentage of hydrogen utilisation in the blast furnace has furthermore the characteristic that it decreases with increasing hydrogen input into the blast furnace. This means when one wants to use more hydrogen in the blast furnace, the efficiency of its utilisation strongly decreases and a much bigger portion of the hydrogen introduced in the blast furnace is leaving it with the top gas. In consequence also the attainable coke rate reduction per kg of injected hydrogen decreases which indirectly reduces the CO2 reduction potential of the injected hydrogen.
  • auxiliary fuel i.e. hydrogen containing gas
  • the enrichment of oxygen must be increased in order to maintain the flame temperature.
  • Increasing the oxygen enrichment in the blast furnace signifies reducing the amount of natural blast (air) that will be used in the blast furnace. In consequence the overall amount of hot blast entering the blast furnace is decreased. This means that less blast furnace gas can be used for heating the hot blast.
  • the blast furnace uses only coke and pulverised coal injection at the tuyere, whereas in case 1 , cold hydrogen is additionally injected at the tuyere level of the blast furnace.
  • the cowper plant as well as the reforming plant shall preferably be equipped with heat recovery systems for preheating the combustion air and/or combustion gas.
  • the efficiency of both plants should be above 70%, more specifically above 80%.
  • cCO means the molar concentration of CO in the syngas
  • cH 2 means the molar concentration of H 2 in the syngas
  • cH 2 0 means the molar concentration of H 2 0 in the syngas
  • cC0 2 means the molar concentration of C0 2 in the syngas.
  • the syngas is used for specific applications, such as pure hydrogen production, ammonia or the production of other chemical components. Thereby a specific ratio of hydrogen to CO within the syngas is generally required.
  • the object of using syngas in a blast furnace is the reduction of ore, which is achieved with both reducing components, CO and hydrogen. While there is a difference between the reduction of ore with CO or hydrogen, this difference is relatively marginal considering that syngas is only one part of the reducing gas used within the blast furnace.
  • the hydrogen can simply be added at the tuyere of the blast furnace, in form of H2 and also in the form of hydrocarbon. However, it is possible to also use the hydrogen addition to positively impact the syngas production and its injection at the shaft of the blast furnace.
  • a stream of hydrogen preferably renewable hydrogen
  • reduction potential and reduction degree are used as synonym for one another and both refers to the molar ratio (cC0+cH2)/(cH20+cC02).
  • Hydrocarbon gas reforming such as natural gas reforming can principally be performed by following reactions:
  • This heat can be supplied indirectly by burning a fuel gas and transferring the flue gas heat to the reactor, or also by combining the reforming reaction with a partial oxidation reaction according the below formula:
  • This acetylene can then be a molecule (precursor) in the creation of aromatic hydrocarbons which are part of the soot or can be thermally decomposed according to following reaction:
  • FIG. 1 illustrates an embodiment of a first variant of the present method for operating a blast furnace comprising the simultaneous injection of a first stream of syngas through the shaft of a blast furnace and of a second stream of syngas through the tuyere of the blast furnace.
  • Blast furnace gas 10 exiting the blast furnace 12 is collected at the top of a blast furnace 12.
  • the collected blast furnace gas 10 is generally pre-treated upon exiting the blast furnace.
  • Pre-treatment of the stream of blast furnace gas comprises first a cooling to reduce its vapor content, a cleaning, in particular a removing of dust and/or HCI and/or metal compounds, and then a pressurization to have a pressure sufficient for an eventual desulphurization, the heating, the reforming process and injection in the blast furnace.
  • the cooling, cleaning and pressurization of the blast furnace gas occurs in a cooling, cleaning and pressuring unit 14.
  • separate units could be used, each unit performing either one of cooling, cleaning or pressuring the blast furnace gas.
  • one unit may be responsible for two of cooling, cleaning and pressuring the blast furnace gas, the third pre-treatment step being performed in a separate unit.
  • a cooling, cleaning and pressuring unit is a unit configured to cool, clean and pressurize a stream of gas, without assuming that it is mandatory to perform the various steps (cooling, cleaning and pressuring) in this order.
  • the pressurization can take place upstream of the cleaning, such as e.g. in embodiments wherein the cleaning of the stream of gas is a desulphurization.
  • the stream of blast furnace gas is split in three streams.
  • a first stream of blast furnace gas 16 is fed to a first reforming plant 18 and a second stream of blast furnace gas 20 is fed to a second reforming plant 22.
  • both reforming plants are regenerative type reforming plants.
  • a third stream of blast furnace gas 27 is referred to as blast furnace export gas and corresponds to blast furnace gas being fed to another unit of a steel making plant comprising the blast furnace plant with the reforming plants 18, 22.
  • a stream 24 of coke oven gas and/or natural gas is fed to the reforming plants 18, 22.
  • Basic oxygen furnace gas and/or steam might optionally be added to the stream of blast furnace gas (upstream and/or downstream of the cooling, cleaning and pressuring unit 14) and/or the stream of hydrocarbon containing gas 24 and/or directly to a reforming plant 18, 22 (not shown).
  • a reforming of the first stream of blast furnace gas 16 along with the stream 24 of coke oven gas and/or natural gas is done in the first reforming plant 18 to produce a first stream of syngas 26.
  • a reforming of the second stream of blast furnace gas 20 along with the stream 24 of coke oven gas and/or hydrocarbon containing gas is done in the reforming plant 22 to produce a second stream of syngas 28.
  • Both reforming processes are dry and/or wet reforming processes, possibly also in combination with a partial oxidation, leading to the formation of two streams of syngas 26, 28 with high CO and hh contents. Reforming processes occurs at pressure between 1 ,5 and 10 barg and depending on the reforming plant at a temperature above 900 °C, preferably above 950 °C, more preferably above 1000 °C.
  • Blast furnace gas and/or hydrocarbon containing gas might optionally be heated prior to the reforming process (not shown). Heating might be performed e.g. by using tube bundle heat exchangers.
  • the second stream of syngas 28 exiting the second reforming plant 22 is fed to the blast furnace through the tuyere 30 with a temperature of about 1200 °C and a pressure of 2 to 6 barg.
  • the blast furnace installation comprises an electrolysis cell 32 fueled by electrical power 34 to produce a stream of H236 by electrolysis, preferably by water/steam electrolysis.
  • the electrical power 34 fueling the electrolysis cell 32 is preferably renewable or “green”, i.e. obtained from a renewable source such as wind, solar and/or hydropower.
  • said hydrogen can be produced from natural gas through a pyrolysis process with solid carbon formation, or with combined Carbon Capture and Storage (CCS) technology and/or Carbon Capture and Utilization (CCU) technology. Hydrogen might also be produced by methane thermal cracking or steam methane reforming with combined CCS and/or CCU technology.
  • CCS Carbon Capture and Storage
  • CCU Carbon Capture and Utilization
  • the stream of H236 produced by the electrolysis cell is added to the first stream of syngas 26 downstream of the first reforming plant 18 and upstream of gas inlets 38 disposed through the shaft inside the blast furnace 12.
  • the first stream of syngas 26 added with hydrogen 36 form a stream of H2-enriched gas 40, which is fed to the blast furnace through the gas inlets 38 at the shaft level, with a temperature of about 900°C and a typical pressure of 1 ,5 to 4 barg.
  • the stream of H2 36 acts as a coolant of the first stream of syngas 26.
  • Using said hydrogen in this way i.e. as a coolant, completely eliminates the need of heating said hydrogen prior to its injection through the shaft of the blast furnace 12 in an expensive heating device. Indeed, the excess heat of the syngas 26 heats said hydrogen. This allows to increase the efficiency of the process by eliminating both the need for syngas cooling and hydrogen heating.
  • FIG. 2 illustrates an embodiment of a second variant of the present method for operating a blast furnace comprising the simultaneous injection of a first stream of syngas through the shaft of a blast furnace and of a second stream of syngas through the tuyere of the blast furnace.
  • Blast furnace gas 110 exiting the blast furnace 112 is collected at the top of a blast furnace 112.
  • the collected blast furnace gas 110 is generally pre-treated upon exiting the blast furnace.
  • Pre-treatment of the stream of blast furnace gas comprises first a cooling to reduce its vapor content, a cleaning, in particular a removing of dust and/or HCI and/or metal compounds and/or sulfurous components, and then a pressurization to have a pressure sufficient for the reforming process and its injection in the blast furnace.
  • the cooling, cleaning and pressurization of the blast furnace gas occurs in a cooling, cleaning and pressuring unit 114.
  • separate units could be used, each unit performing either one of cooling, cleaning or pressuring the blast furnace gas.
  • one unit may be responsible for two of cooling, cleaning and pressuring the blast furnace gas, the third pre-treatment step being performed in a separate unit.
  • the stream of blast furnace gas is split in three streams.
  • a first stream of blast furnace gas 116 is fed to a first reforming plant 118 and a second stream of blast furnace gas 120 is fed to a second reforming plant 122.
  • both reforming plants are regenerative type reforming plants.
  • a third stream of blast furnace gas 127 is referred to as blast furnace export gas and corresponds to blast furnace gas being fed to another unit of a steel making plant comprising the blast furnace plant with the reforming plants 118, 122.
  • the blast furnace installation comprises, in addition to the blast furnace and the cooling, cleaning and pressuring unit 114, a source for a stream 124 of coke oven gas and/or natural gas in fluidic communication with each of the reforming plants 118, 122, and an electrolysis cell 132 fueled by electrical power 134 to produce a stream of hh 136 by electrolysis, preferably by water electrolysis.
  • the electrical power 134 fueling the electrolysis cell 132 is preferably renewable or “green”, i.e. obtained from a renewable source such as wind, solar and/or hydropower.
  • the stream of hh 136 produced by the electrolysis cell is added to the stream 124 of coke oven gas and/or natural gas upstream of the reforming plants 118, 122 to form a stream of hh-enriched hydrocarbon containing gas 142, which is fed to each of the reforming plants 118, 122.
  • Basic oxygen furnace gas and/or steam might optionally be added to the stream of blast furnace gas (upstream and/or downstream of the cooling, cleaning and pressuring unit 114) and/or the stream of hydrocarbon containing gas 124 and/or to the stream of hh 136 and/or directly to a reforming plant 118, 122 (not shown).
  • a reforming of the first stream of blast furnace gas 116 along with the stream of hh-enriched hydrocarbon containing gas 142 is done in the first reforming plant 118 to produce a first stream of syngas 126.
  • a reforming of the second stream of blast furnace gas 120 along with the stream of hh-enriched hydrocarbon containing gas 142 is done in the second reforming plant 122 to produce a second stream of syngas 128.
  • Both reforming processes are dry reforming, leading to the formation of two streams of syngas 126, 128 with high CO and hh contents. Reforming processes occurs at pressure between 1 ,5 and 10 barg and depending on the reforming plant at temperatures above 900 °C, preferably 1000 °C, more preferably above 1200 °C.
  • Blast furnace gas and/or hydrogen containing gas might optionally be heated prior to the reforming process (not shown). Heating might be performed e.g. by using tube bundle heat exchangers.
  • the first stream of syngas 126 exiting the second reforming plant 118 is fed to the blast furnace through gas inlets 138 disposed through the shaft inside the blast furnace 112 (i.e. the second stream of syngas 126 is fed through the shaft of the blast furnace) with a temperature of about 950 °C and a pressure of 1 ,5 to 4 barg.
  • the second stream of syngas may be cooled prior to being fed through the shaft of the blast furnace to a temperature of about 950 °C.
  • the second stream of syngas 128 exiting the second reforming plant 122 is fed to the blast furnace through the tuyere 130 with a temperature of about 1200 °C and a pressure of 2 to 6 barg.
  • FIG. 3 illustrates a third embodiment of the present method for operating a blast furnace comprising the simultaneous injection of a first stream of syngas through the shaft of a blast furnace together with the injection of a cold hydrogen and/or a hydrocarbon containing gas and possibly also pulverized coal through the tuyere of the blast furnace.
  • Blast furnace gas 210 exiting the blast furnace 212 is collected at the top of a blast furnace 212.
  • the collected blast furnace gas 210 is generally pre-treated in a gas cleaning and cooling unit 214 upon exiting the blast furnace.
  • Pre-treatment of the stream of blast furnace gas comprises first a cooling to reduce its vapor content, a cleaning, in particular a removing of dust and/or HCI and/or metal compounds.
  • Part of the cleaned blast furnace gas 219 is used as part of the fuel, along with humid air 223, and often along with other high calorific gases (not shown) in the burners of the cowper plant 221 for heating of the blast that is injected in the blast furnace at its tuyere level. Both, gases and air may be preheated or not.
  • blast furnace gas 217 is used as part of the fuel, along with humid air 223, and often along with other high calorific gases (not shown) in the burners of the reforming plant 218. Both gases and air may be preheated or not.
  • Another stream 216 of the blast furnace gas is used within the reforming reaction. This stream is further fed to a compressor (pressuring unit) 215 for compressing the blast furnace gas to the required pressure level for reforming and injection in the blast furnace.
  • blast furnace export gas 227 Remaining blast furnace gas exiting the blast furnace 212 and not being used in either the reforming plant or the cowper plant is referred to a blast furnace export gas 227 and is fed to other units within a steel plant comprising the blast furnace 212.
  • a stream 224 of coke oven gas and/or natural gas is fed to the reforming plants 218.
  • the gas 224 can be desulphurized in the desulphurization unit 250. Desulphurization of the gas 224 can be performed along desulphurization of blast furnace gas (Fig.3). Alternatively, the gas 224 can be desulphurized in a separate desulphurization unit (not shown). In such embodiments, hydrogen may be added to natural gas for the hydrogenation of organic sulphur contained in the natural gas (not shown).
  • Basic oxygen furnace gas and/or steam 225 might optionally be added to the stream of blast furnace gas (upstream and/or downstream of the pressuring unit 215), to the hydrogenation and desulphurization unit 250, to the stream of hydrocarbon containing gas 224 (not shown) and/or directly to a reforming plant 218 or after the reforming plant 224.
  • the reforming of the stream of blast furnace gas 216 along with the stream 224 of coke oven gas and/or natural gas is done in the reforming plant 218 to produce a stream of syngas 226.
  • the two gas streams of blast furnace gas 216 and hydrocarbon containing gas need to be mixed prior entering the reforming plant 218, within the reforming plant 218 and/or prior to entering the hydrogenation and desulphurization plant 250.
  • the reforming processes are dry and/or wet reforming processes, possibly also in combination with a partial oxidation, leading to the formation of a stream of syngas 226, with high CO and Fh contents. Reforming processes occurs at pressure between 1 ,5 and 10 barg and depending on the reforming plant at a temperature above 900 °C, preferably above 950 °C, more preferably above 1000 °C.
  • Blast furnace gas and/or hydrogen containing gas may optionally be heated prior to the reforming process (not shown). Heating might be performed e.g. by using tube bundle heat exchangers transferring part of the heat of the flue gas from the reforming plant. The same applies to the gas mixture comprising blast furnace gas and hydrocarbon containing gas entering the reforming plant, which will preferably also be heated to at least 350°C, more preferably to above 400°C and preferred to above 450°C.
  • blast furnace gas and air used in the burners of the cowper plant and/or of the reforming plant may also be heated transferring part of the heat of the flue gas from the reforming plant in heat exchangers e.g. as tube bundle heat exchanger.
  • the blast furnace installation comprises an electrolysis cell 232 fueled by electrical power 234 to produce a stream of hh 236 by electrolysis, preferably by water/steam electrolysis.
  • the electrical power 234 fueling the electrolysis cell 232 is preferably renewable or “green”, i.e. obtained from a renewable source such as wind, solar and/or hydropower.
  • said hydrogen can be produced from natural gas through a pyrolysis process with solid carbon formation, or with combined Carbon Capture and Storage (CCS) technology and/or Carbon Capture and Utilization (CCU) technology. Hydrogen might also be produced by methane thermal cracking or steam methane reforming with combined CCS and/or CCU technology.
  • CCS Carbon Capture and Storage
  • CCU Carbon Capture and Utilization
  • the stream of H2236 produced by the electrolysis cell, or a part of it, is added to the stream 224 of coke oven gas and/or natural gas upstream of the reforming plant 218 to form a stream of H2-enriched hydrocarbon containing gas, which is fed to the reforming plant 218 and / or a part of it is fed to the stream of hydrocarbon containing gas prior to the hydrogenation step and/or is fed cold at the tuyere of the blast furnace on its own or together with other auxiliary fuels such as coal, natural gas, plastics, biomass and the like.
  • Basic oxygen furnace gas and/or steam might optionally be added to the stream of blast furnace gas (upstream and/or downstream of the pressuring unit 215 or the hydrogenation unit 250) (not shown) and/or the stream of hydrocarbon containing gas 224 (not shown) and/or to the stream of H2 236 (not shown) and/or directly to the reforming plant 218 or after the reforming plant 218.
  • Part of the stream of H2 236 may be added to the stream of syngas 226 downstream of the reforming plant 218 and upstream of gas inlets 238 disposed through the shaft inside the blast furnace 212.
  • the stream of syngas 226 added with hydrogen 236 form a stream of H2-enriched gas 240, which is fed to the blast furnace through the gas inlets 238 at the shaft level, with a temperature of about 900°C and a typical pressure of 1 ,5 to 4 barg.
  • Part of the Hydrogen 236 and/or hydrocarbon containing gas 224 may also be directly injected through the tuyere 230 of the blast furnace. In embodiments, injection of hydrogen 236 and/or hydrocarbon containing gas 224 may be performed along with injection of solid fuels, such as e.g. pulverized coal injection 229. [00164] Part of the stream of hh 236 may be used as a coolant of the first stream of syngas 226. Using said hydrogen in this way, i.e. as a coolant, completely eliminates the need of heating said hydrogen prior to its injection through the shaft of the blast furnace 212 in an expensive heating device. Indeed, the excess heat of the syngas 226 heats said hydrogen. This allows to increase the efficiency of the process by eliminating both the need for syngas cooling and hydrogen heating.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • Manufacture Of Iron (AREA)
  • Blast Furnaces (AREA)
  • Furnace Details (AREA)

Abstract

L'invention concerne un procédé de fonctionnement d'un haut-fourneau, ledit procédé comprenant les étapes consistant à collecter un flux de gaz de haut-fourneau provenant du haut-fourneau ; alimenter ledit flux de gaz de haut-fourneau et un gaz contenant des hydrocarbures dans une installation de reformage comprenant au moins un reformeur ; reformer ledit flux de gaz de haut-fourneau et ledit gaz contenant des hydrocarbures dans l'installation de reformage pour produire un flux de gaz de synthèse ; et alimenter au moins une partie dudit flux de gaz de synthèse dans le haut-fourneau ; un flux de h½ étant ajouté au gaz contenant des hydrocarbures avant l'étape (c) et/ou au flux de gaz de haut-fourneau avant l'étape (c) et/ou au flux de gaz de synthèse avant l'étape (d) et/ou à la tuyère du haut-fourneau, l'alimentation d'au moins une partie dudit flux de gaz de synthèse dans le haut-fourneau se produisant à travers l'arbre du haut-fourneau et/ou à travers la tuyère du haut-fourneau, et l'efficacité d'utilisation de l'hydrogène dans une installation de haut-fourneau comprenant le haut-fourneau, l'installation de reformage et une installation de purification étant supérieure à 60 %.
PCT/EP2022/065003 2021-06-03 2022-06-02 Procédé de fonctionnement d'une installation de haut-fourneau WO2022253938A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
CN202280037764.0A CN117377778A (zh) 2021-06-03 2022-06-02 用于对高炉装置进行操作的方法
BR112023024416A BR112023024416A2 (pt) 2021-06-03 2022-06-02 Método de operação de um alto-forno, usina de alto-forno e instalação de alto-forno
JP2023572537A JP2024522088A (ja) 2021-06-03 2022-06-02 高炉設備の運転方法
EP22731244.4A EP4347897A1 (fr) 2021-06-03 2022-06-02 Procédé de fonctionnement d'une installation de haut-fourneau
KR1020237040652A KR20240016962A (ko) 2021-06-03 2022-06-02 고로 설비의 작동방법
AU2022284294A AU2022284294A1 (en) 2021-06-03 2022-06-02 Method for operating a blast furnace installation

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8287620B2 (en) * 2008-02-15 2012-10-16 Siemens Vai Metals Technologies Gmbh Method for the melting of pig iron with the recirculation of blast furnace gas and with the addition of hydrocarbons
EP2543743A1 (fr) * 2010-03-02 2013-01-09 JFE Steel Corporation Procédé d'exploitation d'un haut-fourneau, procédé d'exploitation d'un broyeur de ferraille, et procédé d'utilisation d'un gaz contenant des oxydes de carbone
EP2886666A1 (fr) 2013-12-20 2015-06-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé d'opération d'une installation de hait-fourneau avec recyclage de gaz de gueulard
WO2017111415A1 (fr) * 2015-12-23 2017-06-29 주식회사 포스코 Procédé de décomposition et de recyclage du dioxyde de carbone avec un four chaud
JP6843490B1 (ja) * 2020-08-04 2021-03-17 積水化学工業株式会社 ガス製造装置、ガス製造システム、製鉄システム、化学品製造システムおよびガス製造方法
US20210095354A1 (en) * 2019-09-27 2021-04-01 Midrex Technologies, Inc. Direct reduction process utilizing hydrogen

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8287620B2 (en) * 2008-02-15 2012-10-16 Siemens Vai Metals Technologies Gmbh Method for the melting of pig iron with the recirculation of blast furnace gas and with the addition of hydrocarbons
EP2543743A1 (fr) * 2010-03-02 2013-01-09 JFE Steel Corporation Procédé d'exploitation d'un haut-fourneau, procédé d'exploitation d'un broyeur de ferraille, et procédé d'utilisation d'un gaz contenant des oxydes de carbone
EP2886666A1 (fr) 2013-12-20 2015-06-24 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Procédé d'opération d'une installation de hait-fourneau avec recyclage de gaz de gueulard
WO2017111415A1 (fr) * 2015-12-23 2017-06-29 주식회사 포스코 Procédé de décomposition et de recyclage du dioxyde de carbone avec un four chaud
US20210095354A1 (en) * 2019-09-27 2021-04-01 Midrex Technologies, Inc. Direct reduction process utilizing hydrogen
JP6843490B1 (ja) * 2020-08-04 2021-03-17 積水化学工業株式会社 ガス製造装置、ガス製造システム、製鉄システム、化学品製造システムおよびガス製造方法

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CN117377778A (zh) 2024-01-09
AU2022284294A1 (en) 2023-12-07
JP2024522088A (ja) 2024-06-11
EP4347897A1 (fr) 2024-04-10
TW202336237A (zh) 2023-09-16
BR112023024416A2 (pt) 2024-02-20
KR20240016962A (ko) 2024-02-06

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