Patent Application
20250011888
The present disclosure generally relates to a method for reducing carbon footprint in operating a metallurgical plant for producing pig iron and a metallurgical plant for producing pig iron with a reduced carbon footprint.
The necessity as well as the duty to reduce global CO2 emissions is influencing the steel industry as one of the main responsible player. The worldwide decarbonisation is pushing the steelmakers towards a transition for a more-sustainable production, based on maximization of so-called “green” sources, like “green” electrical energy and renewable reductant and fuels, as replacement of fossil ones.
Hydrogen appears to be the new key factor for CO2 reduction at the present days and in particular for a future decarbonised steel production. To fulfil the decarbonisation target, the hydrogen should be produced without carbon dioxide emissions, which means production for instance via electrolysis process fed by electrical energy from renewable sources. In this way, a “green” hydrogen is produced, completely free from carbon dioxide emissions. Nevertheless, green hydrogen production costs are currently high and, although a decreasing is foreseen in next years, this can compromise the feasibility of its application in the steelmaking sector, even in future scenarios, due to the huge energy and flowrate demand in iron and steel production processes.
The present disclosure provides a new route for a more sustainable pig iron production from iron ore fines, in particular a method for pig iron production suitable to be installed in metallurgical plants, such as in integrated steel works, which method should offer the flexibility to be operated in a range from limited to zero carbon dioxide emissions, such as for allowing either to ensure a more gradual transition in reducing carbon footprint or to operate at least at low carbon dioxide emissions in case of temporary non-availability of certain renewable resources.
In order to overcome the above-mentioned problem, the present disclosure proposes, in a first aspect, a method for reducing carbon footprint in operating a metallurgical plant for producing pig iron, the method comprising the steps of:
In a second aspect, the disclosure proposes a metallurgical plant for producing pig iron with a reduced carbon footprint, preferably by implementing the method for reducing carbon footprint in operating a metallurgical plant for producing pig iron according to the first aspect, the metallurgical plant comprising:
In the context of the disclosure, other off-gases from the metallurgical plant may be any available and appropriate CO-containing off-gas or mixtures of two or more thereof. They may be selected from one or more off-gases from a coke oven plant, a DRI (Direct Reduced Iron) plant, a basic oxygen furnace, an electric furnace (other than of the submerged arc furnace used in the present method), etc.
As such, the core of the proposed method and metallurgical plant is based on a partial (pre-) reduction step in one or more fluidized bed reactors to a metallization degree of 55 to 75%, preferably 60 to 70%, based only on hot gaseous reductants, followed by an electric smelter of the submerged arc furnace (SAF) type, where smelting and the completion of the reduction take place.
Consequently, the disclosure takes advantage of a combination of three findings: (1) that the kinetics curve of the iron ore fines reduction is very steep up to 70 to 75%, meaning that the metallization degree of 75% can be reached e.g. within 20 to 30 minutes, whereas the further metallization from 75% to 95% in the same conditions would then take more than two hours; (2) that this partial reduction can be obtained when effected with only hot reducing gas as a reductant, which moreover can be at least partially based on off-gases available on a metallurgical plant, such as the off-gas of the submerged arc furnace of the method itself or of other processes, but also other off-gases as further detailed below, (3) that this partial reduction can be obtained at least partially based on natural gas, biomethane or mixtures thereof and/or blast furnace gas, off-gas of the submerged arc furnace, other off-gases from the metallurgical plant or mixtures thereof, if they are converted in a catalytic or non-catalytic reforming reactor into an efficient reducing (syn) gas to be used directly as such or in combination with variable proportions of hydrogen and/or other CO rich available off-gas(es); and (4) that the further treatment in a submerged arc furnace in the presence of a solid carbonaceous material acting as further reductant allows to transform the only partially reduced iron ore into pig iron.
According to the disclosure, the hot reducing gas in step b), comprises or consists of hydrogen, syngas, off-gas of the fluidized bed reactor(s), off-gas of the submerged arc furnace, other (CO-containing) off-gases from the metallurgical plant, or mixtures thereof. Preferably, said hot reducing gas comprises or consists of at least syngas as defined in the present context, meaning a syngas produced from natural gas or biomethane, blast furnace gas, off-gas of the fluidized bed reactor(s), off-gas of the submerged arc furnace, other off-gases from the metallurgical plant, or mixtures of two or more thereof in one or more (catalytic or non-catalytic) reforming reactors in the presence of air or oxygen-enriched air, steam or carbon dioxide (depending on the reforming process used). It optionally advantageously comprises (additional) hydrogen, off-gas of the fluidized bed reactor(s), off-gas of the submerged arc furnace, other (CO-containing) off-gases from the metallurgical plant, or mixtures of two or more thereof. In embodiments, said hot reducing gas comprises or consists of said syngas, (additional) hydrogen and at least one gas selected from off-gas of the fluidized bed reactor(s), off-gas of the submerged arc furnace and other (CO-containing) off-gases from the metallurgical plant.
A preferred fluidized bed reactor for this purpose is a circulating type fluidized bed reactor providing high slip velocity between gas and solids resulting in high mass and heat transfer coefficients. Hence, the one or more fluidized bed reactors are preferably of the circulating type.
A Submerged Arc Furnace (SAF) is a special type of electric (arc) furnace suitable to perform reduction process. In the submerged arc furnace, the tips of electrodes are buried in the slag, where the active power is converted into thermal energy by Joule effect and where the reactions take place. The burden, consisting of lump ore and/or agglomerated fine and/or pre-reduced ore, fluxes and carbon carriers, descends according to the furnace throughput and is heated. When entering in the reaction zone, the oxides with the lowest melting point are liquefied. As the energy density increases towards the electrodes, all oxides are finally molten. Thus, carbo-thermic reduction by means of solid carbon bearing material take place. Depending on the temperature control and the slag melting point, the metal oxides are reduced, in the order of the demand of electric energy required for the reduction with carbon. The slag forms a liquid layer, made mainly by gangue, through which the reduced metal droplets descend to form the metal bath at the bottom of the hearth. The bath is carbon saturated, in order to guarantee the carbo-thermic reduction in the slag, and the final product is therefore hot pig iron, e.g. with a carbon content of 3-4%. In the context of this disclosure, the term “submerged arc furnace” or “SAF” includes all the different possible electric arc furnace types optimized for the specific application, e.g Direct Current furnace, Alternate Current furnace, Open Bath Furnace, circular types, rectangular types, etc.
Consequently, the submerged arc furnace can be considered a flexible electric smelter, able to perform reduction of metal oxides, charged both as iron ore or as pre-reduced iron (or direct reduced iron, DRI). Generally speaking, for iron making applications, its advisable to have a pre-reduction step between the submerged arc furnace, to limit the electrical energy consumption and improve the overall plant efficiency. Nevertheless, a high DRI metallization is not required by a submerged arc furnace, unlike in the case of state-of-art Electric Arc Furnace (EAF). This allowed the inventors to find the optimal trade-off operational point for the present disclosure of 55 to 75%, preferably 60 to 70% of metallization, being the last part of metalization performed in a separated reactor, which has been experienced as the most critical part, due to availability issues (mainly for sticking problems) and constraints which can compromise the feasibility, such as lower productivity, higher residence time, lower efficiency, etc.
Furthermore, the method and metallurgical plant described herein are particularly adapted to make use of renewable resources as energy source and solid and gaseous reducing agents, such as “green” hydrogen, bio-char and “green” electricity. Moreover, the method can be flexibly and gradually converted to a full green operation (zero carbon dioxide emission), depending on the resources availability: hydrogen for the fluidized bed reactor can be produced by electrolysis using (only) renewable electricity (“green” H2) or produced by fossil resources with application of CO2 capture technology (“blue” H2) or produced by fossil resources (“grey” H2); fossil coal and/or bio-char can be used in the submerged arc furnace; other metallurgic plant off-gases, such as integrated steelworks gases, can be fed into the fluidized bed reactor. The method is also particularly aimed at allowing for a mixed operation with (varying proportions of) hydrogen, recirculated CO-containing metallurgical off-gas(es) and syngas, with an enhanced flexibility in conversion to “green” operation depending on sources availability and costs. In this regard, the proposed method can be flexibly operated from completely avoiding carbon dioxide emissions to limited emissions, depending on type and quantity of energy resources used: the same metallurgical plant can be fed only by renewable energy sources, reducing gas, biomethane and solid reductant (carbonaceous material), with zero CO2 emissions or it can still be partially fed by fossil resources (e.g. grey/blue hydrogen, coal, natural gas, electricity from fossil fuel, etc.) with a limited CO2 footprint, but in any case lower than currently used iron-making technologies.
Biomethane is a renewable energy source derived from agricultural biomass (dedicated crops, by-products and agricultural waste and animal waste), agro-industrial (waste from the food processing chain) and the Organic Fraction Municipal Solid Waste (OFMSW). Biomethane is obtained in two phases: raw biogas production—predominantly through anaerobic digestion of biomass—and subsequent removal of non-compatible components (CO2), a process also known as “upgrading”. Biomethane has a quality similar to fossil natural gas, having a methane concentration of 90% or greater. Hence, the product of the present disclosure is a “green” pig iron which can be produced totally CO2-free, if only renewable sources are used as energy input and solid and gaseous reductants.
As a consequence, in advantageous embodiments, at least part, preferably all of the electric energy needed in the method or in the metallurgical plant is renewable electricity. In particular, at least part the electrical energy needed in the pre-heater(s) and the submerged arc furnace is renewable electricity.
Alternatively or additionally, the carbonaceous material in step d) comprises (or consists of) bio-char produced by biomass, optionally including demolition wood, such as up to 40 wt.-%, and/or waste plastics, such as up to 20 wt.-%. The carbonaceous material can be fed to the submerged arc furnace as such and separately form the partially reduced iron. It may be of benefit however to feed the carbonaceous material at least partially to the submerged arc furnace in combination or admixture with the partially reduced iron. One particularly advantageous way to add said carbonaceous material will be described herein below.
Moreover, the process can easily be configured to recycle a certain percentage of integrated steel solid residues, either by addition to the feed of iron ore fines in step a) and/or to the pre-heated iron ore fines obtained in step a) and/or to the partially reduced iron obtained in step b), in accordance with the “circular economy” concept, with additional both environmental and economic benefits.
The reforming in the present disclosure can be done in any appropriate reforming reactor or combinations of two or more reforming reactors, which may be of the same type or use a different technology and are known in the art of syngas production. The reforming reactors are either catalytic or non-catalytic reforming reactors and examples of such reactors are steam reforming reactors, such as catalytic steam reforming (CSR) reactors, dry reforming (DR) reactors, autothermal reforming (ATR) reactors, partial oxidation (POX) reactors, such as catalytic partial oxidation (CPO) reactors, membrane reforming (MR) reactors, or any combination of two or more different types of reactors.
Steam reforming (SMR) is a process for producing syngas by reaction of hydrocarbons with water in the form of steam. The reaction can be represented by the following reaction:
CH4+H2OCO+3H2 (1)
Dry reforming (DR), also known as carbon dioxide reforming, is a process of producing syngas from the reaction of hydrocarbons such as methane with carbon dioxide with the aid of noble metal catalysts, such as typically Ni or Ni alloys. The dry reforming reaction may be represented by:
CH4+CO22CO+2H2 (2)
Autothermal reforming (ATR) uses oxygen and carbon dioxide or steam in a reaction with methane to form syngas. The reaction takes place in a single chamber where the methane is partially oxidized. The reaction is exothermic. When the ATR uses carbon dioxide, the H2:CO ratio produced is 1:1; when the ATR uses steam, the H2:CO ratio produced is 2.5:1. The outlet temperature of the syngas is between 950-1100° C. In addition to reaction (1), ATR introduces the following reaction:
CH4+0.5O2CO+2H2 (3)
Partial oxidation (POX) occurs when a substoichiometric fuel-air mixture is partially combusted in a reformer, creating a hydrogen-rich syngas. A distinction is made between thermal partial oxidation (TPO) and catalytic partial oxidation (CPO).
The process of catalytic partial oxidation (CPO) is also based on reaction (3), where oxygen can come from air or oxygen-enriched air or a combination of oxygen and nitrogen conducted by colliding for few milliseconds, gaseous premixed reactant flows through extremely hot catalytic surfaces. The fast and selective chemistry that is originated is confined inside a thin solid-gas interphase zone surrounding the catalyst particles. Here, the molecules typically spend very short time at temperatures variable between 60° and 1200° C. A key issue for the technological exploitation is in the possibility of avoiding the propagation of reactions into the gas phase, which has to remain at a “relatively low” temperature. This condition favors the formation of primary reaction products (namely CO and H2) inhibiting chain reactions.
A membrane reforming (MR) reactor is a reactor wherein oxygen separation, steam reforming (SR) and partial oxidation (POX) are combined in a single step.
In preferred embodiments, the hydrogen and/or the blast furnace gas, the off-gas of the submerged arc furnace, the other off-gases from the metallurgical plant, or mixtures thereof is/are pre-heated in one or more further (e.g. second or second and third) electric pre-heater(s) based on Joule effect and/or microwave heating to a temperature above 700° C. before being fed to the fluidized bed reactor, preferably before being mixed to the (already hot) syngas from the catalytic or non-catalytic reforming reactor, said syngas having been produced from natural gas or biomethane and, optionally a certain percentage of blast furnace gas. In case of circulating fluidized bed reactor(s), their exhaust is preferably re-heated before being recirculated, either in a separate electric heater or advantageously also in the second electric pre-heater.
In further preferred embodiments, the iron ore fines have a grainsize distribution in the range 0.05-2 mm, advantageously in the range of 0.1-1 mm.
If necessary or desired, the method further comprises in step b) the (hot) briquetting of the partially reduced iron ore fines to obtain briquetted partially reduced iron, which preferably are the hot-charged to the submerged arc furnace. As already briefly mentioned above, the carbonaceous material is advantageously at least partially (such as to at least 60 wt.-%, e.g. at least 80 wt.-% or even at least 90 wt-%), preferably entirely fed to the submerged arc furnace in combination or admixture with the partially reduced iron. Most preferably, at least part of, preferably the entirety of the carbonaceous material is first introduced into the briquetted partially reduced iron during hot briquetting and then fed to the submerged arc furnace in step d). In such embodiments, the carbonaceous material is thus briquetted with the partially reduced iron into (mixed carbonaceous and) partially reduced iron briquettes, ready for use in step d). The carbonaceous material added to the briquettes and that added separately may be different, such as coal and bio-char, etc. Mixing a certain fraction of carbonaceous fine material with the DRI fines to produce DRI briquettes with a certain carbon content may be useful to optimize the electric smelter process, including better control of the final C content of the hot metal. The remaining part of carbonaceous materials required for HBI smelting can be separately charged into the electric smelter, as done in state-of-art processes.
In fact, in the state-of-art electric smelter processes for Direct Reduced Iron (DRI) and Hot Briquetted Iron (HBI) smelting, such as in an Electric Arc Furnace or Submerged Arc Furnace, solid carbon is generally used to complete iron oxide reduction: solid coal is top-charged in the electric furnace together with other input feed, in addition to the carbon content from DRI.
However, the inventors found that the carbonaceous material added to the partially reduced iron (before its feeding to the electric arc furnace) is more efficient within the electric smelter process than carbonaceous material fed separately, such as externally charged coal/bio-char. Indeed, the inventors noted lower consumptions, optimized process parameters and more flexible carbon content to be reached in the final product. It is admitted by the inventors that these advantages are due to the fact that the carbonaceous material admixed and/or briquetted with the partially reduced iron is in fine grainsize form and homogenously mixed with the partially reduced iron fines, making more efficient the coal use in the smelter process, while in the separate coal charging, some undesirable phenomena have been observed, such as coal carry-over with the offgas, carbon burnt out and lower reduction efficiency, all of which lead to higher consumptions and less productivity.
One topic of particular interest is the C content in the metal product which is required depending on its use and the C content which is provided during the early steps of the present process due to the context of its installation in integrated steelworks. In fact, in order to be able to exploit the availability of existing downstream processes (e.g. Blast Oxygen Furnace), >4 wt.-% C content (typically 4.5 wt.-%) are required in the produced hot metal, similar to Blast Furnace Hot Metal. If this target is met, there is no need of installing/modifying the existing downstream hot metal treatment plant.
However, the C content of the partially reduced iron strongly depends on the direct reduction process, and in case of gas based direct reduction as in the present method, a certain C content in the partially reduced iron basically stems from CO-containing reductants, such as syngas. The use of a reducing gas with low CO content and thus higher hydrogen content than the reducing gas from natural gas reforming processes commonly used in state-of-art technologies, means lower carbon content in the partially reduced iron, such as in a range of 0.1 to 3 wt.-%, depending on the specific reduction reactor type. This also means that the total replacement of C containing fuel and reductant with hydrogen, will lead to partially reduced iron with zero or almost zero carbon content.
In particular in the cases of such zero or very low carbon contents, direct coal charging in the electric furnace is not optimal for the smelting process in step d), which as explained above lead to higher consumption, lower productivity and lower flexibility in product characteristics (mainly referring to carbon content in the metal product). Moreover, this would more than likely increase the CO2 footprint of the overall electric smelter process as well.
As a conclusion, the present disclosure aims at producing “green” pig iron inside an integrated steelwork or metallurgical plant, exploiting the availability of CO-rich syngas enhanced by the enrichment with syngas from catalytic or non-catalytic reforming of natural gas or biomethane, limiting the degree of reduction of the iron ore fines and completing the reduction in a submerged arc furnace using different renewable energy sources and selecting specific solutions to improve the economic feasibility of the application. The method is flexible to be also operated totally or partially with fossil fuel and reductant, depending on specific local availability and costs, such that a certain carbon dioxide footprint may be foreseen, but limited in comparison with state-of-art routes and including the possibility of further reduction moving towards higher amount of “green” resources, when available at feasible costs.
Preferred embodiments of the disclosure will now be described, by way of example, with reference to the accompanying drawing:
Further details and advantages of the present disclosure will be apparent from the following detailed description of several not limiting embodiments with reference to the attached drawing.
The plant is fed by iron ore fines, even low grade, with a grainsize distribution generally in the range from 0.05-5 mm, such as from 0.1-1 mm, which could include pre-agglomerated ultra-fines particles. In this context, it is noteworthy that iron ore fines generally contain hematite, goethite and magnetite with varying iron content having a bulk density range from 1,500 to 3,500 kg/m3. Such iron ore fines are particularly well suited for methods as disclosed herein, which comprise the partial reduction when fluidized with reducing gases. Should integrated steel solid residues be added to the feed of step a), they preferably have particle sizes similar to those of the iron ore fines. The iron ore fines A are first conveyed from a storage area to the a first electric pre-heater 10. Pre-heating is performed by means of an electric pre-heater based on Joule effect or microwave heating, optionally coupled with a heat recovery system, exploiting the available residual heat from the integrated steelwork or the fluidized bed reactor syngas.
The preheated iron ore fines B are then conveyed to a fluidized bed charging system through handling equipment suitable for fines transportation, such as chain conveyors or pneumatic transport, to be fed to a fluidized bed reactor 50. The fluidized bed reactor 50 preferably is of the circulating type, wherein the exhaust of fluidized bed reactor C is recirculated, preferably after being (p)re-heated in the second electric pre-heater 20, allowing for an enhanced flexibility in fines grainsize distribution, as well as the optimal process efficiency, with regards to thermal exchanges and residence time.
Green or blue or grey hydrogen (or a mixture of them) D can be used as reducing gas J in the fluidized bed reactor 50. Due to the completely endothermic iron oxide reduction reactions with hydrogen D, other (recirculated) metallurgical plant offgas(es) H, syngas I, or mixtures thereof J, not only iron ore fines, but preferably also hydrogen and any other metallurgical plant off gases are pre-heated in one or more further pre-heaters 10, 20, 30 before being fed into the fluidized bed reactor 50, up to a temperature of approx. 800° C. In preferred embodiments, a second electric pre-heater 20 is provided for pre-heating hydrogen D and the recirculated exhaust of fluidized bed reactor C, optionally coupled with an heat recovery system from available steelwork gases; and a third electric pre-heater 30 is provided for pre-heating the off-gas of the submerged arc furnace and any other metallurgical plant off gases (except blast furnace gas, which is fed to the catalytic or non-catalytic reforming reactor). This allows to reduce the consumption of hydrogen used as a fuel.
The hydrogen D fed into the fluidized bed reactor 50 can be partially replaced by a syngas I and other (CO-containing) off-gas(es) of the metallurgical plant H. Said syngas, rich in carbon monoxide and with a certain amount of hydrogen, which is produced in a catalytic or non-catalytic reforming reactor or reformer 40, fed by natural gas and/or biomethane F, blast furnace gas G, off-gas O of the submerged arc furnace and/or other off-gases from the metallurgical plant H and air or oxygen enriched air (autothermal reforming or (catalytic) partial oxidation), steam (autothermal reforming or steam reforming) or carbon dioxide (dry reforming) E depending on the reforming technology used, see reactions (1) to (3) above. In other words, if off-gas O of the submerged arc furnace and/or other off-gases H from the metallurgical plant are used, they can be used either as such or with prior reforming, or both. The main advantage of this “recycling” is the reduction of hydrogen consumption, exploiting availability of CO-rich gas at limited calorific value, such as blast furnace gas, which can be more efficiently used in a reduction process than for energy production. Moreover the use of CO containing syngas in the fluidized bed reactor 50 provides benefits to the process, due to the exothermic CO combustion reaction with heat release and to a certain carbon content remaining in the partially reduced iron K or L, with consequent reduction of the consumption of carbonaceous material M, such as coal/bio-char, in the submerged arc furnace 70, more efficient reduction process in the submerged arc furnace 70 and limited re-oxidation phenomena in the hot partially reduced iron K or L handling. The carbonaceous material M may also comprise further additives, such as slag forming agents, etc.
The partially reduced iron K in the form of fines, with a pre-reduction degree of metallization limited at e.g. about 60-70% are discharged and conveyed from the reactor in an inert atmosphere (e.g. nitrogen or argon) to avoid re-oxidation phenomena. Then, the partially reduced iron fines K are either directly fed to the submerged arc furnace 70, or preferably hot briquetted in a hot briquetting unit 60 in order to improve their mechanical characteristics, before being handled into the downstream electric arc furnace charging system. The selection among hot partially reduced iron charging into submerged arc furnace as fines or briquettes depends on the specific project conditions (such as raw materials characteristics, utilities, price, etc.), impacting on submerged arc furnace design and performance. If required by the hot briquetting process (depending on the specific equipment type), the hot partially reduced iron fines, discharged from the fluidized bed reactor at a temperature of 600-650° C. can be heated up to 700-750° C., via for instance a third electric heater (e.g. based on Joule effect concept or on microwave heating). In advantageous embodiments, at least part of the carbonaceous material can be fed to the electric arc furnace in combination or admixture with the partially reduced iron. It is of particular benefit to introduce at least part of the carbonaceous material within the briquetted reduced iron. Indeed, the concept of hot briquetting the partially reduced fines with a certain amount of carbonaceous material, such as coal, is advantageous to optimize the smelting process. In comparison to the partially reduced iron fines hot briquetting without carbonaceous material, this beneficial solution to help facilitating a proper feeding to the electric furnace may further include:
Such a carbonaceous material and partially reduced iron briquetting allows to homogenize and compact the admixture of carbonaceous material and partially reduced iron fines to limit the loss of efficiency of external carbonaceous material charging into the electric smelter, mainly due to coal carry-over, burn out and coarser grainsize.
The briquetting system (and possibly upstream and downstream thereof) will preferably be configured to work under an inert atmosphere to avoid an undesirable re-oxidation of the partially reduced iron.
The partially reduced iron in the form of fines K or briquettes L (containing carbonaceous material or not) are then hot charged at approx. 700° C. into the electric smelter, submerged arc furnace type 70, where the reduction completion and smelting is performed by a carbonaceous material M (contained in the briquettes L and/or added separately).
For a completely carbon dioxide free pig iron production, in the proposed disclosure, bio-char is used as the carbonaceous material M (reductant) in the submerged arc furnace 70 (added as part of the briquettes L and/or separately), instead of the conventionally used fossil coal, such as anthracite or coke. Bio-char can be produced by biomass torrefaction process, eventually including a certain percentage of demolition wood (up to 40%) and waste plastics (up to 20%). The bio-char characteristics depend on the type of input biomass and torrefaction process, being in any case suitable for the use into the submerged arc furnace 70.
The submerged arc furnace 70 is able also to recycle a certain percentage of integrated steelworks solid residues as a solid waste injection N, such as for instance dust and sludge from blast furnace or basic oxygen furnace, mill scales, de-dusting dust, etc. Solid residue recycling improves the feasibility of the present disclosure application, as well as the environmental benefit, due to the avoiding of landfill, the recovery of the iron, carbon and zinc content of solid waste. A residues flowrate up to 5% of total submerged arc furnace input feed can be directly injected in the furnace metal bath, in the form of dry dust (moisture <3%) with a grainsize 100%<250 micron. Wet and/or coarse residues have to be pre-treated in a dryer and/or a mill before electric submerged arc furnace injection, while low moisture and fines dust (such for instance stockhouse dust, BOF dust, . . . ) can be directly injected without any pre-treatment. In case of solid waste injection flowrate higher than 5% of total submerged arc furnace input feed, the additional waste can be top charged in form of dry pellets or cold briquettes, after a suitable cold agglomeration treatment, consisting in mixing, pelletizing or briquetting and drying process. In case of carbon bearing solid residues, such for instance blast furnace sludge and dust, no additional bio-char is required for waste iron ore reduction and an overall saving in bio-char (or coal) consumption can be obtained.
The flexibility of submerged arc furnace type electric smelter operations allows to accept also a not optimal quality of partially reduced iron briquettes, and a certain amount of partially reduced iron briquette fines coming from the screening of hot briquetting; this improves the availability of hot briquetting process, avoiding totally or partially the fines internal recirculation.
The hot reducing gas J fed into the fluidized bed 50 can be a mixture of different proportions of hydrogen D, of the CO-rich submerged arc furnace offgas O, of other recirculated metallurgical off-gas(es) H and of the syngas I produced in the catalytic or non-catalytic reforming reactor/reformer 40 fed by natural gas or biomethane F, blast furnace gas G, off-gas O of the submerged arc furnace and/or other off-gases from the metallurgical plant H and air or oxygen-enriched air, steam or carbon dioxide E: The product of this catalytic or non-catalytic reforming reactor 40 is a syngas I suitable to be used as a reducing gas J in the fluidized bed reactor, e.g. by replacing a certain amount of hydrogen or other recirculated offgas(es). This option can have a significant OpEx advantage due to the replacement of a certain amount of hydrogen D with the syngas I produced by natural gas or biomethane F and blast furnace gas G, off-gas O of the submerged arc furnace and/or other off-gases from the metallurgical plant H.
The proposed method and metallurgical plant has a modular size: each fluidized bed reactor 50 can reach e.g. a maximum production of 550 kty DRI, each submerged arc furnace 70 a maximum size of 1.5 Mtpy of hot pig iron P.
The hot pig iron P may be thereafter cast as cast pig iron Q in a casting unit 80.
| Number | Date | Country | Kind |
|---|---|---|---|
| LU500764 | Oct 2021 | LU | national |
| LU502634 | Aug 2022 | LU | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2022/078607 | 10/14/2022 | WO |
