LU500764B1

LU500764B1 - Method for reducing carbon footprint in operating a metallurgical plant for producing pig iron

Info

Publication number: LU500764B1
Application number: LU500764A
Authority: LU
Inventors: Katia PAPALIA; Jan Krull; Thomas Hansmann
Original assignee: Wurth Paul Sa
Priority date: 2021-10-19
Filing date: 2021-10-19
Publication date: 2023-04-20

Abstract

A method for reducing carbon footprint in operating a metallurgical plant for producing pig iron (P), the method comprising the steps of: (a) pre-heating iron ore fines (A) in a first electric pre-heater (10) based on Joule effect and/or microwave heating to a temperature above 600 °C to obtain pre-heated iron ore fines (B), (b) partially reducing the pre-heated iron ore fines (B) in one or more fluidized bed reactors (50) in the presence of a hot reducing gas (J) to obtain partially reduced iron (K, L); (c) feeding the partially reduced iron (K, L) to a submerged arc furnace (70) comprising a bath of molten metal with a top slag layer; (d) further reducing and melting the partially reduced iron (K, L) within the submerged arc furnace (70) in the presence of a carbonaceous material (M) to obtain molten pig iron (P); wherein, in step (b), the hot reducing gas (J) comprises hydrogen (D), syngas (I), off-gas (O) of the submerged arc furnace, other off-gases (H) from the metallurgical plant, or mixtures thereof, wherein said syngas (I) is produced from natural gas or biomethane (F), blast furnace gas (G), or mixtures thereof in the presence of air or oxygen enriched air (E) in one or more catalytic partial oxidation reactors (40), wherein, in step b), the hot reducing gas (J) has a temperature above 550 °C, and wherein, in step b), the partially reduced iron (K, L) has a metallization degree of 55 to 75 %, preferably 60 to 70 %.

Description

METHOD FOR REDUCING CARBON FOOTPRINT IN OPERATING A

METALLURGICAL PLANT FOR PRODUCING PIG IRON

Technical field

[0001] The present invention 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.

Background Art

[0002] The necessity as well as the duty to reduce global COz 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.

[0003] Hydrogen appears to be the new key factor for CO 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.

Technical problem

[0004] It is an object of the present invention to provide 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.

General Description of the Invention

[0005] In order to overcome the above-mentioned problem, the present invention 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: a) pre-heating iron ore fines in a first electric pre-heater based on Joule effect and/or microwave heating to a temperature above 600 °C, preferably from 700 to 900 °C, in particular from 750 °C to 850 °C, such as about 800 °C, to obtain pre-heated iron ore fines; b) partially reducing the pre-heated iron ore fines in one or more fluidized bed reactors in the presence of a hot reducing gas to obtain partially reduced iron; c) feeding the partially reduced iron to a submerged arc furnace comprising a bath of molten metal with a top slag layer; d) further reducing and melting the partially reduced iron within the submerged arc furnace in the presence of a carbonaceous material to obtain molten pig iron; wherein, in step b), the hot reducing gas comprises hydrogen, syngas, i.e. synthetic gas, off-gas of the submerged arc furnace, other (CO-containing) off-gases from the metallurgical plant (preferably selected from one or more off-gases from a coke oven plant, a DRI (Direct Reduced Iron) plant and a basic oxygen furnace), or mixtures thereof, wherein said syngas is produced from natural gas or biomethane, blast furnace gas, or mixtures thereof in the presence of air or oxygen-enriched air in one or more catalytic partial oxidation reactors; wherein, in step b), the hot reducing gas has a temperature above 550 °C; and wherein, in step b), the partially reduced iron has a metallization degree of 55 to 75 %, preferably 60 to 70 %.

[0006] In a second aspect, the invention 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: - a first electric pre-heater configured for pre-heating iron ore fines based on

Joule effect and/or microwave heating into pre-heated iron ore fines at a temperature above 600 °C, preferably from 700 to 900 °C, in particular from 750 °C to 850 °C, such as about 800 °C; - one or more fluidized bed reactors configured for partially reducing the pre- heated iron ore fines in the presence of a hot reducing gas into partially reduced iron to a metallization degree of 55 to 75 %, preferably 60 to 70 %; - a submerged arc furnace comprising a bath of molten metal with a top slag layer, configured for receiving the partially reduced iron and further reducing and melting the partially reduced iron in the presence of a carbonaceous material to obtain molten pig iron; wherein the metallurgical plant further comprises one or more catalytic partial oxidation reactors configured for producing a syngas from a feed of natural gas or biomethane, a feed of blast furnace gas or a feed of mixtures thereof and a feed of air or oxygen-enriched air (E); a feed of hydrogen; one or more feeds of an off-gas of the submerged arc furnace and other (CO-containing) off-gases of the metallurgical plant (preferably selected from one or more of off-gases from a coke oven plant, a DRI plant and a basic oxygen furnace); a hot reducing gas mixing device fluidly connected upstream to the one or more catalytic partial oxidation reactors and to the feed of hydrogen, to said one or more feeds of an off-gas of the submerged arc furnace and of other off-gases of the metallurgical plant and downstream to an inlet of the one or more fluidized bed reactors, said hot reducing gas mixing device being configured for providing hot reducing gas at a temperature above 550 °C comprising hydrogen, syngas, off-gas of the submerged arc furnace, other off-gases of the metallurgical plant, or mixtures thereof. The hot reducing gas mixing device may be a dedicated mixing unit or may only be the confluence of feed of (pre-heated) hydrogen, the syngas from the catalytic partial oxidation reactor, the off-gas of the submerged arc furnace and the other off-gases of the metallurgical plant.

[0007] 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 %, followed by an electric smelter of the submerged arc furnace (SAF) type, where smelting and the completion of the reduction take place.

[0008] Consequently, the invention 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 at least partially based on off-gases available on a metallurgical plant, such as the off-gas of the submerged arc furnace itself, 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 preferably blast furnace gas, if they are converted in a catalytic partial oxidation 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 carbonaceous material acting as further reductant allows to transform the only partially reduced iron ore into pig iron.

[0009] 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.

[0010] 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 %.

[0011] 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 invention 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 compromize the feasibility, such as lower productivity, higher residence time, lower efficiency, etc.

[0012] 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 renewable electricity (“green” Hz) or produced by fossil resources with application of COz capture technology (“blue” Hz) or produced by fossil resources (“grey” Hz); 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 CO» 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 CO» footprint, but in any case lower than currently used iron-making technologies.

[0013] 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 (COz), 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 invention is a “green” pig iron which can be produced totally COz-free, if only renewable sources are used as energy input and solid and gaseous reductants.

[0014] As a consequence, in advantageous embodiments, at least part, preferably all of the electric energy needed in the method 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.

[0015] 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.-%.

[0016] 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.

[0017] Catalytic partial oxidation reactors are known in the art of syngas production. The process of Catalytic Partial Oxidation (CPO) is based on the following reaction, where oxygen can also come from air or oxygen-enriched air or a combination of oxygen and nitrogen:

CH4 + %2 O2 + CO + H2 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 600 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 Hz) inhibiting chain reactions.

[0018] Experimental studies indicate that partial oxidation products are directly produced through parallel and competing surface reactions and that the formation of partial oxidation products is favored under the CPO conditions due to the very high surface temperatures. The occurrence of the reactions in these local environments determines in some cases conversion and selectivity values higher than those predicted by the thermodynamic equilibrium at the reactor exit temperatures.

[0019] Catalytic Partial Oxidation, and in particular Short Contact Time Catalytic

Partial Oxidation (SCT-CPO), combine heterogeneous catalysis characteristics and flameless combustion in porous media and is known for example from

WO2011072877, WO2011151082, and L.E. Basini and A. Guarinoni, “Short Contact

Time Catalytic Partial Oxidation (SCT-CPO) for Synthesis Gas Processes and

Olefins Production”, Ind. Eng. Chem. Res. 2013, 52, 17023-17037. While SCT-CPO is known, the main advantages of catalytic partial oxidation applied for the production of syngas to be injected in a blast furnace can be summarized as follows:

- small dimensions (reactor dimensions are reduced of more than 2 orders of magnitude respect than a classic Steam Reforming reactor): - technical and operational simplicity (much reduced complexity in comparison to e.g. classic steam reforming); - low CAPEX per kg syngas/hr produced; - possibility of modular construction of pre-fabricated and skid mounted units; - flexibility towards feedstock composition & production capacity; and - reduction of investment costs and energy consumption.

[0020] In preferred embodiments, the hydrogen and/or the blast furnace gas 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 partial oxidation 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.

[0021] 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.

[0022] 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.

[0023] As a conclusion, the present invention 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 partial oxidation 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.

Brief Description of the Drawings

[0024] Preferred embodiments of the invention will now be described, by way of example, with reference to the accompanying drawing:

Fig. 1 is a schematic view of an embodiment of a metallurgical plant for producing pig iron with a reduced carbon footprint or a method for reducing carbon footprint in operating a metallurgical plant for producing pig iron.

[0025] Further details and advantages of the present invention will be apparent from the following detailed description of several not limiting embodiments with reference to the attached drawing.

Description of Preferred Embodiments

[0026] The plant is fed by iron ore fines, even low grade, with a grainsize distribution generally in the range 0,1 - 1 mm. The iron ore fines A are first conveyed from a storage area to the a first elecrtic 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 fludized bed reactor syngas.

[0027] 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 flexilibity in fines grainsize distribution, as well as the optimal process efficiency, with regards to thermal exchanges and residence time.

[0028] 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 |, 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 partial oxidation reactor). This allows to reduce the consumption of hydrogen used as a fuel.

[0029] The hydrogen D fed into the fluidized bed reactor 50 can be partially replaced by a syngas | 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 Partial Oxidation reactor or reformer 40, fed by natural gas and/or biomethane F, as well as blast furnace gas G and air or oxygen enriched air E. 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 efficienlty 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.

[0030] 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). The partially reduced iron in the form of fines K or briquettes L 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.

[0031] For a completely carbon dioxide free pig iron production, in the proposed invention bio-char is used as the carbonaceous material M (reductant) in the submerged arc furnace 70, 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.

[0032] 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 invention 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, consisiting in mixing, pellettizing or briquetting and drying process. In case of carbon bearing solid reasidues, 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.

[0033] 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, avoinding totally or partially the fines internal recirculation.

[0034] 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 | produced in the catalytic partial oxydation reactor/reformer 40 fed by natural gas or biomethane

F, blast furnace gas G and air or oxygen-enriched air E: The product of this catalytic partial oxyation reactor 40 is a syngas | 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 | produced by natural gas or biomethane F and blast furnace furnace gas G.

[0035] The proposed method and metallurgical plant has a modular size: each fuidized 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.

[0036] The hot pig iron P may be thereafter cast as cast pig iron Q in a casting unit 80.

Legend:

First electric pre-heater

Second electric pre-heater

Third electric pre-heater

Catalytic partial oxidation reactor

Fluidized bed reactor 60 Hot briquetting unit 70 Submerged arc furnace 80 Casting unit

A Iron ore fines

B Pre-heated iron ore fines

C Exhaust of fluidized bed reactor

D Hydrogen

E Air or oxygen enriched air

F Natural gas or biomethane

G Blast furnace gas

H Other metallurgical plant off-gas(es)

Syngas

J (Hot) reducing gas

K Partially reduced iron (fines)

L Partially reduced iron (briquettes)

M Carbonaceous material (and additives)

N Solid waste injection

O Submerged arc furnace off-gas

P Hot metal/molten pig iron

Q Cast pig iron

Claims

1. A method for reducing carbon footprint in operating a metallurgical plant for producing pig iron (P), the method comprising the steps of: a) pre-heating iron ore fines (A) in a first electric pre-heater (10) based on Joule effect and/or microwave heating to a temperature above 600 °C to obtain pre-heated iron ore fines (B); b) partially reducing the pre-heated iron ore fines (B) in one or more fluidized bed reactors (50) in presence of a hot reducing gas (J) to obtain partially reduced iron (K, L); c) feeding the partially reduced iron (K, L) to a submerged arc furnace (70) comprising a bath of molten metal with a top slag layer; d) further reducing and melting the partially reduced iron (K, L) within the submerged arc furnace (70) in the presence of a carbonaceous material (M) to obtain molten pig iron (P); wherein, in step b), the hot reducing gas (J) comprises hydrogen (D), syngas (I), off-gas (O) of the submerged arc furnace, other off-gases (H) from the metallurgical plant, or mixtures thereof, wherein said syngas (I) is produced from natural gas or biomethane (F), blast furnace gas (G), or mixtures thereof in the presence of air or oxygen-enriched air (E) in one or more catalytic partial oxidation reactors (40); wherein, in step b), the hot reducing gas (J) has a temperature above 550 °C; and wherein, in step b), the partially reduced iron (K, L) has a metallization degree of 55 to 75 %, preferably 60 to 70 %.

2. The method according to claim 1, wherein the one or more fluidized bed reactors (50) is/are of a circulating type.

3. The method according to claim 1 or 2, wherein the hydrogen (D) is pre-heated in a second electric pre-heater (20) and off-gas (O) of the submerged arc furnace and optional other off-gases (H) from the metallurgical plant are pre-heated in a third electric pre-heater (30), both second and third pre-heaters being independently based on Joule effect and/or microwave heating to a temperature above 700 °C.

4. The method according to any one of the preceding claims, wherein the carbonaceous material (M) 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.-%.

5. The method according to any one of preceding claims, wherein the iron ore fines (A) have a grainsize distribution in the range 0,1 — 1 mm.

6. The method according to any one of the preceding claims, wherein step b) further comprises hot briquetting partially reduced iron ore fines (K) to obtain briquetted partially reduced iron (L).

7. The method according to any one of the preceding claims, wherein the other off- gases (H) of the metallurgical plant comprise one or more of off-gases from a coke oven plant, a Direct Reduced Iron plant and basic oxygen furnace.

8. The method according to any one of the preceding claims, wherein at least part of, preferably all electrical energy needed in the pre-heater(s) and the submerged arc furnace, more preferably in all of the steps of the method is renewable electricity.

9. A metallurgical plant for producing pig iron (P) with a reduced carbon footprint, preferably by implementing the method according any of claims 1 to 8, the metallurgical plant comprising: - a first electric pre-heater (10) configured for pre-heating iron ore fines (A) based on Joule effect and/or microwave heating into pre-heated iron ore fines (B) at a temperature above 600 °C; - one or more fluidized bed reactors (50) configured for partially reducing the pre-heated iron ore fines (B) in the presence of a hot reducing gas (J) into partially reduced iron (K, L) to a metallization degree of 55 to 75 %, preferably 60 to 70 %: - a submerged arc furnace (70) comprising a bath of molten metal with a top slag layer, configured for receiving the partially reduced iron (K, L) and further reducing and melting the partially reduced iron (K, L) in the presence of a carbonaceous material (M) to obtain molten pig iron (P); wherein the metallurgical plant further comprises one or more catalytic partial oxidation reactors (40) configured for producing a syngas (l) from a feed of natural gas or biomethane (F), a feed of blast furnace gas (G) or a feed of mixtures thereof and a feed of air or oxygen-enriched air (E); a feed of hydrogen

(D); one or more feeds of an off-gas (O) of the submerged arc furnace and other off-gases (H) of the metallurgical plant; a hot reducing gas mixing device fluidly connected upstream to the one or more catalytic partial oxidation reactors (40) and to the feed of hydrogen (D), to said one or more feeds of an off-gas (O) of the submerged arc furnace and of other off-gases (H) of the metallurgical plant and downstream to an inlet of the one or more fluidized bed reactors (50), said hot reducing gas mixing device being configured for providing hot reducing gas (J) at a temperature above 550 °C comprising hydrogen (D), off-gas (O) of the submerged arc furnace, other off-gases (H) of the metallurgical plant, syngas (I) or mixtures thereof.

10. The metallurgical plant according to claim 9, wherein the one or more fluidized bed reactors (50) is/are of a circulating type.

11. The metallurgical plant according to claim 9 or 10, comprising a second electric pre-heater (20) based on Joule effect and/or microwave heating fluidly connected between said feed of hydrogen (D) and the hot reducing gas mixing device, and a third electric pre-heater (30) based on Joule effect and/or microwave heating fluidly connected between said one or more feeds of off-gas (O) of the submerged arc furnace and other off-gases (H) of the metallurgical plant and the hot reducing gas mixing device, said second and third electric pre- heaters (20, 30) being configured for pre-heating the relevant off-gas(es) and syngas to a temperature above 700 °C.

12. The metallurgical plant according to any of claims 9 to 11, wherein the carbonaceous material (M) is provided from a source comprising or consisting 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.-%.

13. The metallurgical plant according to any one of claims 9 to 12, further comprising a hot briquetting apparatus configured for briquetting partially reduced iron ore fines (K) into briquetted partially reduced iron (L).

14. The metallurgical plant according to any one of claims 9 to 13, wherein the metallurgical plant comprises on or more among, a coke oven plant, a Direct Reduced Iron plant, a blast furnace and basic oxygen furnace, providing said other off-gases (H) of the metallurgical plant.

15. The metallurgical plant according to any one of claims 9 to 14, wherein at least part of, preferably all electrical energy needed in the pre-heater(s) and the submerged arc furnace, more preferably in all of the steps of the method is renewable electricity.