RO120854B1 - Process and installation for melt electrolysis, for obtaining iron alloys, as well as inert anodes for electrolysis of metal melts - Google Patents

Abstract

The invention relates to a process and an installation for smelting electrolysis, for obtaining iron alloys as well as to inert anodes for smelting electrolysis. According to the invention, the process consists in preparing the iron ores and/or iron agglomerate and the electrolyte components by crushing, sorting, homogenizing and agglomerating, followed by successively melting the same in an electric furnace with a three-phase arc, the molten materials being introduced into a vat where the electrolysis takes place at a temperature of 1500 - 1560 C, then the obtained alloy is extracted by means of a vacuum extraction pot. According to the invention, the installation for carrying out the process comprises an electrolysis vat consisting of a metal casing (1) containing inert anodes (16) and some cathode blocks (10), having at the upper side a refractory vault (A), consisting a movable sectors independent from one another, sustained by a metal ring (22) and inside a vault sector there are located sealing rings (25), cooled by the water circulation. The inert anodes claimed by the invention are constituted of a preliminarily burnt carbon block, of a compact metal block or resistive ceramic materials, embedded in a metal container made of refractory plates coated by spraying, with a protective coating consisting of: MoSi2, WSi2 or ZrBe13, Zr2Be17, NbBe12, Nb2Be17, Nb2Be19, TaBe12, Ta2Be17 as well as of the type TiB2, ZrB2. A stamped carbonic mass is used to seal.

Description

The invention relates to a process and an installation for obtaining iron-based alloys, by electrolysis in melts, as well as to the inert anodes with which the molten electrolysis tank is equipped.

Methods of direct extraction of iron from ores consisting of reducing iron oxides in solid state at a temperature below that of sintering ores (950 '-1100'C) are known which depend on the characteristics of the reducing environment, temperature and pressure. . The product obtained, the iron sponge is used in steelworks as a raw material for charging electric ovens, but also in the furnace as pre-cast pallets.

Also known is the Krupp process, which results in iron in the form of magnifying glasses.

These processes fail to lower the carbon content of steels manufactured below 0.02%.

There are known installations for obtaining iron-based alloys that include blast furnaces, reduction installations for obtaining the iron sponge or the magnifying glass, oxygen blowing converters or electric arc furnaces.

However, these installations are complex and polluting.

Also known are precooked carbon anodes that are part of the equipment of electrolysis installations in smelting for the manufacture of aluminum. These anodes should be changed periodically, after they have been consumed in the proportion of 2/3 or 3/4 of the original size. Sometimes, at these anodes, due to the heat shock, exfoliations appear at the lower ends or cracks in case they need to be replaced.

The technical problem solved by the invention consists in obtaining high quality ferrous alloys, in particular of low carbon steels directly from the elaboration, under the least pollution conditions and with the help of a simple and safe installation in operation.

The process according to the invention solves the proposed technical problem by providing for the gradual heating with flame of methane gas of an electrolysis tank, in order to finally obtain a temperature of at least 1250'C, a tank in which an extramural steel made in the oven is introduced. electric with three-phase arc, with chemical composition in mass percentages: C <0.05%; Mn <0.25%; If <0.20%; P <0.020%; S <0.025%; Al <0.06%; and the sum S, P, Ni, Cr, Al be> 0.6%, steel representing the amount of metal permanently maintained in the electrolysis tank throughout its operation, representing the liquid cathode with the height from 30 to 200 mm, in the electrolyte filling the tank is also introduced, so that the height from the surface of the liquid cathode to the anode sole, which represents the interpolar distance, is between 40 and 400 mm, to which is added the partial insertion height of electrolyte anodes from 50 to 200 mm, after which the electrolysis tank is connected to the electrical installation and the electrolysis takes place at a temperature of 1500 ... 1560 ° C, after the electrolysis the obtained alloy is extracted from the tank using a vacuum pot and unloaded into another pot where the secondary alloying takes place which is then subjected to refining and alloying to obtain the desired steel mark.

The installation for carrying out the process according to the invention comprises an electrolysis tank provided with a vault formed by mobile sectors and independent of each other, supported by a metal ring, and within a vault sector are sealed rings cooled by water circulation. .

The inert anodes that form part of the electrolysis tank of the installation according to the invention are constituted by a precocious carbon block; compact metal block or of resistive ceramic materials embedded in a metal container made of spray-coated refractory plates with a protective layer consisting of: MoSi ₂ , WSi ₂ or ZrBe ₁₃ , Zr ₂ Be ₁₇ , NbBe ₁₂ , Nb ₂ Be ₁₇ , Nb ₂ Be ₁₉ , TaBe ₁₂ , Ta ₂ Be ₁₇ , as of type TiB ₂ , ZrB ₂ . For sealing, use carbon stamped mass.

RO 120854 Β1

The process and installation according to the invention have the following advantages: 1

- it allows to obtain high quality alloys, for example of low carbon steels, in a simplified technological flow; 3

- eliminates the need for the blast furnace sector with related installations, direct reduction installations and oxygen blowers or electric arc furnaces; 5

- ensures good protection of the environment by preventing polluting emissions, improving working conditions, in accordance with the regulations of the 7th European Age and the Office of Comprehensive Pollution Prevention and Control.

The invention will be further presented in relation to the figure representing a vertical section through the melt electrolysis installation, according to the invention.

The process according to the invention provides for the introduction in an electrolysis tank of the components of the electrolyte, as well as of the iron ores and / or of the iron agglomerate in molten or solid state, but in the latter case it has a higher consumption of energy involves 13 when also the inherent difficulties of melting.

In the case of using molten electrolyte, the dosed components of the electrolyte are melted in 15 three-phase electric arc furnace, or in rotary fuel heated oven, through a front-mounted burner in the axis of the furnace. 17

Once melted, the electrolyte is discharged from the furnace into a casting pot, from which it is then discharged into electrolysis tanks. 19

The iron ores and / or the agglomerate of iron travel the same flux as the electrolyte, specifying that for the storage and thermal and compositional homogenization of the ores, 21 of the iron and / or molten agglomerate, according to the invention there is a mixer, heated with fuel, with which electrolysis tanks are supplied rhythmically. 23 Next, the liquid alloy obtained in the electrolysis tanks, according to a rigorously respected graph, is extracted by means of a vacuum extraction pot. 25

The liquid alloy is passed to a plant for deoxidization and alloying, then to a vacuum plant, if necessary, after which the casting can be done with the aid of a 27 continuous casting plant, or in ingots or parts, after which the technological flow is following its normal course. 29 in the metallurgical processes two liquid phases appear: the metallic bath and the slag.

These phases are immiscible due to the large difference in density. 31 in their structure, the metallurgical slags comprise systems with several constituents.

Generally, slag is formed by a melt of oxides from mineral tailings, fluxes, fuel ash, oxidation or reduction processes, etc.

As a result, slag plays an important technological role, influencing the development of all 35 physico-chemical processes in metallurgy.

Roentgenostructural analysis of molten carbonates, sulphates and nitrates, proved the presence of the same cations and anions as in solid state.

Research has shown that all constituents of metallurgical slags (oxides, silicates, aluminaes, 39 phosphates, etc.) have solid ionic structures. It is normal to consider that, by melting the slags, their ionic character is preserved, precisely because of properties such as: viscosity, electrical conductivity, thermal conductivity, surface tension, melting temperature, melting heat, etc. 43

Of the properties of liquid metallurgical slags, a special interest is the electrical conductivity and their ability to electrolyze, proving directly their 45 electrolytic character.

The fact that molten slags are good conductors of electricity, allowed the development of 47 steel, welding flows and any type of white or carbide slag, in three-phase arc electric furnace, as well as the electric re-melting of steels and alloys. 49

RO 120854 Β1

Numerous experimental data show that molten slags with an electrical conductivity of between 20 and 449 O ' ¹ m' ¹ , ie of the same order of magnitude, as the electrical conductivity of the molten salts and in general of the typical electrolytes.

The resemblance of the metallurgical slags melted with the molten salts, also consists in the significant increase of the electrical conductivity of the slags with the increase of the temperature.

The molten metallurgical slags have an ionic conductivity, and some slags have an electronic conductivity, so they behave like semiconductors!

Even more recent research has shown that in slags with a high content of iron oxides, the high value of the electrical conductivity is due to the superposition over the ionic conductivity of an important electronic conductivity, due precisely to the presence of oxysilordefier. Indeed, research has shown that FeO-Fe ₂ O ₃ iron oxide melts have a much higher electrical conductivity than other metallurgical slags, reaching 20,000 Q ' ¹ m' ¹ , at 1400 ° C.

In the liquid metallurgical slags are present the simple cations of some metals (Fe ²⁺ ; Mn ²⁺ ; Ca ²⁺ ; Mg ²⁺ etc), simple anions (O ² '; S ² ), and complex anions (SiO ⁴ '; SixOy ² '; AIO2etc).

Iron ores which are the basic raw material of this process and whose chemical composition is compulsory is in mass percentages; Fe>60%; AI ₂ O ₃ <2%; CaO 1%; MgO and 0.7%; SiO ₂ <;8%; Mn and 0.5%; P <0.04%; S <0.05%; As <0.02%, they produce by melting a metallurgical slag with a high content of iron oxides and with the properties listed above.

In the balance diagram of the iron-oxygen system, the different domains in which the whole field of the diagram is divided correspond to the solutions of oxygen in iron, in all the allotropic states of iron, α, γ, δ, tracing the phase domains starting from the upper oxide. , the ferric oxide Fe ₂ O ₃ to the ferrous ferric oxide Fe ₃ O ₄ towards the lower oxide the ferrous oxide FeO, determining the characteristic points of the diagram. In an electrolysis tank, the molten iron ore and / or the molten iron agglomerate interact with the electrolyte in the interpolar space and dissociate into iron, manganese ions. which are directed under the action of the electric field towards the liquid cathode and the negative oxygen ions, etc. which is released at the anode.

Determining the melting temperature of Fe ₂ O ₃ is difficult because this oxide has high dissociation voltage at high temperatures and decomposes, forming a melt with an intermediate composition between Fe ₂ O ₃ and Fe ₃ O ₄ so that at higher temperatures 1455 ° C Fe ₂ O ₃ phase disappears as an independent phase.

It was found that the stability of the oxides decreases from FeO to Fe ₂ O ₃ , Fe ₂ O ₃ having the maximum dissociation voltage, and FeO the minimum dissociation voltage.

Starting from pure ferric oxide schematically the process of reduction in the electrolysis tank can be written as follows: 7? Fe ₂ O ₃ = Fe +% O ₂ and, as a result, the iron cation goes to the cathode and the oxygen anion to the anode.

In order to carry out the electrolysis process, in the optimum conditions, the molten iron ores and / or the molten agglomerate are introduced in the basin so that the necessary energy, for heating them up to the melting point, is consumed in the electric arc furnace.

According to the invention, in table 1 are presented the obligatory chemical compositions of iron ores, fluorine, quartzite, bauxite, magnesite, limestone, burning deflection resulting from the lamination, forging, or flaming of steel ingots, as well as welded slag from glass. the heating ovens from the mills, after applying their process of ennobling, of the fine-grained iron concentrates from the enrichment of the iron ores, of the burned lime and of the agglomerate of iron, which determines the technological process to the optimal parameters, both from the point in view of the specific consumption of materials, as well as of the energy consumption.

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RO 120854 Β1

The technological flow according to the invention, shown in the figure, comprises some deposits of raw materials for fluorine, quartz, bauxite, magnesite, limestone, iron burn, welded slag, fine-grained iron concentrates since the enrichment of the ores.

Deposits have the role of storing these raw materials, ensuring the functioning of electrolysis tanks for a period of 30 days.

The raw materials are transported by means of transport, such as: railway wagons, minerals by sea or river and brought to a unloading station, after which they are directed to the storage areas.

Generally, transport from the unloading station to warehouses and work bunkers is carried out with conveyor belts.

The technological process for electrolysis in melts in the electrolysis tank comprises the steps described below.

Preparation of the tank for a new electrolysis

After finishing the lining works with ceramic refractory material and metal refractory material, their control and reception are executed.

Then the tank is cleaned inside and it is gradually heated with methane gas flame, in order to obtain a minimum temperature of 1250 C.

The heating system is similar to the one practiced when heating the casting pots, in which the steel developed in the electric arc furnace is to be unloaded.

Elaboration of steel

The steel that is made in the electric arc furnace is an extramural steel, with the chemical composition in mass percentages: C <0.05%; Mn <0.25%; If <0.20%; S <0.025%; At <0.06%. The sum of S, P, Ni, Cr, Al must be <0.6%.

The elaborated steel represents the amount of metal permanently maintained in the electrolysis tank, during the entire operation representing the liquid cathode with a height from 30 mm to 200 mm.

The production of extramural steel is done by known processes.

Electrolyte preparation and elaboration

The type of electrolyte is chosen and the batch calculation is made to determine the quantities of raw materials. The required amount of liquid electrolyte, represents the quantity that fills the tank, so that the height from the surface of the liquid cathode to the soles of the anodes, which represents the interpolar distance, should be between 40 and 400 mm, to which is added the height of partial insertion of the anodes in electrolyte from 50 to 200 mm.

The formation of ore stacks, as well as their sorting and homogenization from a compositional point of view, take place in a sorting station from where the ore is stored in a working bunker. Other materials: fluorine, bauxite, magnesite, burnt lime; the iron-based agglomerate, the welded iron burner and welded slag and the iron concentrates are also brought into work bunkers.

The raw materials in the work bunkers are subjected to the preparation operations consisting of: sorting on grating, crushing, burning, cooling, grinding, magnetic separation and sorting by size in vibrating screens.

Sorted and homogenized iron ores, quartz, bauxite, magnesite, with the exception of fluorine, are passed from working bunkers over mobile grills with 80 mm mesh. From these grates, the fractions + 80 mm, like fluorine in the working bunker, pass into jaw crushers.

Fractions - 80 mm from the mobile grills, pass through vibrating screens, as do the fractions - 40 mm, which results from the jaw crushers.

RO 120854 Β1

The fractions + 40 mm are recycled to the jaw crushers. 1

Fractions - 40 mm from vibrating screens, pass into conical crushers and then onto vibrating screens, which have 0 10 mm mesh. 3

The fractions + 10 mm are passed in waiting bunkers, and the fractions -10 mm are directed to the agglomeration and pelletizing plant, according to their granulations, 5 problems known in industrial practice. From the warehouse the granulation limestone between 0 60 and 80 mm is brought to a lime factory on conveyor belts, where with the help of a skip 7 it is loaded at the top of a combustion furnace.

The furnace is heated with methane gas, reaching a temperature of 1250'C in the zone 9 of the burners, so that on its descent, the limestone is dissociated, obtaining the burnt lime, known process. 11

The burned lime is cooled and is brought with the chitter to the working bunker.

From the working bunker the burned lime is passed through a jaw crusher and from here 13 falls on a vibrating sieve, from which the fraction + 40 mm is recirculated to the jaw crusher, and the fraction - 40 mm is divided into equal parts. 15

The first part is directed to the waiting hopper, and the second part of the burned lime is passed to a hammer mill and then to the vibrating sieve, where the fraction + 3 mm is recirculated to the hammer mill, and the fraction - 3 mm it is directed to the agglomeration plant, where a part enters the agglomeration load, and a part is used in the form of 19 lime milk as a binder for agglomeration in the second mixer - drum.

The iron burn and the welded slag are processed in an ennobling plant, 21 consisting of their burning in a rotary oven at 700 ° C, after which they pass through a tubular cooler and then into a hammer mill, by where it falls on a vibrating sieve. 2. 3

The fraction + 1 mm is recirculated in the hammer mill, and the fraction -1 mm is passed through a magnetic separator, which works dry and from where the magnetic grains are sent to the working hopper and from here they are directed to the agglomeration plant.

The tailings (non-magnetic grains) are directed to the landfill. 27

From the waiting bunkers, the materials pass into automatic dispensers with gravimetric system with weighing tape, after which the materials dosed in the respective quantities, corresponding to the composition in mass percent of the charge for the electrolyte, pass into a dosing trolley, after which the dosed materials they are discharged into a hump. 31

The chibla is placed on the platform of a stroller.

The platform trolley is driven in a tunnel furnace heated to a temperature of 300 ° C33 with burners mounted in the furnace vault, in order to remove moisture from the load, so that the materials have at the exit of the tunnel furnace traces of moisture in mass percentages.35

After exiting the tunnel kiln, the chivel is lifted by the crane hook and is directed to the three-phase electric arc furnace.37 As the charging of the electric furnace is done at the top, it is constructed with a pivoting vault, which allows it to be lifted and rotated and of the mounting brackets. electrodes.39 At this time, the slag on the surface of the liquid steel is completely removed with the help of the drigle (known operation), after which the vault of the electric furnace is lifted and 41 rotated.

The chibla reached above the electric oven with the load is discharged in portions, with the help of the 43 central axis, which descends over the steel bath; each time the vault returns to its place and the electric furnace is connected to the electrical grid, after each new charge, up to 45 at its total melting.

After the steel temperature has reached 1530 ° ± 30 ° C, the extruded steel 47 and the electrolyte are discharged into a pre-heated casting pot at a minimum temperature of 1250 ° C and directed to the electrolysis tank, where the discharge and connecting the 49 vats to the transformer-rectifier electrical network.

RO 120854 Β1

Preparation and smelting of iron ores and / or iron agglomerate

Simultaneously with the preparation and elaboration of the extramural steel and the electrolyte, the preparation and smelting of iron ores and / or the agglomerate of iron is also performed.

The same preparatory operations also occur for iron ores and / or iron agglomerate, specifying that, after chipping with the iron ores and / or the iron agglomerate exits the tunnel furnace, the chib is directed to another three-phase arc furnace, where it is discharged, by placing the cable on the upper edge of the electric oven, after the protective vault has been raised and rotated.

After placing the target, its central axis descends, allowing the charge to be emptied into the electric oven. After the chisel is lifted by the crane hook, the vault with electrode supports is rotated and placed on the oven.

The melting begins by lowering the electrodes, connecting the furnace to the mains with the help of the high voltage switch.

After the melt has a temperature of 1530 '± 30', it is poured into a pouring pot, previously heated to a minimum temperature of 1250 ° C.

The casting pot is supported by the main hook of the crane, and for its tilting the second hook of the crane is used.

Therefore, the casting pot loaded with iron ore melt and / or iron glomerate, is directed to the mixer, where the melt is poured through the mixer mouth.

The mixer is tilting, cylindrical in shape and is lined with refractory material.

Its role is to store, homogenize and ensure the temperature within the melt as tight as possible.

By opening and tilting the mixer, the melt is evacuated in a casting pot and directed to the electrolysis tank, to begin the electrolysis process.

The iron ore melting tank is fed at a constant rate, according to an experimentally established graph.

The operating parameters of the electrolysis tank

The main parameters to be followed for the control, correction and supervision of the electrolysis process, in order to achieve an optimum gait, that is to say a thermally stable operation and of the bath composition, at the highest possible performance, which corresponds to the optimal energy consumption are:

- electric intensity;

- the electrical voltage;

- the height of the alloy before extraction;

- the chemical composition of the electrolyte,

- concentration of iron ore and / or agglomerate in the bath;

- the temperature of the electrolysis bath.

For the correct appreciation of the obtained alloy production, its correlation with the height of metal remaining in the tank is used.

Extraction of molten alloy

The extraction of the liquid alloy is done according to a graph established on the basis of experiments depending on the capacity of the electrolysis tank.

The extraction of the molten alloy from the tank is made using an extraction pot constructed from a metal housing and has a sealed lid.

It is lined with refractory material, resistant to the action and temperature of liquid steel. It also has a connection to the vacuum system connected to components of the vacuum system, and a suction tube made of zirconium oxide.

RO 120854 Β1

The drained pot is directed to the electrolysis tank, where the suction tube 1 is inserted and the molten alloy is admitted into the drained chamber of the pot.

After extraction of the alloy, the empty pot is unloaded into the pot of the LF plant, which is 3 directed to a LF plant, where the secondary elaboration stage takes place, the so-called metallurgy in the pot, where the alloy is subjected to the process of refining and alloying, for a certain brand. 5 steel

Treatment and processing of steel 7 further, according to the technological flow, the liquid steel can be treated under vacuum by recirculation in a pre-emptied enclosure, or be left untreated, followed by the casting of the 9-steel directly into the parts, or the casting of the steel in the form of ingots, or semi-finished products in the form of molds, continuous, or the electric repainting of the blums, or forging of the REZ ingots in the form of semi-finished, or cold-deformed plastics, respectively cold, in finished products (flat products, depending on the chemical composition of the 13 steel and the shape of the product to be made.

The agglomeration and pelletizing operations of the 10-mm fractions of iron ores, 15 iron concentrates, iron burns, welded slag, other materials and the return from the agglomeration are known to take place on a continuous band with the air aspiration. 17

The agglomeration plant comprises 2 subsections, of which a preparation subsection, which includes work bunkers and a raw material preparation and loading station, and an agglomeration subsection, which includes an agglomeration machine. Working bunkers store fractions -10 mm from: 21

- iron ore;

- fluorine; 23

- quartzite;

- bauxite; 25

- magnesite;

- fine-grained iron concentrates, from the enrichment of iron ores; 27

- return for loading from the agglomeration, directed to the work hopper.

Also stored are: 29

- iron burn, -1 mm fraction;

- welded slag, fraction -1 mm, 31

- burnt lime, fraction - 3 mm;

- small coke, grain size <3 mm, 33

- small anthracite, granulation <3 mm;

- return for the bed from the agglomeration, fractions 10-25 mm, directed to the bunker of 35 work.

The raw materials for agglomeration are brought into the work bunkers by means of trans-37 conveyors with unloading trolleys.

From the work bunkers, the materials pass into the automatic gravity dosing system - 39 with a weighing tape, in the established quantities contained in the manufacturing recipe and then taken over by the metering trolley. 41

From the metering trolley, the load is discharged onto a conveyor belt, which takes it to the mixing plant, composed of two drum mixers. 43 in the first mixer - snail drum, only a partial wetting with 5% water is made with respect to the weight of the load, and the remaining water between 5 and 18% is made in the second 45 mixer - drum.

Under these conditions, the gas permeability of the load expressed in units of volume 47 of air passing through a surface unit of the load for one second must have values between 0.5 and 1.0 m ³ / m ² s, which corresponds to an air velocity of 0.5-1.0 m / s. 49

RO 120854 Β1

The water for dampening the load is brought through θ25.4 mm steel pipes, centered in the shaft of mixers with holes of 0,5 mm in the case of the first mixer and with holes of 2 mm in the case of the second.

In the second mixer - lime milk is also introduced, through a steel pipe of 25.4 mm, in an amount of 2 - 4% compared to the weight of the load.

From the second mixer - drum, the particle load is sent to the agglomeration machine through a pendulum gutter feeding device, which moves continuously back and forth, distributing the material over the entire width of the hopper above the drum feeder, which is on top of the drum. the agglomeration band.

The width of the hopper and the drum feeder corresponds to the width of the trolley carriers.

In front of the bunker, for the load for the agglomeration, a bunker is provided for the bed material, loaded with the return from the agglomeration, the fraction 10-25 mm, brought from the working hopper on conveyor belts, so that the bed corresponds to approx. 20 kg material for 1 m ² of barbecue with bars.

The point of the bedding material is to cover the spaces between the bars. Then, over the bed, the cargo destined for congestion is deposited.

the load for the agglomeration is loaded in a layer with a thickness of 200-250 mm.

The bottom of the moving trolleys is formed, as previously shown, from the bars of the agglomeration grid under which the suction chambers are located and with the help of an exhaust fan, a depression between 500 and 1000 mm water column is created in them.

The ignition of the load is started by means of an ignition oven, which is located above the belt, equipped with burners located in the oven vault.

The fuel used in the agglomeration either, because it is the coke minced or the small anthracite, has a granulation 3 mm and represents between 3 and 7% of the mass of the load.

The combustion of the fuel is done with an excess of air between 2.5 and 3.5.

After the conglomeration process is completed on the tape at the end of the suction chambers, the carriages on the treadmill unload the conglomerate, and then return through the lower part of the belt, on the empty running line, at the loading end. The agglomeration machine has a star drive wheel and a turning wheel.

The agglomerate falls on a sloping plane, into a crusher consisting of a cylinder fitted with teeth and then passes through a hot sieve plant, consisting of a sloping grate with fixed bars under which a Schenk conveyor vibrating sieve is installed, which realizes the separation of the fraction - 25 mm, representing the hot return. It is first passed through the cooler and then falls on a vibrating screen, where the fraction + 10 mm separates, which represents the return for the bed and is directed to the working hopper and the fraction - 10 mm, which represents the return for the load and is directed at the work bunker. The agglomerate, representing the 25 mm fraction, with a temperature of 600-700 ° C, is passed in a linear conveyor belt type cooler and is directed to the working hopper or is directed directly to the load, in the sieve.

The chibla is placed on a platform trolley for its transport.

After loading the target, the platform stroller is transported to the electric arc furnace for melting.

The flue gases resulting from the agglomeration process are sucked into the main gas pipeline, depositing the dust contained in the cyclone, so that finally the purified gases have a dust content below 100 mg / m ³ n.

The collected dust is reintroduced in the agglomeration process.

In Table 2 are presented 15 types of electrolytes with the indicative from A to O, in which the electrolytes are formed of oxide components such as: SiO ₂ , CaO, MgO, AI ₂ O ₃ , and some of them are present calcium calcium (CaF ₂ ), specifying that all electrolyte components are expressed in mass percentages.

RO 120854 Β1

Electrolysis baths contain in mass percentages between 5 and 100% molten iron ore 1 and / or molten agglomerate, and the rest is the molten electrolyte.

The working temperature of the molten electrolyte is higher than the alloy with the iron base deposited 3 at the cathode and is located between 1500 'and 1560'C.

During the electrolysis process, measurements must be performed at 5 well-defined intervals, which include: temperature in the electrolysis tank, chemical composition of the electrolyte, the height of the alloy, the concentration of iron ores and / or the iron agglomerate in 7 baths, the electrical voltage and the current intensity in the tank.

These parameters help to correctly determine the technological state of the vessel and allow 9 measures to be taken to correct and supervise the electrolysis process, in order to achieve optimum flow, ie thermally stable functioning, and of the composition 11 of the bath, at the highest possible efficiency, which corresponds to an optimal energy consumption. 13

Table 2

Electrolyte indicator Chemical composition % As a MgO AI ₂ O ₃ Yes ₂ 2CaO SiO ₂ CaF ₂ A 5-10 - - - - 90-95 B 15-25 - - - - 75-85 C - 15-20 - - - 80-85 D - - 20-25 - - 75-80 E 20-30 - - 1-3 - 65-75 F 45-55 - - 15-25 - 20-30 G 20-25 - 20-25 - - 60-65 H - 5-10 10-15 - - 75-85 I - 30-40 - 15-25 - 45-55 J 5-15 - - - 55-65 35-45 K - 20-30 10-20 50-60 - - IT 35-45 10-20 - 40-50 - - M 40-50 - 5-15 45-55 - - N 10-15 - 4-8 4-8 - 65-70 A 45-50 5-10 10-15 35-40 - -

It also aims to carry out the process of electrolysis from the qualitative aspect of some phenomena of the electrolyte, regarding the aspects of the flame, whether it is alive or lazy, 35 the aspect of the color of the flame and the movement of the electrolyte. The electrolyte level must be permanently maintained at an optimum level, through the technological bath correction operation. 37

The dosage of the bath composition must be made rapidly by fluorescence X-ray diffraction, either by the melting procedure or by the compaction procedure of the sample of 39 electrolytes, or by ores and / or agglomerate.

RO 120854 Β1

The installation for carrying out the process according to the invention comprises an electrolysis tank in which the process of electrolysis in melts takes place, and which has the following main components:

- the infrastructure in which the production and collection of the iron-based liquid alloy takes place;

- the superstructure, which has the role of supporting the anodic assembly and the various devices used in the technological process;

- the electrical conductors, which realize the connection of the anode and the cathode of the tank to the electrical installation;

- the control, control and supervision equipment of the electrolysis process with modern automated systems and individually adjusted of each electrolysis tank, for a stable operation, from the technical point of view and of the composition of the bath at the highest Faraday efficiency.

The infrastructure of the tank is formed by a metal drawer 1, usually of rectangular section.

The casing of the tank is made in a self-supporting construction with a metal bottom made of sheet with a thickness that is a function of the capacity of the tank.

The assembly of the tank is done by welding, or by another process with vertical and horizontal reinforcements, and the bottom solidarity is executed with longitudinal and transverse metal beams profiled.

The supporting columns of the vessel are sized to support without deformations: the gravitational loads, ie the weight of the drawer, the refractory masonry, the metallic refractory material, the liquid alloy and the liquid electrolyte and possibly the refractory bolt, if it is placed on the cup. The interior of the metal casing comprises the refractory masonry of the glass and the side walls.

The masonry of the glass is executed as follows: on the bottom of the metal drawer is made an insulation formed of a layer of asbestos 2 of 15 mm thick, over which a layer with powder of chamomile 3 with a thickness between 20 and 40 mm is placed and then a row of porous brick bricks 4 wide with a thickness of 65 mm, compactly built with refractory mortar.

After the insulation is dried, the masonry is continued with a layer of magnesite granules with dehydrated tar 5 approx. 20 mm thick and then 2 to 4 rows of normal magnesite bricks 6, or wide stabilized dolomite or 1 or 2 rows per width and 1 or 2 rows per edge, depending on the capacity of the vessel. The perfectly dry bricks are built without mortar with 0.5 mm joints, which are filled with magnesite dust.

Above them is printed a layer of carbon mass 7 of 15 mm thick cast in a hot state, ensuring the horizontal surface of the seating surface of precoated carbon blocks 10 with lengths from 0.4 to 2 m, widths from 0.4 to 0 , 8 m and heights from 0.4 to 0.6 m depending on the capacity of the vessel.

Each carbon block has a longitudinal groove usually profiled in the swallowtail.

The cathode of the vessel is made by assembling several carbon blocks on a cathode bar 8, of steel. The free space, between the channel walls of the carbon blocks and the cathode bar of steel, is filled for sealing and electrical contact with printed carbon mass.

Over the carbon blocks 10 the carbon mass 13 is stamped. The casing of the vessel is provided with the outlet holes of the ends of the cathode bar, having at the ends an insulating ceramic bush 9.

The casing of the basin on the sides is insulated with asbestos plates 2 15 mm thick and a row of magnesite 11, wide, with a thickness of 65 mm, which in fact represents the masonry.

RO 120854 Β1 the side walls above the level of the glass of the basin, so that between this masonry and the one of the insulation there is a space of approx. 40 mm filled with magnesite granules mixed with dehydrated tar 12.3

On the inner sides of the lateral wall are placed cathode precoated carbon side plates 14 with a length between 0.6 and 0.8 m, a width between 0.4 and 0.5 m and a thickness between 5 0.15 and 0.25 m, fixed one inclined to make the crucible of the vessel.

Between the cathodic side carbon plates 14 and the masonry formed by the magnic-7 bricks 11 the carbon mass 13 is printed in successive layers.

Next, a new carbon mass layer is printed on the carbon plates 13.9

Both the carbon mass on the hearth and the lateral one have the role of sealing and electrical contact with some 15 metallic plates of refractory alloy both on the hearth and on the side walls.11

The cathodic refractory metal plates are made from one of the refractory alloys, whose chemical compositions expressed in mass percentages are presented in table 3 and have an index of 1 to 28.

It is not compulsory for the metal plates of refractory alloys for the anode and for the 15 cathodes to have the same chemical composition.

The role of the metal plates is to avoid the contact of the liquid alloy with the carbon of the 17 carbon mass, or of the carbon blocks and plates so as not to produce the carbide of the liquid alloy.19 In general, the electrolysis tanks are equipped with 16 pre-formed carbon anodes. prismatic with dimensions of approx. 800 mm long, 600 mm wide and 600 mm high. 21 As these anodes are known to work under high oxidability conditions at high temperatures, continuous depolarization of oxygen occurs during electrolysis. The details of the 23 chemical reactions involved are not yet fully known, but it is certain that the oxygen ions from the dissociation of iron oxides as in the case of the Hali-Heroult process, electrolyte 25 is discharged to the carbonic anodes, with the formation of anodic gases containing mainly carbon dioxide and small amounts of carbon monoxide. 27 »

You can write the total reaction.

Fe ₂ O ₃ + 3C = 4Fe + 3 CO ₂

RO 120854 Β1

Chemical composition,% The base i- u. N N > > > > Nb Z z Nb Nb Nb jd Z _Q z Your CD 1- Your T 0,5-1 4 t 4 1 4 4 1 4 4 1 4 4 4 4 t T co 0.06 to 0.08 and 1 1 t and 1 4 4 1 4 4 1 t 1 OT 0.2-0.4 1 • 4 1 4 4 1 1 1 4 4 4 1 1 1 > 0.6 to 1.3 0.05-0.1 1 1 4 4 4 4 0.02 to 0.05 1 • 1 1 1 1 1 4 > 4-6 CO -4- 5-8 1 4 1 1 1 1 4 1 4 4 1 4 1 Your 1-3 3-6 4 1 0.5-1.5 1 1 I 8-18 30-34 4 1 4 1 25-29 1 1 1 $ 4-6 0.4-0.8 4 1 0.5-1.5 1 • 4-6 4 1 10-20 4 4-6 10-14 16-22 10-14 15-25 8-12 Nb 2.4 IO t tf a 40-50 4 I 16-24 15-25 15-25 • • 1 4 1 • • 4 4 N 3-6 CO 4 T ~ 1 and 0.4-0.8 0,5-1 1-3 6-10 CS1 cp 4 4 4 0.5-1.5 A 2 X 1 LO 0,5-1 1 0.5-1.5 1 1 3-5 • 4-8 1 4-7 5-9 1 1 C0 3-7 a CM 1 A 3-7 t 3-7 6-10 • 5-9 5-7 1 1 6-12 • • Co. 1 1 1 1 1 • 1 1 • 4 Indicative CM CO IO co CO cn A - CM CO iO V co r 00

io A> t CO io CD T ~ V " x- MAN

τ- CO

IO

CO

CO

CQ

CD H (0

a

a

L_ o k_ o

co t

CM

CQ

RO 120854 Β1

And the O

N

The CL

o O <O O o

a A T CM CO τ ^- CM CM CM CM

τΓ m CD b- 00 CM CM CM CM CM

RO 120854 Β1

Inert anodes for equipping the plant according to the invention can be realized in several ways.

Bins equipped with precooked carbon anodes use a number of precooked carbon blocks, which are embedded in metal containers, comprising the lower, upper and side surfaces, to protect against oxidation.

The container is made of refractory metal plates with the same chemical composition as the cathodic side carbon plates, or with another chemical composition from those presented in table 3.

The precoating anodes are embedded in containers, using a printed carbon mass, to seal and obtain a perfect electrical contact. The refractory metal plates can be welded, or joined by various processes, to obtain the container.

The inert anode, with a geometry similar to the precooked carbon anode, is made of a compact metal block with the chemical composition of some of the refractory alloys presented in table 3.

The inert anode is made of resistive ceramic materials composed of yttrium trioxide (Y ₂ O ₃ ) and stabilized zirconium oxide (ZrO ₂ ).

In order for the anodic refractory metal plates to withstand the intense oxidation process at high temperatures, they are covered by spraying, electrodeposition, or other coating processes, with a protective layer consisting of: MoSi ₂ , WSi ₂ , or of the type: ZrBe ₁₃ , Zr ₂ Be ₁₇ , NbBe ₁₂ , Nb ₂ Be- | ₇ , Nb ₂ Be-i ₉ , TaBe- | ₂ , Ta ₂ Be ₁₇ as of type: TiB _2i ZrB ₂ . Melting electrolysis is also practiced for the industrial elaboration of metals such as: aluminum, alkaline, alkaline-earth, palladium, uranium, titanium, thallium, tantalum, boron etc.

the embedding of precoated carbon anodes into metal containers, includes the lower, upper and lateral surfaces.

The container can be made from:

- metal plates from one of the refractory alloys whose chemical composition is presented in table 3;

- metal plates from one of the brands of austenitic laminated or forged refractory steels provided in table 4;

- metal plates from one of the brands of austenitic refractory cast steel listed in table 5.

the precoating anodes are embedded according to the mentioned procedure.

The refractory metal plates can be welded or joined by different processes.

The inert anode is made from a block of weldable carbon steel obtained by forging or molding containerized by refractory metal plates, the connection between the 2 metals being made by metallothermal welding by electrode welding or another process.

The coating of the refractory anodic metal plates is done by the same processes and with the same materials, as previously exposed.

For electrolysis in melts at maximum working temperatures of 1000 ° C the inert anode is made of forged electrolytic copper containerized with refractory metal plates.

Such types of containerized anodes are considered as inert anodes, as they have the following characteristics:

- insolubility in the melts of the electrolyte, of the molten iron ore and / or of the molten agglomerate;

- resistance to the action of anodic oxygen;

- low electrical resistance and low contact resistance with the metallic current conductor;

- lack of contamination of the alloy with liquid iron base deposited at the cathode;

RO 120854 Β1

- thermal stability and thermal shock resistance;

- saving precocious carbon anodes, which in fact represent consumption, only the initial quantities contained, or the complete absence of precocious carbon anodes if steel blocks or electrolytic copper blocks are used;

- long service life without anode change operations, which disrupts the technological process and causes thermal imbalance

- elimination of the production of polluting gases by: carbon dioxide, carbon monoxide, as well as other gases.

Table 4

Germany Verkstoff mark France AFNOR mark 1.4335 X6 Cr Ni 25.20 Z 8 NC 32-21 1.4577 X5 Cr Ni Mo Ti 25.25 Z12NC 37-18 1.4587 X35 Cr Ni Nb 25.24 1.4830 X15CrNi Yes 25.20 British standard England mark 1.4841 X12Cr Ni 25.20 1648 Grade F 1.4842 X12CrNi 25.21 1648 Grade G 1.4845 X15NÎ CrNb 32.21 1648 Grade N 1 1.4850 X35 Ni Cr 36.25 1648 Grade N 2 1.4859 X12NÎ Cr 36.18 1648 Grade K 1.4863 Χ12ΝΪ Cr Si 36.16 3072 NA 15 1.4864 X10NÍ CRAI Ti 36.20 3072 At 16 1.4876 Neither Mo 16CrW 4238 Grade F C 2.4537 S-Ni Cr 20 Nb 4238 Grade H 1 C 2.4806 4238 Grade H 2 C - A 22 Nb - A 11 Ti

Germany Verkstoff mark 1.4465 G-X2 Cr Ni Mo N 25.25 1.4840 G-X15 CrNi 25.20 1.4848 G-X40 CrNiSi 25.20 1.4849 G-X40 Ni CrSi Nb 38.18

RO 120854 Β1

Table 4 (continued)

Germany Verkstoff mark 1.4852 G-X40 Ni Cr Nb 35.25 1.4855 G-X30 Cr Ni Si Nb 24.24 1.4857 G-X35 Cr Ni Si 35.25 1.4865 G-X40 Ni Cr Si 38.18 1.4868 G-X50 Cr Ni 30.30 1.4872 2.4679 G-Ni Cr 28 W 2.4813 G-Ni Cr 50 Nb 2.4879 G-X 50 Ni Cr W 48.28

The metal bath is composed of two layers that are not immiscible between them: on the one hand the liquid alloy based on iron and the molten electrolyte with the molten iron ores and / or the molten agglomerate.

The superstructure of the electrolysis tank supports the anode assembly, aiming that the distance between the lower surface of the anodes and the surface of the liquid alloy, ie the interpolar distance, is maintained at the optimum value for the normal conducting of the electrolysis process.

The superstructure of the electrolysis tank comprises the following subassemblies:

- the pillars supporting the fixed frame and the anode assembly;

- the electro-mechanical device for vertical displacement of the anode assembly;

- the four pivoting bolts above the electrolysis tank in case the bolt assembly does not rest on the tank;

- gas collection hotels resulted in the electrolysis process.

The electrolysis tank is equipped at the top with a refractory bolt A, which represents the most required thermal and mechanical construction element, and which contributes to the reduction of thermal losses and, as a consequence, to the increase of the efficiency of the tank.

From a constructive point of view, the vault is made up of movable and independent vault sectors allowing each other to raise and rotate them during the technological works in the basin, which involve: changes of anodes, introduction of molten electrolyte, molten iron ore and / or molten agglomerate, extraction of molten alloy, etc.

The vaulted sectors are made of bricks 24, refractory, specially designed for the vault, bricks 23, which rest on the outside on refractory bricks of support and which in turn are supported by a ring 22, metallic, supported on the metal drawer 1 of the vessel or on a tank-independent construction that allows individual mobility of the vault sectors.

inside the refractory vault sector are water-cooled welded steel sealing rings 25, which on the one hand cool the most thermally demanded part of the vault, and on the other hand, they cool the hot gases that have been technologically produced, having a beneficial effect. on the anodes.

The containerized anodes are mounted on an anodic rod made of refractory steel 18, fixed by the movable frame of the vessel, allowing their removal and replacement in the electrolysis process, if applicable.

RO 120854 Β1

The interpolar distance adjustment is made by moving the movable anode frame 19, of 1 which are fixed the rods with containerized anodes, by the vertical displacement device of the anode assembly. The figure also shows the fixing system between the anode and the anodic rod in 3 refractory steel.

Above the entire superstructure of the electrolysis tank is a hood with the piping 5 necessary for collecting the gases and sending them for dry treatment, followed by a wet treatment. 7

An example of embodiment of the invention is given, assuming the beginning of the electrolysis process with an electrolysis tank prepared for a new campaign. 9

The casing of the tank is of a construction with bottom and the metal sides provided with a system of longitudinal and transverse metal beams calculated to support without deforestation the weight of the casing, the weight of the reinforcement with ceramic refractory material and metallic refractory material, the weight of the liquid alloy and the liquid electrolyte. 13

The superstructure of the tank consists of the following subassemblies: pillars for supporting the fixed frame and the anodic assembly, the anodic assembly, the electro-mechanical device 15 for vertical displacement of the anodic assembly, the sectors of the vault, the exhaust gas collection hood in the electrolysis process. 17

It works with precoated anodes, containerized, from a refractory alloy of the type: 5% Ti;

20% Nb, the rest V, in mass percentages.19

The cathodic metal plates both the bottom and the side parts are made of the type of refractory alloy. 0.5% Zr; 3% W, the rest Mo in mass percentages.21

After cleaning the tank inside it proceeds to the gradual heating with flame of methane gas, in order to finally obtain a temperature of 1250 ° C, a well-known practice. 23 In the first stage, an extramural steel with a three-phase arc is developed in the electric oven. chemical composition in mass percent: C 0.04%; Mn 0.20%; S 0.18%; P 0.015%; 25

S 0.020%; 0.04%; and the sum of the elements S, P, Ni, Cr, Al 0.5%.

The elaborated steel represents the amount of metal permanently kept in the tub throughout its 27 lifetime, representing the liquid cathode with a height of 60 mm.

For electrolyte the following chemical composition was chosen in mass percent: CaO 29 27%; SiO ₂ 3%, CaF ₂ 70%.

The raw materials needed are: burnt lime, quartzite and fluorine, which are subjected to grinding operations except lime, crushing, sorting on vibrating screens, grinding in conical crushers except lime, which is passed into the hammer mill, after 33 which follows a new sorting on vibrating screens and then they are placed in the waiting bunker. The amount of liquid electrolyte required to fill the tank represents the height from the cathode 35 liquid to the anode sole of 100 mm, to which is added the height of partial insertion of the anodes into electrolyte of 120 mm. 37

From the waiting bunkers, the materials pass into automatic dispensers, after which the materials dosed in the quantities according to the calculation of load pass into the dispenser cart and from it 39 are discharged into a sieve, placed on the platform of a trolley.

The platform trolley is guided into the tunnel furnace, heated to a temperature of 300 ° C, 41 to remove moisture from the load.

After exiting the tunnel kiln, the chibra is lifted by the crane hook and directed 43 to the three-phase electric arc furnace.

at this time the slag from the surface of the liquid steel is completely removed with the help of the drigle, known operation, after which the electric oven vault is raised and rotated.

The chibla reached above the electric oven with the load is discharged in portions, 47 so that after each portion the electric arc is primed and this is repeated until it has completely melted. 49

RO 120854 Β1

After the steel temperature has reached 1530C, the extramolar steel and electrolyte are discharged into a pre-heated casting pot at 1260 ° C and directed to the electrolysis tank, where the vat is connected and connected to the transformer-rectifier electrical grid.

Simultaneously with the preparation and elaboration of the extramural steel and the electrolyte, the iron ore is being prepared and melted, which is a hematite from Itabiri-Brazil. The chemical composition in mass percentages is: Fe 68.9%; Mn 0.09%; P 0.03%; S 0.01%; SiO ₂ 0.5%; AI ₂ O ₃ 0.6%; CaO 0.1%; MgO 0.1%; H ₂ O 1.7%.

The same preparatory operations also apply to the iron ore, with the indication that after the iron ore quit comes out of the tunnel kiln, the chib is directed to another three-phase electric arc furnace, where it is discharged.

The melting begins by lowering the electrodes, connecting the furnace to the mains. When the melting has reached the temperature of 1530 'C, it is passed to its discharge in a casting pot, previously heated to 1250 "C

The casting pot is directed to the ore melter storage mixer.

From the mixer, the melt is evacuated into a casting pot, which is directed to the electrolysis tank, to begin the electrolysis process.

The iron ore melting tank is fed at a constant rate according to an experimentally established graphite. Also, the extraction of the liquid alloy is done according to a graph established on the basis of experiments, depending on the capacity of the electrolysis tank.

The extraction of the alloy is done by means of a vacuum extraction pot provided with a suction tube made of zirconium oxide

The drained pot is directed to the electrolysis tank, where the suction tube is introduced into the tank and the admission of the molten alloy into the drained chamber of the pot.

After extraction of the alloy, the emptied pot is unloaded into the LF pot, which is directed to the LF plant, where the secondary elaboration stage takes place, ie the alloy is subjected to the refining and alloying process for a certain steel mark.

Further, the liquid steel is treated in vacuo, followed by the casting of the steel in the form of ingots or in the form of blums continuously cast, or deformed hot or cold, respectively, in finished products (flat, long or tubular), in depending on the chemical composition of the steel and the shape of the product to be made.

Claims (9)

claims 1 anodic refraction being performed by the same processes and with the same materials as in the last part of claim 12, and for electrolysis in melts, with maximum working temperatures of 1. A process of electrolysis in melts, for obtaining iron-based alloys, characterized in that it provides for the gradual heating with flame of methane gas of an electrolysis tank, to finally obtain a temperature of at least 1250 "C, pan in which an extramural steel made in three-phase electric arc furnace is introduced, with the chemical composition in mass percentages: C <0.05%; Mn <0.25%; If <0.20%; P <0.020%; S <0.025%; Al <0.06%; wherein the sum of S, P, Ni, Cr, Al must be> 0.6%, steel representing the amount of metal permanently maintained in the electrolysis tank throughout its operation representing the liquid cathode with the height from 30 to 200 mm, In the basin an electrolyte filling the tank is also introduced, so that the height from the surface of the liquid cathode to the soles of the anodes representing the interpolar distance is between 40 and 400 mm, to which is added the height of partial insertion of the anodes into the electrolyte. from 50 to 200 mm, after which the electrolysis tank is connected to the electrical installation and the electrolysis takes place at a temperature of 1500 ... 1560 ° C, after the electrolysis the obtained alloy is extracted from the tank with the help of a vacuum pot and discharged into the another pot in which the secondary alloy elaboration takes place, which is subjected to refining and alloying, to obtain the desired steel mark. RO 120854 Β1 2 60%; Iron concentrates: Fe>66%; CaO <3%; SiO ₂ <6%; Mn <0.05%; P <0.03%; 13 S <0.03%; As <0.05%; Var ars: MgO <1%; SiO ₂ <1%; S <0.1%; AI ₂ O ₃ + Fe ₂ O ₃ <1; CaO + MgO 93%; PC <4%; ? Iron agglomerate: Fe>66%; CaO <3%; SiO ₂ <6%; P <0.03%; 15 S <0.03%; As <0.05%. 2. Process according to claim 1, characterized in that the materials used 1 must correspond to the chemical percentages, by mass, presented in table 1, for carrying out the technological process at the optimal parameters both from the point of view of the specific consumption of materials, as well as of energy consumption, namely for: Iron Ores: Fe>60%; AI ₂ O ₃ 2 2%; CaO 2 1%; MgO 0.7%; SiO ₂ τ 8%; Mn 2 0.5%; 5 P;>0.04%; S z 0.05%; As 0.02%; fluorine: CaO 5%; SiO ₂ 2.5%; S τ 0.2%; CaF ₂ 2 96%; AI ₂ O ₃ + Fe ₂ O ₃ 0.3%; a quartzite: AI ₂ O ₃ τ 0.8%; CaO <0.3%; MgO <0.2%; SiO ₂ τ7 96%; Fe ₂ O ₃ <0.5%; PC <0.5%; o Bauxite: AI ₂ O ₃ t 77%; CaO <0.05%; SiO ₂ <9%; Fe ₂ O ₃ <10%; TiO ₂ <0.6%; PC <1%; Magnesite: CaO <4%; MgO 2 88%; SiO ₂ <4%; PC <1%; 9 Limestone: AI ₂ O ₃ <0.5%;CaO>56%; MgO <1.5%; SiO ₂ <2%; P <0.009%; S <0.07%; Fe ₂ O ₃ <0.5%; MnO <1.5%; AI ₂ O ₃ + Fe ₂ O ₃ <2%; PC <43 Burn of iron: Fe>68%; AI ₂ O ₃ 11 <0.9%; SiO ₂ <0.8%; P <0.02%; S <0.02%; MnO <1.5%; C <0.15%; Welded slag: Fe 3 1000'C the inert anode is made of a forged electrolytic copper block containerized with metal plates from refractory alloys whose chemical composition is found in tables 3, 5 4 or 5. 14. An installation according to claims 9 ... 13, characterized in that in the part 3. Process according to claims 1 and 2, characterized in that both the electrolyte components and the iron ores and / or iron agglomerate can also be introduced in a solid state, with a higher energy consumption.19 4. The process according to claims 1,2 and 3, characterized in that the electrolytes must correspond to the chemical compositions in mass percent shown in table 2, namely 21: Indicative A: CaO 5-10%; CaF ₂ 90-95%; for electrolyte B: CaO 15-25%; CaF ₂ 75-85%, 23 for MgO electrolyte 15-20%; CaF ₂ 80-85%; for the electrolyte AI ₂ O ₃ 20-25%; CaF ₂ 7580%; for CaO electrolyte 20-30%; SiO ₂ 1 -3%; CaF ₂ 65-75%; for CaO electrolyte 45-25 55%; SiO ₂ 15-25%; CaF ₂ 20-30%; for CaO electrolyte 20-25%; AI ₂ O ₃ 20-25%; CaF ₂ 6065%; for MgO electrolyte 5-10%; AI ₂ O ₃ 10-15%; CaF ₂ 75-85%; for electrolyte MgO 30-27 40%; SiO ₂ 15-25%; CaF ₂ 45-55%; for CaO electrolyte 5-15%; 2 CaO SiO ₂ 55-65%; CaF ₂ 35-45%; MgO 20-30%; A ₂ 0 ₃ 10-20%; SiO ₂ 50-60%; for CaO electrolyte 35-45%; 29 for Mg010-20% electrolyte; SiO ₂ 40-50%; CaO 40-50%; AI ₂ O ₃ 5-15%; SiO ₂ 45-55%; for CaO electrolyte 10-15%; AI ₂ O ₃ 4-8%; SiO ₂ 4-8%; CaF ₂ 65-70%; and for CaO electrolyte 31 45-50%; MgO 5-10%; AI ₂ O ₃ 10-15%; SiO ₂ 35-40%, the electrolytes being formed of oxide components such as: SiO ₂ , CaO, MgO, AI ₂ O ₃ and some of them also present calcium fluoride (CaF ₂ ). 33 5. Process according to claims 1,2, 3 and 4, characterized in that, in the electrolyte, the concentration of molten iron ore and / or molten agglomerate in mass percent is between 5 and 100%: 6. Process according to claims 1,2, 3,4 and 5, characterized in that the working temperature of the molten electrolyte is between 1500 and 1560 ° C, above the melting temperature of the alloy with the iron base deposited on the cathode. 39 7 upper, the electrolysis tank is equipped with a refractory vault (A) formed from mobile sectors and independent of each other, allowing them to be lifted and rotated during the execution 7. Process according to claims 1, 2, 3, 4, 5, 6 and 7, characterized in that the dosage of the bath composition is made rapidly, by X-ray diffraction, fluorescence, or 41 by the melting procedure, or by procedure for compacting the sample from electrolyte, or from ores and / or agglomerate 43 8. An installation for carrying out the process according to claim 1, characterized in that it consists of electrolysis tanks in which the electrolysis process takes place, the infrastructure of a tank according to being formed of a metal drawer (1), usually of rectangular section. , made in a self-supporting construction with metallic bottom, executed from 47 RO 120854 Β1 sheet with a thickness, depending on the capacity of the vessel, at which the assembly of the vessel is done by welding, or by another process with vertical and horizontal reinforcements, and the bottom solidarity is executed with longitudinal and transverse metal beams profiled, the supporting posts of the vessel. the vessel being provided to support the weight of the drawer (1), the refractory masonry, the refractory metal material, the liquid alloy and the liquid electrolyte and, possibly, the refractory vault, if it is located on the basin. 9. An installation according to claim 8, characterized in that the masonry of the glass pan comprises an insulation mounted on the bottom of the metal drawer (1) and formed of a layer of asbestos (2) of 15 mm thick, over which a layer of powder is applied ( 3) of chamomile with a thickness between 20 and 40 mm and then a row of bricks (4) of porous chamomile on the side with a thickness of 65 mm, compactly built with refractory mortar, after drying the insulation, the masonry continuing with a layer of magnesite ( 5) granules with a dehydrated tar of approx. 20 mm thick and further 2 to 4 rows of bricks (6) normal magnesite, or wide stabilized dolomite or 1 or 2 rows wide and 1 or 2 rows per edge, depending on the capacity of the vessel, above which it is printed a layer of carbon mass (7) 15 mm thick, cast in a hot state, ensuring a horizontal surface of the surface of precoated carbon blocks (10) with lengths from 0.4 to 2 m, widths from 0 , 4 to 0.8 m and heights from 0.4 to 0.6 m depending on the capacity of the vessel, over which the carbon mass (13) is stamped, each carbon block having a longitudinal profile profiled channel, usually in the swallow tail and the cathode of the vessel is made by assembling several carbon blocks on a steel cathode bar (8), the free space, between the channel walls of the carbon blocks and the cathode bar of steel, is filled for sealing and electrical contact with stamped carbon mass, for u the ends of the cathode bar (8) being provided in the drawer (1) of the vessel with some outlet holes having at the ends an insulating ceramic shell (9), the drawer of the vessel being laterally insulated with asbestos plates (2) 15 mm thick and with a row of magnesite bricks (11) wide with a thickness of 65 mm, which in fact represents the masonry of the side walls above the level of the glass of the basin, so that between this masonry and the insulation there is a space of approx. 40 mm, filled with magnesite granules mixed with dehydrated tar (12), on the inner sides of the lateral wall being placed cathode precoated carbon side plates (14) with a length between 0.6 and 0.8 m, a width between 0.4 and 0 , 5 m and the thickness between 0.15 and 0.25 m, fixed to each other inclined, to make the glass crucible, so that between the cathodic side carbon plates (14) and the masonry formed by the magnesite bricks (11) to be stamped carbon mass (13) in successive layers, both carbon mass on the hearth and the lateral one, having the role of sealing and electrical contact with the metal plates of a refractory alloy (15), both on the hearth and on the side walls. 10. An installation according to claim 9, characterized in that the cathodic refractory metal plates (14) are made from one of the refractory alloys whose chemical compositions expressed in mass percentages are presented in table 3 and have for: Indicative 1: Mo 5-7%; Zr 3-6%; Nb 2-4%; W 4-6%; Of 1-3%; V 4-6%; Y 0.6-1.3%; If 0.20.4%; B 0.06-0.08%; Hf 0.5-1%; basic Ti; Indicative 2. Ti 4-6%; Mo 0.5-1%; Nb 0.4-5%; W 0.4-0.8%; Of 3-6%; V 4-8%; Y 0.05-0.1%; basic Zr; Indicative 3: Ti 3-7%; Nb 40-50%; V 5-8%; basic Zr; Indicative 4; Ti 10-20%; basic V; Indicative 5: Ti 3-7%; Mo 0.51,5%; Zr 1-3%; Nb 16-24%; W 0.5-1.5%; Ta 0.5-1.5%; basic V; Indicative 6: Nb 15-25%; basic V; Call sign 7; Ti 3-7%; Nb 15-25%; basic V; RO 120854 Β1 Indicator 8: Ti 6-10%; 3-5% mo; Zr 0.4-0.8%; W 4-6%; Of 8-18%; basic Nb; 1 Indicative 9: Zr 0.5-1%; Of 30-34%; basic Nb; Indicative 10: Mo 4-8%; Zr 1-3%; Y 0.02-0.05%; basic Nb; 3 Indicative 11: Ti 5-9%; W 10-20%; basic Nb; Indicative 12: Ti 5-7%; Zr6-10%; basic Nb; 5 Indicative 13: Mo 4-7%; Zr 1-2%; W 4-6%; basic Nb; Indicative 14: Zr 1-3%; W 10-14%; Ta 25-29%; basic Nb; 7 Indicative 15: Ti -12%; 5-9% mo; W 16-22%; basic Nb; Indicator 16: W 10-14%; Your base; 9 Indicator 17: W 15-25%; Your base; indicative 18: Zr 0.5-1.5%; W 8-12%; Your base; 11 Indicative 19: W 14-22%; Hf 1-4%; Your base; Indicative 20: Nb 2-6%; Hf 2-6%; Your base; 13 Indicative 21: Ti 0.5-1.65%; Zr 0.1-0.5%; basic Mo; Indicative 22: Zr 0.1-0.5%; W 1-4%; basic Mo; 15 Indicative 23: Zr 12-18%; basic W; Indicative 24: Nb 2-6%; Of 2-6%; basic W; 17 Indicative 25: Ti 0.1-0.5%; V 0.1-0.5%; Y 0.2-1.5%; base Cr; Indicator 26: Ti 0.1-0.5%; Zr 0.1-0.5%; Y 0.2-1.5%; basic Cr; 19 Indicative 27: Ti 0.2-7%; Zr 0.05-0.3%; V 0.8-4%; B 0.1-0.8%; base Cr; Indicative 28: Co 0.1-0.6%; Ti 0.1-3.5%; Zr 1-8%; Nb 0.3-2.2%; W 0.01-0.7%; V 0.2-2.2%; 21 Y 0.1-1.2%; B 0.05-0.2%; base Cr. 11. The plant according to claims 9 and 10, characterized in that it uses 23 for equipping the precolourized carbon anode electrolysis tanks. 12. Installation according to claims 9 ... 11, characterized in that the precoated carbon-25 anodes use precoated carbon blocks, embedded in metal containers from refractory alloys with the same chemical composition as the metal plates from refractory alloys 27, which it covers the carbon blocks and the cathodic side carbon plates, or with another chemical composition from those presented in table 3, the embedding of precycled carbon anodes 29 into containers is made, using stamped carbon mass for sealing and obtaining an optimal electrical contact, or an inert anodes with a geometry similar to the precocious carbon anode 31 made from a compact metal block with the chemical composition of one of the refractory alloys presented in table 3, the inert anodes can be made of resistive ceramic materials composed of yttrium trioxide (Y ₂ O ₃ ) and zirconium oxide (ZrO ₂ ) stabilized, and for that the anodic refractory metal plates to withstand the intense oxidation process at elevated temperatures, both in the case of precycled carbon anodes and in the case of inert anodes with a similar geometry, are covered by spraying, electrodeposition or other plating processes 37 with a coating layer. protection consisting of: MoSi ₂ , WSi ₂ , ZrBe ₁₃ , Zr ₂ Be ₁₇ , NbBe ₁₂ , Nbj3e ₁₇ , Nb £ Be ₁₉ , TaBe ₁₂ , Ta ₂ Be ₁₇ as well as type: TiB ₂ , ZrB ₂₎ . 39 13. An installation according to claims 9 ... 12, characterized in that, for electrolysis in melts, practiced for the industrial elaboration of metals such as aluminum, alkaline, alkaline-earth, palladium, uranium, titanium, thallium, tantalum, boron etc. . the realization of the inert anodes takes place by the embedding of the carbonic anodes precopulated in metal containers 43 comprising the lower part, the upper one and the lateral surfaces, the container being made of metal plates from one of the refractory alloys whose chemical composition is presented in table 3, from the plates metallic from one of the laminated or forged austenitic refractory steels listed in table 4 or metallic plates from one of the cast austenitic refractory steels 47 provided in table 5, coating the metallic plates from the alloys RO 120854 Β1 9 technological works in the basin, which involve changes of anodes, introduction of molten electrolyte, molten iron ores and / or molten agglomerate, extraction of molten alloy, bad vault section11 being constructed of bricks (14) shaped refractories that are supported on the outside on bricks (23) refractory to support and which in turn are supported by a waist ring 13 (22), which rests on the metal drawer (1) of the vat, or on an independent construction of the basin and which allows the individual mobility of the vault sectors, inside the 15 refractory vault sectors, provided with sealing rings (25) of welded sheet cooled with water circulation, which, on the one hand, cool the part of the vault most requested thermally, and on the other 17 On the one hand, they cool the hot gases with technological results.