METHOD AND DEVICE FOR OBTAINING STEEL IN A LIQUID BATH

Abstract: The proposed method is characterized in that the liquid bath is constituted by the melt of a low-carbon steel and molten slag. Oxidation and reducing zones are created through which, along a closed path on the surface of the molten low-carbon steel, is circulated the molten slag, into which are blown powder slag materials which are melted with the heat of a fuel-oxygen torch immersed into the melt. The said method is carried out in a melting reservoir shaped as a closed annular chamber (1) provided with partitions (11) hermetically dividing the gas space above the molten slag into oxidation (6) and reducing (7) zones.

Description: The present invention relates to ferrous metallurgy and more particularly to a method of making steel in a liquid bath and to an apparatus for effecting the same. Widely known in the prior art are traditional methods of making steel according to a multistage technological scheme: agglomeration-coke chemistry-open hearth process-steel melting processes (converter, open-hearth, electric steel melting). All these processes suffer from substantial disadvantages: a great quantity of expensive main processing units with complex auxiliary equipment; large total expenditures (labor consumption included) for their maintenance and repair; large interstage heat losses associated with the cooling of intermediate products; substantial expenditures for interstage transportation of intermediate products; substantial total heat losses made up of heat losses of each processing unit; substantial total losses of extracted iron; limited possibilities in utilization of the starting metal charge; substantial environmental pollution by production wastes at each processing stage. Known in the prior art is a method of making steel in a liquid bath by using charge materials comprising iron-bearing materials and slag-forming fluxes. The method essentially resides in making low-carbon steel by way of interaction of iron oxides with a reducing agent, in combustion of fuel in a oxygen-bearing gas to provide the process with heat and in introduction of additions by an off-furnace method into the low-carbon steel for making the steel of a preset chemical composition. (Pokhvisnev A.N., Kozhevnikov I.Ju., Spektor A.N., Yarkho E.N. "Off-Furnace Production of Iron Abroad", Metallurgy, Moscow, 1964, pp. 314-315). In the known method a liquid bath is formed first for melting metal iron, for example, steel scrap. The iron melt is continuously or periodically carburized by saturating it with a reducing agent by way of dipping carbon electrodes into the iron melt or by injecting a carbon power therein with the aid of methane. Lumps of iron ore and slag-forming fluxes are continuously or periodically loaded on the surface of the iron-carbon melt. Due to an intimate contact with the reducing agent, viz. carbon dissolved in the iron melt the iron is reduced, thereby increasing the mass of the iron-carbon melt. In this case oxides of the waste ore contained in the iron ore are melted together with the slag-forming fluxes, thereby forming a melted slag on the surface of the iron melt. The processes of melting the charge materials and reducing the iron are provided with heat obtained by combustion of fuel in an oxygen-bearing gas over the liquid bath. Prior to tapping the iron-carbon melt is decarburized by stopping in advance the delivery of the carbon-bearing reducing agent. The obtained low-carbon steel is delivered for correcting the chemical composition thereof to preset parameters by using the off-furnace method. Known in the prior art is an apparatus for making steel in a liquid bath which is essentially an open-hearth furnace comprising a melting space for melting charge materials and forming a liquid bath for making therein a low-carbon steel. The melting space is formed by a hearth, walls and a roof, and is provided with a device for introducing an iron reducing agent into the liquid bath, a means for loading charge materials therein and a means for the tapping of steel and slag therefrom, a burning device for combustion of fuel inside the melting space at the expense of an oxygen-bearing gas, and a duct for discharge of combustion products from the melting space. An essential feature of this known method and apparatus resides in a common processing zone for carrying out the oxidizing and reducing processes. In this known case the atmosphere in the open-hearth furnace working space is of a a strongly oxidizing character in relation to metal which is caused by the need for complete combustion of fuel. In addition, the oxidizing atmosphere retards the process of reducing the iron which when brought into contact with oxidizing gases, viz. combustion products (CO 2 and H 2 O) is actively oxidized. Thus, in the known method two opposite metallurgical processes take place simultaneously: at the boundary of metal contact with the slag containing iron oxides the latter are reduced, while at the "metal-gas" boundary the iron is oxidized. But mainly the iron is oxidized at the expense of reoxidizing the iron oxides in the slag by the gas atmosphere of the furnace. Finally it leads to an increase in the specific consumption of the reducing agent and decreases the rate of the reducing process. Provision of a reducing atmosphere over the melt by way of incomplete combustion of fuel will lead to an abrupt increase in the specific consumption of fuel. A similar result will be obtained when using a variant of decreasing an adverse effect of the furnace oxidizing atmosphere on the reducing process by increasing the thickness of a slag layer which will retard not only the oxidation of metal but also, to a greater extent, will retard the take-up of heat by the melt. Conditions of the heat transfer in a reverberatory furnace are of low effect principally due to a relatively small contact surface between the combustion flame jet and the melt mainly presented by the slag which even on boiling has a very low heat conduction. This makes it impossible to accelerate the process of melting and mainly due to this fact it features the low output, low heat efficiency and the high specific consumption of fuel. The reverberatory furnace does not allow the air used for combustion of fuel to be replaced with oxygen without disturbing stability of said furnace and without melting losses of metal because of which the heat efficiency of the process cannot be stepped up substantially. The present invention is essentially aimed at providing such a method of making steel in a liquid bath and an apparatus for effecting the same which will provide improvements in the technical and economical indices of making steel from any metal charge by using a direct (single-step) process. According to the present invention there is provided a continuous method of making liquid steel comprising: a) a steel melt and a starting slag melt which is in chemical equilibrium with the steel, are disposed in an annular shaped bath, and the starting slag melt is forced to constantly circulate through a closed circular circuit divided into an oxidizing and a reducing zone; b) crushed ore and flux materials together with a submersible fuel-oxygen combustion flame jet by means of which said ore and flux are melted, are blown into the circulating slag melt at an initial region of an oxidizing zone while sulphur is removed from the slag into a gaseous phase, and oxidised with oxygen; c) blowing a submersible fuel-oxygen combustion flame jet to superheat slag, into the circulating slag melt between middle and final sections of the oxidising zone, a dispersed reducing agent which reduces Fe 3 0 4 only to Fe0 being then also introduced into said slag; d) introducing a disperse reducing agent, sufficient for the reduction of Fe0 to iron, into the circulating superheated slag melt at an initial region of the reducing zone, said iron settling out of the slag and pass into the steel melt; e) loading steel scrap evenly into the steel melt under slag in the region of the middle section of the oxidizing zone and blowing an oxidizing gas through the metal melt surrounding said scrap to obtain rapid scrap melting, iron oxides passing into the slag being reduced; f) constantly removing the steel thus obtained from the melting process and delivering the steel to an off-furnace location for correction of its chemical composition to preset parameters; g) ejecting gaseous products of reducing iron formed in the reducing zone, into the oxidizing zone in the fuel-oxygen combustion flame jet submerged in the slag melt, together with oxygen or natural gas wherein said gaseous products are used both as a fuel and as a reducing agent for Fe 3 0 4 → FeO; and h) maintaining the mass of the slag melt equivalent to the starting mass, the remainder of said slag melt being continuously removed from the melting process at the end of the reducing zone. The present invention thus provides a method of making steel in a liquid bath using charge materials comprising iron-bearing raw materials and slag-forming fluxes. Said method contemplates the making of a low-carbon steel by interaction of iron oxides with a reducing agent, combustion of fuel in an oxygen-bearing gas to provide the process with heat and by introduction of additions injected in the low-carbon steel by an off-furnace method and intended for providing a preset chemical composition of the steel. According to the invention, a liquid bath is formed of a starting melt of the low-carbon steel and a starting melt of the steelmaking slag in chemical equilibrium therewith. Oxidizing and reducing zones are formed through which the starting melted slag is moved on the surface of the low-carbon steel through a closed circuit under the dynamic action of the combustion flame jets formed by burning fuel in an oxygen-bearing gas and submerged in the oxidizing zone into the melted slag into which powdered charge materials are injected with air to increase the concentration of iron oxides and to form a refined slag. At the expense of heat of the sumbersible fuel-oxygen flame jet said powdered charge materials are melted and the melt of slag is reheated in relation to a temperature of the low-carbon steel melt to provide heat for the process of reducing the iron from the melted slag. Further at the expense of oxygen contained in the air used for injection of powdered materials into the melted slag and oxygen of the fuel-oxygen combustion flame jet the sulfur contained in the melted slag is oxidized and removed into the gas phase, and the iron reducing agent is injected into the reheated slag melt delivered in the reducing zone. As a result the low-carbon steel is obtained in the form of drops which are settled out of the melted slag and supplement the starting melt of said low-carbon steel, the gaseous products of reduction are removed from the melted slag into the gas phase over the latter. The chemical composition of this melted slag is reduced to the starting chemical composition of the starting slag melt the starting mass of which is delivered into the oxidizing zone for carrying out a next processing cycle, while the excessive amount of the melted slag which is formed is removed from the further process and the low-carbon steel obtained is delivered for correcting its chemical composition to preset parameters by using the off-furnace method. The flame jet of fuel combustion in oxygen submerged in the melted slag and used in the proposed method for providing the steelmaking process with heat increases the heat utilization coefficient of this fuel approximately by 2.5-3.0 times in comparison with the method of the fuel combustion in the air of a furnace of the open-hearth type. This improvement in utilization of the fuel is attained as the submersible flame jet intensively mixes with the melted slag and increases the magnitude of the contact surface of division therebetween by tens and a hundred times in comparison with the contact surface between the melted slag and the flame jet of fuel burned in the air over the melted slag in an open-hearth furnace. The rate of the heat transfer to the melt increases in direct proportion with the increase of said contact surface. The heat exchange accelerated in this way makes it possible to abruptly intensify the metallurgical process and to minimize heat losses through discharged combustion products. These heat losses are further decreased due to replacement of the air consumed for combustion of fuel with oxygen which practically contains no nitrogen. Due to application of the submersible fuel-oxygen flame jet the steelmaking process is intensified and the specific consumption of fuel is reduced. Further, the accomplishment of the metallurgical process of steelmaking according to the proposed method sequentially in two zones instead of one common zone makes it possible to carry out the process of reducing the iron from a melted slag and to provide this process and the process of melting charge materials with heat under the most favourable conditions. If these processes are carried out in the common zone under semireducing-semioxidizing conditions, then they proceed at a a retarded rate with a substantially greater consumption of fuel and iron reducing agent, as the products of complete fuel combustion oxidize the iron reducing agent, thereby involving additional consumption of a great amount of fuel and reducing agent for this "parasitic" process. Thus, the process of steelmaking according to the proposed method in two processing zones instead of one common zone allows the specific consumption of fuel and reducing agent to be substantially cut down and the process of steelmaking to be intensified, all other factors being equal. In the proposed method of steelmaking the heat required for carrying out the reducing process is transferred in tne reducing zone by means of a melted slag provided with iron oxides and respectively reheated to a temperature of the steel to be obtained. As was described hereinbefore, the reheating is accomplished with a high efficiency in the reducing zone by means of a submersible combustion flame jet. This efficiency is maintained due to a repeated increase in the mass of the melted slag at the expense of its starting portion, sharp reduction of the required reheating temperature and, consequently, of heat losses through discharged products of fuel combustion in the submersible flame jet. For maintaining this highly efficient heat supply of the reducing zone the mass of the starting slag melt is directed from the reducing zone again in the oxidizing zone for a next processing cycle, thereby eliminating the consumption of heat for preparation of the starting slag melt. The use of a great mass of the starting slag melt employed as a heat generator and moved in a circulating mode through a closed processing circuit makes it possible to maintain at a maximum the low specific consumption of fuel and iron reducing agent by providing a two-zone steelmaking process. Also the low specific consumption of the fuel and the reducing agent decreases the environmental pollution with combustion products, carbon dioxide included, and improves the ecological environment. In order to provide maximum efficiency in using the melted slag as a heat carrier for the reducing zone, it is advantageous to form a starting slag melt in an amount proceeding from the ratio 2-15 kg of the melted slag per kg of iron reduced from the melted slag and forming low-carbon steel, and the reheating temperature of the melted slag before its delivery into the reducing cone may suitably be taken in a range of 50 to 300°C. All this makes it possible to provide a high coefficient of fuel utilization and a substantially high strength refractory lining which in places of contact with the melted slag is cooled. For providing a minimum specific consumption of the agent for reducing iron from its oxides, it is desirable that the reducing agent be introduced in the reducing zone by a dispersion method in an amount not less than it is stoichiometrically necessary for reduction of iron from its oxides. For providing a minimum specific consumption of fuel the gaseous products of iron reduction formed in the reducing zone may suitably be ejected in a submersible fuel-oxygen flame jet wherein said products are reburned in oxygen. For minimizing the specific consumption of the reducing agent and fuel, extending the service life of the melting chamber refractory lining and for accelerating the process, it is advantageous that the reducing agent in an amount sufficient for reduction of Fe 3 O 4 to FeO, be introduced by the dispersion method into the melted slag contained in the oxidizing zone. For providing accelerated processing of the steel scrap contained in the charge, the steel scrap may preferably be loaded into the low-carbon steel melt under the melted slag, and the surrounding melt of the low-carbon steel may suitably be blown through with streams of the oxidizing gas to melt the scrap and to transfer into the melted slag the formed iron oxides which thereafter will be reduced until a low-carbon steel is obtained. For minimizing heat losses and decreasing the specific consumption of fuel in the process of scrap melting, oxygen may advantageously be used as an oxidizing gas. For minimizing the formation of red fume in the process of scrap melting and for reducing iron losses through said red fume, as well as for cutting down the expenditure for gas cleaning, the products of complete combustion of the fuel-oxygen flame jet may suitably be used as an oxidizing gas, and it is desirable that in the melted slat flowing over the combustion flame jets the concentration of Fe 3 O 4 be maintained at a level sufficient for its conversion into FeO, and for conversion of formed CO and H 2 into CO 2 and H 2 O. For providing a more efficient utilization of the fuel used for melting the scap by a fuel-oxygen flame jet, the required concentration of Fe 3 O 4 in the melted slag may advantageously be maintained by way of introducing an appropriate amount of iron ore material into the melted slag. For providing a more efficient utilization of the fuel used for melting the scrap at the expense of blowing through the steel melt with the fuel-oxygen flame jet with a small fraction of tne iron ore material in the charge, a required concentration of Fe 3 O 4 in the melted slag is maintained by blowing it through with oxygen. For increasing the value of the slag incidentally formed in the process of steelmaking, it is advantageous to select such a ratio of the powdered step-forming flux materials blown in the melted slag which will ensure its chemical composition at the end of the reducing zone to be closer to the chemical composition of portland cement. For cheapening the production of alloy steels, the ore raw materials comprising oxides of appropriate alloying elements are introduced into the melted slag in the oxidizing zone. According to a further aspect of the present invention there is provided an apparatus for effecting the method of the present invention, said apparatus comprising a circular melting chamber with gas-separating walls tuyeres for introducing various reagents into the liquid bath and creating circulation of the slag melt, devices for tapping metal and slag from the melting chamber and removing gas-forming products therefrom characterized in that: a) the circular melting chamber is divided by two gas-separating walls into two processing zones: an oxidizing zone and a reducing zone, the oxidizing zone comprising initial and final sections between which a middle section is located; b) at the initial section of the oxidizing zone tuyeres for blowing powdered ore and flux materials only, into the slag melt, and tuyeres with horizontal nozzles for blowing a fuel-oxygen flame jet into said melt only, are disposed; c) a scrap-loading opening is disposed in the roof of the middle section of the oxidising zone, and scrap-melting oxygen and fuel-oxygen tuyeres are disposed around said opening; d) tuyeres with vertical nozzles for blowing the submersible fuel-oxygen combustion flame jet and a dispersed reducing agent into the slag melt only are provided between the middle and final sections of the oxidizing zone; e) tuyeres for dispersed introduction of a reducing agent into the slag melt only, are provided in the initial section of the reducing zone; f) a circular melting chamber is provided with a gas transfer ejector-type duct, connecting the gas space of the reducing zone with the fuel-oxygen tuyeres in the oxidizing zone and the tuyeres for introducing the reducing agent provided nearby; h) the walls of the circular melting chamber and gas separating partitions in the place of contact with a slag melt are provided with metal panels which are cooled by a damp water steam from the outside; i) an opening for tapping of waste slag being provided at the end of the reducing zone, and in the bottom section of the reducing zone an opening for tapping steel is provided. This further apsect of the present invention thus allows the steelmaking process to be organized more efficiently, as the melting chamber is divided along the circular circuit into a plurality of processing sections through which the melted slag is continuously moved, each part of said melted slag passing in succession through these sections and being subjected to appropriate operations. So, after entering the oxidising zone the melted slag passes through a section accommodating tuyeres for injecting powdered charge materials into said melted slag and tuyeres for combustion of fuel in oxygen by using ... a sumbersible combustion flame jet. Then the melted slag is delivered to a section provided with tuyeres for reheating the melted slag by the sumbersible fuel-oxygen flame jet. Due to the nozzles installed in the fuel-oxygen tuyeres and oriented in the direction of flow of the melted slag the latter is dynamically acted upon by the combustion flame jets and is continuously moved through the closed circular melting chamber. After entering the reducing zone the melted slag passes through a section provided with tuyeres for injecting the iron reducing agent in said melted slag, then this melted slag flows through a section for settling out reduced drops of the low-carbon steel. At the end of the reducing zone and the section for settling out the reduced drops the mass of a fresh slag formed during the processing cycle is removed from the melting chamber through the tapping device. Due to the closed circular melting chamber the mass of the starting slag is retained in the process and enters the oxidizing zone for taking part in a new processing cycle. Thus, the closed circular melting chamber allows the starting melted slag to be repeatedly used which provides substantial savings in materials and energy for its preparation. An embodiment of an apparatus with the gas space hermetically separated over the melted slag by transverse partitions into oxidizing and reducing zones of the melting chamber made in the form of a closed ring provided in the oxidising zone with tuyeres for injecting powdered charge materials and a fuel-oxygen flame jet into the melt, and also provided in the reducing zone with tuyeres for introducing an iron reducing agent allows the method of the present invention to be effected with the maximum efficiency. The fuel-oxygen tuyeres may advantageously be disposed vertically and their lower side surface may be provided with injection nozzles the orifices of which are oriented in the direction of movement of the melted slag. This makes it possible to use the submersible combustion flame jet with a maximum efficiency for heating the melted slag and for its movement through the circular melting chamber. The apparatus may suitably be provided in the middle section of the oxidizing zone with a scrap-loading opening and with scrap-melting oxygen or fuel-oxygen tuyeres arrayed on both sides of said scrap-loading opening. This makes it possible to organize a highly efficient loading and melting of steel scrap. The tuyeres for delivery of a reducing agent in the melted slag and the fuel-oxygen tuyeres for reheating the melt may be disposed to advantage at the beginning (when looking in the direction of the slag melt movement) of the second portion of the oxidizing zone. This makes it possible to organize a highly efficient reheating of the melted slag with a preliminary reduction of iron before the delivery of the melted slag in the reducing zone. It is desirable that the apparatus be provided with a means for introducing the liquid iron in the melted slag and that this means be disposed at the initial (when looking in the direction of the melted slag movement) section of the reducing zone followed by a section for settling out the reduced iron. This allows the liquid iron to be most efficiently used as an iron reducing agent. It is expedient to provide the reducing zone with a gas pressure relief valve. Such a solution will prevent any emergency situation in case of an abrupt rise of gas pressure in the reducing zone. In order to make the most use of potential heat energy of gaseous products of the iron reduction, the apparatus may suitably be provided with an ejector-type gas transfer duct for connecting the gas space of the reducing zone with the tuyeres for injecting oxygen and fuel in the melted slag and for burning the fuel therein. The present invention will now be further described, by way of example, with reference to the accompanying drawings, in which:- Fig. 1 is a schematic plan view of one embodiment of apparatus constructed according to the present invention; Fig. 2 is a transverse sectional view along line II-II in Fig. 1; and Fig. 3 is a linear representation of part of the annular bath of Figs. 1 and 2. The steelmaking process according to the present invention proceeds in the following way. Initially a liquid bath is formed of a starting melt of the low-carbon steel and a starting steel-melting slag which is in chemical equilibrium therewith, and which is continuously moved in a circulating mode through a closed circuit separated into oxidizing and reducing zones. The following processing operations are carried out in succession in the oxidizing zone. A powdered charge and a fuel-oxygen flame jet are introduced with air in the starting slag melt for melting this charge and for removing at the same time sulfur from the slag at the expense of oxygen and air. Before delivery into the reducing zone, the melted slag is reheated by means of a submersible fuel-oxygen combustion flame jet for providing heat for the process of reducing the iron from FeO which under definite conditions may be followed by an additional purification of the melted slag from sulfur. After delivery of the melted slag from the oxidizing zone into the reducing zone, the following operations are carried out. The reducing agent is introduced into the melted slag. The reducing agent may be gaseous (for example, natural gas or hydrogen), or liquid (for example, fuel oil), or powdered (for example, carbon powder) and be blown or injected into a volume of the slag flow. Combined use of these reducing agents is possible. The amount of a reducing agent should not be less than it is stoichometrically necessary for reduction of iron from FeO to a preset residual concentration in the slag of the latter and which is stipulated in particular by the process of dephosphorization. After introduction of the reducing agent into the melted slag the latter is moved through a quiet section of metal separation from the final melted slag by way of settling out drops of metal into the bottom portion comprising a metallic melt of the low-carbon steel. After settling of the reduced metal is completed the mass of the melted slag at the end of the reducing zone is divided into two portions: the initial starting portion (the mass of this slag flow remains constant) is directed to the oxidizing zone for use in a next processing cycle and the dump portion of the melted slag is removed from the further processing cycle. The obtained low-carbon steel is removed from the process and directed for off-furnace correction of its chemical composition. For optimization of the obtained technical effectiveness, the method of the present invention can be modified by a plurality of additional specific features. Firstly, the optimum reheating temperature of the common slag flow comprising the starting slag mixed with the ore -flux melt is maintained before its delivery into the reducing zone at a level higher than the temperature of the metallic bath in a range of 50 to 300°C and resulting on for example, a temperature up to 1650-1900°C. In this case the optimum mass of the starting melted slag flowing through the section for iron reduction from FeO, is maintained in a range of 2 to 15 kg per kg of the reduced iron. These quantitative parameters which are intimately interrelated are established on the base of analysis and calculations of heat balances of the steelmaking process according to the proposed technological scheme. In this case a maximum suitable temperature for reheating the melted slag was determined as 1900°C. Any further increase of this temperature would sharply impair the strength of the melting plant refractory lining in places of contact with the melted slag, considerably decrease the thermal efficiency of the melting plant and would substantially increase the specific consumption of fuel. Secondly, taking into account the possibility of regulating the chemical composition of the melted slag according to the proposed technological scheme, it is advantageous to maintain the optimum chemical composition of a regenerative starting melted slag close to typical steel-melting slags having an increased basicity (2.5-3.5) with a content of CaO (55-60%) and reduced concentration of FeO (6-8%) and MgO (2-4%). This slag possesses not only good refining properties but by its composition is fit for use as an almost prepared raw material for the production of portland cement. Thirdly, a reducing agent is blown in the melted slag comprising iron oxides introduced together with the charge, in an amount not less than it is stoichiometrically necessary for reduction of said iron oxides only to FeO. Fourthly, for accelerating the process of melting the steel scrap used in the charge a method of oxidizing the iron with a gaseous oxygen is employed. To this end, the scrap is loaded by uniform portions into a metallic bath of the low-carbon steel melt under the slag and oxygen jets blow through the steel in the zone of scrap loading. As a result, the liquid metal, mainly the iron is oxidized and the temperature of the metallic bath is respectively increased. Due to the high heat conductivity of this bath and the bubbling with oxygen jets, the heat is rapidly transferred to the scrap which melts at an accelerated rate. As the calculations imply, for complete melting of the scrap, it is necessary to oxidize, mainly to FeO, 1/3 of the iron from the mass of the iron scrap. If with such blowing, it becomes necessary to reduce evaooration of the iron, then a fuel-oxygen flame jet is blown through the metallic bath. When the fuel-oxygen flame jets are blown through the metallic bath the products of complete combustion (CO 2 and H 2 O) oxidize the metal and dissociate with CO and H 2 . In order to additionally utilize the heat and chemical energy of said products of complete combustion the concentration of Fe 3 O 4 in the melted slag (in the vicinity of slag melting) may be maintained in an amount that will be sufficient for oxidizing (approximately by 95-99%) the bubbles with CO and H 2 to CO 2 and H 2 O when they emerge from the slag. As calculations imply, the mass of Fe 3 O 4 in the slag interacting with CO and H 2 should exceed, at least by 7.5 times, the mass of oxygen in the submersible combustion flame jet by means of which the scrap is melted. Such a concentration of Fe 3 O 4 is attained automatically when the steel is melted from a charge which in addition to the scrap contains an ore concentrate in an amount sufficient for this purpose (for example, when the iron is converted from the scrap into the steel in an amount not exceeding 20-25%). If the steel is melted from the scrap alone, then in order to maintain a required concentration of Fe 3 O 4 , use is made of a method which oxygen and oxygen alone, is blown into the melted slag in the vicinity of scrap-melting fuel-oxygen tuyeres, for example, by delivery of oxygen through an upper row of oxygen nozzles arranged in the same tuyeres. At the expense of these oxygen jets the ferrous oxide (FeO) will be oxidized to Fe 3 O 4 producing a substantial amount of heat in the slag. As calculations imply, the amount of oxygen for this purpose approximately comprises at least half (50%) the amount of oxygen consumed in the sumbersible combustion flame jet used for melting the scrap. Practically, tne optimum concentration of Fe 3 O 4 in the melted slag is maintained on the basis of a continuous express-analysis of gases evolved from the melt in the zone of scrap melting. The iron oxides formed in the process of slag blowing or when the metallic bath is blown through both with oxygen and the fuel-oxygen flame jet, are passed into the melted slag from which the iron is extracted in the reducing zone and passed into the low-carbon steel by means of the methods described hereinbefore. The calculations imply that a method of accelerated conversion of scrap into steel requires, in comparison with the known methods, a minimum total consumption of energy and makes it possible to obtain the maximum yield of iron from the scrap. The ratio of scrap-to-one concentrate in the charge may be of any value (from zero to 100%). The same technological scheme may be used for melting scrap containing alloying elements which in this case are retained in a substantial amount in the obtained steel. A method of direct blowing of scrap with oxygen jets or fuel-oxygen flame jets may also be used to advantage. Fifthly, when melting the steel which should contain alloying elements, the latter in the form of hard or liquid ferroalloys are added in a required amount into the low-carbon steel tapped into a steel-teeming ladle. An apppropriate amount of carbon-bearing material is added into said low-carbon steel to provide a required concentration of carbon in the steel. Sixthly, when melting an alloy steel, especially a low-alloy steel, the alloying elements may be added therein in the process of melting by way of reducing said alloying elements according to the technological scheme described hereinbefore and used for the reduction of iron. To this end, an appropriate amount of ore or concentrate comprising oxides of elements required for steel alloying are blown together with the iron ore concentrate in the starting slag flow. According to the same technological scheme the proposed apparatus may be used to advantage for melting ferroalloys, raising, if required, the upper temperature level of the metallic bath (for example, to 1850°C) and of the melted slag (for example, to 2000°C). Seventhly, if the liquid iron is used as a reducing agent, then it is introduced into a volume of the melted slag in the form of droplets. Eighthly, a combustible gas formed in the process of reduction may be sucked by means of a special ejecting device from the reducing gas space and directed into fuel-oxygen tuyeres of the submersible flame jet in the oxidizing zone wherein it is used as a fuel or a reducing agent. A comparative analysis of a prototype makes it possible to conclude that the method of steelmaking according to the present invention is based on a radically new technological solution of the problem concerning the delivery of heat in the reaction zone of iron reduction. This solution resides in imparting a new additional function to the melted slag, i.e. the function of a sole heat carrier for said zone. This function of the slag is crested by way of a new combination of methods: artificial increase in the mass of the melted slag and its reheating in relation to the temperature of the obtained steel. In this case the mass of the melted slag is increased at the expense of mixing an ore-flux melt with a starting melted slag whose chemical composition corresponds to the chemical composition of the final slag when the steel is produced by the given method, and which are in chemical equilibrium. In the given technological scheme the starting melted slag is constantly used in a recirculating mode. Reheating of the melted slag (flow) is accomplished prior to the process of iron reduction by means of a submersible fuel-oxygen flame jet and a combustible gas ejected from the reducing zone may be used as an additional fuel. Due to a hermetic separation of the oxidizing zone gas space of the circular melting chamber, wherein the melted slag is reheated, from the gas space of the reducing zone accommodating the reaction zone of reducing iron from FeO, the latter is not subjected to oxidizing action of the combustion products which steDs up the efficiency of the process. In addition, a radically novel feature of the proposed technological scheme is a new combination of methods making it possible to produce steel with a high efficiency from the iron scrap in combination with any amount of the ore component of the charge (from 0 to 100%). This combination includes an accelerated melting of the scrap at the expense of intentive oxidation of iron by a gaseous oxidizing agent (O 2 or CO 2 and H 2 O) and a subsequent reduction of iron oxides according to the technological scheme described hereinbefore. This makes it possible to use the proposed method for cokeless single-stage direct production of a high quality steel from any metal charge with high output, low specific consumption of fuel, lesser pollution of the atmosphere and also with production of the slag in the form of a semiproduct for portland cement, and in the long run it allows for a specific consumption of fuel and hence the pollution of the atmosphere by combustion products to be reduced by 1.5-2.5 times. The proposed method of steelmaking is effected with a maximum efficiency in an apparatus being essentially a melting chamber 1 (Fig. 1) made in the form of a hollow contour of any configuration, preferably, in the form of a circle. The melting chamber 1 is made up of a circular external all 2 and a circular internal wall 3, a bottom 4 (Fig. 2) and a roof 5. In cross-section the melting chamber 1 may preferably be of a rectangular shape. The circular melting chamber 1 comprises two processing zones: an oxidizing zone 6 (Fig. 3) and a reducing zone 7. A gas space 8 disposed over a melted slag 9 in the oxidizing zone 6 is hermetically separated from a gas space 10 disposed over the melted slag 9 in the reducing zone 7 by transverse partitions 11. The walls 2 and 3, and the partitions 11 in the place of contact with the melted slag 9 are provided from the outside with cooling means, for example, panels 12. Wet water vapor is preferably used as a cooling agent. The walls 2 and 3 disposed over the melted slag 9 (nonfoamed) may be inclined in the direction away from an axial circular plane III - III, which, with the constant height of the melting chamber 1, will increase the volume of the gas spaces 3 and 10, thus preventing them from overfilling with the foamed melted slag 9. The melting chamber 1 in its oxidizing zone 6 internally accommodates vertical submersible fuel-oxygen tuyeres 13 (Fig. 1) the lower side surface of which are provided with blowing nozzles having orifices 14 (Fig. 3) which are oriented in the direction (along arrow A) of movement of the melted slag 9. The tuyeres 13 are arranged in two groups: one group is in the first half of the zone 6 when looking in the direction (along arrow A) of movement of the melted slag 9, and the other group is in the second half of said zone. The same zone 6 internally accommodates gas-powder tuyeres 15 (Fig. 1) designed for blowing powdered charge materials into the melted slag 9 through a pipeline 16 by means of a pneumatic conveying unit 17. The number of such units is determined by specific operating conditions and capacity of said units. Vertical submersible blowing tuyeres 18 disposed in the same oxidizing zone 6 right after the tuyeres 13 and 15 when looking in the direction (along arrow A) of movement of the melted slag are designed for blowing a powdered reducing agent in the melted slag 9 for reducing Fe 3 O 4 to FeO. The powdered reducing agent is delivered into the tuyeres 18 through a pipeline 20 by means of a pneumatic conveying unit 19. When use is made of a gaseous or a liquid reducing agent, it is introduced in the tuyeres 18 through a pipeline 21. The total number of the tuyeres 13, 15 and 18 in the apparatus, their number in one row arranged across the circular melting chamber 1 and the number of these rows, depend on dimensions of this melting chamber, output of the apparatus and on the specific modes of the steel making process. Alternately the tuyeres 15 and 18 may be arranged in one row with the tuyeres 13. In the middle portion of the oxidizing zone 6 the roof 5 is provided with a scrap-loading opening 22 designed for pouring steel melts and melted slag for forming an initial liquid bath and for loading a steel scrap 22 1 if this scrap is a component part of iron-bearing materials. Besides, this opening 22 may be used for loading charge materials in the form of lumps. Movable scrap-melting oxygen and/or fuel-oxygen tuyeres 23 are arranged around the scrap-loading opening 22. These tuyeres 23 as well as the tuyeres 13, 15 and 18, are provided with a mechanism (not shown on the Drawing) for their vertical movement. In addition, the tuyeres 23 may be provided with a swinging mechanism 24 (Fig. 2) by means of which said tuyeres 23 may accomplish a pendulum motion at a preset angle α (Fig. 3) from the vertical. All the tuyeres are cooled with water or wet vapour. The apparatus is provided with a gas transfer ejector-Type duct 25 (Fig. 3) connecting the gas space 10 of the reducing zone 7 with the fuel-oxygen tuyeres 13 and 23. This duct 25 is designed for conveying the formed gaseous products of the iron reduction in the direction of arrow B into the tuyeres 13 and 23, wherein said products are mixed with oxygen and burned in the submersible combustion flame jet. The internal space of the melting chamber 1 in its reducing zone 7 on the side which receives the melted slag 9 from the oxidizing zone 6, accommodates tuyeres 26 for blowing the iron reducing agent into the melted slag 9. For the case using a powdered reducing agent the tuyeres 26 are connected with the pipeline 20 through which the reducing agent is delivered from the pneumatic conveying unit 19. The number of these units 19 and tuyeres 26, and the specific arrangement of the latter on a given section of the zone 7 are determined by specific overall dimensions of the steelmaking apparatus, its output and technological parameters. If a gaseous or a liquid reducing agent is used, then it is introduced in the tuyeres 26 through the pipeline 21. When liquid iron is used as a reducing agent the section for arrangement of the tuyeres 26 is provided with a means comprising a funnel 27 with a pulverizer for introducing the iron pulverized into droplets in the melted slag 9. The steelmaking apparatus is provided with an opening 28 used for tapping an obtained steel 29, provided with a tapping device insuring a continuous steel tapping and disposed in the reducing zone 7, preferably in the middle portion thereof. An opening 30 for tapping the mass of the melted slag 9 (dump slag) which is formed in the process of making the steel 29 is disposed at the end of the zone 7 when looking along the arrow A in the direction of movement of the melted slag 9. The apparatus is provided with a gas outlet duct 31 arranged in the oxidizing zone 6 and designed as an outlet for combustion products in the direction shown by arrow D (Fig. 3). This duct may be combined with the opening 23 and a unit (not shown on the Drawing) for heating the scrap using outgoing gases, as well as with a recuperator (not shown on the Drawing) for heating oxygen and fuel by means of said outgoing gases. To provide safety in operation of the apparatus the reducing zone 7 is provided with a pressure-relief valve 32 allowing the pressure of gas in this zone to be automatically maintained at a level not exceeding the preset value. The steelmaking process according to the proposed method proceeds as follows. At the beginning a liquid bath is formed in the circular melting chamber 1 by filling this chamber with a low-carbon steel prepared in another steelmaking apparatus. Then, the melted slag 9, for example, a blast-furnace slag, is poured onto the steel melt and the fuel-oxygen tuyeres 13 are submerged into said blast-furnace slag, with the delivery of fuel and oxygen into said tuyeres 13 preliminarily switched on. After heating of the melted slag to an optimum working temperature of 1600-1750°C, its chemical composition and the mass are corrected to suit the preset parameters for obtaining the composition of the starting slag. This correction is carried out by way of blowing a required amount of appropriate powdered charge materials into the melted slag 9 by means of the pneumatic conveying unit 17 and the tuyeres 15. In this case the tuyere 13 is used for providing the melted slag with an appropriate amount of heat sufficient for melting the material introduced into the melted slag. After the liquid bath has been formed the powdered charge materials required for obtaining the steel are blown into the melted slag 9 by means of the gas-powder tuyeres 15 and the pneumatic conveying unit 17. By means of the fuel-oxygen tuyeres 13 arranged in the first half of the zone 6 these materials are melted by way of maintaining an optimum temperature of the melted slag 9 in a range of 1600-1650°C, and conditions are provided for the flow of said melted slag 9 towards the zone where the scrap 22 1 . is melted. A next portion of the scrap 22 1 loaded on the hearth 4 through the opening 22 with the aid of the scrap-loading mechanism, is subjected to intensive melting due to switching the scrap-melting tuyeres 23 and, if required, their swinging mechanisms 24, into operation. Due to a maximum approach of nozzles of the tuyeres 23 to the scrap surface or to the metallic bath the scrap 22 1 is melted and simultaneously the iron is intensively oxidized from the surface thereof or from the melt of the low-carbon steel 29, and in the form of FeO it is passed into the slag. In this case, impurities of the molten metal are subjected to deep oxidation as a result of which the metal scrap is transformed into the low-carbon steel. An intensive process takes place in the oxidizing zone 6 of purifying the melted slag 9 from sulfur which is oxidized by the oxygen of the combustion flame jet, air from the pneumatic conveying unit and jets of the scrap oxidizing agent, and is removed from the apparatus (along arrow D) in the form of a sulfurous gas together with the combustion products. Such a process of melted slag desulfurization permits the melting of a low-sulfur steel. Then, the reducing agent is delivered to the tuyeres 18 and blown by means of the tuyeres 18, into the melted slag 9 for a preliminary reduction (Fe 3 O 4 → FeO). If use is made of a powdered reducing agent, then it is delivered to the tuyeres 18 by means of the pneumatic conveying unit 19. If use is made of a gaseous or a liquid reducing agent, then it is delivered into the tuyeres 15 from the pipeline 21. When the melted slag 9 comprising the iron oxides only in the form of Fe0, is delivered to the section accommodating the second group of the fuel-oxygen tuyeres 13, said melted slag 9 is reheated by means of the latter to a temperature of 1650-1900°C and moved into the reducing zone 7. When the melted slag enters this zone the tuyeres 26 are used for blowing the reducing agent into said melted slag. If the reducing agent is in the form of powder, then it is delivered into the tuyeres 26 with the aid of the pneumatic conveying unit 19. If use is made on a a gaseous or liquid reducing agent, then it is delivered into the tuyeres 26 from the pipeline 21. If liquid iron is used as a reducing agent, said liquid iron is poured (along arrow C) through the funnel 27 and the pulverizer onto the melted slag. The liquid iron pulverized into droplets settles down through the melted slag and reduces the iron. In this case, a definite balance is maintained between the mass of the iron and the mass of the melted slag interacting therewith, and said balance makes it possible to obtain a preset refining of the iron to a low-carbon steel and to simultaneously reduce the preset amount of iron from the melted slag 9. In the process of settling the steel droplets are purified from phosphorus and sulfur, and are admitted into the melt of the low-carbon steel. The metal from the melted scrap is also admitted into the melt of the low-carbon steel. When these metallic melts are mixed, it should be taken into account that the metal obtained from the scrap both by the direct melting and by way of reduction from its oxidized portion will be perfectly pure in relation to the content of impurities. When use is made of a liquid iron and it is necessary to obtain a medium-carbon steel and a high-carbon steel, the iron is refined proceeding from the necessity of obtaining therein a residual carbon which upon mixing with the remaining low-carbon metal will make it possible to obtain a preset concentration of carbon in the steel. The chemical composition of the stell obtained is finally corrected after said steel has been tapped through the tap opening 28, by using the off-furnace method, for example, in a ladle. The metal may also be carburized in the steelmaking apparatus by way of blowing a carbon-bearing powder into the metal with the aid of the tuyeres 26 submerged in the metal. After passing through the settling zone the melted slag 9 freed from the steel droplets, is divided into a dump portion which is tapped through the tap opening 30 and into a starting portion remaining in the apparatus and directed into the oxidizing zone 6 for using in the next steelmaking cycle which proceeds in a continuous recirculating regime. Example 1:- Steel was produced from an iron-bearing raw material which comprised only pure steel scrap that contained: C=0.3%; Si=0.15%; Mn=0.3%; P=0.045%; S=0.045%. In the front portion of the oxidizing zone appropriate powdered slag-forming flux materials (lime, bauxite,iron scale, etc.) ) were blown into the starting slag melt and a fresh portion of the melted slag (refinery slag) was formed with the same composition as the starting slag melt (CaO-60%; SiO 2 =20%, Al 2 O 3 =8.0%; MgO=3.0 %; FeO = 7.0%; MnO=1.0%; basicity 3.0). The amount of the refinery slag was equal to 250 kg/t scrap. The amount of the starting slag melt was maintained at a level of 7.5 kg/kg of the reduced iron which corresponded to 2430 kg per ton of the scrap to be melted. By blowing the melted slag into this zone with the help of the fuel-oxygen combustion flame jet (with α=1.0-1.1) the melt was provided with the heat required for melting the slag-forming materials blown into said melt and for maintaining the temperature of the melted slag at a level of 1600-1650°C. A combustible gas from the reducing zone was used as a fuel and was ejected by oxygen into the fuel-oxygen tuyeres by means of ejector nozzles. The amount of this gas comprised approximately 38% of the total mass of the gas formed in the process of reduction and made up of CO, H 2 , CO 2 , H 2 O and nitrogen. The amount of oxygen consumed for ejection and combustion of said combustible gas comprised 30.0 m 3 /t. A portion of the evolved heat was consumed for heating the air of the pneumatic conveying units and for compensation of heat losses through the housing of the apparatus in this zone. At the expense of free oxygen in the submersible combustion flame jet (α > 1.0, but < 1.1) the melted slag was vigorously desulfurized by way of oxidizing sulfur to SO 2 and removed from the melt together with the products of complete combustion. The residual concentration of sulfur in the melted slag was not over 0.01 %. In the oxidizing zone the scrap was loaded through the scrap-loading opening and submerged in the steel bath through which oxygen was blown with a specific consumption of 68.5 m 3 /t scrap. At the expense of oxidizing iron of the low-carbon steel melt (324.5 kg per ton scrap) an amount of heat was evolved therefrom due to which the scrap was rapidly melted and heated to a temperature of 1600-1630°C. As a result, due to a vigorous bubbling contact with the melted slag the melted metal was purified of sulfur and phosphorus, and at the expense of oxygen the melted metal was purified of carbon silicon and manganese. Enriched by iron oxides, mainly FeO formed by oxidation of the low-carbon steel melt due to oxygen being blown therethrough, and a definite amount of Fe 3 0 4 which contained about 60 kg of Fe per ton of the scrap, the melted slag was moved toward the end of the oxidizing zone wherein it as subjected to a preliminary reduction and reheating. To this end, said melted slag was subjected to the combustion flame jet with a definite lack of oxygen (α=0.96-0.98). The remaining portion (62%) of the combustible gas from the reducing zone was used as fuel. The amount of oxygen for combustion of said combustible gas comprised 43.0 m 3 per ton scrap. As a result, after passing through this section of treatment the melted slag was freed of oxide Fe 3 O 4 (only oxides FeO remained in the melted slag) and was reheated to a temperature of 1735°C (by 135°C). After such treatment the melted slag with an increased content of FeO (its concentration was raised up from 7% to 22.5% at the expense of the scrap melting) was admitted into the initial section of the reducing zone wherein a milled coal was blown into said melted slag with the help of nitrogen (1 ton of scrap required 68 kg of coal which contained: C=90%; H 2 =4%; and S=0.4%; humidity < 2%; ash content = 10%). An amount of 324.5 kg of iron per ton of the scrap which was oxidized in the process of the scrap melting was reduced from the melted slag and returned into the refined melt of the low-carbon steel. The metal yield with the account of the iron of the slag-forming materials (bauxite, scale) comprised 98%. The chemical composition (%) of the obtained metal: C=0.05; Si=traces; Mn=0.05; P=0.004; S=0.004. Upon settling of the reduced iron from the slag flow into the melt of the low-carbon steel at the settling section, the melted slag (its chemical composition complied with the chemical composition of the starting slag melt) was divided into two portions: one portion with a mass of 260 kg/t scrap (250 kg of slag-forming materials + 10 kg of impurities from the scrap- SiO 2 ; Mn); P 2 O 5 ; S and others) was removed from the apparatus as a dump slag utilized as a clinker for portland cement, while the remaining mass (2430 kg/t scrap) of the melted slag flowed into the oxidizing zone for the next steelmaking cycle. The low-carbon steel of the composition described hereinbefore was tapped at a temperature of 1620°C into a steel-teeming ladle wherein it was corrected in relation to carbon and other elements by introducing required additions and deoxidizing agents into said low-carbon steel. In the given example the production of 1 ton of high-quality steel consumed: 1 t of scrap, 250 kg of slag-forming materials (lime, bauxite, scale), 68 kg of power-generating coal and 137 m 3 of oxygen with a purity of 95%. The total power consumption for the steelmaking process (with account of power consumption for obtaining oxygen) comprised in the given example 92.9 kg of equivalent fuel which in comparison with a conventional electric steelmaking process (with account of the fuel consumption at thermal power stations, losses in the electricity supply network and transformers), consumption of power for producing the iron as a component of the charge (10%) was approximately 2.5-3 times smaller. Example 2:- Liquid low-carbon steel was produced from an iron-ore concentrate containing: Fe total =67.7%; Fe 2 O 5 =65.46%; FeO=28.17%; SiO 2 =5.12%; S=0.096%; P 2 O 5 =0.029%. In the front portion of the oxidizing zone a powdered ore concentrate (1508 kg per ton of lime and 114 kg of bauxite per ton of steel) was blown into the starting slag melt at a temperature of 1600°C. The heat required for melting these material, for heating the air by means of which these materials were blown in, to a melting temperature, for carrying out the reaction Fe 2 O 3 → Fe 3 O 4 , and for compensation of 50% of heat losses through the housing of the apparatus in the oxidizing zone, was obtained at the expense of a combustion flame jet submerged into the melted slag. Used as fuel were a natural gas (76.4 m 3 /t steel) and a gas from the reducing zone (36.2% total mass), which were ejected into the fuel-oxygen tuyeres by means of the natural gas and oxygen (222.0 m 3 ). Due to a developed contact surface between the compressed air by means of which the charge was blown in and the combustion products and the melted slag, the latter was intensively desulfurized (up to 0.01 %). The method slag at t=1600°C was admitted into the section of the oxidizing zone wherein the reduction reaction Fe 3 O 4 → FeO was accomplished at the expense of the natural gas (47.2 m 3 /t steel) and the melted slag was reheated (by 77°C). To this end, 63.8% of the combustible gas from the reducing zone and 136 m 3 of the natural gas were burned in said melted slag with a consumption of 390 m 3 of oxygen with a purity of 95%. As for reducing the iron from FeO, use was made of coal as in the first example, but with a high content of sulfur (1.7%), and then the ratio of the starting slag melt was selected at a maximum (15 kg/kg reduced iron) which comprised 15,315 kg/t steel. When the melted slag entered the reducing zone the slag temperature was equal to 1770°C (reheated by 70°C). The concentration of FeO in the slag was equal to 15%. Carbon powder (221.1 kg per ton steel) was blown into said melted slag by means of nitrogen for reduction of the iron. Due to this process and during the further movement of the melted slag accompanied by settling of liquid steel droplets into the metallic bath, the temperature of the melted slag was decreased to 1600°C (reheat -0°C) end the concentration of FeO was reduced to 7%. The dump portion of the melted slag (582 kg/t steel) the chemical composition of which was the same as of the starting portion of the slag, and the same as in the first example, i.e. complied with the chemical composition of cement clinker, and was removed from the apparatus, while the remaining portion was delivered into the oxidizing zone for use in the next steel-making cycle. The production of 1 ton of the liquid steel (C=0.05%; Si=traces; Mn=0.05%; P=0.002%; S=0.0045%) consumed: 221.1 kg of coal; 258.7 m 3 of natural gas and 612 m 3 of oxygen with a purity of 95%. The consumption of power given in this example for production of steel only from the iron-ore concentrate (with account of the power consumption for obtaining oxygen and cement clinker) in comparison with the traditional method (agglomeration, coke-chemical, blast-furnace, converter process without scrap but with agglomerate) turned out to be by 40-50% smaller. A substantial additional advantage of the proposed method resides in the obtaining of steel of perfect purity in relation to phosphorus and sulfur. By conventional methods this level of purity is attained by additional methods for special treatment of iron and steel. Example 3:- The same steel as used in the preceding examples in which 50% of its mass was obtained from the scrap and the other half was obtained from the iron-ore concentrate of the same composition as in Example 2, was melted. In the front portion of the oxidizing zone a powdered ore concentrate (754 kg per ton steel) and slag-forming fluxes (lime, bauxite) in amount of 490 kg per ton steel were blown into the starting slag melt which had a temperature of 1600°C. Simultaneously the melted slag was supplied with beat from a submersible combustion flame jet in which 38.2 m 3 of natural gas and 34% of combustible gas ejected from the reducing zone were burned (per ton of steel) 121.25 m 3 of oxygen with a purity of 95% being consumed for burning said gases. At the same time the loaded scrap was intensively melted in the oxidizing zone by way of blowing oxygen into the metallic bath (34.25 m 3 per ton steel). Enriched by iron oxides both at the expense of the said blowing of oxygen, and at the expense of the iron-ore concentrate, the melted slag after passing the scrap-melting zone entered the section for reducing Fe 3 O 4 to FeO and for reheating the melted slag. To this end, the melted slag was subjected to the combustion flame jet with α =0.96-0.98. The natural gas (23.6 m 3 /t steel) and the combustible gas from the reducing zone (66%) were used as a fuel. Oxygen was consumed In this case in an amount of 253 m 3 per ton steel. As in Example 2, use was made of a high-sulfur coal for reducing iron (FeO→Fe) and therefore a high ratio of the starting slag melt (15 kg/t reduced iron) which in the given example comprised 9,933 kg/t steel, was used. Taking account of the dump slag which comprises 420 kg the specific mass of the melted slag was equal to 10,350 kg/t steel. To completely provide the reducing zone with heat, the melted slag was reheated by 75°C (to 1675°C). Milled coal in an amount of 144.5 kg per ton of steel was blown into the melted slag when it entered this zone, with the help of nitrogen At the end of the settling section droplets of the reduced iron (approximately 662 kg/t steel) settled in the melt of the low-carbon steel and the melted slag acquired the chemical composition which complied with the chemical composition of the starting slag melt (similar to Example 1 and 2). The dump portion (420 kg per ton steel) of the melted slag was removed from the apparatus, while the remaining portion flowed into the oxidizing zone for use in the next steel-making cycle. The production of steel described in this example required approximately 350 kg of equivalent fuel, consequently in comparison with the production of steel in an open-hearth furnace (with the same fraction of scrap in the charge and with account of fuel consumption for all conversion stages) the steelmaking in this example turned out to be 2 times smaller in power consumption. With regard to a higher quality of the steel obtained in the given example and to consumption of heat for producing the slag in the form of a cement clinker this difference will be even greater. Example 4:- Steel of the following chemical composition, % : C=0.2; Si=traces; Mn=0.3; P≤0.01; S < 0.01. was melted. The metal charge comprises the steel scrap (42.5%) and liquid steelmaking iron (57.5%) at a temperature of 1300°C. The chemical composition of the steelmaking iron, % : C=4.5; Si=0.5; Mn=0.3; P=0.1; S=0.04. A fresh melted slag (220 kg/t steel) of the same kind as was described in the preceding examples was formed in the oxidizing zone and the whole mass of the gaseous products from the reducing zone (made up only of CO - 85% and CO 2 -15%) and 33.3 m 3 of oxygen (purity - 95%) per ton of steel were used for supplying the melted slag with heat. The melting of the scrap consumed 29.1 m 3 of oxygen per ton of the obtained steel. The low-sulfur charge made it possible to reduce the ratio of the starting portion of the melted slag to 2 kg/kg reduced iron (283.5 kg/t steel). Taking account of a heat capacity of the melted slag (approximately 0.565 kcal/°C) the latter was reheated by 300°C (up to 1900°C). The mass of the melted slag (690 kg/t steel) allowed all the processes in the reducing zone to be provided with heat, including the reheating of the iron by 300°C. The reheating consumed 22.5 m 3 of natural gas and 43 m 3 of oxygen with a purity of 95% per ton of steel. In the reducing zone the melted slag was treated with a steelmaking iron which reduced Fe from FeO to a residual content in the slag FeO=5%, as compared with its initial level of 32.5 %. The iron proper was oxidized to a low-carbon steel. The yield of metal comprised 97%. The mass rate of the iron tapping into the melted slag was controlled by the consumption of oxygen spent for the process of melting the scrap and by the chemical express-analysis of the final melts of slag and steel. The production of 1 ton of the low-carbon steel consumed in all: 437.1 kg of scrap, 593.8 kg of iron, 22.5 m 3 of natural gas and 105.4 m 3 of oxygen with a purity of 95%. In comparison with the melting in an open-hearth furnace loaded with the same charge (consumption of equivalent fuel - 144 kg/t) the fuel consumption in the given example (with account of the fuel consumption for obtaining oxygen) turned out to be equal to 40 kg of equivalent fuel per ton of steel, i.e. it was 3.5 times smaller. Example 5:- The melting in this example was characterized in that the ratio of the starting slag melt was maintained at a maximum (15 kg per kg of reduced iron or 2,128 kg per ton of steel) due to which the use of a high-sulfur iron (S=0.2%) made it possible to provide the concentration of sulfur < 0.01% in the steel obtained. Besides, the temperature of iron before its mixing with the melted slag was equal to 1500°C. With regard to the foregoing, the reheating of the melted slag admitted into the reducing zone had to be reduced to 50°C (1650°C). In other respects this Example did not differ from Example 4. Example 6:- The steel was melted in much the same way as in Example 1. The difference resided in that the scrap was melted not at the expense of oxygen jets but at the expense of blowing the melt of a low-carbon steel with jets of a fuel-oxygen complete combustion flame. Products of the submersible combustion flame jet contained a substantial amount of carbon monoxide (CO) and hydrogen (H 2 ) evolved from the melt of the low-carbon steel into the melted slag, and were additionally oxidized in the melted slag at the expense of a secondary oxygen. In the main, this additional oxidation was accomplished through an intermediate process in which said oxygen oxidized FeO to Fe 3 O 4 , and then by interaction of the latter with CO and H 2 . The melted slag received a substantial amount of heat which was used for melting the slag-forming fluxes. In compliance with the balance of heat from the afterburning of the reduction process products ejected from the reducing zone of which approximately 70% were used for reheating the melted slag, and the remaining portion was used for melting the slag-forming fluxes. Due to the fact that the scrap was partially melted at the expense of the heat of the complete combustion flame jet itself the amount of oxidized iron in this example was approximately equal to only 235 kg instead of 324.5 kg per ton of scrap in Example 1. Respectively, a smaller amount of coal was needed in the reducing zone (49.3 kg instead of 68 kg). However, the total consumption of heat energy in this example in comparison with Example 1 is substantially greater due the consumption of a considerable amount of the natural gas (48.17 m 3 /t scrap) which was determined by the character of scrap melting by jets of the fuel-oxygen complete combustion flame blown into the melt of the low-carbon steel. A greater portion of the heat energy received from burning natural gas in oxygen was evolved in the melted slag and was advantageously used for additional melting of the slag-forming fluxes. As a result, 562 kg of a fresh slag melt per ton of scrap were obtained and at the end of the steelmaking process were removed with a chemical composition complied with the portland cement the production of which by a conventional method of sintering the components would require from 136 to 172 kg of furl. The consumption of power in this example was equal to 144.3 kg of fuel per ton of scrap, i.e. it was commensurable with the ordinary consumption of power for producing only the portland cement and was appoximately 1.5-2 times smaller in comparison with the steelmaking from scrap in an electric arc furnace. Inasmuch as in this example the amount of a dump (refinery) slag was more than two times greater than in Example 1, the concentration of phosphorus and sulfur in the obtained metal was respectively smaller: phosphorus < 0.002%, sulfur < 0.002%. The present invention cuts down the number of devices used for steelmaking, decreases the specific consumption of power and steps up the yield of liquid metal. Besides, this invention allows steelmaking with any content of steel scrap in the charge, whereas with the open-hearth and especially the converter methods this is not allowed because of a substantial impairment of the technical and economic indicators (decrease of output and rise of power consumption). The present invention also allows steelmaking without a steelmaking iron and practically with any ratio of scrap and iron-ore materials in the metal charge. Output of the apparatuses with the circular melting chamber wherein the proposed method is effected may practically be of any value: from a level characteristic of small steelmaking furnaces to a level of oxygen converters and much higher. Industrial Applicability The present invention may be effected to advantages at metallurgical enterprises engaged in steelmaking for the production of rolled products (sheet, rails, beams, angles and other sections). In addition, the present invention along with the known methods and apparatuses, may be used in the machine-building industry for the production of steel castings.

Claims: A continuous method of making liquid steel comprising: a) a steel melt and a starting slag melt which is in chemical equilibrium with the steel, are disposed in an annular shaped bath, and the starting slag melt is forced to constantly circulate through a closed circular circuit divided into an oxidizing and a reducing zone; b) crushed ore and flux materials together with a submersible fuel-oxygen combustion flame jet by means of which said ore and flux are melted, are blown into the circulating slag melt at an initial region of an oxidizing zone while sulphur is removed from the slag into a gaseous phase, and oxidised with oxygen; c) blowing a submersible fuel-oxygen combustion flame jet to superheat slag, into the circulating slag melt between middle and final sections of the oxidising zone, a dispersed reducing agent which reduces Fe 3 0 4 only to Fe0 being then also introduced into said slag; d) introducing a disperse reducing agent, sufficient for the reduction of Fe0 to iron, into the circulating superheated slag melt at an initial region of the reducing zone, said iron settling out of the slag and pass into the steel melt; e) loading steel scrap evenly into the steel melt under slag in the region of the middle section of the oxidizing zone and blowing an oxidizing gas through the metal melt surrounding said scrap to obtain rapid scrap melting, iron oxides passing into the slag being reduced; f) constantly removing the steel thus obtained from the melting process and delivering the steel to an off-furnace location for correction of its chemical composition to preset parameters; g) ejecting gaseous products of reducing iron formed in the reducing zone, into the oxidizing zone in the fuel-oxygen combustion flame jet submerged in the slag melt, together with oxygen or natural gas wherein said gaseous products are used both as a fuel and as a reducing agent for Fe 3 0 4 → Fe0; and h) maintaining the mass of the slag melt equivalent to the starting mass, the remainder of said slag melt being continuously removed from the melting process at the end of the reducing zone. A method as claimed in claim 1, wherein; a) the starting slag melt is utilised in an least a ratio of 2-15 kg of the mass thereof per kilogram of the iron reduced from said melted slag; b) the superheating temperature of the circulating slag melt before the delivery thereof into the reducing zone is taken in a range of 50 to 300°C higher than the temperature of the liquid metal in the annular bath. A method as claimed in claim 1 wherein; a) oxygen is used as an oxidizing gas; b) products of complete combustion of the fuel-oxygen flame gas are used as an oxidising gas; c) a concentration of Fe 3 0 4 , sufficient for conversion of formed CO and H 2 into CO 2 and H 2 0, respectively, is maintained in the slag melt in the blowing zone due to the introduction of an appropriate amount of iron ore material into the slag, reducing thereby fuel consumption; d) a required concentration of Fe 3 0 4 is maintained in the slag melt by blowing oxygen through said melt in the blowing zone thereby reducing fuel consumption. A method as claimed in any one of claims 1 to 3, wherein; a) the ratio of components in the slag melt is maintained at a level permitting removal of waste slag, the chemical composition of the latter approximating to the utmost the chemical composition of portland-cement clinker; and b) an ore raw material, comprising oxides of appropriate alloying elements is introduced into the slag melt in the oxidizing zone. An apparatus for effecting a method as claimed in any one of claims 1 to 4, comprising a circular melting chamber (1) with gas-separating walls (2,3) tuyeres (13,15,18,23,26) for introducing various reagents into the liquid bath and creating circulation of the slag melt, devices for tapping metal (28) and slag (30) from the melting chamber and removing gas-forming products therefrom (31,32) characterized in that: a) the circular melting chamber (1) is divided by two gas-separating walls (11) into two processing zones: an oxidizing zone (6) and a reducing zone (7), the oxidizing zone (6) comprising initial and final sections between which a middle section is located; b) at the initial section of the oxidizing zone (6) tuyeres for blowing powdered ore and flux materials (15) only, into the slag melt, and tuyeres with horizontal nozzles for blowing a fuel-oxygen flame jet (13) into said melt only, are disposed; c) a scrap-loading opening (22) is disposed in the roof (5) of the middle section of the oxidising zone (6), and scrap-melting oxygen and fuel-oxygen tuyeres (23) are disposed around said opening; d) tuyeres with vertical nozzles for blowing the submersible fuel-oxygen combustion flame jet (13) and a dispersed reducing agent (18) into the slag melt only are provided between the middle and final sections of the oxidizing zone; e) tuyeres for dispersed introduction of a reducing agent (26) into the slag melt only, are provided in the initial section of the reducing zone (7) ; f) a circular melting chamber (1) is provided with a gas transfer ejector-type duct (25), connecting the gas space of the reducing zone with the fuel-oxygen tuyeres (13) in the oxidizing zone and the tuyeres for introducing the reducing agent (18) provided nearby; h) the walls of the circular melting chamber (1) and gas separating partitions (11) in the place of contact with a slag melt are provided with metal panels (12) which are cooled by a damp water steam from the outside; i) an opening for tapping of waste slag (30) being provided at the end of the reducing zone (7), and in the bottom section of the reducing zone (7) an opening for tapping steel (28) is provided. A device as claimed in claim 5, wherein means for introducing liquid iron (27) scattered into drops, into the slag melt, is provided in a roof (5) of the bath in the initial section of the reducing zone (7). A device as claimed in claim 5 or 6, wherein a unit for reheating scrap by waste gases is provided. A device as claimed in claim 5 or 6, wherein a recuperator for heating oxygen and fuel by waste gases, is provided.

Inventors: LUPEIKO VITOLD MARIANOVICH, LUPEIKO, VITOLD MARIANOVICH
Applicants: LUPEIKO VITOLD MARIANOVICH, LUPEIKO, VITOLD MARIANOVICH
Application year: 1991
Main classification: C21C5
IPC codes: C21C5