RU2371482C2 - Method of direct reduction of metals with receiving of synthetic gas and assembly for its implementation - Google Patents

Abstract

FIELD: metallurgy.

SUBSTANCE: invention relates to metallurgy field, particularly to receiving of metal in liquid-phase continuously working aggregate, and to gasification of solid fuel.

EFFECT: invention provides creation of conditions for more flexible with low dependence on manufacturing method of metal control of compound of effluent gas ensured by separation of flows, metal, slag and gas, and also providing of correction of gas content, effluent from manufacturing aggregate, up to parametres of conditional synthetic gas and reduction of expenditure of energy ensured by consistent connection into united workflow of metallurgical aggregate, slag-receiver and chambers correcting gas' content.

2 cl, 1 dwg, 6 tbl

Description

The invention relates to metallurgy, in particular to the production of metal in liquid-phase units of continuous operation, and to gasification of solid fuel.

A number of processes and units of liquid-phase reduction are known, in which along with the metal along the way energy gas is produced. The most characteristic of them are the processes and aggregates of Korex and Romelt [1, 2]. In the Koreks unit [1], the reduction of oxides is carried out in two stages: in the first unit, solid-phase reduction of oxides is carried out, this intermediate is transferred by screw feeders to the second liquid-phase unit in which pig iron is obtained. This second unit is called a melting gasifier, since in it, along with cast iron, combustible gas is obtained. However, due to the close connection with the technology, this gas has a relatively low calorie content, and therefore, it is very difficult to bring its composition to the composition of synthesis gas. It is used for energy purposes.

This process and the unit has been brought to commercial implementation, however, it is distinguished by a rather complex design, high capital intensity and energy intensity. The complexity of the design is largely determined by the presence of auger transport of the intermediate, which is also the reason for additional energy consumption, as well as the fact that the processes in the second, liquid-phase, unit are close to the state of thermodynamic equilibrium, and the metal, slag and gas are in contact with each other for a long time different, therefore, in this unit the control of the gas composition without serious intervention in the technology is impossible.

In the Romelt process [2], all direct reduction processes are combined in one unit, however, the processes, like in the Korex unit, are close to the state of thermodynamic equilibrium, therefore, only cast iron can be obtained here and it is almost impossible to vary the gas composition without affecting the main technologies. Here you can only burn part of the carbon monoxide to improve the heat balance and use gas for energy purposes.

The process of gasification of coal in special units [3] has a fairly high capital intensity and cost, while the resulting gas has a relatively low calorific value, which complicates its conversion to synthesis gas and requires large energy costs.

Known units for producing synthesis gas from natural gas [4, 5] are very complex and capital intensive, while the cost of natural gas is quite high and continues to grow.

Closest to the proposed one is [6] a method for producing metals from ore materials, including supplying bulk materials to the reaction chamber, introducing oxygen and a reducing agent, completely transferring the metal and slag into the foamy emulsion, creating an increased pulsating pressure in the reaction chamber within 0.4- 3.0 MPa and a significant deviation of the system from thermodynamic equilibrium by organizing the outflow of a two-phase medium from the reaction chamber into the refining settler at a critical rate, separation in the refining compartment oynike metal and slag and a gas outlet through a high layer of the emulsion.

This method is implemented in the unit [6], containing a spherical reaction chamber with a device for feeding bulk materials and a device for supplying satellite flows of oxygen and a gaseous or dust-like reducing agent towards each other, a connecting channel, a refining settler connected by an inclined slag notch with a slag receiver and having a lance, counter-located with a connecting channel, a piggy bank with a tap hole for metal removal and a device for supplying carbon-containing bulk materials.

This method and unit have a number of significant advantages compared to those discussed above [1, 2]: a small specific volume of the unit, low capital and energy intensity, high rates of chemical reactions in conditions of a significant deviation of processes from thermodynamic equilibrium.

However, in this unit, the composition of the resulting gas is quite closely related to metallurgical technology, its calorific value varies greatly depending on the nature of the process, it is not adjusted to synthesis gas, and therefore most often it is simply released into the atmosphere, while both physical and chemical energy are lost gas component of 40-50% of the heat balance.

The objective of the invention is to create conditions for a more flexible one with little dependence on the technology for producing metal, controlling the composition of the exhaust gases by separating the flows of metal, slag and gas, as well as providing correction of the composition of the gas leaving the process unit to the parameters of the conditioned synthesis gas and reduction of energy costs due to the serial connection into a single process stream of a metallurgical unit, a slag receiver and a gas composition correction chamber.

The essence of the invention lies in the fact that in the method of direct reduction of metals to produce synthesis gas, which includes supplying bulk materials in the form of an ore mixture of metal oxides and coal into the reaction chamber, introducing oxygen and a reducing fuel, completely transferring the formed metal and slag to a two-phase medium in the form of a foamy emulsion, the creation in the reaction chamber of an increased pulsating pressure in the range of 0.4-3.0 MPa and the deviation of the system from thermodynamic equilibrium by organizing the outflow of a two-phase medium from the reaction ion chamber into a refining sump with a critical speed, separation of metal and slag in it and gas removal through a high emulsion layer, metal recovery from ores and coal ash are carried out simultaneously with coal gasification, oxygen and a reducing fuel are introduced into the reaction chamber through opposite lances flows, and the ratio of oxygen, including oxygen contained in the reduced oxides, and a reducing agent supplied to the reaction chamber and the refining sedimentation tank, including coal supplied in a mixture with the charge oh, they are calculated from the stoichiometry condition that oxidizes solid carbon to CO or converts natural gas to CO and H ₂ , and to obtain a conditioned synthesis gas suitable for processing into dimethyl ether or methanol, its composition is adjusted in a gas composition correction chamber having the lattice, on which there is a constantly replenished layer of coke or coal, while steam is supplied under the lattice of the chamber, and natural gas and oxygen are supplied above the lattice, while ensuring the volumetric ratio of CO to H ₂ in the produced gas 2/3 or 1/2, respectively but.

The method is carried out in a unit for direct reduction of metals to produce synthesis gas, containing a spherical reaction chamber with a device for feeding bulk materials in the form of an ore mixture of metal oxides and coal and a device for supplying satellite flows of oxygen and a gaseous or dust-like reducing agent towards each other, a connecting channel, a refining sump connected by an inclined slag notch with a slag receiver and having a lance opposite to the connecting channel, a piggy bank with a notch a metal ode and a device for supplying carbon-containing bulk materials, the reaction chamber, the refining sump and the slag receiver being connected in series, the slag receiver is equipped with a roll slag granulator and a gas composition correction chamber installed above it and combined with it, having a channel for removing part of the gas from under the refining dome a sump, tuyeres for supplying natural gas and oxygen and a channel for removing the resulting synthesis gas to a recovery boiler and gas purification, the gas composition correction chamber being connected with a slag receiver with an opening with a cooled grate, under which tuyeres for supplying steam are installed.

The essence of the invention, therefore, boils down to the fact that to solve the problem, it is necessary to change the design of the unit so that it allows you to separate the flow of slag and gas and provide, by supplying steam passing through a layer of coal or natural gas, a correction of the composition of the resulting gas to the parameters of the conditioned synthesis gas.

The direct reduction of metals to produce synthesis gas is implemented in the unit shown in the drawing.

The unit includes a spherical reaction chamber 1 with a device 2 for supplying bulk materials and a device 3 for supplying satellite flows of oxygen and a gaseous or pulverulent reducing agent towards each other, a connecting channel 4, a refining settler 5 with a lance 6 opposite to the connecting channel 4, a piggy bank 7 s with a tap hole 8 for removing metal into the bucket 9, with a device 10 for supplying carbon-containing bulk materials, the refining sump 5 is connected by an inclined slag tap 11 with a slag receiver 12 provided with a roll a slag granulator 13, and above the slag receiver there is a gas composition correction chamber 14 connected to the slag receiver 12 with an opening with a cooled grate 15, tuyeres 16 for supplying steam are installed under the grate, and the gas composition correction chamber 14 is equipped with tuyeres 17 for supplying natural gas and tuyeres 18 for oxygen supply, this chamber 14 is connected by a channel 19 to divert part of the gas from under the dome of the refining sedimentation tank, it has a device 20 for supplying coal or coke and a channel 21 for diverting the produced commercial gas to the waste heat boiler 22 and gas 23 weave.

The method in accordance with the task is as follows.

A powder mixture consisting of a mixture of iron oxides and other metals, together with coal, which plays the role of a reducing agent and fuel, by a device 2 is fed into the central zone of the reaction chamber 1, where at the meeting point of the confluent oxygen and, for example, natural gas flows supplied through the device 3 , a compaction disk is formed on which, as a result of the dynamic interaction of the jets, intense turbulization of the charge stream and the formation of large surfaces for heterogeneous chemical interaction occur. Moreover, due to incomplete combustion in the reaction chamber 1 of a part of coal, natural gas or another reducing agent, heating and partial reduction of oxides occur in accordance with the fraction of oxygen supplied.

The total ratio of reducing agents and oxygen supplied to the reaction chamber 1 and the refining sump 5 is calculated from the conditions for obtaining a gas composition in the upper part of the refining sump 5 with a total content of CO and H ₂ in the range of 70-90%, which is due to the heat balance associated with the chemical the composition of metal ore and its relative amount in the charge, as well as the necessary completeness of recovery. The correction of the gas composition is carried out by additional supply of coal or coke from the device 10 to the upper layer of the emulsion.

In the present invention, in particular, it is possible to process, that is, gasification, 100% of coal without the addition of ore or with its minimum addition only in order to reduce the temperature of the process and obtain a foamy slag emulsion. With this version of the technology, metals (iron, manganese, titanium, etc.) are recovered from coal ash. In this case, the gas composition by the sum of CO and H ₂ approaches 90%. In this embodiment, the proposed unit turns into a gasifier, but which has a significant advantage over the known gasifiers in that, in addition to gasification, metals are extracted from coal ash and components of the slag emulsion, as well as highly porous, easily granulated slag that can be used as an adsorbent or raw materials for cement production.

The gas suspension formed in the reaction chamber 1 with a gas content of 0.98-0.99 through the connecting channel 4 is fed into the lower part of the refining settler 5 above the upper cut of the piggy bank 7. In this case, the two-phase jet emerging from the connecting stream plays the role of a kind of dynamic cushion or failure grid, separating pillar of foam gas-slag emulsion, which simultaneously plays the role of wet gas cleaning, as well as a slag separator and metal accumulating in the piggy bank 7, due to lowering along the vertical wall pits metal droplets, the resulting reduction processes in gazoshlakovoy emulsion. Thus, taking into account the counteraction of gravitational and aerodynamic forces in the refining settler 5, metal and slag are separated, and an uneven (in density, gas content and chemical composition) distribution of parameters along the height of this unit occurs. The distribution of the content of metal oxides in height is also determined by the thermodynamically nonequilibrium nature of the processes occurring in the reaction chamber 1 and the refining settler 5, including the intense flows of matter and energy coming from below through the connecting channel 4 from the reaction chamber 1.

Thus, the use of a vertical column reactor with a lower reaction gas suspension as a refining settler in combination with a significant deviation of processes from thermodynamic equilibrium is the most important factor that determines the possibility of separation of the metal flow deposited in the piggy bank 7 and the gas-slag emulsion flow diverted along an inclined channel 11 to the slag pit 12, where the separation of slag and gas. To bring the composition of the associated process gas coming from the slag receiver 12 through the cooled grate 15 to the gas composition correction chamber 14 to the conditioned composition of the synthesis gas suitable for processing into dimethyl ether or methanol, under the grate 15 with it constantly being replenished using the device 19 with a layer of coke or coal, steam is supplied, and above the grate 15, natural gas and oxygen are supplied to the gas composition correction chamber 14, while providing a volumetric ratio of CO to H ₂ in the produced gas 2/3 or 1/2, respectively, for the floor teachings of dimethyl ether or methanol. The resulting synthesis gas from the chamber 14 through the channel 21 is supplied to a cooler (for example, a waste heat boiler) 22, a gas purifier 23, and then to a consumer, for example, to a catalytic synthesis unit for dimethyl ether or methanol or for energy purposes. But in the latter case, the addition of natural gas to chamber 14 is not necessary, since in this case it is not necessary to observe the ratio of CO to H ₂ . The sludge generated in the gas treatment 23 is recycled to the process, which allows to obtain a smokeless technology.

The advantage of this invention compared to the prototype is that the use of coal as a fuel and reducing agent and the installation of a gas composition correction chamber 14 in combination with the slag receiver 12 and slag granulator 13 in series with the refining settler 5 gives a number of additional effects. First of all, the possibility arises of flexible (almost independent) control of the gas composition at the outlet of the refining sump 5 and at the outlet of the unit as a whole, more precisely from chamber 14. Combining a coal gasifier (chamber 14) with a metallurgical unit (reaction chamber 1 and refining sump 5) and slag receiver 12 allows you to use the physical heat of the associated gas and slag to increase the calorific value and the amount of commercial gas. Thus, based on the chamber 14, a chemical heat recovery apparatus is obtained. If you get gas in a special gasifier (gas generator), then a significant amount of thermal energy is spent on maintaining the temperature (800-1000 ° C) in the gasification center [3]. The increased pressure created in the reaction chamber 1, allows you to push the reaction gas through all the elements of the unit, which results in a small specific volume of the unit and eliminates the need to use flow inducers and smoke exhausters.

The most important advantage of combining a vapor-coal gasifier (chamber 14) with a metallurgical unit is the possibility of converting associated process gas into a conditioned synthesis gas suitable for producing motor fuel and creating smokeless energy metallurgical technology, since the exhaust gas (smoke) is converted into a useful commercial product.

An embodiment of the invention is considered by the example of direct reduction of iron with simultaneous production of synthesis gas in a pilot sample of an aggregate with an ore productivity of 1 kg / s or 3.6 tons / hour. The method is implemented in the unit shown in the drawing, as follows. Iron ore having the following composition by main components,%:

Table 1 FeO Fe ₂ O ₃ MnO SiO ₂ CaO MgO Al ₂ O ₃ P ₂ O ₅ 22.02% 48.28% 0.52% 11.70% 7.05% 1.60% 2.83% 0.26%

and coal of the following chemical composition

table 2 FROM S Moisture Ash Volatile 68.43% 0.59% 8.00% 10.90% 20.08%

using a vertical screw feeder-dispenser 2 are fed into the spherical reaction chamber 1. The mass flow rate of ore is 1 kg / s, and the mass flow rate of solid reducing agent of 0.4 kg / s. This charge stream enters the compaction disk, which is created in the center of the chamber, at the meeting point of the confluent oxygen and gaseous or liquid fuel reducers formed by the devices 3. As a result of the interaction of the vertical flow of bulk materials with the compaction disk and counterpropagating satellite flows, a high degree of turbulization is created and a gas suspension is formed with a volumetric gas content of 0.98-0.99, which is supplied through the connecting channel 4 to the refining settler 5.

The existence of a critical flow rate of a two-phase medium and the dependence of the velocity of this medium on its gas content allows us to use the connecting channel 4 as a dynamic shutter. By changing the diameter of the connecting channel 4, as well as the ratio of the influx and drain of substances, it is possible to change the working pressure in the reaction chamber 1, which in this case varies in the range of 2-3 atmospheres.

The combustion of fuel in the reaction chamber 1 is carried out with a lack of oxygen, there is heating and partial reduction of oxides, but the main task solved in this chamber is the creation of a gas suspension.

Most of the recovery processes are completed in the refining sump 5. Here, partial afterburning of carbon monoxide to dioxide is also carried out. In this case, the afterburning occurs inside the gas-slag emulsion by supplying oxygen through the lance 6.

First, consider a prototype process.

The total oxygen consumption is selected in accordance with the heat balance and is about 0.525 kg / s. To balance the process with temperature, the degree of afterburning of CO and the amount of gaseous oxygen are changed.

In this case, priority is given to the production of metal and slag of a given composition, which is presented in Table 3 below.

Table 3 Metal Total Fe FROM Mn Si S % 100.0% 99.01% 0.50% 0.49% 0.00% 0.00% 0.00% kg / s 0.532 0.526 0.003 0.003 0,000 0,000 0,000 Slag Total FeO Fe ₂ O ₃ CaO SiO ₂ Al ₂ O ₃ MgO % one hundred% 5.19% 0.00% 40.93% 37.21% 9.99% 4.87% kg / s 0.403 0,021 0,000 0.165 0.150 0,040 0,020 Gas Total CO CO ₂ N ₂ H ₂ H ₂ O O ₂ % one hundred% 25.44% 62.04% 0.73% 0.54% 11.25% 0.00% kg / s 1,059 0.269 0.657 0.008 0.006 0.119 0,000

Here, due to the addition of oxygen to the refining sump, almost complete afterburning of H ₂ and afterburning of CO to 25% was carried out. In this case, quite satisfactory economic indicators for metal smelting are obtained, but the gas is practically waste. You can use only its physical heat. We have set the task of obtaining, along with the metal, also conditioned syngas.

This problem is solved as follows.

When coal is added in excess of that necessary for metallurgical technology, excess heat is naturally generated in the exhaust gas system. The balancing of the system by heat is achieved by reducing the degree of afterburning of CO and H ₂ .

Next, the task is to convert the resulting gas into a more high-calorie gas by using the physical heat of the gas and slag (which must be cooled with steam or water before granulation) to carry out the following chemical reactions:

In the presence of free oxygen, in addition, the following reactions can occur, which is accompanied by an increase in gas flow and an increase in temperature.

The operation of correcting the gas composition is carried out in a chamber 14 located above the slag receiver 12, gas from which, together with injected steam, passes into the chamber 14 through a water-cooled grate 15, on which a constantly replenished layer of coke or coal is created.

Close to optimal is the option when the process gas has a composition according to the main components: 50% CO and 50% H ₂ . Such a composition of combustion products is often rational both from the point of view of technology (completeness of iron reduction), and from the point of view of heat engineering (further heat use). In this case, when 3 moles of H ₂ O and 3 moles of C are fed into the chamber, it is possible to obtain a gas with the composition 3CO + 3H ₂ , that is, we obtain a triple volume of gas with a CO / H ₂ ratio of 1/1, which is enough close to the composition of the conditioned synthesis gas.

Now the question is whether there is enough physical heat to ensure that the temperature in the chamber 14 of the gas correction is not lower than 600-800 ° C, that is, so that the coke remains hot. To solve this problem, thermodynamic calculations were carried out to correct the composition of associated process gas using a software-instrumental system based on the Astra database [7, 8]. The calculations were carried out in the following sequence.

First, using this system, thermodynamically acceptable conditions and compositions of metal, slag and gas were obtained for an ore flow rate of 1 kg / s. At a coal flow rate of 0.674 kg / s and an oxygen flow rate of 0.382 kg / s, a metal was obtained with a carbon content of 0.52% and a temperature of 1878 K, as well as exhaust gas in an amount of 1.06 kg / s, the composition of which is shown below in table 4.

Table 4 Content% With CO ₂ H ₂ H ₂ O N ₂ CH ₄ By weight 1.06 92.83 3.21 2.14 1.74 0.02 0.00 By volume 1.41 72.78 1,60 23.49 2.13 0.01 0.00

This gas is in close contact with the slag (in the form of a gas-slag emulsion) through the channel 11 enters the slag receiver 12, where steam is blown towards the slag stream through the lance 16. Due to the heat of the slag, the steam is heated from 150 to 700 ° C and through the grate 15 together with the process gas, separated from the slag and having a temperature of 1500 ° C, continuously enters the layer of coal (coke) in the chamber 14. In this layer and flow over it reactions (1) - (3) under conditions of excess carbon.

Table 5 shows the variant calculations of gas correction, the composition of which is presented in table 4, due to its interaction with coal and steam.

Table 5 Control actions Volumetric composition of gas,% The ratio of CO / N ₂ No. Coal, kg / s Steam kg / s T _g , ° K Gas mass, kg / s CH ₄ With CO ₂ H ₂ H ₂ O one 0.2 0.3 1100 1,53 0.42 60.47 3.18 34.11 1.82 1.77 / 1 2 0.25 0.375 1065 1.65 0.62 56.16 5.08 35.27 2.87 1,59 / 1 3 0.3 0.45 1042 1.73 0.81 52.32 6.79 36.21 3.87 1.44 / 1

Since the coal in the layer is in excess, the control is carried out by changing the amount of steam supplied. As can be seen from table 5, in the third version of the control it was possible to increase the content of H ₂ from 23.49 to 36.21%, and the CO content was reduced from 72.78 to 52.32%. However, movement in this direction (correction due to coal and steam) becomes ineffective, since the content of CO ₂ and H ₂ O increases due to a decrease in temperature in chamber 14.

Therefore, further correction of the gas composition is carried out due to oxygen reforming of methane CH ₄ supplied to the chamber 14 through the lance 17, and oxygen supplied through the lance 18, by the reaction:

As can be seen from the reaction and from table 6 (options 1 and 2), in this case, the content of H ₂ in the resulting gas mixture increases with a slight increase in the temperature of the mixture.

Table 6 Control actions Volumetric composition of gas,% The ratio of CO / N ₂ No. Coal, kg / s Steam kg / s CH ₄ , kg / s O ₂ kg / s T _g , ° K Gas mass, kg / s CH ₄ With CO ₂ H ₂ H ₂ O one 0.3 0.45 0.20 0.20 1051 2.12 1.09 46.88 4,56 43.83 3.64 1.07 / 1 2 0.3 0.45 0.25 0.25 1053 2.22 1.13 45.95 4.22 45.13 3.57 1/1 3 0.3 0.45 0.45 0.25 1006 2.22 2,37 34.13 5.82 51,4 6.26 2/3 four 0.3 0.45 0.60 0.25 980 2.20 3.52 27.40 6.40 54.52 8.15 1/2

As can be seen from the second version of the thermodynamic calculation (table 6), synthesis gas was obtained with a volumetric ratio of CO / H ₂ close to 1/1, more precisely 45.95 / 45.13, which can already be considered a good result, since high-calorie gas is obtained , which can be used both as energy fuel and as a raw material for producing synthetic fuel. However, with this gas composition, the synthetic fuel in the catalytic synthesis unit, for example, will be produced in smaller quantities and of poorer quality (due to dilution with unreacted ballast components) than is possible if the optimal stoichiometric ratio is observed. To obtain dimethyl ether (synthetic diesel fuel) in accordance with its stoichiometric formula CH ₃ -O-CH _{3 the} optimum ratio is CO / H ₂ equal to 2/3.

We set the task in accordance with the claims to obtain the ratio CO / H ₂ equal to 2/3.

Considering (see Table 6, option 2) that there is a certain margin in gas temperature (1053 K), we decide to reach the final stage of gas composition correction due to the temperature reforming of methane by the reaction:

As can be seen from a comparison of options 2 and 3 (table 6), the solution to the problem was achieved by increasing the methane consumption by 0.2 kg / s without increasing the oxygen consumption. At the same time, a gas with a volumetric content of CO and H _{2 of} 34.14 and 51.4, respectively, was obtained, which just corresponds to the CO / H ₂ ratio of 2/3.

Similarly, by temperature reforming of methane according to reaction (7), a CO / H ₂ ratio of 1/2 was obtained, which is optimal for producing methanol. The solution to this problem corresponds to option 4 in table 6, which is achieved by increasing the methane consumption by 0.15 kg / s, ceteris paribus. At the same time, a gas was obtained with the contents of CO and H _{2 of} 27.40 and 54.52, respectively, which is close enough to the optimal ratio for methanol production.

Thus, the presented example confirms the feasibility of the invention.

Based on the considered example, we emphasize once again the advantages achieved by the implementation of this invention.

The combination of direct reduction of metals from oxides with coal gasification, taking into account the proposed method and design of the unit allows you to:

- create a smokeless energy metallurgical unit in which the exhaust gas is converted into a useful commercial product;

- to avoid the need to use smoke exhausters or other high-temperature cost drivers, since due to the high pressure potential created in the reaction chamber and the complete closure of the process from the atmosphere, it is possible to push gas through any devices installed behind the process unit;

- make full use of the chemical and physical energy of the associated process gas, having obtained a chemical heat utilizer based on chamber 14, and this will double the amount of marketable gas (2.22 instead of 1.06 kg / s) compared to the original, and its calorific value increases from 6432 to 20832 kJ / kg with the cost of natural gas only about 20% of the mass of gas produced;

- to obtain the process gas requires two times less oxygen gas than with conventional gasification, since half of the oxygen is taken from metal oxides, for example, by the reactions:

или

;

or

;

- due to the fact that hot gas is used for steam-gasification (about 1600 ° C), and also at high pressure, the design of the gasifier-reformer (chamber 14) is extremely simplified, and the energy consumption for gasification and gas reforming is significantly reduced;

- when reducing manganese as a result of the application of this invention, an even higher effect can be obtained, since in this case, to ensure a reducing atmosphere, the process exhaust gas must have a total CO and H ₂ content _of about 90%.

Information sources

1. H.B. Lüngen, C. Mülheim, R. Steffen. Current state of direct reduction processes and reduction smelting of iron ores. // Black metals. - 2001. No. 10. - p.20-35.

2. Romenets V.A., Wegman E.F., Sakir N.F. The process of liquid phase recovery. // Proceedings of universities. Ferrous metallurgy. - 1993. - No. 7. p. 9-19.

3. Schilling G.-D., Bonn B., Kraus W. Gasification of coal. / Per. with him. and ed. S.R. Islamova. - M .: Subsoil. - 1986. - 175 p.

4. Terentyev G.A., Tyukov V.M., Smal F.V. Engine fuel from alternative raw materials. - M .: Chemistry. - 1989. - 271 p.

5. Plate N. Synthetic gasoline. // Science and life. - 2004. - No. 11. - p. 66-68.

6. Pat. Russia 2272849 C1. A method of producing metals from ore materials and an aggregate for its implementation. / V.P. Tsymbal, S.P. Mochalov. - 2004122183/02; Announced on 7/19/2004; Publ. 03.3.2006, PCT Bulletin, Bull. 9; Priority 19.7.2004. - 12 p.: Ill.

7. Sinyarev G.B., Vatolin N.A., Trusov B.G. and others. The use of computers for thermodynamic calculations of metallurgical processes. - M .: Science. - 1982. - 260 s.

8. Klimov V.Yu., Mochalov S.P., Rybenko I.A. Development of an automated system for calculating and optimizing technologies for the production of metals and alloys. // Modeling, software and high technology in metallurgy: Proceedings of the All-Russian Scientific and Practical Conference. - Novokuznetsk: Publishing. SibGIU. - 2001. - p. 435-439.

Claims (2)

1. A method of direct reduction of metals to produce synthesis gas, comprising supplying bulk materials to the reaction chamber in the form of an ore mixture of metal oxides and coal, introducing oxygen and a reducing fuel, completely transferring the formed metal and slag to a two-phase medium in the form of a foamy emulsion, in the reaction chamber of increased pulsating pressure in the range of 0.4-3.0 MPa and the deviation of the system from thermodynamic equilibrium by organizing the outflow of a two-phase medium from the reaction chamber into a refining sump with At the same time, the separation of metal and slag in it and the removal of gas through a high emulsion layer, characterized in that the reduction of metals from ores and coal ash is carried out simultaneously with coal gasification, oxygen and a reducing fuel are introduced into the reaction chamber through opposing tuyeres by satellite flows, and the ratio of oxygen, including oxygen contained in the reducible oxides, and a reducing agent supplied to the reaction chamber and refining sump, including coal supplied in a mixture with the charge, is calculated from the conditions Via stoichiometry ensuring oxidation of solid carbon to CO or natural gas conversion to CO and H _2, and to obtain conditioned synthesis gas suitable for conversion into dimethyl ether, or methanol, its composition is adjusted in the gas composition adjustment chamber having a grate in which a constantly replenished layer of coke or coal is located, while steam is supplied under the grate of the chamber, and natural gas and oxygen are supplied above the grate, while providing a volumetric ratio of CO to H ₂ in the produced gas of 2/3 or 1/2, respectively. 2. A unit for direct reduction of metals to produce synthesis gas, comprising a spherical reaction chamber with a device for feeding bulk materials in the form of an ore mixture of metal oxides and coal and a device for supplying satellite flows of oxygen and a gaseous or dust-like reducing agent towards each other, a connecting channel, refining a sump connected by an inclined slag notch with a slag receiver and having a lance opposite to the connecting channel, a piggy bank with a notch for the removal of metal and devices for supplying carbon-containing bulk materials, the reaction chamber, the refining sump and the slag receiver being connected in series, characterized in that the slag receiver is equipped with a roll slag granulator and a gas composition correction chamber installed above it and combined with it, having a channel for removing part of the gas from under the refining dome a settling tank, tuyeres for supplying natural gas and oxygen, and a channel for removing the resulting synthesis gas to a recovery boiler and gas purification, the gas composition correction chamber being connected to shlakopriemnikom hole with cooled grate, under which there are tuyeres for feeding steam.