CN101317067A - Device for processing powdery raw material containing lead and zinc - Google Patents

Abstract

An apparatus for processing a powdered lead and zinc containing raw material, the apparatus being related to non-ferrous metallurgy and primarily to a plant for processing a powdered lead and zinc containing raw material which may contain copper and precious metals. The object of the invention is to increase both the direct recovery of lead to lead bullion and the specific capacity of the device. An apparatus for processing a powdered lead and zinc containing raw material comprising: the device comprises a vertical smelting chamber with a rectangular cross section of a combustion chamber, a gas cooler pipe body, a partition wall with a water-cooling copper element for separating the smelting chamber from the gas cooler pipe body, an electric furnace separated from the smelting chamber by the partition wall with the water-cooling copper element, a jacket conveyor belt, a device for flowing out smelting products and a hearth. It is possible to install not more than two tuyeres at the level of the lower edge of the partition separating the gas cooler shaft from the melting chamber, which tuyeres are inclined at an angle to the horizontal towards the hearth (fig. 1). In the case of two tuyeres, they are arranged on each of the opposite side walls of the gas cooler shaft and are displaced mirror-like in relation to the axial cross-section of the gas cooler shaft, the ratio of which to the internal length of the gas cooler shaft amounts to 0.25-0.30.

Description

Plants for processing raw materials containing lead and zinc in powder form

technical field

This invention relates to non-ferrous metallurgy and primarily to equipment for processing powdered lead and zinc containing raw materials which may contain copper and precious metals.

When upgrading plants for processing raw materials containing lead and zinc, which may contain zinc, copper and other valuable elements in addition to lead, the most important task is to increase the recovery of metals into marketable products and to expand the raw materials processed Process intensification in terms of scope, said raw materials including lead-containing materials produced as by-products in other industrial processes, the storage of which presents significant ecological hazards.

There are a wide variety of lead-containing materials such as residues from hydrometallurgical processes, matte conversion dust, neutralization and process solution purification slurries that are raw or processed in insufficient volumes in known installations to accumulate in piles . In addition to lead, all the above-mentioned materials also contain significant amounts of zinc and copper, which reduces the complexity of recovering non-ferrous metals from natural mineral raw materials.

current technology

1987，#9，第20-22页)。Plants are known for processing pulverulent raw materials containing lead and zinc, in which there is a vertical melting chamber with a rectangular cross-section of the burner, a gas cooler, a vertical cooling chamber separating said melting chamber from the gas cooler A partition wall, an electric furnace separated from the melting chamber by said vertical cooling partition wall, a jacketed conveyor belt, equipment for the outflow of the smelted product, and a furnace chamber. Thus, the ratio of the level difference of the lower edge of the partition to the distance from the top of the melting chamber to the lower edge of the partition separating the electric furnace from the melting chamber reaches 0.30 and the distance from the lower edge of the partition to the furnace is equal to the distance from the lower edge of the partition The ratio between the differences in levels reached 1.23. (Slobodkin LVNew technology at leadplant UKSZK//Non-ferrous

1987, #9, pp. 20-22).

A disadvantage of this plant is the low direct lead recovery to crude lead due to the high entrainment of feed dust from the smelting chamber with the reaction gases at a given ratio of the structural components of the plant. Increased content of recycled sulphate dust in the feed (which is continuously returned through the combustion chamber for roasting-smelting) leads to a decrease in the temperature of the flame melt and the rate and extent of lead oxide reduction in the associated carbon reductant layer decrease.

The closest technical content of the invention is a plant for processing powdery raw materials containing lead and zinc, in which there is a vertical smelting chamber with a rectangular cross-section of the burner, a gas cooler, connecting said smelting chamber with the gas A partition wall separating the cooler, an electric furnace separated from the smelting chamber by said partition wall, a jacketed conveyor belt, equipment for the outflow of the smelted product, and the furnace. Thus, the ratio of the level difference of the lower edge of the partition to the distance from the top of the melting chamber to the lower edge of the partition separating the electric furnace from the melting chamber reaches 0.15-0.29 and the distance from the lower edge of the partition to the hearth is equal to that of the partition The ratio between the differences in the lower edge level reaches 1.25-2.10. (Patent No. 8705 of the Republic of Kazakhstan, MPK F27B 17/00, C22B 13/02, published on April 15, 2005, Bulletin No. 4).

The disadvantage of this device is that the specific capacity of the device and the direct recovery of lead to crude lead are simultaneously reduced due to the separation of the slag melt dead zone at the outer end wall of the gas cooler tube opposite the partition from the smelting chamber. The self-cooling of the slag melt in the region of the plant leads to the formation of slag crusts and a reduction in the intensity of the circulation of the slag melt between the electric furnace, the melting chamber and the gas cooler tube. This reduces the heat input from the electric furnace to the carbon reductant layer and leads to a slowdown of the flame melt carbothermal reduction process.

The engineering problem of the invention is to provide an additional heat input into the carbon reducing agent layer by slowing down the crust formation process on the walls of the bottom region of the gas cooler tube, accelerating the circulation and increasing the heat content of the slag melt flow and corresponding acceleration of the flame smelt reduction process to simultaneously increase the direct lead recovery to crude lead and the specific capacity of the improved plant. This problem can be solved by organizing the heat input to the slag melt bath below the gas cooler tube.

public profile

The specified task is achieved by a known device for processing powdery raw materials containing lead and zinc, in which there is a vertical smelting chamber with a rectangular cross-section of the burner, a gas cooler tube, connecting said smelting chamber with The partition wall with water-cooled copper elements separated by the gas cooler tube, the electric furnace separated from the smelting chamber by the partition wall with water-cooled copper elements, the jacketed conveyor belt, the equipment for the outflow of smelted products, and the furnace. Thus, the ratio of the level difference of the lower edge of the partition to the distance from the top of the melting chamber to the lower edge of the partition separating the electric furnace from the melting chamber reaches 0.15-0.29 and the distance from the lower edge of the partition to the hearth is equal to that of the partition The ratio between the horizontal differences of the lower edge of the board reaches 1.25-2.10. According to the invention, no more than two tuyeres can be installed on the wall of the gas cooler tube at a certain level at the lower edge of the partition separating the gas cooler tube from the smelting chamber, and which are at an angle to the horizontal plane towards the furnace Tilt, the angle is defined by the formula

α=arctg(k·ΔH/B)

Where α- tuyere inclination;

k-wind outlet inclination coefficient, equal to 1.11-1.25;

ΔH - the difference in the level of the lower edge of the partition;

B - Internal width of the gas cooler tube body.

According to the invention, it is reasonable when installing the two tuyeres to arrange them on each opposite side wall of the gas cooler tube with a mirror-like displacement with respect to the axial cross-section of the air cooler, which is aligned with the gas The ratio of the inner length of the cooler tube body reaches 0.25-0.30.

The installation of the tuyeres and their arrangement allow the supply of oxygen-containing gas onto the surface of the layer of carbon material floating on the slag melt bath in the bottom region of the gas cooler tube where the reaction gas is supplied from the smelting chamber. This provides an opportunity for afterburning the carbon monoxide contained in the reaction gases of the smelting chamber due to the oxidation of the oxide melt in the carbon reductant layer floating on the slag melt bath below the smelting chamber burner flame. The result of the reduction reaction, and the opportunity to incompletely burn the solid carbon fuel in the flame that is introduced into the feed with the low calorific value of the raw material being processed. When the smelting chamber reaction gas contains a large amount of carbon monoxide, the oxygen introduced via the tuyeres is consumed together with the oxygen-containing gas for burning solid carbon in the layer of carbon material floating on the slag melt in the bottom region of the gas cooler tube.

When the carbon monoxide contained in the reaction gas of the smelting chamber burns, or when the solid carbon in the layer of carbon material floating on the slag melt in the bottom area of the gas cooler tube burns, heat is generated, part of which is used to improve the plant The temperature of the slag melt in this dead zone. The increase in the temperature of the slag melt prevents the formation of slag crusts on the bottom of the gas cooler tube walls and accelerates the circulation of the slag melt flow between the electric furnace, melting chamber and gas cooler tube while increasing its heat content. This leads to an increased heat input into the working area of the carbon-reductant layer below the burner with a circulating flow of slag melt and a corresponding acceleration of the reduction of the flame melt. As a result, direct lead recovery to crude lead is increased and offers the potential for improved plant specific capacity.

Direct lead recovery to crude lead is increased and at the same time specific capacity of the plant is increased through a reduction in dust carryover and a corresponding reduction in recycled sulphate dust content in the feed to the burner due to the tuyeres being inclined to the plant hearth. Oxygen-containing gases are injected into the reaction gas stream exiting the smelting chamber through tuyeres with a downward flow velocity component, which decelerates them at the inlet of the gas cooler tube and increases the rate of precipitation of dust particles by the reaction gas from the smelting chamber speed.

When tuyeres are installed in the wall of the gas cooler tube at a level below the level of the lower edge of the partition separating the gas cooler tube from the smelting chamber, the exothermic action is retained at the surface of the slag melt. However, part of the reactant gas begins to pass over the flow of oxygen-containing gas injected through the tuyeres. This leads to a reduction in the deceleration effect of the reaction gases and a reduction in the speed of precipitation of dust particles by the reaction gases from the smelting chamber. In addition, the proximity of the oxygen-containing gas jet from the tuyere to the surface of the slag bath will lead to an increase in the entrainment of already settled dust particles. As a result, smelting dust production and their fraction in the feed will increase and flame temperature, reduction rate of the oxide melt in the carbon reductant layer, direct lead recovery to crude lead and plant specific capacity will decrease.

When the tuyere is installed at a level higher than the level of the lower edge of the partition, the heat release area is away from the surface of the slag melt. In addition, higher tuyere installation levels result in reduced contact between the oxygen-containing gas and the carbon material layer when the carbon monoxide content in the reaction gas in the melting chamber is insufficient. This will reduce the heat input to the slag bath below the gas cooler tube. As a result, the heat content and circulation intensity of the slag melt flow between the electric furnace, melting chamber and gas cooler tubes will be reduced, which will lead to a slowing of the heat input into the working zone of the carbon reductant layer below the burner. Accordingly, the speed of flame smelt reduction, direct lead recovery to crude lead and specific capacity of the plant will decrease.

If the tuyere is set to be inclined to the horizontal plane at a certain angle, and the k coefficient is less than 1.11, the heat release area generated by the secondary combustion of carbon monoxide in the reaction gas in the smelting chamber will leave the surface of the slag melt. Additionally, the oxygen-containing gas injected through the tuyeres will not come into contact with the layer of carbon material in the gas cooler tube during certain periods of plant operating time after slag discharge. As a result, the overall heat flow into the slag bath below the gas cooler tube will be reduced. This will reduce the slowing effect of the crust formation process on the bottom of the gas cooler tube wall and the circulation intensity of the slag melt flow between the electric furnace, the melting chamber and the gas cooler tube. Thus, the heat input into the carbon reductant layer below the burner flame will be reduced and at the same time the rate of flame melt reduction will be reduced. As a result, the direct lead recovery to crude lead and the specific capacity of the plant will be reduced. In this case, the reduction in the speed of dust particle precipitation by the reaction gases from the smelting chamber results in direct lead recovery to crude lead and a reduction in the specific capacity of the plant. Thus, the production of smelting dust and its fraction in the feed will increase while the temperature of the flame and the rate of reduction of the oxide melt in the carbon reductant layer will decrease. As a result, direct lead recovery to crude lead and plant specific capacity will both be reduced.

Set the tuyere at an angle inclined to the horizontal plane, and the k coefficient is greater than 1.25, and when the tuyere is installed at a level lower than the lower edge level of the partition separating the gas cooler tube body from the melting chamber, part of the reaction gas will start to pass through Oxygen-containing gas flow injected from the tuyeres. This leads to a reduction in the slowing effect of the reaction gases and a reduction in the settling speed of the dust particles by the reaction gases from the smelting chamber. In addition, an increase in the angle of inclination of the tuyere to the surface of the slag bath will result in the blowing of settled dust particles and the splashing of droplets of slag melt into the upward flow of reaction gas. As a result, the production of smelting dust and its fraction in the feed will increase while the flame temperature and the reduction rate of the oxide melt in the carbon reductant layer will decrease. Consequently, the direct lead recovery to crude lead and the specific capacity of the plant will also be reduced.

When two tuyeres are installed, which are located on each side wall of the gas cooler tube and are mirror-like displaced with respect to its axial cross-section, the effect of the specified task is improved. This is determined by the following two factors.

First, two tuyeres are installed whose axes are mirror-like shifted relative to the axial cross-section of the gas cooler tube, resulting in combustion of the carbon monoxide reaction gas from the smelting chamber or from solid carbon in the carbon reductant layer The increase of the heat transfer surface to the slag bath. Correspondingly, the heat gain to the slag bath volume below the gas cooler tube increases under the same thermal effect from the secondary combustion of the reactant gases or from the combustion of solid carbon in the carbon reductant layer on the surface of the slag melt. An increase in the heat content of the slag melt leads to an acceleration of its circulation and an increase in the heat gain into the region of the reducing reaction flow. The result is additionally increased direct lead recovery to crude lead and improved specific capacity of the plant.

Secondly, two tuyeres are installed, which are located on each side wall of the gas cooler tube and are mirror-like displaced relative to the axial cross-section of the gas cooler tube, which leads to entrainment by dust and thus into combustion The additional effects of increased recycled sulfate dust content in the feed to the reactor, direct lead recovery to crude lead and increased specific capacity of the device. In this case, the dust entrainment is reduced by injecting the oxygen-containing gas through two tuyeres mounted on opposite side walls of the gas cooler tube and relative to the axis of the gas cooler tube. The mirror-like shift towards the cross-section and causes the gas cooler tubes to spin the upflow of reactant gases exiting the melting chamber. As a result, there is a centrifugal component of particle velocity that promotes complete settling of the particles on the gas cooler tube walls.

When the distance of each tuyere to the axial cross-section of the gas cooler tube body is increased, the effect of achieving the set task is increased. This is achieved by enlarging the total heat transfer surface between the exothermic area for secondary combustion by the reaction gases or combustion by the solid carbon and the area of the slag bath. Correspondingly, the heat gain into the slag bath volume increases, its heat content increases and the circulation rate of the slag melt in this region of the plant increases. This leads to an increase in the amount of heat incorporated into the reduction reaction zone and their acceleration. The result is direct lead recovery and increased specific capacity. In addition, the increased distance between the tuyere axes enhances the effect of the gas cooler body to rotate the upflow of reactant gas, which results in a more complete settling of the dust particles on the gas cooler body wall.

The strongest effect is achieved when the ratio of the distance from the tuyere axis to the axial cross-section of the gas cooler tube body and its internal length reaches 0.25-0.30. The maximum contact surface of the exothermic area with the slag melt bath is achieved at this distance as long as the combustion gas flow from the opposite tuyeres is shut off. In addition, at this distance, the significant effect of rotating the upflow of the reaction gas and the acceleration of the deposition of dust particles on the wall of the gas cooler tube are achieved without the jacket being damaged by secondary combustion of carbon monoxide (or on the surface of the carbon material layer). Combustion of solid carbon) The combustion gas stream is superheated.

When the ratio of the distance from the tuyere axis to the axial cross-section of the gas cooler tube body to its internal length is less than 0.25, the heat exchange surface of the hot gas and slag bath and the effect of rotating the rising reactant gas is reduced. As a result, the transfer of heat flow into the slag melt bath volume and the degree of deposition of dust particles on the walls of the gas cooler tubes are simultaneously reduced. Correspondingly, the additional heat content of the slag melt reduces the effect of a corresponding acceleration of its circulation in the slag bath and reduces the effect of reducing the carryover of recirculated sulfate dust from the plant. Thus, blowing through the tuyeres does not lead to an increase in the specific capacity of the plant and to coarse The maximum possible enhancement of the effect of direct lead recovery of lead, which will accelerate the reduction of the oxide melt in the carbon reducer layer.

When the ratio of the distance from the tuyere axis to the axial cross-section of the gas cooler tube body to its internal length is greater than 0.30, the heat transfer from the combustion gas to the slag melt bath and the dust deposition on the wall of the gas cooler tube body are determined The effect of rotating the rising reactant gas will not be increased to any extent. However, the high temperature combustion zone of carbon monoxide in the reaction gas and solid carbon in the carbon layer is close to the wall of the device, which significantly increases the specific heat load on the jacketed belt in this localized area and increases the possibility of jacket burnthrough.

The invention is illustrated by the drawings. Fig. 1 is a schematic diagram of a device for processing powdery raw materials containing lead and zinc; Fig. 2 and Fig. 3 are AA and BB sections of the gas cooler tube body shown in Fig. 1 with a tuyere installed; Fig. 4 is installed with two The BB section of the gas cooler tube body shown in Figure 1 of the tuyere.

The plant is composed as follows: a vertical smelting chamber 1 of rectangular cross-section, on the top of which is installed a burner 2 for feeding feed, oxygen, recycled dust and solid reducing agent; a partition 3 with water-cooled copper elements, the The partition is installed vertically and separates the smelting chamber 1 from the gas cooler tube body 4, and the tuyere 5, 6 for oxygen-containing gas supply is installed on the side wall of the gas cooler tube body; the electric furnace 7, which is connected to the smelting The chamber is adjacent and separated from this melting chamber by said partition 8 with water-cooled copper elements, completely dedicated to the melting chamber; electric furnace and furnace gas cooler tube 9; jacketed conveyor belt 10 and equipment for the outflow of smelted products 11.

The device works in the following manner.

Lead and lead-zinc raw materials (lead, lead-zinc, lead-copper, lead-copper-zinc, lead-silver concentrate, lead powder, lead-containing residue, crude lead refining recovery, battery paste and other secondary lead material), flux and (if required) solid carbon fuel (coke, petroleum coke, carbon black, brown charcoal or charcoal) is dried to a moisture content of less than 1% with crushed carbon reducing agent (coke, Petroleum coke, carbon black or charcoal) are mixed and transferred to the burner 2 (see Figure 1 ), through which a stream of process oxygen (94-99% _O2 ) is blown into the smelting chamber 1 of the plant. In the melting chamber 1, the feed is ignited, oxidized and melted in suspension under the action of radiation from the flame and high temperature (T=1100-1200° C.) of the rising furnace gas, producing a dispersed oxide melt. At the bottom of the melting chamber 1, the flame temperature reaches 1350-1450°C. The degree of feed desulfurization is controlled by varying the ratio of feed to oxygen consumption in burner 2.

The crushed carbon reductant feed (ie coke, petroleum coke, carbon black or charcoal) transferred along with the feed having a particle size of 5-20 mm is heated as it moves towards the flame and onto the surface of the slag bath. The presence in the structure of a partition 8 arranged downwards from the furnace roof and partly submerged in the slag melt allows to separate the gas space of the smelting chamber 1 and the electric furnace 7 and to create a desired height on the surface of the slag bath below the burners Porous layer of carbon reducing agent. This provides a reduction in the loss of non-ferrous metals in the slag melt by creating a reducing atmosphere in the electric furnace, and accelerates the precipitation of small particles of reduced metals to the bottom metal phase produced by their agglomeration, and makes the carbon in the porous structure Coarsening of the reducing agent layer.

Selective reduction occurs when the dispersed oxide melt formed during flash melting reaches and leaks through the porous layer of fractured carbon reductant. The oxides of lead are reduced to metallic lead while the zinc oxide remains in the slag melt which, together with the metallic lead, flows from the smelting chamber 1 below the partition 8 into the electric furnace 7, which serves to accumulate and settle the smelted products and They are separated by specific gravity and, if necessary, the zinc is partially expelled from the slag melt by feeding a carbon reducing agent of small size on the surface of the slag bath of the electric furnace. Similar to lead oxides, copper oxides are reduced to metals in the carbon reducing agent layer and transferred to crude lead, non-ferrous metal sulfides exist in dispersed flame melts, and their degree of desulfurization by feed is greater than 90 -94% or with a lower degree of desulfurization of the feed is divided into metal phases or slag phases, which form a single matte phase, which forms a product that settles in the electric furnace during the smelting process. This allows crude decoppering of crude lead directly in the unit, recovering excess copper from the processed lead and zinc containing raw material into the polymetallic mass.

Part of the thermal energy released from the electric furnace flows to the smelting chamber together with the slag melt circulation flow of the total slag bath and is partially soaked by the carbon reducing agent layer. Together with the heat flow that flows with the flame melt, the heat gain from the electric furnace allows to compensate the heat consumption of the endothermic reaction of oxide reduction in the porous carbon layer.

Slag and lead flow from the electric furnace 7 through equipment 11 and are transferred to be processed to make goods.

Sulfur dioxide reaction gas from the smelting chamber 1 formed during the feed flash melts enters below the partition 3 and then enters the gas cooler tube 4 for cooling, the partition is set down from the furnace roof but it does not reach the bottom of the slag melt surface.

At the bottom of the gas cooler tube 4, the reaction gas containing carbon monoxide is post-combusted by an oxygen-containing gas supply via the tuyeres 5,6. Part of the thermal energy thus released is absorbed by the flow of slag melt circulating in the slag bath of the entire plant and flows towards the melting chamber into the carbon reducing agent layer, increasing the heat flow together with the flame melt and the slag melt from the electric furnace. This increases the possibility to compensate for the heat consumption of the endothermic reaction of oxide reduction in the porous carbon layer. The carbon monoxide consumed reaction gases ascend to the outlet of the gas cooler tube and are cooled by heat exchange with the water-cooled surface of the tube wall.

After purification of the gas cooler 4 gas in an electrostatic precipitator (not shown in the figure), the utilization of sulfur is then carried out to produce commercial products (sulfuric acid, elemental sulfur, sulfuric anhydride or salts). Dust captured by the electrostatic precipitator is continuously returned for smelting.

The invention is illustrated by means of an example of device operation.

Example 1 (as a prototype). The ratio between the level difference of the lower edge of the partition and the distance from the top of the melting chamber separating the electric furnace from the melting chamber to the lower edge of the partition is equal to 0.28 and the distance from the lower edge of the partition separating the electric furnace from the melting chamber to the furnace chamber The ratio between the distance and the horizontal difference of the lower edge of the partition is equal to KIVCET of 1.25 (cross-sectional area of the melting chamber - 1.4m ² , height of the melting chamber - 3.3m, cross-sectional area of the gas cooler tube - 1.44m ² , furnace area of the electric furnace - 5m ² , power generation capacity of electric furnace transformer - 1200kW) in the test device, the lead-containing residue produced from sulfide lead concentrate, lead powder, zinc, battery paste, quartz and lime flux with the following composition (%) was prepared Feed materials for processing: 34.0 lead, 9.6 zinc, 1.1 copper, 12.3 iron, 10.2 sulfur, 8.4 silica, 4.1 calcium oxide. To compensate for the low calorific value of the feed, pulverized coal of the following composition, %: 42.5 solid carbon, 28.0 volatiles and 30.0 ash containing, %: 9.0 iron, 55.8 silica and 4.5 Calcium Oxide.

Coke chips were used as reducing agent, which contained, %: 85.5 carbon, 1.3 iron, 7.2 silica, 1.3 calcium oxide. During the trial, 50 tons of feed material were processed. In Table 1 are given the results obtained for the operation of the plant - comparison of prototype operating data with a proposed plant with one tuyere.

Example 2. According to the KIVCET notification invention (claim 1) test device with the parameters and conditions as in Example 1, the test was carried out in a new way. Thus, on the side wall of the gas cooler, in the flat surface of its axial cross-section, a tuyere is installed at the level of the lower edge of the partition separating the electric furnace from the melting chamber, which tuyere is inclined to the furnace at an angle to the horizontal plane, the The angle is determined by a k-factor equal to 1.2. A total of 48 tons of incoming material are processed.

Example 3. The test was carried out under similar conditions as in Example 2, except that the tuyeres were moved horizontally downwards by Δh from the lower edge of the partition separating the electric furnace from the smelting chamber, and the distance was different from the level difference of the lower edge of the partition The ratio of ΔH is 0.2.

Example 4. The test was carried out under similar conditions as in Example 2, except that the tuyeres were moved horizontally upwards by a distance of Δh from the lower edge of the partition separating the electric furnace from the smelting chamber, and the level difference between the distance and the lower edge of the partition was ΔH The ratio is 0.2.

Example 5. The tests were carried out under similar conditions as in Example 2, except that the tuyeres were inclined towards the furnace at an angle to the horizontal determined by a k-factor equal to 1.11.

Example 6. The tests were carried out under similar conditions as in Example 2, except that the tuyeres were inclined towards the furnace at an angle to the horizontal determined by a k-factor equal to 1.25.

Example 7. The tests were carried out under similar conditions as in Example 2, except that the tuyeres were inclined towards the furnace at an angle to the horizontal determined by a k-factor equal to 1.00.

Example 8. The tests were carried out under similar conditions as in Example 2, except that the tuyeres were inclined towards the furnace at an angle to the horizontal determined by a k-factor equal to 1.30.

Example 9. The test was carried out under similar conditions as in Example 2, except that the tuyere was installed on the end wall of the gas cooler tube body in the flat surface of the longitudinal axis section, and was inclined towards the furnace at an angle to the horizontal plane, The angle is determined by a k-factor equal to 1.20.

In Table 1 the test results of Examples 1-9 are given.

Example 10. The test was carried out under similar conditions as in Example 2, except that two tuyeres were installed for the supply of oxygen-containing gas, the tuyeres being located on each opposite side wall of the gas cooler. The tuyere is installed on a flat surface of the axial cross-section of the gas cooler tube body at the level of the lower edge of the partition separating the electric furnace from the smelting chamber, and is inclined to the furnace at an angle to the horizontal plane, which is determined by Determined by a k-factor equal to 1.20.

Example 11. The test was carried out under similar conditions as in Example 2, except that two tuyeres were installed as in Example 10, and the difference was that one tuyere moved a distance Δl from the axial cross-section of the gas cooler tube body, which was the same as the shaft The ratio of the inner length L reaches 0.27.

Example 12. The test was carried out under similar conditions as in Example 2, except that two tuyeres were installed as in Example 10, and the difference was that each of the two opposite tuyeres moved by a certain amount from the axial cross-section of the gas cooler tube body. distance, the ratio of this distance to its internal length -Δl/L reaches 0.20.

Example 13. The test was carried out under similar conditions as in Example 2, except that two tuyeres were installed as in Example 10, and the difference was that each of the two opposite tuyeres moved by a certain amount from the axial cross-section of the gas cooler tube body. distance, the ratio of this distance to its internal length - Δl/L reaches 0.25.

Example 14. The test was carried out under similar conditions as in Example 2, except that two tuyeres were installed as in Example 10, and the difference was that each of the two opposite tuyeres moved by a certain amount from the axial cross-section of the gas cooler tube body. distance, the ratio of this distance to its internal length -Δl/L reaches 0.27.

Example 15. The test was carried out under similar conditions as in Example 2, except that two tuyeres were installed as in Example 10, and the difference was that each of the two opposite tuyeres moved by a certain amount from the axial cross-section of the gas cooler tube body. distance, the ratio of this distance to its internal length -Δl/L reaches 0.30.

Example 16. The test was carried out under similar conditions as in Example 2, except that two tuyeres were installed as in Example 10, and the difference was that each of the two opposite tuyeres moved by a certain amount from the axial cross-section of the gas cooler tube body. distance, the ratio of this distance to its internal length -Δl/L reaches 0.35.

The plant operating data for Examples 10-16 (comparison of operating data for proposed plants with one and two tuyeres) is given in Table 2 for comparison with the data for Example 2 in Table 1 .

From the comparison of the data of Examples 1 and 2-9 in Table 1 it can be seen that the proposed device compared to the prototype allows a relative increase in direct lead recovery to crude lead of 3.03-3.06% and a relative increase in the specific capacity of the device of 0.4-0.6%. This demonstrates that direct lead recovery to crude lead and higher values of device specific capacity are achieved using the suggested tuyere mounting locations and range of inclination angles to the furnace (compare Examples 2, 5 and 6 with Examples 3, 4, 7 and 8 ).

It has also been shown that the choice of the wall of the gas cooler tube has practically no effect on the operating values of the device when installing a tuyere to supply the oxygen-containing gas (compare examples 2 and 9).

A variant with two tuyeres installed on each opposite side wall of the gas cooler body than if each of these tuyeres were in one and the same cross-section of the gas cooler body In contrast, this does not increase the operating value of the device (compare Examples 2 and 10 in Table 2).

The non-mirror-like displacement of the tuyere axis relative to the gas cooler tube body provided an improvement in the operational value of the device, but did not achieve the maximum possible additive effect in the specified task solution (compare Examples 2 and 11 with Table 2 Examples 13-15). Using the suggested range of ratios (0.25-0.30) of the distance from the tuyere axis to the axial cross-section of the gas cooler body to its internal length, the mirror-like tuyere shift relative to the axial cross-section of the gas cooler body makes The direct recovery of lead was additionally increased by 0.13% relative to the variant using one tuyere and the specific capacity of the device was increased by 0.33% relative (compare Example 12 with 13-15). A reduction of this ratio below the suggested range of 0.25 reduces the direct lead recovery and the specific capacity of the plant, bringing these values closer to the operating variant of the plant with one tuyere (compare Examples 12 and 2). Increasing this ratio beyond the suggested range of 0.30 did not lead to further improvements in plant operating data (Comparative Examples 15-16), but due to the proximity of the high temperature regions of the secondary combustion of the reactant gases in the smelting chamber to them, there was less risk of jacket thermal damage. Possibilities increase significantly.

Furthermore, as can be seen from Tables 1 and 2, the invention allows a relative reduction in the specific cost of electrical power by 6.2- 6.8% and increases the lifetime of the unit by 3-5%.

Claims (3)

1. Plant for processing powdery raw materials containing lead and zinc, comprising a vertical melting chamber with a rectangular cross-section of the combustion chamber, a gas cooler tube, with a Partition walls for water-cooled copper elements, electric furnace separated from the melting chamber by said partition walls with water-cooled copper elements, jacketed conveyor belts, equipment for the outflow of smelted products, furnace, whereby the level of the lower edge of the partition The proportion difference between the distance from the top of the smelting chamber to the lower edge of the partition separating the electric furnace from the smelting chamber reaches 0.15-0.29, and the difference between the distance from the lower edge of the partition to the furnace and the level of the lower edge of the partition The ratio reaches 1.25-2.10, with the difference that no more than two tuyeres are installed on the wall of the gas cooler tube at the level of the lower edge of the partition separating the electric furnace from the melting chamber, which are at an angle to the horizontal plane towards the furnace Tilt, the angle is defined by the following formula: α=arctg(k·ΔH/B) Where α- tuyere inclination; k-wind outlet inclination coefficient, equal to 1.11-1.25; ΔH - the level difference of the lower edge of the partition; B - Internal width of the gas cooler tube body. 2. The device for processing powdery raw materials containing lead and zinc according to claim 1, the difference is that when installing two tuyeres, they are arranged on each of the opposite side walls of the gas cooler tube body and opposite to the gas The axial cross-section of the cooler tube is shifted mirror-like. 3. claim 1, the device of the processing powdery raw material that contains lead and zinc of claim 2, difference is that when two tuyeres are installed, each of them is arranged at distance from the axial cross-section of gas cooler pipe body At a certain distance, the ratio of said distance to the inner length of the gas cooler tube reaches 0.25-0.30.

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