FI104267B - Method for Increasing the Melting Capacity of Conventional Vertical Suspension Melting, or Flame Melting, of Sulfide Concentrates, Especially in Production of Precious Metal-Rich Copper and / or Nickel Sulfide Stones or Crude Metal - Google Patents

Description

104267

A process for increasing the melting capacity of the conventional vertical suspension melting or flame smelting process of sulphide concentrates, in particular for the production of high-value copper and / or nickel sulphide or crude metal

The method according to the invention includes vertical suspension melting or so-called. promoting the heterogeneous conversion melting reactions following suspension oxidation of the sulfide concentrate as a subprocess of the flame smelting process by modifying the conventional vertical process.

By far the most important of the conversion reactions is the reaction between the solid magnetite formed as the main product of suspension oxidation and molten iron sulphide in the discharge region of the oxidation suspension, in the transition layer of the furnace pool below the oxidation zone. The witite formed as a product of this reaction forms a feed blend with silica, which in turn dissolves significant amounts of solid slag oxides and magnetite.

By promoting conversion reactions, it is possible to increase the surface area and volume equipment capacity of the thawing process substantially compared to the conventional method. These endothermic conversion reactions are promoted, depending on the 25 concentrates to be processed, mainly by: - restoring the correct sulfide / oxide ratio in both quantitative and qualitative suspension oxidation product, especially when oxidation is non-selective with respect to precious metal and iron 30 - transferring both by lowering the rate of descent and by increasing the thickness of the reaction layer 5 - by making, on a case-by-case basis, slight structural changes required to promote said reactions in the conventional melting apparatus.

The process according to the invention is particularly suitable for the preparation of precious metal rich sulfide stones and crude metal of copper and 10 nickel.

Due to the complicated mechanism of the vertical suspension melting process, the related sub-processes, and in particular the properties of the conversion reactions, and the state of the art of the sub-processes, will be examined in detail through the related patents and publications.

In the first processing step, the sulphide concentrate is partially decanted as a slurry in the reaction shaft of the smelting furnace to the extent that the shaft oxidation product obtained in the next processing step forms a sulphide crystal of precious metals. This partial oxidation process seeks to selectively decompose (for slagging) iron in the sulphide concentrate away from the precious metal sulphide. However, iron is partially oxidized to 3 -value, whereby at conventional oxidation temperatures the oxidation product mainly consists of: solid magnetite (in the case of iron-rich stones, also solid witite). The result of suspension oxidation is strongly dependent on the structure of the complex mineral containing the metal sulfide to be oxidized. The oxidation of iron of the conventional nickel mimetal, pentlandite ((Ni, Fe) 9S8), is not selective and nickel is oxidized significantly at the same time as iron. In the oxidation of nickel sulfide concentrates, the strong slagging of nickel immediately begins as 5-iron iron oxidation progresses to a pentlandite-like assembly. Copper sulfide concentrates exhibit non-selectivity for iron oxidation, particularly with cubanite, chalcopyrite, and boronite minerals (CuFe2S3, CuFeS2, Cu5FeS4), but due to their stability conditions are much less pronounced than those of nickel-10.

The formation and quality of suspension oxidation products corresponding to the manufacture of precious metal skins and rich nickel and copper sulphide stones as well as the structures, analytical and volume ratios of the resulting rock and slag phases (in production zero melting systems) have been demonstrated in: US 3,754,891, US 4,669,725, US 4,668,157 et al. / 1 /.

The reaction rates of slurry oxidation are very high / 2 /, so that the slip delay time in the oxidation shaft is also low, 20 and thus the shaft dimensions become correspondingly advantageous. The partial oxidation of the sulphide concentrate in the suspension is thus both. technically and economically a very advantageous subprocess of precious metal processing. 1 2 3 4 5 6

The oxidized suspension discharges to the melt surface of the furnace basin 2 below the suspension oxidation shaft to a rather limited area 3/3 /. This disintegrating suspension consists of a heterogeneous mixture of solids and 4: molten with 5 solids as magnetite and slag oxides and 6 as the salt phases mainly precious metals and partially iron containing sulfide phases (as separate and as alloys). The quantitative ratios of the various phases depend on both the concentration of the concentrate 4 104267 and the degree of oxidation of the concentrate required by the product sulphide rock having the desired value of the precious metal. Particularly noteworthy here is the structural over-oxidation of complex minerals required for the production of precious metal-rich and iron-poor sulfide stones, whereby, in addition to ferric oxides of high iron oxidation, precious metal oxides are produced due to the non-selectivity of the oxidation process. Due to the oxidation and disassembly mode of the concentrate suspension, the sulfur and oxygen contents of the oxidation product 10 at the time of disassembly are already fairly evenly distributed on the micrometer scale.

Substantial sulfide rock and slag formation reactions occurring in the transition region formed by the effluent suspension as the components of the oxidation products react. Of these, the so-called. the most important of the conversion reactions is the magnetite reduction reaction and the associated iron silicate formation / 3,1 /: 20Fe304 (s) + FeS (1) = 10FeO (s) + SO2 (g) (1) 10FeO (s) + 5SiO2 (s) = 5Fe2Si04 (l) (2) 3Fe304 (s) + FeS (l) + SiO2 (s) = 5Fe2SiO4 (l) + SO2 (g) (3) These reactions, which are essential for rock-slag formation, do not as such dominate the equilibrium system from the reaction equation . Analyzes of suspended samples of the oxidation product of the suspension state (magnetic and X-ray microscope measurements, Br-CH3OH liquid separation analysis, etc.) show solid magnetite to be the dominant iron oxidation product in the case of medium and high sulphide oxidation products.

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As an example of the ratios of oxidation products, in the preparation of (exemplary part) concentrates of copper and iron (by weight) of 21.00 and 36.49 sulfide stones of copper 5, 51 and 61, the iron content of the feed is oxidized with 68 and 79% conversion respectively. followed by 74 and 86%, respectively. The rate of iron oxidation in the suspension state is thus very high, in total more than 90% of the total fracture.

In particular, high concentrations of solid phases, magnetite (liq 1: 1597 ° C) and silica (tridymite, liq 1: 1723 ° C) at normal discharge temperatures of the shaft suspension are to be noted. The above sulfide rocks (51 and 15 61% Cu) have a solid phase (Fe304 +

SiO 2) to the molten phase (Cu 2 S + FeS) at 1.21 and 1.63 by weight and 1.58 and 2.20 by volume respectively. The weight percentages for molten iron sulfide are 2.97 and 5.47, respectively.

Although the conversion reaction (1) plays a minor role in the oxidation of the orbit, it touches the majority of the total oxidation of iron in the form of ferric / ferric iron conversion.

On the other hand, the solid / molten phase ratios indicate that in the rather heterogeneous suspension oxidation product system, the space conditions are by no means advantageous to the conversion process.

A: The general reaction of reactions (1) and (2), i.e. the formation of a stoichiometric caustic connector from a solid, stoichiometric magnetite and molten stoichiometric iron sulfide, at the conversion reaction temperatures, is strongly endothermic throughout the? 6104267 temperature range. The actual reaction system, with non-stoichiometric compounds and solutions, cannot substantially differ from the enthalpy values of the stoichiometric components / 4 /. In the temperature range 1493-1800 K, the reactive heat of the general reaction (3) is ΔΗ = 53.42 T + 95531 cal / 3 moles of Fe304 (4).

The reaction heat corresponding to reaction (1) in the temperature ranges 1468-1650 K and 1650-1800 K is ΔΗ = 7.02 T + 72551 cal / 3 moles Fe304 (5) 10 ΔΗ = 16.52, respectively. T + 114431 cal / 3 moles Fe304 (6)

Implementation of the conversion reactions thus requires the transfer of considerable amounts of heat to the reaction space, which in practice makes it difficult to reduce the magnetite.

In conventional vertical suspension melting equipment (LS furnace equipment), the baking suspension is discharged below the oxidation shaft by a very limited portion of the furnace pool melt surface and forms a relatively immobile reaction layer horizontally.

In the melting system, the rate of melt formation corresponding to the conversion reaction equation (1-3) should be equivalent to the discharge of the oxidation products, otherwise an unreacted solids deposit will form in the reaction zone below the shaft and the melting process will be interrupted.

The rate of reaction (1) in the reaction zone can be described by the simulating reaction equation d (NS02) dt = k [N0] 2 [Ns], where (7) N0 and Ns are the mole percentages of reactive oxygen and sulfur in the oxidation product in that portion, which does not include slag oxides (SiO 2, CaO, MgO, Al 2 O 3, etc.). The simulation reaction equation (7) is based on several tens of production and test runs. The equation satisfactorily simulates the behavior of the heterogeneous reaction system under consideration.

The reaction rate coefficient corresponding to the experimental results and equation (7) is not exactly constant but appears to be slightly increasing as a function of the oxide phase content of the gap product. However, this apparent increase in velocity coefficient results from an approximately linear increase in the reaction delay time as a function of the increase in the solids and sulfide melt fractions of the shaft oxidation product.

As a function of this, the apparent viscosity of the heterogeneous reaction mixture also increases, whereby the separation of the sulfide and oxide moieties of the mixture slows down and, at the same time, the reaction time increases.

It should be noted that domestic and some foreign chalcopyrite-15 concentrates (> 20 wt.% Cu) gave (44 test series) the value of the rate of reaction (1), k = 0.72 s and the reaction delay time equation: t, s = c (1-MeS) / MeS, where MeS is the percentage by weight of the sulfide phase of the fibrous product. Air as such or in oxygen enrichment was used as the suspension oxidant.

The productive suspension shafts had 11.62, 14.52 and 19.63 m2 cross sections.

The autogenous or controlled reduction of ferrous iron from slurry oxidation (with its associated heat requirement) is undoubtedly the most important step in the smooth process of smelting, especially in the production of rich sulfide rocks. Therefore, solutions for this processing step of some domestic and foreign smelting processes will be considered in detail.

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During the early decades of the industrial application of the vertical flame smelting process (US 2,506,557 / 12 /), thin sulfide rocks were produced and additionally at low concentrate feed rates with respect to furnace size, so there were no significant problems caused by ferric iron and 5 solid magnetite. As concentrate feed rates increase, e.g. as the suspension oxidation technique developed and the values of the precious metals in the rocks increased (45-65 wt.%), the elevated ferrous iron content, which increases the precious metal content of the slags, was continuously reduced by adding li-10 to the slag phase. cast iron scrap, lump ore, coal, etc .: US 3,790,366 / 5 /. the oxidized slag in the gas space above the surface of the fossil fuel is produced, if necessary, heat losses in the part and the deoxidating-congeal process heat required by volume.

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The process according to U.S. Pat. No. 3,790,366 / 5 / is used to make iron-poor copper sulphide stone. The amount of ferrous iron produced in the slag is reduced by reducing it above the slag surface by means of the gas phase flowing in the furnace space. The high degree of reduction of the gas-20 phase results in the sulphidation of the metals present in the suspension (Cu, Ni, Co, Zn, Pb, Fe, etc.) and these compounds. Both the direct gas reduction and the sulphidated suspension still settling on the slag surface reduce the ferrous iron slag as well as the copper content 25. The behavior of the melting system can be observed in the detailed material and temperature balances of UN 5. As a result of the sulphidation of the residual suspension of the gas phase, both the magnetite and sulphate growth troughs in the riser shaft, the boiler cucumber, disappear.

The process according to the patent is excellent for sulfidation of the residual suspension (and thus for minimizing process malfunctions), but at high feed rates it is inadequate as a ferric iron lowering agent due to the long delay time required for reduction. There is not enough reduction power for magnetite aggregates to settle on the sides of the slag and 5 stones in the furnace basin and on the bottom of the furnace. Total reduction of the gas phase of the furnace for sulfur recovery significantly increases the gas phase reduction power while improving the economics of the process.

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The process of U.S. Pat. No. 3,754,891 / 6 / discloses the preparation of an iron-poor nickel-copper sulfide rock from a pentland-dithiopyrrhotite-based concentrate by suspension melting.

The process (6.1) shows that nickel oxidizes and enters the slag phase as the iron oxidation of the concentrate advances below the iron content of pentlandite, so that iron-poor nickel sulfide rock cannot be produced without oxidation of pentlandic iron. For the reduction of both magnetite and nickel ferrite in the oxidation product 20, the process has developed a vertical zone-based shaft suspension reduction process, which results in the required product to produce a small amount of active iron sulfide for the downstream furnace reduction process. In the -25 reduction process, a narrow vertical reduction zone is formed by injecting a portion of the suspension height at the mid-point of the suspension height (after the oxidation reactions). fossil fuel. In the process description, the oxidation-reduction process is described in detail with its balance of substances and heat. The method works well if the amount of oxidation to partial concentration is adequately controlled. It should be noted that in the reduction process, the oxides and ferrites of nickel are reduced before the formation of silicate slags which are difficult to reduce (eg garnishite fusions).

The process according to U.S. Pat. No. 3,900,310 / 7/5 performs smelting of finely divided oxide and sulfide concentrates of copper and nickel into the corresponding sulfide stones. The process demonstrates that the temperature of the oxide concentrates at the top of the suspension sphere can also be technically raised so high that the endothermic reduction and sulfidation processes can be carried out in the suspension state using zone reduction (elemental or oxide sulfur addition). However, the essential function of the method is to indicate the position, nature and amount of the oxidation product discharge from the suspension and to indicate the significance of the reaction rate equation for suspension capacity and the corresponding dimension of the magnetite-sputosulfide reaction in the lower furnace transition zone. The description of the method includes a very detailed mechanism-based study of the processing of both oxide (Mala-20 chitin, garnerite) and sulfide (chalcopyrite, pentlandite) concentrates.

The process according to US 4,669,725 / 8 / is carried out by suspending and evaporating copper-dominated polymetallic complex concentrates. At the top of the suspension oxidation shaft, decomposition and release oxidation of complex minerals from the concentrate matrix and at the bottom of the shaft are subjected to band reduction of the suspension, whereupon the oxidized, solid or molten components evaporated to oxidation, solidification or melting are resuspended. As the complex minerals of the feed concentrate decompose during the oxidation phase, its copper and iron sulfides are conventionally oxidized. To reduce ferrous iron and to sulfide small amounts of copper oxide, a zone reduction 5 is produced utilizing active iron sulfide, and after conversion, a rich copper sulfide rock is formed.

The process according to U.S. Pat. No. 4,139,371 / 9 / one produces copper-rich crude metal and 10 nickel-rich, very iron poor, metallised sulphide stones in one furnace unit. In the process, the magnetite of the suspension oxidation product is reduced by zone reduction with active iron sulphide, whereby an iron-poor copper or Nickel stone and the corresponding slag phase are obtained in the furnace basin. The manufacture of Bliste-15 copper pair or metallized sulfur-poor nickel is deposited in a sulphide or crude metal bed below a suspension discharge region (conversion reaction zone) where oxygen is blown at a sufficient rate through the chimneys or flanges. Method 20 thus prevents the magnetite from being segregated on the walls and bottom of the furnace as a whole. The process uses the amount of heat generated by blasting the crude metal to fill the heat deficiency of the lower furnace due to conversion and melting alpha and heat loss. In the manufacture of raw copper 25, one can utilize e.g. a fast conversion process according to U.S. Pat. No. 4,308,058 / 30 / f, wherein oxygen blowing is carried out on the crude metal layer and the resulting oxide-sulfide conversion produces crude metal under controlled low oxygen pressure.

The extension of the furnace conversion zone is a slag reduction zone, where the Slag Slag is formed by electrical heat and a suitable slag, with the resulting slag as a return stream to the sulphide rock of the suspension melt.

The processing according to US 4,339,371 is quite advantageous energetically and process technically, but it has to be done carefully with regard to the subprocesses. A disadvantage of the process is the foaming of both copper and nickel sulphides (and metal) due to the blasting method into the slag layer / 9 /, thus increasing the need for slag treatment.

The slight increase in slag losses in the production of blister copper is of little importance, since it is preferable to carry out the slag cooling reduction (instead of the electric furnace reduction) according to, for example, US 4,304,596 / 16 /.

15 There are still some domestic proposals, both old and new, for carrying out the vertical suspension melting process.

In the process according to patent FI 56397/10 /, the temperature of 20 suspension oxidation products is raised to such an extent that its thermal content is sufficient to compensate for the furnace endothermic. the amount of heat needed for reactions, melt enthalpies, and heat losses. This method of digestion is well known in the art because it forms the basis of autogenous digestion processes.

The description of the basic manufacturing method for vertical suspension melting, FI 22694/12 /, states that roasting: sulphide concentrate in a vertical suspension (downstream, decreasing oxygen pressure and elevated temperature) with or without the use of preheated air, 13 104267, while the heat content of the exhaust gases is still sufficient to preheat both the concentrate and the air.

The height of the shaft and the so-called shaft height discussed in the description of patent FI 56397. the focus position is a function of the concentration of concentrate and product 5 (including Fe, S, and O contents) and the technical implementation of the suspension preparation and oxidation. The actual oxidation reactions are very rapid / 2 /. In the older methods FI 47380/6 / and FI 48202/7 /, the analogous nickel structure (gap height 8 m + melting distance 1.4 m) mentioned in the specification (FI 56397) is used in the production of value-rich copper and nickel stones. In said processes, the concentrate has been oxidized to the oxidation degree corresponding to the rich sulphite rock even before the half-shaft gap / melt surface distance (0.46 * total distance), i.e. quite close to the 5th and 6th ratios of claims FI 56397. Thus, in the suspension process alone, with the equipment used, the oxidation height in the above methods could be less than 4.3 m (instead of 9.4 m used). There is no requirement to shorten the gap in either method, since 20 things are generally known.

When evaluating method FI 56397, it is important to note that raising the product enthalpy by raising the temperature to produce iron-poor sulphide concentrates rich in iron-rich sulphides is not at the temperatures permitted by conventional technology (cf. DE 1.758.084 / 17,

85506/31 /, EN 54809/15 /) sufficient to cover the temperature of endothermic reactions and losses in the lower sink. This can be stated with sufficient detail from the material and temperature balances made (eg / 6 /, / 7 /, / 9 /). It is also important to note that the furnace capacity and dimensioning kinetics of the oxidation product magnetite reduction reactions have not been treated at all in the process (/ 1 /, / 6 /, / 7 /).

In the process according to patent FI 52358/11 /, 5 impure (including Pb, As, Sb, Bi, Zn) copper-enriched crude metals are prepared directly as a product of suspension oxidation. Below the suspension reaction zone, a melt is formed with only layers of crude copper and slag. In the process, the copper concentrate is oxidized to such an extent in the reaction shaft that the ha-10 petrification product (before it hits the furnace melt) contains up to 1% sulfur and 60% of its iron content is oxidized to ferric. The method is very suitable for iron-poor concentrates, mainly based on covalellin-calcosite.

Due to the iron-poor concentrates, the reduction of magnetite and ferric iron is of minor importance in the process, but the process needs to be considered due to its processing criteria.

The method according to patent FI 52358 is difficult to evaluate due to the shortcomings of the method description. These include deficient feed and product analyzes (including slag components), processing temperatures and thermal balances. The potential drawing of the method, Figure 7, lacks both the processing temperatures and the positions of the important sulfur dioxide isobars in the process. It can be noted that the thermodynamic values (/ 4 /: Janaf-Kellogg) in the Cu-S-O system give 1480 and 1279 ° C (Pb-S-O: 1348 and 1191 ° C) temperatures for the graph. The deviations of the potential drawing from the isotherm are thus so large that it is too imprecise to describe the operating limits of the method.

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Theoretically, metallic copper is formed, for example, at an intersection point of isobar, PSO2 = 1.0 atm, below the oxygen pressure corresponding to the equilibrium Cu20 / Cu from the isobar and Cu / Cu2S equilibrium. Under conditions similar to Figure 7 of the method, the equilibrium is operated at partial pressures so low that the gas phase does not have the potential to be used for the required material transfers as the delay times available. However, under operating conditions such partial pressures of oxygen are employed that oxidation of the copper sulfide to the oxide stage cannot be avoided at the relevant processing temperatures. Thus, it is not possible to produce metallic copper in a manner similar to the process, using a very conventional smelting technique. The obvious reaction path for copper formation is through the Cu20 / Cu2S reaction. Thus, in the case of Example 15 of Table 2 (Table 2), the sulfur content of the gap product would be about 3.7 wt%. Copper formation reaction site and manner play an important role in designing furnace structures along with the "patenting" because, if the metal is only formed as a result of conversion reactions in the furnace pool, the copious amount of copper oxide and oxygen-containing wettable molten metal is discharged from the furnace suspension.

The process according to FI 52358 thus returns as a conversion process to conventional, known processes for the production of crude copper, such as pioneering work / 12 / US I '20203.331 / SE 96977 and US 2,506,557 / FI 22694, and its partly analogous process US 3,674,463 / 27 /. It should be noted that T.R. Haglund's invention SE 96977/12 / has also been considered as a known pioneering process for vertical suspension melting, as well as many other domestic slurry methods: 9 /. Finally, the thermodynamics of the removal of the impurity metals at various stages of the copper production process was quite well controlled (including the prior art) / 13 / even before the invention of FI 52358.

Among the domestic applications of the slurry melting process in recent years are those disclosed in FI-B 84363, FI-B 10 84368, FI-B 94538, FI-B 91238 and patent FI 92151.

The method / 14 / of FI-B 84363 provides for the suspension melting of pyrite-pyrrhotite concentrate, iron roast and fluxes with oxygen-enriched air. As a smelting product, the process produces sulfur dioxide and / or elemental sulfur, sulfur-free fiumite slag and, occasionally, valuable metal sulfide rock.

The method description lacks a complete description of the state of the art 20 as well as the material and thermal balances required to evaluate the method. Based on the description of the method, the estimation method fully revert to the previously known domestic and foreign methods for suspending pyrite and precious metal sulphides (eg EN 22694/12 /, EN 32465/14 /, EN 25 44797/14 /, EN 45948/14 /, EN 47380/6 /, FI 48202/7 /, FI

52112/9 /, FI 54147/8 /, FI 54809/15 /, FI 58946/16 /, SE 96977/12 /).

The ferrous iron slag reduction of the slag phase is not considered further in the process.

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In the processes according to FI-B 84368 and FI-B 94538, suspension melting is prepared using nickel-rich iron-poor nickel-copper sulphide stones.

In process FI-B 84368/17 /, conventional iron-melt nickel-copper nickel-copper sulphide rock and slag containing about 3% nickel are prepared from nickel concentrate by conventional slurry melting. In the electric furnace, slag is conventionally reduced to scrap metal and metallized nickel-10 copper. The slag is fed either melted or granulated back into the flame furnace to help reduce the melt slag. The detailed material and thermal details of the process are missing from the description as well as a review of the prior art. However, the method returns to previously known domestic and foreign methods (e.g., FI 47380/6 /, FI 48202/7 /, FI 52112/9 /, US 4,036,636 / 28 /, US 3,674,463 / 27 /, US 1,758). .084 / 17 /, FI 22694/12 /, Publications / 17 /).

In process FI-B 94538/18 / an iron-poor nickel-copper sulphide idol and a nickel-rich slag are produced in a conventional smelting furnace with a conventional tex-20. The slag is reduced in the electric furnace to waste and slag. Both flame smelting and slag are suitable per se for leaching for further processing of precious metals. In the description of the method, only the method according to FI-B 84368 is mentioned as a state of the art.

The material and thermal balances required for the evaluation of method FI-B 94538 are missing from the method description. The method does not reduce the ferrous iron obtained as a sus-pension oxidation product in a sus-30 pension melting unit.

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In terms of novelty, the process returns to fully known suspension melting and slag purification techniques and the like (e.g., FI 35938/18 /, FI 47380/6 /, FI 50638/19 /, FI 52112/9 /, FI 56398/20 / FI) 58946 (16).

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In the method / 21 / of the publication FI-B 91283, the temperature and mixing efficiency of the substantially non-combustible solids particles in the suspension are raised so that the desired melting and evaporation is achieved.

In the method, the solid is fed through a diffuser from the center of the vault of the reaction furnace of the flame melting furnace to a combustion zone provided by at least three burners for slurry formation and heating of the solids. At least one symmetrical pol-15 tin set is provided at the top of the reaction shaft for melting the solids of the suspension. The behavior of the magnetite resulting from the decomposition of exemplary jarosite in a furnace basin is not discussed in the description. The method according to FI-A 910692 is also closely related to the method.

Method FI-B cannot be accurately evaluated due to the lack of examples of material and temperature, but judged both in terms of explanation and requirements, it returns to previously known methods (e.g., DE 1.052.692 / 29 /, EN 24574/21 /, EN 54147 / 8 /, FI 48202/7 /, FI 52112/9 /, FI 32465/14 /, FI 25 47380/6 /, FI 91285/21 /).

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The process according to patent FI 92151/22 / involves the melting of gypsum and iron-containing material (sulphates, sulphides, oxides) in a flame smelting furnace to give sulfur dioxide (gas phase: 4-92% SO2) and slag containing less than 1% sulfur (olive oil). 19 104267 and calcium ferrite slags). According to the method, the feed material is oxidized or reduced in the reaction shaft of the flame smelting furnace, whereby the oxidation-reduction potential of the process is adjusted by the oxygen coefficient of the fuel such that the ferro-ferro-iron ratio of the product slag requires melting at the desired temperature range. The operating range of the extremely wide range of feed and product ranges is determined to be a temperature range of 1150-1400 ° C and a slag compositing range of 10-45% CaO and a Fe + 2 / Fe + 3 ratio of 0.4 to 3.0.

10 The method according to patent FI 92151 is difficult to evaluate because the process material balances are too deficient and the thermal balances are completely absent. The examples given refer only to calcium ferrite slags, but not to complex olive slags.

The use of gypsum (as well as ferrous sulphate) for sulphidation, oxidation and sulfur recovery and for the simultaneous formation of silicate and ferritic slags is well known in the metallurgy of copper, nickel, lead, etc. in old metallurgical textbooks and in other publications / 22 /.

The structural oxygenates of ferritic slags in the process description examples are well known / 23 /. The equilibrium oxygen pressure (atm.) At 1400 ° C for the slag corresponding to Example 1 is, P02 = 1.27 * 10 9. Based on the analysis and input data provided in Example 25, an analysis of the gas phase / 4 / %): 15.38 H2, 6.39 H2S, 35.63 H2O, 21.29 CO, 0.39 COS, 14.54 CO2, 5.36 S2 and 1.01 SO2. In the gas phase conditions, the sulfides of calcium and iron would be stable, which cannot be processed as indicated in the example and method description.

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The equilibrium oxygen pressures of the slags corresponding to Example 2 are of the order of magnitude as in Example 1. The oxygen pressure of the final slag corresponding to the pyrite process is, P02 = 9.04 * 10'10. Since, according to the process description, the Fe + 2 / Fe + 3 ratio is controlled in the suspension shaft, the conditions in the reaction shaft thus corresponding to Example 1 are highly reducing and thus correspond to the stability of iron sulfide. Gasase equilibria for pyrite suspension melting and suspension sulfidation are disclosed in several patents and examples / 14, 16, 10-9 /. However, even before the oxidation of the iron monosulfide stage, the presence of ferric iron and, as oxidation progresses, a high degree of magnetic formation in the products can be demonstrated / 24 /. T. R. Haglund's method US 2,209,331 / 12 /, assigns suspension oxidation of a pyrite-pyrrhotite concentrate to a magnetite stage 15 to produce iron ore, sulfur dioxide and / or elemental sulfur. If iron ore is not desired, the method can slag iron oxides (CaO, SiO 2 addition).

The simultaneous presence of magnetite and iron sulphide in the shaft product requires conversion reactions in the lower 20 furnace, which is not required in the process of method FI 92151. However, the method description does not provide the material and thermal balance of the shaft but only the final product and overall process data. However, it is obvious that the pyrite cannot be melted as shown in the method description. 25: Further foreign suspension methods are discussed, particularly with respect to the ferrous iron reduction and the additional heat required by the conversion reactions.

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In the process of U.S. Pat. No. 2,668,107 / 25 /, nickel and copper sulphide ores are melt-suspended using the horizontal suspension melting process.

The horizontal suspension method does not use an oxidation shaft, but oxidation of the suspension is carried out in a furnace space above the rock and slag layers. Also, the oxidized suspension is discharged in almost the entire furnace basin, resulting in a reduction capacity of the resulting large-scale transition layer that is higher than the vertical methods. The heat-10 requirement for the reduction reactions is then also more easily met compared to vertical methods. In the horizontal process, the autogenicity of the process is achieved by the use of technical oxygen or oxygen-rich air in the oxidation.

In the process according to the patent, Sludge Slag is produced by melt-melting slag ferrous sulfide obtained periodically in a melting furnace in the same furnace unit by spraying molten iron as a suspension oxidation product of a pyrite-pyrrhotite concentrate.

The resulting iron-rich slag requires low concentrations of the precious metal in the wreck.

20

The method and apparatus of CA 751854/26 / A are developed from a conventional Harjavalta type vertical suspension melting process. The process produces crude copper from ore or concentrate in one unit. In addition to the conventional suspension oxidation shaft (I), the Me-25 method has another suspension oxidation shaft (II) with a riser shaft located between these shaft. In the second shaft (I), the copper concentrate is oxidized to form a rich copper rock and a precious metal and ferrous iron rich slag phase in the furnace.

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In the second shaft (II), the pyrite-pyrrhotite concentrate is oxidized to an iron sulphide rock, by means of which the aforementioned slag is reduced and sulphidated to a waste slag and slag. The slag flows under a sloping furnace bottom (upstream of the slag-5 phase) below the shaft (I), where a small amount of iron still contained in the shale is blown by blowing through a duct placed in the rock layer. The product stone flows through the Arutz saphon into the space outside the suspension furnace, where it is blown with raw copper. In the process, the slag reduction already touches the entire slag phase and not the solid and melt phases of the ferrous iron discharge site, prior to the actual slag formation.

The process of U.S. Pat. No. 3,674,463,27 / 27 performs smelting and conversion of copper concentrate to crude metal, and additionally controlling the formation of ferrous iron in suspension mode in a vertical shaft in an almost conventional slurry furnace unit.

The method adjusts the oxygen to feed sulfide ratio so that 35 to 75% of the feed alloy copper in the suspension is converted to metal. This metal is mainly formed as a result of the oxidation of the rich rock. The oxidation of the concentrate produces rich rock which is fed back into the suspension shaft via the rich power divider. Copper as well as stone and slag phases 25 are continuously removed from the furnace. According to the method, concentrate or iron sulfides are fed to the lower part of the suspension shaft. According to the disclosure, the additional spray concentrate acts as a shield against high oxygen partial pressures which would otherwise cause magnetite formation. The slag layer under the shaft is required to dissolve any magnetite formed which has not already been reduced by the low oxygen 23 2324267 zone just above the slag layer. In the process description, only one processing-related temperature, 1200 ° C, is given, which is the approximate temperature of the gas phase of the reaction shaft.

5 It can be noted that there are no preconditions for the production of crude copper in the reaction pit in the conditions described in the process description. This issue has been addressed in method FI 52358/11 /. It should be noted that the difference in equilibrium oxygen pressures at 1227 ° C is only 4.44 * 10 "6 atm in chalcosite-10 cuprite-copper and calcosite-oxygen-copper equilibrium, so that the cuprite reaction is difficult to avoid. in suspension mode to reduce to the maximum solubility limit due to extremely short delay time.

15

In the process of US 4,036,636 / 28 /, the precious metal content of highly oxidized slags or similar minerals is recovered by reducing these slags in a single or multi-stage electric furnace reactor. The slags are slags and intermediates of high-value, stable-rich nickel and nickel-copper rocks or crude metals, having high oxidation (7-30% Fe304), slurry and shaft furnace processes and conversion processes. The slags are reduced by metal, silicides, carbides, sulfides, carbon, etc. The reducing agent and the slag melt are mixed in a reduction reactor (electric heat) with a mechanical stirrer, whereby the rate of magnetite reduction is strongly accelerated. The reactor produces a sulphide rock containing precious metals in addition to the wreck, which is fed back into the melting furnace of the slurry and the like (Example-30 balances in the description). The temperature of the slag in the reduction mixture is in the range of 1200 to 1250 ° C.

24 104267

Suspension methods based on cyclone oxidation and thawing are briefly considered. In these processes, the oxidation of polymetallic sulfide concentrates is usually performed with technical oxygen at very high temperatures in horizontal or vertical cyclone devices / 29 /. In a cyclone, the suspension oxidation product is directed to the cyclone wall where a large part of the reduction and other conversion reactions take place. The product components undergo close contact and mixing in the cyclone 10, whereby the conversion reactions are effected efficiently, and no transition layer limiting processing and device capacity is formed. The cyclone is located horizontally and vertically at the top of a shaftless and shaftless furnace basin, whereby a partially oxidized product already reacting to the rock-slag separation flows through the dam wall facing the cyclone (as the dam wall promotes the conversion of residual reactions). Cyclone processes and equipment are followed by conventional clarification, slag purification and side metal recovery processes and equipment.

20 Cyclone smelting processes have undergone vigorous development and a large number of applications have emerged. Almost all applications require electric furnace equipment for the heat demand of sub-processes following a cyclone.

Examples of intermediate forms of cyclone and cyclone and free-flow suspension methods include those described in DE 1,052,692, US 3,555,166, US 3,687,656, US 3,759,501, US 4,247,087 and FI 91285.

There are some interfaces to the conversion reactions of slurry smelting processes as well as to the processes for the production of crude granule / 6, 7, 9, 30 / in the refining process for precious metals according to US 4,252,560 / 31 /. The patent process is not a slurry process, but the oxidation and melting of sulfide ores is carried out by "smelting in melt" in an extended shaft furnace-like apparatus with a flue level 5.

According to the process description and Example 1, the process of US 4,252,560 has features such as: - The dimensions of the furnace are: 2.5 * 8.0 m2 and height 7.0 m. The furnace is divided by end walls and siphons into 10 compartments of sulfide stones, for the separation and processing of precious metals and crude metals.

- Furnace capacity: The feed mixture (20% Cu) at 66.6 t / h (80 t / m2 * 24 h) produces rock (50% Cu, 1200 ° C) 26.5 t / h, slag (0.4% Cu, 5.0% Fe 3 O 4, 32% SiO 2, 1250-1300 ° C) 26.7 t / h and gases (40 vol% SO 2, 1300 ° C) 18000 Nm 3 / h.

The amount of oxygen-enriched process air (60 vol% O 2) is 21000 Nm 3 / h and the nozzle velocity of the flue air is 230 m / s. The amount of additional fuel (natural gas) is 2100 Nm3 / h.

- The surface heights of the feathers are: rock melt 0.75 m, slag melt 2.5 20 (2.0) m; the flue level is 0.4 m below the surface of the (Pacific) slag layer.

- Processing: The ore, concentrate and, if necessary, the coke are fed through the furnace roof vault to the surface of a "sparkling", gas-saturated heterogeneous melt (height 1.5-2.2 m from the chimney level, 25 1350 ° C) where it oxidizes and melts. The melt contains about 10-30% by volume of sulfides and the rest of the slag. Reaction gases cause effective mixing of the reaction components into larger, rapidly falling droplets of fine sulfide droplets. Any additional fuel (carbon dust, natural gas, etc.) that may be required to achieve the system temperature economy is fed into the heterogeneous melt through the concentrate oxidation chimneys.

The evaluation of the method according to US 4,252,560 is hampered in particular by the lack of description of the rock and slag analyzes, e.g. iron and sulfur concentrations. Under conditions similar to Example 1, oxidation (1350 ° C, iron silicate slag, Fe 304 and SiO 2 impregnation: 41.9 Fe 3 O 4 (28.9% Fe 2 O 3, 30.4% SiO 2) can be obtained by oxidation of the final slag (5% Fe 3 O 4), 32% SiO 2). 10 oxidation slags with a maximum oxygen content of 25.9 kg per tonne of slag (other than iron oxides and silicic acid) The amount of oxygen required is approximately 178 kg per tonne of feed mixture, thus providing a very large amount of 6 However, it is evident that a significant part of the oxidation of the sulphides is effected by the gas phase. caused by precious metal oxidation as well as providing a remarkably effective blend sulfide melting-oxidation zone. 1 30

From the examination of the prior art, it can be noted that, except for some domestic methods, the transition layer and related conversion reactions of the application have been treated very little in the context of suspension methods.

27 104267

Characteristics of the novel process combination according to the patent application are: The sulfide concentrates of nickel and copper are oxidized in suspension mode in the reaction shaft of the vertical process (Figure 3A) using conventional techniques. In order to prepare the oxidation product corresponding to the rich sulfide rock, especially in the processing of Nikke lime concentrates, the formation of nickel oxide and ferrites, as well as magnetite, is noteworthy as the oxidation of the iron sulfide proceeds and its activity in the molten sulfide alloy decreases.

The suspension oxidation product discharges to the molten surface under the reaction shaft in a rather limited area of this melt surface and forms a heterogeneous melt (Fig. 3A, 7, 9 /), which is characterized in particular by the high amount of solid components (Fe304, SiO2 / MgO, . Due to the manner of oxidation and deprotection, the sulfide and oxide components of the oxidation product are well mixed at least on a macroscale scale.

After disassembly, the oxidation product begins with the said product. reactions between components that are unbalanced under conditions, and slag and rock formation reactions. When the solid magnetite and the molten iron sulphide react with each other, a product of witite is reacted which reacts with the solid silicic acid and a fused lithium melt is formed. This melt dissolves both magnetite and iron sulfide as well as slag components. Also in the faija-30 distillate, ferric iron begins to be reduced and equilibrated with respect to its environment. The speed and heat demand of these endothermic conversion reactions determine the melt formation and thus the capacity of the melting system as a whole.

Particularly in the processing of pentlandite nickel concentrates, but also many copper concentrates, due to the non-selectivity of oxidation, the oxidation of iron bound to complex minerals in the suspension results in simultaneous oxidation of the precious metal. As a result, in the production of precious metal rich sulphide stones, a considerable part of the precious metal contained in the concentrate is transferred to the slagase. To overcome this drawback, using the zone reduction method (6, 9), the required amount of high-active iron sulfide in the slurry is prepared from the shaft oxidation product to reduce the precious metal / the dissolution. 1 2 3 4 5 6 7 8 9 10 11

After the oxidation suspension has been discharged, the 2 conversion reactions in the oxidation product are limited by both their speed and the considerable heat demand due to endothermic heat. Using conventional melting technique 4, the high viscous conversion reaction layer is horizontally almost immobile and vertically (gravitationally) movable as a function of the amount of rock-slag generated 7. The mixing conditions both in the layer 8 and between the layer and its slag phase 9 are thus quite unfavorable.

10

With high iron and slag component quantities in the feed mixture and high value metal sulphide rock to be produced, higher heat quantities must be introduced into the conversion reaction layer to meet the heat requirements for endothermic reactions and for the melting and dissolving of the slag components. Bringing sufficient heat to the conversion reaction layer 5 by raising the temperature of the shaft oxidation product is not possible using the temperatures permitted by furnace technology (conventional iron-rich concentrates in high-capacity processing). On the other hand, the heat content of the gas phase of the suspension cannot be transferred during its short delay time in the lower furnace space when using a sufficient amount of heat, with a moderate temperature gradient. In an electric furnace generally located in a slurry furnace lower furnace basin for the purpose of slag reduction, very high local temperature points (as well as mixing material streams) can be obtained to cover the processing needs of processing. However, the required heat output to the conversion reaction layer cannot be transferred in this way unless the electrode location is changed to or near the conversion reaction layer.

Close to the solution of the heat transfer problem is undoubtedly the method according to the aforementioned crude metal manufacturing method / 9 /, where mixing of the conversion layer with the slag melt below and heat transfer is effected by passing hot reaction gases of rock conversion through the (rock) slag melt. However, in the process, the mixing and heat transfer only affect part of the reaction layer. The product gas phase of the process also has high capacities as follows:. great that the very fine foaming of the sulphide rock into the slag phase occurs considerably and slag problems arise. In the method, the reaction gas phase is contacted with a sulfide rock, whereby its oxidation degree decreases and moves towards equilibrium / 33 /, Ps02 = 1 atm., T = 1573 K, PO2 = 2.23 * 10'® 30 104267 atm / O% Cu , 3.31 * 10'8 / 50, 6.17 * 10'8 / 70) to prevent oxidation of the slag.

The effect of another factor limiting the melting capacity 5 of the vertical suspension melting process, the magnetite-iron sulfide conversion rate in the system, has already been discussed at the beginning of this process description. The rate of the heterogeneous conversion reaction can be simulated with the empirical rate equation / 7 /. A laminar conversion reaction movement corresponding to a conventional vertical suspension portion-10 charge yields a maximum conversion rate for the melting capacity of the copper concentrates of AFe304 = 125-135 g / m 2 * s. Exceeding this conversion rate corresponds to concentrate feed rates, the ferric iron content of the slags rises sharply, and at the same time the unreacted oxidation product begins to accumulate in mm. part of the furnace basin under suspension shaft.

Based on the observations of the new process, the conversion rate can be increased by 2 to 3 times by causing the conversion layer to disintegrate and mix with the 20 slag melt below. Simultaneously, melting and dissolving of the slag components can be accelerated sufficiently to correspond to the increased conversion rate.

From the material balances of Example I (A, B) of this method description, it can be noted that in the preparation of iron poor (2.5 / 2.6% Fe) nickel sulphide stone using conventional suspension oxidation (oxidized + zone reduction), 92.6 ( 90.5) and 90.0 (84.2)%. The solids content of the suspension oxidation product (metal oxides + slag oxides) is 88.2 (83.1)%. In the conversion reactions, magnetite 69.3 (81.5) 104267% is converted from the oxidation product. In the zone reduction, the magnetite content of the oxidized shaft product is reduced by 2.2% and the amount of iron sulphide increases by 29.8%. It can be noted that the changes in the components of the balance due to zone reduction in the production of high-value nickel-rich nickel are quite small but significant both as a slag loss reducing agent and as an enhancer of nickel intake in the sulphide rock. Both in the oxidation of the suspension and in the oxidation-reduction the solids content of the formed fibrous product is very high. Although the amounts of reactive oxygen and sulfur are relatively uniformly distributed in the discharged suspension due to the oxidation mode, due to the defective contacts between the low iron sulfide phase and the large magnetite phase, (especially when using large capacities).

Several methods known per se are available for mixing the conversion layer and transferring the required amount of heat. The choice of these depends on the quality of the concentrates, intermediate and end products, melting capacity, equipment technology, etc.

The method description has previously discussed raising the temperature of the gap pension (oxidation product + gas phase) to cover the temperature requirement of 25 lower furnaces, and bypassing electric and mechanical heating and reducing agent mixing methods / 9, 10, 11, 28, 29, 17, 18 /.

The cheapest way to effect heat transfer and mixing in the conversion bed is to oxidize the fossil fuel and blast the hot combustion gases (or fuel and oxygen) at a sufficient rate (surface blast) to the slag layer 32104267 or below. In the corresponding reaction blasts, high blast rate values (at least sound velocity in air, i.e.,> 338 m / s / 9, 30 /) have been used for high melt heights at high melt heights, but the lower blast speeds due to low slag melt density and low bed height.

It should be noted that especially when blown into the slag phase, below the conversion layer, ferrous iron from the slag phase can also be oxidized with good efficiency and the oxidized slag phase used to oxidize the residual iron of the sulfide rock / 9, 30, 31 /.

When using electric heat for transfer of energy (submersible electrodes and ohmic heat), the mixing of the conversion layer can also be carried out with inert gases as both surface and permeation blasting (side flues, wear flanges, etc.). Vacuum and vacuum buoy flow methods / 34 / can be successfully used especially for heat transfer and mixing of the slag layer below the conversion layer. The resistor, arc, or graphite radiator apparatuses are then housed in a lifting chamber.

Low temperature (5000-8000 ° C) plasmatron equipment (N2, CH4, 25 02, etc. / 34 /), which is significantly more efficient than the resistance and arc systems, can be used for both heat transfer and efficient mixing in the conversion layer (surface blowing analogue). easier to fit.

One of the apparatus combinations used to carry out the process of the present invention, shown in Figure 3A, has a siphon wall (7) fitted to an oven basin that separates the slurry and conversion reaction region (31) from the slag cleaning section (4). In the process, the surface heights of the phases are kept constant, so that the extraction of the smelting products is continuous. Under practical conditions, the slurry discharge area is about 5 to 1 to 2 times the cross-section of the vertical suspension flow, and most of it is located between the suspension shaft and the slag-siphon wall.

The slag melt resulting from the conversion reactions mixes with the slag bed of the furnace basin, and the sulpho-10 disula separated from the slag, with continued conversion and equilibration, sinks through the slag melt (32) and merges with the rock melt (33). Effective mixing of the conversion layer (31), in addition to increasing the number of oxide-sulfide contacts, promotes the integration of the finely divided sulfide droplet into sinking large droplets. The finished sulfide rock can be lowered from the furnace through the furnace space (5) separated by a siphon wall and oxidized to the crude metal either by surface blasting or blasting through the crude metal in the furnace space (5) and lowered from the furnace through the furnace space (6).

In the application of the method corresponding to Figure 3 (feed rate 60-90 t / h), the molten surface heights measured from the bottom of the furnace are: 3.0 m slag surface, 1.2 m stone surface and 0.4 m metal surface. 35 m and metal channel 0.10 m. The figure shows some positions of the 25 granite electrodes (8) and the heating-mixing chimneys (9), which can be changed if necessary. The flues may also be effective side blow flanges submerged in a furnace vault, according to U.S. Pat. No. 4,413,816 / 35 /. The positions of the fuel feed pipes (10) of the zone reduction process 30 are also shown in Figure 3. It should be noted that the minimum dimensions of the suspension shaft of the apparatus are: 4.2 m 34 104267 and height 8.5 m and the minimum spacing of the vault is 1.9 m. The furnace equipment is, except for minor modifications, conventional technology known per se. Parts of the furnace system may be removed as needed: In the refining of nickel concentrate, the raw metal part (6) of the furnace is redundant if the Nikke liquor is dissolved in further processing. The remaining iron in the stone can be oxidized by slag utilizing heating-mixing chimneys. In the processing of copper concentrate, the electric slag cleaning section (4) may be unnecessary if the slag precipitation cooling is programmed and the precious metal is separated by flotation / 16 /.

In order to clarify the processing methods for sulfide and oxide concentrates of copper and nickel, the relationship of these metals to iron to sulfur and oxygen is briefly considered. Copper metallurgy is dominated by the large solubility hole in the Cu-Fe-S system. The molten crude metal is still in equilibrium with the copper-rich molten copper sulphide, but is almost insoluble (separates, deposits). The system 20 Ni-Fe-S lacks such a solubility opening (also for copper-containing systems on the technically important copper-poor side), so that the production of crude metal is quite complicated compared to copper.

The stability ranges of the molten Cu-Fe-S-O-SiO 2 system / 13, 36, 25 8, 9, 30 / at 1250 ° C as a function of oxygen and sulfur pressures are shown in Figure 1. The figure shows SO 2 isobars, certain high concentrations of copper in the copper, as well as the limits of the magnetite activities of SiO 2 saturated faience slags. The limits of metallurgical treatment of copper concentrates can be directly observed from the drawing.

35 104267

Figure 2 shows the stability ranges of the Ni-S-O system as a function of sulfur and oxygen pressures at 1727 ° C, 1477 ° C and 1227 ° C. The figure shows the sulfur isoconcentrations of some molten compositions and the 5 SO2 isobars corresponding to the reference temperatures. It can be seen from the figure that when conventional flash melting temperatures (<1455 ° C) are applied, it is quite difficult to reach low sulfur concentrations at a single atmosphere SO 2 pressure.

The new method for adjusting the capacity of a vertical suspension melting process according to the invention is also described in the first claim, the content of which is also included in the present review.

15 The details of the new method for adjusting the vertical suspension melting capacity are given in the accompanying examples concerning the processing of nickel and copper concentrates. 1

eXAMPLES

In order to clarify the new process, its implementation will be examined in some examples of the processing of sulphide concentrates of nickel and copper. The material and thermal balances corresponding to the examples are summarized in Tables 2-5. Analyzes corresponding to the numbered balance sheet components as well as total enthalpy values are shown in Table 1. The enthalpy values of the gas phases obtained directly from the thermodynamic tables / 4 / are omitted from the table. The effect of temperature changes on the balance sheets of the examples is thus easy to estimate, if necessary, in the vicinity of the temperatures indicated on the balance sheets. This is required at 36 104267 mm. for the evaluation of the effects of changes in the heat losses caused by the device-specific and cooling systems controlling the sub-processes. The heat balance effect of circulating airborne dust is low in the present case studies, so the effect of changes in the amount and composition of flight-5 in the balance sheets has not been assessed.

Example I A and B

In the embodiment of the process of the invention shown in Example I, the preparation of iron-poor nickel is carried out using conventional nickel concentrate suspension-oxidation (A), suspension-oxidation-reduction (B) processes. After the suspension has been discharged, the resulting conversion layer is decomposed and mixed with the slag phase below the layer, e.g. using surface gas blasting. In the method shown in Example IA, iron-poor nickel limestone is prepared using conventional suspension oxidation techniques. However, in order to make an iron-poor stone, 20 of the sulphide iron in the concentrate must be oxidized to such an extent that also (calculated) part of the iron in the pentlandite mineral gets into the oxidation product. Due to the activity conditions of the sulphide melt, a high amount of nickel is also oxidized, resulting in a rather nickel-rich slag phase as the end product of the conversion reactions, in addition to a small amount of iron-poor rocks. From the material balance and analyzes, only about 45% of the nickel in the feed is obtained in the sulphide rock, with a nickel content of 3.4% in the slag. The oxidation product has an oxide to sulfide to weight ratio of 9.7, which is not advantageous for conversion reactions. It should be noted that the oxygen content of the oxidizing air was 23.7 wt% O2 and the sulfur dioxide content of the gas phase 104267 was 28.1 wt%. The balanced oxygen pressure of the slag-rock system was, PO2 = 1.63 * 10 7 atm (1250 ° C).

In order to improve the nickel intake and reduce the nickel content of the slag, more active ferrous sulfide must be introduced into the oxidation system for conversion reactions. According to Example IB, a partial reduction-sulfidation method of iron sulphide is used to prepare iron sulphide, after which, after oxidation reactions, the suspension is sprayed, usually from three nozzle stations, with crude fuel (here 10 naphtha: 84% C and 16% H). . According to the material balance, the yield of nickel in the sulphide rock after the reduction-conversion reactions rises to 85%, and the increase in the amount of stone is 95% compared to the oxidation process of Example IA. The ratio of oxide to sulfide in the shaft oxidation product decreases to 5.9. According to mine product analyzes, the reduction will only increase the amount of iron sulphide used for magnetite conversion (compared to oxidation) by 6.9 kg (per tonne of concentrate), which is low. Due to both the direct reduction and conversion of the oxidized nickel and copper oxides and ferrites, the suspension reducing product is, in its origin, more analytical than the fiber product and gas phase assay values. After suspension reduction, the average gas phase analysis (vol%, 1350 ° C): 0.76 25 CO, 0.01 COS, 2.71 CO 2, 0.31 H 2, 0.09 H 2 S, 3.55 H 2 O, 1.64 S 2 , · · · 9.74 SO 2 and 81.20 N 2. The nickel content of the product slag phase and the oxygen pressure are 0.91% Ni and P02 = 2.62 * 10 &gt; 8 atm (1300 ° C). From the temperature balances, there is a significant balance (139 Mcal ri-30 per dewt) in the conversion processes of Part IA and IB. Thus, the amount of heat corresponding to the equilibrium deficiency must be introduced into the conversion layer, in addition to mixing the layer and the slag matrix portion below it, both of which can be performed simultaneously by high-speed, hot (additional fuel) combustion gases. Because of the low heat transfer efficiency and the relatively modest mixing efficiency, the molten surface blasting process is weaker than the blasting process, but due to the thin conversion layer mixed with the slag molten, the amount of wood blasting process can be used. However, utilizing the ohmic resistance of the slag, the melt must, in addition to the thermal flows, be further mixed with gases (or mechanically). The balances in Table 2 include mixing and heat transfer using fuel gases. In this case, at a feed rate of 15 concentrates at 40 t / h, the amount of gas available for mixing in the conversion zone is 616 Nm / m h.

The sulphide stone obtained as the product of each of the oxidation-conversion processes (A and B) is per se refining, but the smelting slags are purified by conventional means in a furnace or separate electric furnace.

Example II A, B and C

In the process embodiment of Example II, a suspension oxidation product of precious metal-poor nickel and similar slag is initially prepared using conventional nickel-rich thawing techniques (A). Further processing of the resulting suspension acidification product into a precious metal rich sulfide stone 39 104267 is carried out to prevent overoxidation by means of a pre-oxidized slag (B) in a downstream basin, in the bulk discharge region (conversion reaction zone). After the rock-slag separation, the resulting sulfide rock is oxidized to a low sulfur-5 nickel fines (C). The smelting slag phases are reduced to conventional slag and slag using conventional electric furnace technology.

In the sub-process shown in Example IIA, a ta-10 conventional suspension oxidation process is prepared using nickel-enriched iron-rich sulphide rock and the corresponding precious metal slag. From the balance sheets 1 and 3 of the tables it can be seen that the nickel yield in the sulphide rock is 91% of the feed. The slag has a nickel content of 0.6% and a corresponding oxygen pressure of P02 = 4.52 * 10 »B atm (1250 ° C). The feed and product gas concentrations were 25.5 wt% O2 and 30.4 wt% SO2. It should be noted that the magnetite content of the shaft product is quite high, i.e. 42% (Example IB: 48%), respectively, and the magnetite content of the conversion reaction is 33% (IB: 39%). the iron content of the product stone is high, i.e. 29.5% (in Example IB, respectively: 90.5% and 2.6% Fe).

In the sub-process of Example IIB, the oxidation of the residual iron of the sulfide rock corresponding to the pre-25 IIA (in part also the corresponding suspension oxidation product) is carried out with a molten pre-oxidized slag phase, Ferri-Ferro iron conversion. In the conversion methods of Examples IA, B and IIA, the desired amount of iron bonded to the sulfide of the suspension oxidation product is oxidized with solid magnetite, thus also utilizing fer-ferro iron conversions. The process is 40 104267 almost completely selective for iron, i.e. the sulfides of copper and nickel are left unoxidised. Magnetite conversion methods consistently produce faienceite which dissolves e.g. part of the conversion magnet, so that part of the sulfide iron ha-5 will be disappointed in the resulting slag melt, even with Ferri-Ferro-iron reduction. The selective oxidation process is thus the same for both molten and solid phase operations. In the case of Part II IIB, the pre-oxidation of the slag phase to the soluble ferric iron content is carried out using as much as 10 of the naphtha oxygen (under the conversion layer) oxygen air blast. The oxidation product slag and any additional fuel oxidation product gases are mixed with a slurry oxidation product (and / or conversion stone) to provide effective contact between the reaction components. The technique of blasting stone, metal and slag blasting has been investigated and sufficiently tested: blast speeds in the supersonic speed range, bubble size and number, agitation power, etc .: mm. / 9, 30, 35 /.

The analyzes of the oxidation method shown in Example IIB, as well as the material and heat balances, are shown in Tables 1 and 4. Matrix slag (32) is oxidized with oxygen-enriched air to magnetite impregnation at a temperature range of 1350-1400 ° C (pure iron silicate slag, 1400 ° C. : 36.0 FeO 5 + 36.2% FeO + 27.8% SiO 2). The amount of oxidation product gas phases used for mixing the conversion reaction layer 25 (30) and the oxidation slag (32) is obtained with a concentrate feed capacity of 40 t / h, respectively: 107 and 528 Nm 3 / m 2, i.e. a total of 635 NmVm 2 h. 30 The oxidation of the slag and the auxiliary fuel is performed by means of horizontal or vertical flue openings (eg 2 * 4 pieces, nozzle 104267 speed 250-300 m / s) about 30 cm below the molten surface (height depending on technology and amount of oxidation required). The thermal balance (Table 4) also shows the amount of effective matrix slag (37) which, in electrically ohmic heat, produces a heat balance balance (II B: 118 Mcal per tonne of concentrate.) However, in addition to the amount of slag oxidation product gas, the minimum amount is about 250 Nm3 / m2 h.

Analyzes as well as material and thermal balances corresponding to the sub-method of nickel finishing as shown in Example II C are shown in Tables 1 and 5.

Reduction of the sulfur content of iron-poor sulfide rock (Ib, IIB) corresponding to nickel concentrate feed capacity (40 t / h) to or near the crude metal level is accomplished by conventional techniques either by spraying the surface of the coal melt or by inert gas (oxygen enriched air). As well as in the production of crude copper, rapid metal phase controlled oxidation can also be used, where the oxidized metal rises to the rock layer / 30, 9 /. The oxidation is carried out in a stone space separated from the melting space of the furnace device by a siphon wall or in a completely separate apparatus. In the example, the sulfur content of the nickel limestone is reduced to 5.5% by blowing with oxygen at a product temperature of 1450 ° C (PsO 2 = 1-0 atm). When using 25 higher product temperatures or a lower SO2 isobar, the amount of sulfur in the melt can be reduced to the desired value according to the stability drawing (Figure 2). Significant amounts of heat produced by the process can be observed from the thermal balance, which can however be controlled by raising the melt temperature, increasing the heat loss (cooling system) and partial oxygen control in the oxidation.

42 104267

The position points of the "rock-slag equilibria" of the partial examples are plotted in Figure 1.

Examples III, IV A, B, C and V

Examples III, IV and V consider suspension oxidation and conversion processes of chalcopyrite concentrate in the preparation of sulfide stones containing 51, 61 and 72% copper.

The actual subject is the preparation of sulfide rock containing 61% copper content using suspension oxidation and conversion processes (IV). The suspension oxidation product (and / or conversion stone) from the smelting process is further oxidized using pre-oxidized slag melt and ferri-ferro-iron conversion to iron poor copper (IVB).

The resulting precious metal-rich, iron-poor sulfide rock is further oxidized to crude copper (IV C) using gas oxidation. 1 2 3 4 5 6 7 8 9 10 11

In the conventional vertical flame smelting process, the conversion reaction layer 4, which is rich in 3 solids (SiO 2, Fe 3 O 4, CaO, MgO, etc.) formed by the 2 suspension oxidation product, is substantially immobilized vertically and horizontally with respect to the slag melt below.

6

Only the bubbling of the small amount of sulfur dioxide produced by the conversion reactions and the slow deposition of the precious metal sulfides through the slag melt to the bottom 9 of the slag melt interferes with the calmness of the layer. It has already been stated in Method Description 10 that the rate of heterogeneous reactions in the conversion layer can be simulated with sufficient accuracy by a simple third-order rate equation, 43 104267 d (SO 2) / d t = k [NO] 2 [N s]. As the feed capacity of the melter rises too high relative to the rate of the conversion reactions, the accumulation of the discharging semisolid suspension oxidation product on the surface of the conversion reaction layer, just below the suspension-5 ounce, stops the melting process. The limit capacity for the production of medium-rich sulphide rocks (about 20% of copper-rich concentrates of iron), per surface area of the conversion layer, in terms of the amount of magnetite to be converted, is about 130-140 g Fe304 / m2 s.

10

According to the control method under consideration, the amount of convertible magnetite can be increased by multiplying it by breaking the rigid structure of the conversion layer and mixing the layer with the top of the slag melt underneath. Mene-15 system improvement is based on e.g. key improved contact between sulfide and oxidant, increased contact surface, increased reaction delay time for conversion reactions, increased solubility rate of solid components, and accelerated heat transfer. Covering the heat requirements of conversion reactions, melting of reaction components, and Liu-20 lubrication, which is an absolute prerequisite for the above improvements, is accomplished, for example, by electrically heating the oxidation product-slag melt system and / or by combining oxidation of the additional fuel with blending gases. Blending can be accomplished by blowing the blending gases at high speed (nozzle: 250-330 m / s) to the surface of the conversion bed or. * '· About 200-500 mm below the surface of the slag melt. In Example IV

The process embodiment shown in B employs the latter process because the suspension oxidation product (and / or conversion stone) is further oxidized by a pre-oxidized slag melt, which is at the same time a conversion bed blend melt. In addition to the amount of heat generated in the pre-oxidation of the above alloy, additional heat is introduced into the system by oxidation of the additional fuel. The blending gas thus consists of the sum of the product gases of the slag pre-oxidation and fuel oxidation.

The slag phase (IV B) corresponding to the rich sulphide rock is reduced in the electric furnace to a waste and slag stone by conventional techniques or is subjected to a cooling-reduction-sulfidation-flotation process according to FI 58946 or equivalent. Both slag and slag copper process 10 slag are fed as a circulating load back to the smelting unit.

The mass and thermal balances and component analyzes corresponding to the sub-methods of Example IV are shown in Tables 4, 5, and 1. The suspensory oxidation product, rock, and slag analyzes corresponding to Pre-15 Examples III and V are listed in Table 1. (Nos. 50-52).

Some of the relevant substance and temperature values associated with suspension oxidation and the subsequent conversion process are summarized in the table below from Examples IV A, III and V.

Example IV A III V

Conversion Stone: Cu, wt% 61 51 72 25 Oxidation Gas: O, wt% 26.9 29.8 25.4

Product gas: SO2, wt% 33.9 37.5 32.0

Total Iron Oxidation,% Suspension Oxidation 79 68 88 Conversion 86 74 95 30 Conversion Rate Constant: 103k, s 1 0.73 0.62 0.99 104267 Quantity: Fe304, g / m2s 131 133 145

Slag Oxygen Pressure: 108Po2 / atm (1250 ° C) 2.93 0.895 4.56 5 From the values in the example table, it can be stated that the oxidation of the suspension is very high in the oxidation of total iron. It should also be noted that increasing the rock content already reduces the conventional oxygen technology (masonry shaft, water-film cooling on the outside of the furnace jacket) to greatly enhance oxygen enrichment in oxygen. However, this can be remedied by selecting the suspension shaft cooling system, if necessary. The table also clearly shows that the preparation of rich sulfide rocks using vertical suspension oxidation alone is not particularly advantageous due to growing slag problems 15 and unfavorable thermal reasons. The advantage of further refining the ferri-ferro-ferro-iron conversion in solid and molten state, corresponding to the medium-rich sulfide rocks, is obvious.

20

In the method variation shown in Example IV, the concentrate feed capacity is 17.95-18.32 t / h. The effect of concentrate feed rate (18-33 t / h) on the process in the case where the conversion layer following oxidation is of a laminar, rigid and immiscible nature is partially calculated in the table below.

Level A40 - A41 - A42 - A43 - A44

Concentrate Feed: t / h 18.3 20.7 23.8 27.8 32.9 30 Sulfide Rock: Cu,% 61.0 60.4 59.7 59.2 58.6 46 104267

Oxygen pressure: 108PO2, atm (1250 ° C) 2.93 16.4 69.2 258 892

Slag: Cu,% 1.7 2.6 3.8 5.3 7.2 5 Fe304,% 13.3 17.6 21.7 25.8 30.0

It can be seen from the table that the increase in capacity in the laminar conversion layer is followed by a relatively rapid increase in the ferrous slag iron and their structural oxygen pressures 10 and copper contents respectively. The values in the table are based on only a few individual events, but they are quite indicative. Controlled bed mixing and heat transfer to the bottom of the furnace basin, the conversion bed area, will return controlled product values to the system at high-15 concentrate feed rates. Further oxidation of the selective suspension oxidation product of Example IV with pre-oxidized slagase provides, with a concentrate feed capacity of 60 t / h, additional fuel quantities (conversion and melt oxidation heat equivalent amount of 1,800 Mcal / h) for both fuel gas and fuel gas Oxidation air: 0, w / w 23.18 50.0 99.0

Additional fuel: kg / h 19.0 9.4 5.6

Mixing gas: Nm 3 / m2h 947 246 54 25 From the values in the table it can be seen that the amount of high speed gas jet can also be adjusted to suit the process at any time by controlling the oxygen enrichment of the oxidation gas phases.

The positions of the stone-slag systems of the conversion processes of Examples III, IV and V in the stability field at 1250 ° C are shown in Figure 1.

47 104267

In the method description, it has been demonstrated that the new method for adjusting the vertical capacity of the suspension suspension melting is only implemented in essential parts. It should be noted that the highly complicated and multi-step control method of the invention can be varied in many ways, while still remaining within the scope indicated by the method description, the examples given, and the claims. It should also be noted that, even in conventional techniques, the capacity values of a vertical suspension melting melt can be significantly improved by the use of relatively small, e.g. conversion layer mixing steps. In connection with the description and examples, attempts have been made to theorize phenomena related to the control method in order to give a clear scientific picture of the method according to the new invention. However, it is self-evident that not all phenomena related to the method have been explained, either because of their unknown nature or due to the lack of sufficient scientific and scientific results, and the criteria given in the explanation of the new method cannot be solely relied on.

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Peer reviewed publications: / 1 / Proceedings of the First International Flash

Smelting Congress: October 23-27, 1972 (Ed. R. Seeste, T. Tuominen): Satakunnan Kirjateollisuus Oy, 228-234, 245-250, Figures 3, 7, 12, 17/6 /: 6-11, / 8 /: 5-18, / 15 /: 7-10 / 2 / FRA Jorgensen, E.R. Segnit:

Proc Australian. Inst. Min. Metall., No. 261, 1977, 39-46, No. 271, 1979, 21-25, No. 288, 1983, 37-46 F.R.A. Jorgensen:

Trans. Inst. Min. Metall., 90, 1981, C 1-9, C 10-16 Z. Asaki, F. Ajersch, J.M. Toguri:

Met. Trans., 5, 1974, 1753-1759, 3, 1972, 2187-2193 Z. Asaki, S. Mori, M. Ikeda, Y. Kondo:

Met. Trans., 16 B, 1985, 627-638 / 3 / / 1 / Proceedings., 222-228 / 7 / US 3,900,310, US 4,088,310 / 4 / I. Barin, O. Knacke, O. Kubaschewski:

Thermochemical Properties of Inorganic Substances, Springer, 1973, Supplem. 1977, 246-249, 292-294, 251, 256, 304, 584, 656

Bureau of Mines: Bull, no 584, 1960, 160, 182, 95 Janaf Thermochemical Tables, PB 168370-2, 1960 H.H. Kellogg:

Can. Met. Quart., 8, 1969, 3-23 / 5 / US 3.790.366, 14.01.69, FI 45866: 2, 8-21 / 6 / US 3.754.891, 29.03.71, FI 47380/7 / US 3.900. 310, 4.088.310, 19.09.71, FI 48202/8 / US 4.1699.725, 08.11.74, FI 54147/9 / US 4.139.371, 4.236.700, 27.06.74, FI 52112 JF Elliott, M. Mounier:

Can. Met. Quart., 21, 1982, 415-428 A. I. Belyaev:

Surface Phenomena in Metallurgical Processes, Consultant Bureau, New York 1965: S.E. Vaisburd: 138-145 / 30 /, / 16/104267/10 / EN 56397, 05.07.07, US 4.113.470 / 11 / EN 52358, 11.11.74 / 12 / EN 22694, 03.04.47, US 2,506,557 SE 96977, 12.11.36, US 2,209,331 / 13 / A. Yazawa, T. Azakami:

Can. Met. Quart., 8, 1967, 257-261 G. Fischer (A. Lange-J. Barthel:

Freiberger Foschungshefte, Akademie V., Berlin 1958, B 29, 69-149 / 29 / A. Lange et al.

I. A. Onajew:

Neue Hutte, 10, 1965, 210-216 / 19 /, / 8 / EN 54148, 11.10.74, EN 55357, 12.08.08, (prior art) / 14 / EN-B 84363, 23.02.89 EN 32465, 01.10.59, US 3.306.708 FI 44797, 22.02.67, FI 45037, 23.01.67, FI 45948, 20.02.68 / 15 / FI 54809, 06.04.77, US 4.168.157 / 16 / FI 58946, 22.08. 79, US 4.304.596 / 17 / FI-B 84368, 27.01.89 US 1.758.084, 31.03.67 A. Yazawa:

Erzmetall, 30, 1977, 512

Extractive Metallurgy, Mining Ann. Rew., 1982, 291/18 / FI-B 94538, 6/6/92 FI 35938, 21.07.58 / 19 / FI 50638, 22.12.72 / 20 / EN 56398, 31.10.75 / 21 / FI-B 91238, 13.02 .91 EN 91285, 31.03.88 EN 24574, 26.10.48 56 104267/22 / EN 92151, 13.02.91

Victor Tafel:

Lehrbuch der Metallhuttenkunde, S. Hirzel, Leipzig: B 1, 1951, 258-264, 279; B 2, 1953, 41-43; B 3, 1954, 78-85 US 3.533.779, 28.05.68 EN 46263, 24.09.69, EN 49186, 07.01.72 (sulfate stability) T. Rosenqvist:

Met. Trans., 9 B, 1978, 346-350 / 23 / G.R. St.Pierre:

Physical Chemistry of Process Metallurgy, P1, Interscience 1961, 216-218, 227-232, 165-205 Applications for Suspension Melting: S. Mackerel: A method for evaluating the behavior of weather-sensitive iron-containing silicate slag melters. Metal-sulfide-rock-slag-gas phase equilibria in the flame smelting process: HTTK, Docenture Lecture Notes 1973, 1-73 M. Timucin, A.E. Morris:

Met. Trans., 1970, 3193-3201 Y. Takeda, S. Nakazawa, A. Yazawa:

Can. Met. Quart., 19, 1980, 297-305 A. Yazawa, Y. Takeda, Y. Waseda:

Can. Met. Quart., 20, 1981, 129-134 / 16 /: FI 58946, / 15 /: FI 54809/24 / E.D. Dewig, F.D. Richardson: J. Iron Steel Inst., 1960, 446 S.

Melting of sulfur concentrate: Part B, 12-16, 1961, L12B: / 1 /, Proceedings, ref. 266 Z. Asaki, F. Ajersch, J.M. Toguri:

Met. Trans., 5, 1974, 1753-1759 / 25 / US 2.668.107, 13.05.49 ·; / 26 / US 3.460.817, 30.09.63 (AU), CA 751.854 / 27 / US 3.674.463, 04.08.70 / 28 / US 4.0366.636, 22.12.75, US 3.857.700, 05.03.73 104267 / 29 / IM Rafalovich, V.L. Russo:

Tsvetnye Metally, 9, 30-39 A. Lange, 1964:

Metallurgie u. Giessereitechnik, 4, 1954, 538-547 Advances in Extractive Metallurgy, Elsevier, 1968, 206-223 DE 1,052,692, 30,03.55 US 3,555,164, 17,02.67, FI 47112, US 3,687,561, 25.04.69, U.S. Pat. No. 3,759,501, Dec. 31, 7,172, U.S. Pat. No. 4,247,087, Aug. 25, 88.76, U.S. Pat. No. 9,1285, Dec. 25, 5,888 / 30 / U.S. Pat. 32 / EN 85506, 04.09.86 / 33 / A. Yazawa: Can. Met. Quart., 13, 1974, 443-453 / 34 / US 4.226.406, 08.12.78, FI 64651, 26.09.80 / 35 / US 4.304.596, 04.08.80 / 36 / H. Jalkanen: Skand. J. Metallurgy, 10, 1981, 177-184 / 37 / G.A. Meyer, J.S. Warner, Y.K. Rao, H.H. Kellogg:

Met. Trans., & B, 1975, 229-235

Claims (10)

58 104267 A method for adjusting the melting capacity of a vertical suspension melting of fine oxide and / or sulfide ores and concentrates, in particular copper rich copper and nickel 5 ferric concentrates, comprising: is conducted at a reaction temperature at or above the vertically downward suspensiohapetusvyöhykkeeseen the oxidation of suspensiotilaisen material and osasulattamiseksi and then oxidation-15 below the zone suspensiopelkistysvyöhykkeeseen, if necessary osasulfidoimiseksi suspensiotilaisen oxidized material and the band at the bottom to change of suspension flow direction verti-20 radical of a horizontal, wherein the main part of the suspension contained in the material is discharged and collides with flows directly below the reduction zone 1a, a semi-solid, heterogeneous conversion reaction layer and a residual suspension stream are led to an upstream zone where it is optionally post-sulphidated, cooled, and separated from the solids possibly by suspension oxidation. -5 smelting capacity using high feed rates of 45-30% iron content of nickel and / or copper sulphide concentrates for the production of precious metal, iron poor sulphide rocks and / or crude metal; 10b. The desired collection of heterogeneous suspension smelting product is maintained at an accumulation interval corresponding to a degree of oxidation of the iron content of the concentrate in the suspension state from 70% to 90%, i.e. the collection area of sulfide rock from iron rich to 15 poor sulfide stones; c. the conversion layer comprising the heterogeneous suspension oxidation product containing molten and solid phases is blended, with gas jets in the range 200-330 Nm / s, with 20 continuous under-layer, if necessary pre-acidified slag layers, for selective oxidation of ferrous sulfide in the oxidation product iron conversion; 1 2 3 4 5 6 d. a laminar, unmixed conversion reaction layer, 2: the amount of convertible magnetite corresponding to a maximum of 3 inputs of the conventional melting process, per 4 surface areas of the conversion layer, from a maximum of 120 to 140 g / m 2, corresponding to a minimum melting process feed rate; 60 104267 e. Simultaneously mixing with the heterogeneous suspension oxidation product slag melt mixture, the amounts of heat required for heterogeneous oxidation-reduction reactions, dissolution and melting, the amount of slag pre-oxidation, electric heat and / or degassing for mixing; 10f. The heights of the melt layers in the horizontal furnace basin are kept constant and the total slag phase height in the conversion bed region is 5-8 times the slag amount corresponding to the feed capacity, and the total height of the rock (+ metal) phase is 3-4 times the feed capacity; 15g the height of the top of the slag layer used for producing and mixing the slurry product slurry melt slurry is between 0.75 and 1.25 times the amount of slag corresponding to the feed capacity; The sulfide rock and / or crude metal obtained as a product of slurry and heterogeneous magnetite and / or melt version oxidation and slag are continuously discharged from the melting system through siphon wall-separated furnace sections. 25 Method according to Claim 1, characterized in that the melting capacity adjustment is carried out at a feed rate in the range of 10 to 80 t / h. 1 • · A process according to claim 1, characterized in that the conversion bed slag melting system is blended with a melt of at least 200 Nm 3 / m2h per bed area to be mixed. A method according to claim 1, characterized in that the conversion bed slag melting system is blended with a gas having a velocity lower than the velocity of sound in air. The process according to claim 1, characterized in that the post-oxidation suspension is reduced and sulphidated as the sulfur bound iron content of the suspension oxidation product falls below the iron content of the complex mineral containing the precious metal of the concentrate or the corresponding metal activity conditions are formed in the sulphide melt. Process according to Claim 1, characterized in that the suspension oxidation product of the conversion layer is oxidized with a pre-oxidized slag having a maximum degree of oxidation corresponding to saturation of the slag melt with magnetite and silica, i.e., as a function of temperature (T, K) log P02 = 20 2,259 * 10'ZT - 41.176. oxygen pressures (PO2, atm) and having a minimum oxygen pressure after sulfide oxidation, PO2 = 10'9 atm at a reference temperature of 1250 ° C. Process according to Claim 1, characterized in that the conversion bed slag melting system is stirred at a temperature in the range of 1500-1300 ° C, and the drop temperature of the slag and stone products is maintained in the temperature range of 1350-1200 ° C and 1300- 1150 ° C. 62 104267 Process according to Claim 1, characterized in that the sulphide rock is oxidized to an oxygen and sulfur content of less than 1.5% in the crude metal phases. Process according to Claim 1, characterized in that heat is transferred to the conversion reaction layer by conventional methods, which include electrical resistance and / or oxidation of the slag melt and / or oxidation of various fossil and synthetic fuels and associated electrical resistance and fuel supply equipment. Process according to Claim 1, characterized in that the solid-melt flow in the discharge / conversion reaction region of the oxidation suspension is vertical, whereby the horizontal flow of material to the slag reduction or out of the melting device is effected through a siphon barrier. 63 104267