FR2616446A1 - PROCESS FOR THE TREATMENT OF SULFUR LEAD ORES OR LEAD AND ZINC SULFIDES AND / OR THEIR CONCENTRATES - Google Patents

Abstract

The process consists in carrying out the melting of a charge consisting of a starting sulphide product and a flux, together with the recycled oxidized dust, in a vertical torch maintained in an atmosphere of a gas containing oxygen, by obtaining an oxidized molten material, essentially containing metal oxides, and a mixture of oxidized dust recycled with the gases resulting from the fusion; said recycled dust is separated from the fusion gases and this dust is returned to the fusion; metal oxides are reduced by filtration of the oxidized molten material through a layer of solid carbonaceous material, obtaining a crude lead and a zinciferous slag depleted in lead; the slag is decanted, which provides lead-bearing zinc vapors; said vapors are oxidized with an oxygen-containing gas, obtaining coarsely and finely divided oxidized sublimates. As flux, a mixture of limestone or lime with a ferric material CaO is used: FE = 0.43 to 0.76 in a proportion of 5 to 22% of the mass of the starting sulphide product.

Description

The present invention relates to the metallurgy of non-ferrous metals, and

  more specifically, it relates to processes for treating sulphidic lead ores or sulphurized lead and zinc ores and / or

their concentrates.

  The main line of research in perfection-

  pyrometallurgical production of metals

  heavy non-ferrous involves developing

  assigned to extract said metals from materials

  first sulphides using self-processes

  Genoa. The common advantages of autogenous processes

  are: high unit yields, a significant reduction

  of the volume of technological gases, the

  contribution of the calorific value of ores and

  sulfur-centered (the latter factor reduces

  notably the use of external heat sources

  the possibility of efficient processing of raw materials relatively poor in non-ferrous metals. We know different variants of autogenous processes. A distinctive feature common to all of them is the

  taking advantage of the highly developed surface of the ma-

  sulfurized to ensure the autogenous character of

fusion.

  A process is known for treating sulphidic lead ores or lead and zinc ores

  sulfides and / or their concentrates containing

  metals, including those of iron and copper, silicon dioxide, aluminum, calcium and magnesium oxides, according to which a charge consisting of said sulphurized materials and a flux is admitted to fusion together with oxidized dust

  recycled through a device comprising a burner.

  A mixture of quartz sand with limestone or lime is used as the flux. The merger of said

  charge together with oxidized dust

  -2- cycles is carried out in a vertical torch, in an atmosphere of a gas containing oxygen, for

  obtain an oxidized melt containing essential-

  oxides of metals, and a mixture of dust

  oxidized res recycled with the gases resulting from the fu-

  if we. Said recycled oxidized dust is separated

  from the gases resulting from the merger to be returned to the merger. Metal oxides, mainly lead oxide, are reduced to metals by filtration of the oxidized melt through a layer of solid carbonaceous material

  finally obtaining raw lead and a zinc slag

  lead-depleted cifer. Said slag is decanted with the formation of lead-bearing zinc vapors. We oxidize

  the said lead-bearing zinc vapors by a gas containing

  providing oxygen, obtaining oxidized sublimates

  coarsely and finely dispersed (US-A, - 4519836).

  In this process, as a result of the use in the flux composition of a constituent with a high melting point that is quartz sand, a

  increased lead levels in oxy-

  dees recycled due to the sublimation of lead sulfide. In addition, the presence of quartz sand in the composition of the flux used leads to a reduction in the reduction rate of lead oxide on the

  solid carbonaceous reducer and, consequently, an increase

  lead loss with zinc slag.

  The object of the invention is to modify in such a way

  the conditions of fusion in the process for treating sulphidic lead ores or sulphurized lead and zinc ores and / or their concentrates,

  that the lead extraction rate is maximum.

  The problem thus posed is solved with a process

  treatment of sulphidic lead ores or mines-

  lead and zinc sulphides and / or their con-

  centered, containing metal compounds, especially those of iron and copper, silicon dioxide, aluminum, calcium and magnesium oxides, process -3

  which provides for the admission to amalgamation of a charge cons-

  made up of the said sulphide materials and of a flux

  jointing with oxidized dust recycled through

  towards a device fitted with a burner, the fusion of the

  said charge jointly with the oxidized dust in a vertical torch burning in an atmosphere of a gas containing oxygen with obtaining a

  oxidized melt essentially containing oxy-

  metals and a mixture of oxidized dust

  cycled with the gases resulting from the fusion, the separation

  tion of said oxidized dust recycled from

  gases resulting from the fusion and recycling of these pus-

  in the melting stage, the reduction of metal oxides, essentially lead oxide, into metals by filtration of the oxidized molten material through a layer of solid carbonaceous material, obtaining a crude lead and a slag depleted zinciferous

  lead, the settling of this slag which gives off

  lead-fearing zinc fears, oxidation by a con-

  taking oxygen from said lead-zinc fumes

  res with coarsely oxidized sublimates and

  finely dispersed, a process in which, according to the invention

  tion, a mixture of limestone is used as the fondant

  or lime with a ferrous material, the mass ratio

  between the calcium oxide and the iron, within the mixture, being from 0.43 to 0.76, said mixture being

  used in proportion to 5 to 22% of the mass of the medium

  nerai and / Qu of its starting concentrate and the calculation being carried out starting from the totality of the oxide of

  calcium and iron contained in this mixture.

  Thanks to the use, in the proposed process, of a flux containing a low-point constituent

  fusion, namely a ferrous material, we see dimi-

  significantly reduce the amount of lead present in recycled oxidized dust due to the reduction in the degree of sublimation of lead sulfide. This last result is obtained thanks to the fact that the iron component of the flux forms, during the melting, a - 4- eutectic with low melting point which dissolves the sulphide

  lead. In addition, the silicon dioxide being replaced

  placed, within the oxidized melt during formation, by the iron oxides coming from the flux used according to the invention, this dissolved melt

  easily ash formed on the surface of the ma-

  solid carbonaceous during reduction. This results in an improvement in the conditions under which the oxidized molten material comes into contact with the carbon of the

  reducing and therefore an increase in the

  duction of lead oxide and a decrease in its

losses with zinc slag.

  As stated above, the constituents

  fondant (limestone or lime, a ferri-

  fere) are used in such quantities as the ratio

  mass between calcium oxide and iron in the

  either from 0.43 to 0.76, the proportion of the flux

  Before being between 5 and 22% of the mass of the mine-

  rai and / or starting concentrate, calculating from all of the calcium oxide and iron contained

in the fondant.

  The use of a flux having the indicated ratio between calcium oxide and iron, and engaged in the aforementioned proportion, ensures the most favorable conditions for the formation of a eutectic to

  low melting point "iron (II) oxide - cal oxide

  cium - iron sulfide "(F = 8800 C), whereby the lead sulfide passes into the current molten material

  training at a temperature lower than that of

  trée lead in an intense sublimation (T = 1000 C).

  The process of the invention makes it possible to improve the ef-

  efficiency of the separation of lead from zinc at the reduction stage on a solid carbonaceous material, to reduce the level of lead in recycled oxidized dust and thus to increase from 0.9 to 1.1% the rate

  lead extraction compared to the known process.

  In the case where the copper concentration in the starting sulfur products exceeds 1% by mass, it is - recommended, in order to improve the quality of lead

  crude obtained, that is to say to reduce its cooking rate

  vre, to carry out the merger of the charge jointly

  with recycled oxidized dust, the gas flow

  containing oxygen, by calculating oxygen, being less than the stoichiometric amount necessary for complete oxidation of metals and sulfur of

  sulphides, contained in the charge, obtaining final-

  alongside raw lead and zinc zinc slag ap-

  poor in lead, -a mat enriched with copper.

  In the case where the copper concentration in the starting sulfurized products does not exceed 1% by mass, it is advantageous to carry out the melting of the charge together with the recycled oxidized dust, the flow rate of the gas containing oxygen being defined by the following formula:

P = A-B.K (1),

  o P is the flow rate of the oxygen-containing gas, 'by calculating oxygen, in m3N per tonne of charge; A = 1.542 - 3.299 Ca - 7.972 Cb - 4.285 Of +

  <28,851 Cab + 14,657 CaCf + 27,370 bCf -

  - 88.895 Cb oCa (2), o Ca + Cb + f = l is the sum of the contents of the charge in

  acid oxides Ca (SiO2 and A1203), in oxy-

  basic Cb (GaO and MgO) and in oxides

  iron Cf (by calculating in FeO), these te-

  nors being expressed in mass shares; B is the stoichiometric flow rate of the oxygen entering into the composition of the gas which contains it, required

  for complete oxidation of metals and sulfur

  fre of sulphides contained in the load, in m per tonne of the load;

- 0

K = 1+,

  o H is the height of the fusion zone, in meters.

  It is known that the specific speed of a reaction (or, more precisely, the reaction constant of the reaction) of the gas - molten material type depends on the composition of the molten material, including the constituents which do not are not directly involved in the reaction. This is how the influence exerted by the scorifying constituents (CaO, MgO, A1203, SiO2, FeO) on the speed of desulfurization reactions such as PbS + 1.5 02 -PbO + SO2 ZnS 1.5 02 -ZnO ± SO2

  can be explained, firstly, by the dependence of the solu-

  bility of lead and zinc sulfides present in the molten material, and secondly, by that of parameters sensitive to the structure of the

  speed of heterogeneous desulfurization reactions vis-

  with respect to the concentration of said scorific constituents

  fiants in the melt. The constants of vi-

  The size of the desulfurization reactions therefore exhibit a complex dependence on the chemical composition of the starting charge. We also know that the desulfurization rate (the ratio between the quantity of sulfur present in the gases resulting from the fusion

  and the amount of sulfur present in the feed)

  depends on the length of stay of the charge in the melting zone. This duration depends on the height of the

  fusion zone (under physical laws well

  naked). It follows that the oxygen flow actually

  necessary to reach the desulfurization rate re-

  which depends on the content of the load to be treated in

  above-mentioned scorifying constituents and of the high

  of the melting zone. By debit actually required

  saire means an oxygen flow which allows to obtain the expected result of the fusion without giving

  result in the formation of a matte or of an excess quantity

dental iron (III) oxide.

  The indicated relation (formula 1) does not lend itself to theoretical calculation. We have established it experimentally. Carrying out the fusion with a flow of oxygen-containing gas defined by formula (1) allows

  achieve the required desulfurization rate, i.e.

  say the release of the maximum amount of heat ensuring the best conditions for carrying out the fusion and reduction processes, which allows, in the second analysis, to increase from 0.5 to 0.9% the rate

lead extraction.

  In the case where the copper concentration in the starting sulfurized products is higher than 1% by mass, it is recommended to carry out the fusion of the

  charge together with recyc- oxidized dust

  lées with a stoichiometric flow rate of gas containing oxygen, by calculating in oxygen, flow required for a complete oxidation of lead, iron and zinc in the load, and with a flow rate of gas containing oxygen, by calculating in oxygen, flow rate referred to 1 kg of sulfur sulfides contained in the feed and defined by -the following formula: Cou Q = 0.70. (l - n) (3), where Q is the flow of gas containing oxygen, by calculating oxygen, per 1 kg of sulfur sulfides contained in the feed, in m3N;

  n is the masic relationship between the sulfur of sul-

  fures and copper within the oxidized melt, between 0.65 and 1.30; Neck,

  CS are, respectively, the concentrations of cui-

  glass and sulfur sulfides in the feed, in% by mass; whereas the lower layer of raw lead must be cooled to a temperature of 330 ° C to 9000, to finally obtain, next to the raw lead and

  lead-depleted zinc slag, a matte-

rich in copper.

  Such a flow of oxygen for melting and cooling

  dissement of the lower layer of raw lead Jus-

  only at temperatures within the specified limits

  quées allow to obtain a crude lead at low rate

  poor in copper and sulfur (the latter passing essentially

partly in the matte).

  When the ratio of sulfur to sulfides and

  copper, within the oxidized melt, is in-

  below 0.65, the copper does not pass in maximum proportion into the matte from the raw lead. When the ratio between sulfur of sulfides and copper, within the oxidized melt, is greater than 1.30, this results in an excess of sulfur in the raw lead, which causes the formation of lead sulfides. The latter phenomenon is undesirable because, to remove sulfur from raw lead, it is necessary

a special refinement.

  When cooling the bottom layer of

  raw lead up to the above temperatures, the solution

  bility of copper sulfide in crude lead will

  increasing and, as the lead drops descend, its copper content decreases, while the matte particles rise towards the interface

"slag - raw lead".

  Since during the cooling of the cou-

  che lower lead crude lead which. get rid

  of copper and the copper thus released travel against

  -current, this results in a continuous refining of lead

crude and matte formation.

  When the lower layer of raw lead cools down to a temperature above

  900C, the quality of lead refining, which

  rasse of copper, is suddenly depreciated. If the lower layer of raw lead cools down to a temperature below 330 C, the

  quality of lead refining which removes copper from it

  vre is not seen to improve, because there then occurs a gradual reduction in the height of the bath from -9 - molten raw lead, accompanied by an increase in the

  expenditure of electrical energy to maintain the temperature

  Necessary rature of the slag and we see appearing difficulties linked to the evacuation of lead stripped of copper.

  It emerges from what has just been said that the

  lisation of the process with a flow of gas containing

  the oxygen defined by formula (3) and with the cooling

  The lower layer of raw lead improves the quality of the raw lead, and ultimately

  analysis, reduces losses during subsequent refining.

  To ensure an optimum desulfurization rate of the feed, maximum heat release at the melting stage, improvement of the oxidation conditions

  load and reduction of the molten oxy-

  as well as to ensure a maximum extraction rate

  mum of lead, it is recommended to perform admission

  of the merger charge together with the pushers

  recycled beers oxidized through a device fitted with a burner, the effective diameter of the useful opening of which is determined by the following formula:

0.01911 C S.-MSM

  of H (4), where o is the effective diameter of the useful opening of the burner, in m is the desulfurization rate, defined as the ratio of the quantity of sulfur contained in the gases resulting from the fusion to the quantity of sulfur contained in the charge; M is the charge flow rate, in Kg / s f is the density of the oxygen-containing gas, in kg / m3; H is the height of the melting zone, in m

  't = -0.0703 + 0.3031. & -0.0157. & 2 - 8.17.10-5 ..

  ECa0 - 3.64.10-3.Csi +, 83.10-. Ci02 + o 8,899.10'- Cca + 2,76810 3.CCaO in s (5); Ca89-0co +278 CaOs in s (5);

- 10 -

  Os OOaO, being, respectively, the concentra-

  sulfur sulfur, -02 calcium oxide and silicon dioxide asio2 tions in

the load, in% by mass.

  When the effective diameter of the useful opening of the burner does not correspond to the theoretical diameter, calculated according to formula (4), effects are observed

  annoying. In particular, if the effective diameter of the opening

  useful size of the breaker is less than the theoretical diameter

  that (the flow rate of the sulfurized material is

  high), the failure rate cannot be achieved

  sulfurization required due to the short drying time

  day of the material in the melting zone, which

  an increased intensity of the passage of lead in the matte and a reduction in its rate of extraction with the

  raw metal, therefore an increase in its losses. When-

  that the diameter in question is greater than the theoretical diameter, the duration of stay of the material in the

  melting zone becomes more prolonged than it is born

  cessary (the flow velocity of the sulphurous material

  rée is lower than that which is necessary), there is overoxidation of the load, which causes a degradation of the conditions of reduction of lead oxide and, consequently, an increase in losses of lead with

the zinc slag.

  It is advantageous, before the admission of the charge to the fusion through the device provided with a burner, to reduce part of the charge, in proportion from 4.5 to 13% of the mass of the starting charge, up to a particle size 4 to 8 times smaller than that of the particles of the initial charge, and at the

  then mix with the remaining part of the filler.

  We have established that during mine oxidation-

  - sulphide raisins and / or their concentrates under the conditions

  where they are heated by the heat given off as a result of their oxidation, the increase in the speed of this heterogeneous reaction following the reduction of the product is found to be 50 to 80% greater than

- 11 -

  which can be assumed starting from the ratio between the sizes of the particles constituting, respectively, the

  starting charge and its reduced fraction. Thanks to the ac-

  considerable increase in the rate of oxidation of the charge with the particles partly reduced compared to the initial charge, this partly reduced charge oxidizes completely in the upper part of the melting zone, the heat which is released consequently of

  its oxidation goes to heating and melting the frac-

  large particles, predominant in the

  seems to charge, thus intensifying oxidation

  large particles of sulfurized material and ac-

  increasing the extent of the region at high temperatures

  from the fusion zone. By increasing the size of the area at high temperatures, the duration

  load stay in this area is increased

  ter from 2.1 to 3.6 times, whence the considerable increase

  ble both the rate of interaction of sulfides with

  oxygen from the gas phase as from that of the interaction

  tion of higher iron oxides with sulfides.

  Thanks to the increase in the charge's residence time at high temperatures, we see an increase in the rate of oxygen use in the gas phase

  and especially of the combined oxygen entering the compound

  sition of higher iron oxides. The lower content of the resulting oxidized melt in higher iron oxides results in the

  further reduction of this melt, a reduction

  consumption of solid carbonaceous matter

  for the reduction of higher iron oxides.

  We have established that if the frac-

  tion reduced in proportion less than 4.5% of the mass of the starting charge the heat which is released as a result of the reactions is not sufficient to create the temperatures ensuring an intense oxidation of the

  charge in the upper part of the fusion zone.

  Likewise, if used as an additive to a

  particle whose particles are less than

- 12 -

  4 times lower than that of the particles in the starting charge, the oxidation rate of this additive is

  finds insufficient to initiate oxidation of the

  essential part of the charge, that of coarse particles.

  In case of addition of the fraction reduced in pro-

  portion greater than 13% of the mass of the starting charge or in the event of a very high degree of reduction of the sulfurized raw material (the ratio between the sizes of the particles being greater than 8), a

  considerable increase in the amount of dust

* recycled oxidized res as well as a significant increase

  ble of the additional reduction costs of the material.

  It emerges from what has just been said that the re-

  reduction of part of the load will increase the rate of oxygen use, in other words

  convert metals more completely from sul-

  fures in oxides and, therefore, to increase from 0.2 to

  0.5% lead extraction rate at the reduction stage

  tion. In addition, the device in question makes it possible to

  reduce consumption of solid carbonaceous matter.

  It is advantageous for the oxidation of the lead-bearing zinc vapors resulting from the decantation of the lead-depleted zinc-bearing slag by a gas containing - oxygen, to be carried out under a pressure of minus 19.6 to plus 19.6 Pa, by obtaining coarsely divided oxidized sublimates, enriched in zinc oxide, and finely divided oxidized sublimates, enriched in lead oxide, and in sending said sublimates to fusion

finely divided oxidized.

  During the settling of the zinc slag, a

  part of the lead and zinc passes into the vapors.

  During the oxidation of said vapors under pressure

  between minus 19.6 and plus 19.6 Pa, it occurs

  has an effective separation of lead and zinc in the oxidized sublimates obtained: zinc is concentrated in the roughly divided sublimates, and lead in

  the finely divided sublimates that we send to the fu-

if we.

- 13 -

  A high level of lead in the finely divided sublimates, which is higher than the level of lead in the charge, explains the usefulness of their return to fusion, which makes it possible to increase the rate of extraction of lead. The oxidation of lead-bearing zinc vapors under a pressure exceeding the limits recommended by the invention excludes the possibility of enriching the coarsely divided oxidized sublimates with zinc, and the finely divided oxidized sublimates with lead, and therefore makes it impossible to use, during the

  finely divided oxidized sublimates as ma-

recycled content.

  Thanks to the oxidation of lead-bearing zinc vapors - under a pressure ranging from minus 19.6 to more

  19.6 Pa, it therefore becomes possible to enrich the frac-

  tion of the sublimates finely divided into lead, which ac-

  increases its extraction rate by 0.3 to 0.4%.

  The proposed process for processing sul- ores

  lead fumes or sulphide ores of lead and zinc and / or their concentrates, containing metal compounds, in particular those of iron and copper, silicon dioxide, oxides of aluminum, calcium and

  magnesium, is used in the following manner.

  For the realization of the process a fusion group is used ("Tsvetnye metally" n 8, 1977, A.P. Sychev "Kislorodnoélektrotermicheskaya pererabotka

  svintsovykh contsentratov v agregate "EIVCET-CS", p.p.

8 to 15).

  A charge consisting of lead sulphide ores and lead and zinc sulphide ores and / or their concentrates and a flux is dried to

  a humidity not exceeding 1% by mass and, together

  with recycled oxidized dust, brought to melting through a device fitted with a burner,

  which is part of the fusion group. As a foundation

  dant using a mixture of lime or limestone with a ferrous material, the mass ratio between

- 14 -

  the calcium oxide and the iron, present in the mixture, being from 0.43 to 0.76, said mixture being used in proportion to 5 to 22% of the mass of the ore and / or of the

  starting concentrate, calculating the totality of the

  calcium and iron xyde present in this mixture. The

  fusion of said charge, together with the pushers

  recycled oxides, is carried out in a torch

  vertical burning in a gas atmosphere

  holding oxygen. As oxygen-containing gas, for example, oxygen can be used

  technical or oxygen enriched air.

  In the case where the copper concentration in the starting sulfurized products is higher than 1% by mass, it is recommended to carry out the fusion with a flow of gas containing oxygen, by calculating in oxygen, lower than the quantity stoichiometric necessary for complete oxidation of metals and

  sulfur sulphides contained in the feed (ie

  to say that it is recommended to operate the merger so

  that there is formation of a mat enriched with copper).

  If the concentration of copper in the pro-

  sulphide starting materials do not exceed 1% by mass,

  it is useful to operate the fusion without the formation of a matte, with a flow of gas containing oxygen, in

  calculating in oxygen, excess compared to the stoichiometric quantity necessary for

  complete oxidation of metals and sulfur

fures, contained in the charge. -

  At the end of the fusion, a dark matter is obtained.

  oxidized due, containing mainly metal oxides

  rate, and a mixture of recycled oxidized dust with the gases resulting from the fusion. We send said mixture of recycled oxidized dust with gases

  resulting from the merger, through an amount of evacua-

  tion of gases from the melting group, in a device for separating recycled oxidized dust from

  gases resulting from fusion, for example in an electric

  trofilter. Recycled oxidized dust is re-

  merging tours in the merging group.

- 15 -

  The oxidized melt thus obtained is filtered through a layer of solid carbonaceous material which can be, for example, coke or coal. It

  results in a reduction of metal oxides, essential-

  that of lead, up to metals. This produces raw lead and a depleted zinc-bearing slag.

  lead, or the same products and a matte-

  rich in copper. The indicated melted products flow

  slow towards the electrothermal zone of the fusion group, said electrothermal zone having a sole in common with the fusion zone. In the electrothermal zone

  above, there is a settling of the zinc slag

  ciferous and a layer formation: the lower layer

  of raw lead and the upper layer of zinc slag-

  father depleted in lead; if there is a mat enriched with copper, this mat will constitute

  an intermediate layer between the raw lead and the milk

  tier. The slag settling gives rise to the formation

  tion of lead-bearing zinc vapors which, together with the gases from the electrothermal zone, are brought

  in a device, in particular a post-com chamber

  bustion, with a view to the oxidation of said vapors. In this same device we also admit a gas containing

  oxygen (especially oxygen-enriched air).

  The result is coarsely oxidized and finely oxidized sublimates.

  divided, containing practically quantities

  of lead oxide and zinc oxide. The subli-

  coarsely divided meses are deposited in the disposi-

  above mentioned vapor oxidation. The sublimates fine-

  divided, mixed with the gases from the electric zone

  heat, are sent to separation, in particular in a bag filter. The grossly sublimated

  and finely divided are sent to further processing

  laughing in order to extract zinc and lead.

  '' The treatment describes sulfurized materials supplied

  finally nit of raw lead, a zinc-bearing slag ap-

  poor in lead, a minatte enriched with copper (if necessary

  care is), and gases resulting from the merger. Lead -16 -

  raw is sent to further refining, which

  barrel of copper and other impurities, the lead-depleted zinc slag is sent to the extraction of zinc, the matte enriched in copper, to the production of copper, and the gases resulting from the fusion, to the pre-

preparation of sulfuric acid.

  It is recommended, in case the copper concentration in the starting sulfur product does not exceed 1% by mass, to carry out the fusion with a flow of gas containing oxygen defined by the formula (1). For this purpose, it is determined, starting from the contents of the starting charge of lead, zinc, iron, copper and

  sulfur sulfides, the stoichiometric flow rate of oxy-

  gene (B). Then, from the rates of SiO2, A1203, CaO, MgO and Fe (by calculating as FeO) in the charge and

  by setting equal to unity the sum of their concentra-

  tions, parameter A is determined according to formula (2).

  Knowing the height H of the melting zone, we determine

  mine the parameter K. After having determined the values of A, B and K according to formula (1), the necessary flow rate of gas containing oxygen is established (in

  calculating in oxygen) per tonne of charge and we ef-

  then performs the fusion with the indicated gas flow

containing oxygen.

  It is of interest if the concentration of copper in the starting sulfur product is greater than 1%

  in mass, to operate the fusion with a flow of gas

  holding oxygen defined by formula (3), while

  simultaneously cooling, notably by air, up to

  that at a temperature of 330 to 9000C, the lower layer

  raw lead next to the sole of the fu-

  if we. Treatment of sulfurized products with flow

  indicated gas containing oxygen and cooling

  addition of the raw lead and the zinc-bearing slag

  depleted in lead, a mat enriched with copper.

- 17 -

  To ensure the best possible conditions for

  tion of the fusion, the effective diameter of the section

  useful of the braleur can advantageously be chosen

form with formula (4).

  It is advantageous, before the admission of the charge to the fusion through the device provided with a burner, to reduce a part of the charge, in proportion from 4.5 to 13% of the mass of the charge of departure, up to a particle size of 4 to 8 times less than

  that of the particles of the starting charge, and at

  change the reduced fraction with the remaining part of

load.

  It is desirable that lead zinc fumes

  fères which are formed during the decantation of the zinc-bearing slag impoverished in lead are oxidized, in particular

  in a post-combustion chamber, by a contained gas

  oxygen supply (which can be technical oxygen

  or oxygen-enriched air) under al-

  lant from minus 19.6 to plus 19.6 Pa. Proceeding from the

  so, you get roughly oxidized sublimates

  targeted, enriched with zinc oxide, and oxy-

  finely divided dices, enriched with lead oxide. The-

  said grossly divided sublimates are deposited in

  the device where the oxidation of the

  fears, separating from the finely divided sublimates, after which they can be used for the purpose of subsequently extracting zinc. The finely divided sublimates enriched in lead are sent to fusion in the

fusion group.

  Other features and advantages of the invention

  tion will be better understood on reading the description

  tion which will follow from several nonlimiting examples

of its realization.

Example 1

  A sulphide concentrate of lead and zinc is treated, containing 51.12% by mass of lead, 9.11% by mass of zinc, 0.73% by mass of copper, 3.61% by mass of iron, 16, 31% by mass of sulfur of sulphides, 4,948% in -18mass of silicon dioxide, 1.49% by mass of calcium oxide, 0.68% by mass of aluminum oxide and

  0.39% by mass of magnesium oxide.

  To do this, the load is prepared by adding a flux to the starting concentrate. As the fondant, a mixture of limestone (56% by mass of calcium oxide) with pyrite (42% by mass of iron) is used, the mass ratio between the calcium oxide and the iron present in the mixture being 0.60. Said flux is added in proportion to 5% of the mass of the starting concentrate, calculating in total amount of

  the calcium oxide and iron present in the flux.

  The charge consisting of the said sulfur concentrate and the flux is dried to a humidity level of 1%

  en masse and sent to the merger in the group of fu-

  sion, together with recycled oxy-

  through a device fitted with a burner whose effective diameter of the useful section is equal to 0.095 m. The feed rate is 1 t / h. The fusion is carried out in a vertical torch maintained in an atmosphere of technical oxygen (95% of 02) which is admitted to fusion in proportion to 260 m3N per tonne of the load. The height H of the fusion zone of the fusion group is equal to 2.0 m. By proceeding from

  so we get a melt containing

  essentially metal oxides and a mixture of recycled dust oxidized with the gases resulting from the fusion. Said dust is separated from the gases

  resulting from the fusion in an electrostatic precipitator and

  continuously cycle this dust to fusion. The quan-

  dust that is continuously recycled in this way

  sion constitutes 16.4% by mass compared to the quan-

  charge charge; the lead level in the dust

is 61.7% by mass.

  The oxidized melt is filtered through a layer of coke which is used in an amount of 55 kg per tonne of the feed. Under these conditions, metal oxides, mainly lead oxide, are reduced

up to metals.

  -19- At the end of the described treatment, crude lead is obtained, in which the lead contained in the starting concentrate is passed in proportion of 93.0%; a lead-depleted zinc-bearing slag is also obtained, Rdan in which the lead has passed in proportion to 0.79% relative to the mass of lead contained in the concentrate

of departure.

  Said molten products move towards the zone

  electrothermal of the melting group o the zinc slag

  ciferous undergoes decantation. When the slag is decanted, lead-forming zinc vapors are formed

  which, together with the gases from the electrother-

  - mique, are sent to a post-combustion chamber for the oxidation of said vaporso In this same device, air is also admitted. The pressure in the afterburner is less

  49 Pa. Finally, we obtain coarse oxidized sublimates

  securely and finely divided, containing 45% by mass of zinc and 35% in lead measse (6.1% by mass of

  lead contained in the starting concentrate).

Example 2

  The treatment of the lead and zinc sulphide concentrate, described in Example 1, is carried out as in Example 1. To do this, a flux is used which is a mixture of limestone (56% by mass of calcium) with a pyrites residue (51% by mass of iron), the mass ratio between the calcium oxide and the iron present in the mixture being 0.60. Said flux is added in proportion to 22% of the mass of the starting concentrate, calculating in total quantity

  calcium oxide and iron present in the fungus

  dant. Fusion takes place in a vertical torch,

  maintained in an atmosphere of oxygen-enriched air (70% O 2) which is brought to the fusion in quantity of

  301 m3N per tonne of load. The proportion of push-

  oxidized beers recycled continuously during melting is 14.1% by mass relative to the quantity of the filler; the lead level in the dust is 62.3% by mass.

- 20 -

  At the end of the indicated treatment,

  raw lead in which the lead contained in the con-

  starting center increased to 93.1%; we also get

  lead-depleted zinc-bearing slag in the

  what the lead in the starting concentrate is

  increased to 0.75%. In addition, oxy-

  roughly and finely divided, containing 44.8% by mass of zinc and 32.7% by mass of lead (6.05% by mass of the lead contained in the concentrate

departure).

Example 3

  The treatment of the lead and zinc sulphide concentrate, described in Example 1, is carried out as in Example 1. To do this, a flux is used which

  is a mixture of lime (70% by mass of cal

  cium) and pyrite (42% by mass of iron), the mass ratio between the calcium oxide and the iron present in the mixture being 0.60. Said fondant is added

  in proportion to 15% of the mass of the concentrate of

  part, by calculating in total quantity of the oxide of cal-

  cium and iron present in the flux. The fusion is carried out in a vertical torch maintained in an atmosphere of technical oxygen (95% of 02) which is admitted to fusion in an amount of 360 m3N per tonne of the charge. The quantity of oxidized dust recycled

  continuous melting is 9.3% by mass compared to

  carriage to the quantity of the load; the lead level in

  the dust is 62.7% by mass.

  At the end of the indicated treatment,

  raw lead, in which the lead contained in the con-

  starting center increased to 93.2%; we also get

  lead-depleted zinc-bearing slag in the

  what the lead in the starting concentrate is

  increased to 0.81%. In addition, oxy-

  roughly and finely divided, containing 45.1% by mass of zinc and 33.8% by mass of lead (5.9% of

  the mass of lead contained in the starting concentrate).

- 21 -

Example 4

  The treatment of the lead and zinc sulphide concentrate, described in Example 1, is carried out as in

  Example 1. The mass ratio between the cal-

  cium and the iron present in the flux is actually

  rence equal to 0.43. Said fondant is added in proportion

  15% of the mass of the starting concentrate, calculating the total amount of calcium oxide and iron present in the flux. The merger takes place

  in a vertical torch maintained in an atmos-

  technical oxygen sphere (95% of 02) which is admitted to fusion in proportion to 370 m3N per tonne of charge. The quantity of oxidized dust recycled

  continuous melting is 36.4% by mass compared to

  carriage to the quantity of the load; the lead level in

  the dust is 62.3% by mass. The material

  due oxidized is filtered through a layer of coal which is used in an amount of 71.5 kg per tonne

of the load.

  At the end of the indicated treatment,

  raw lead, in which the lead contained in the con-

  starting center went to 93.0% W as well as a lai-

  lead-depleted zinciferous tier, in which lead

  contained in the starting concentrate increased to 0.69%.

  In addition, coarsely and finely divided oxidized sublimates are obtained, containing 44.4% by mass of zinc and 35.1% by mass of lead (6.2% by mass of lead.

  contained in the starting concentrate).

Example 5

  The treatment of the lead and zinc sulphide concentrate, described in Example 1, is carried out as in

  Example 1. The mass ratio between the oxide of cal'-

  cium and the iron present in the flux is actually

  rence equal to 0.76. Said fondant is added in proportion

  15% of the mass of the starting concentrate, calculating the total amount of calcium oxide and iron present in the flux. The merger takes place

  in a vertical torch maintained in an atmos-

- 22 -

  technical oxygen sphere (95% of 02) which is admitted to fusion in proportion to 352 m3A per tonne of charge. The quantity of oxidized dust continuously recycled during melting is 11.0% by mass relative to the quantity of the feed; the lead level in

  dust is 61.9% in masese.

  At the end of the indicated treatment,

  raw lead, in which the lead contained in the concentrate

  starting point increased to 93.1%, as well as a dairy

  lead-depleted zinciferous, in which lead con-

  held in the starting concentrate rose to 0.72%.

  In addition, coarsely and finely divided oxidized sublimates are obtained, containing 45.1% by mass of zinc and 35.1% by mass of lead (6.1% by mass of lead.

  contained in the starting concentrate).

  Example 6 (given by way of comparison) The treatment of the sulfurized lead and zinc concentrate, described in example 1, is carried out according to the known method (US, A, 4519836), operating in the same manner.

  fusion group and under the same technological conditions

* giques. We use in this case a flux which is

  a mixture of limestone (56% by mass of cal-

  cium) and quartz sand (93% by mass of silicon dioxide). The mass ratio, in the charge, of the sum of SiO2 and A1203 to FeO is equal to 0.8; the mass ratio, in the charge, of the sum of CaO and MgO to FeO is equal to 0.51. The fusion is carried out in a vertical torch maintained in an atmosphere of technical oxygen (95% of 02) which one admits to the

  fusion in proportion to 220 m3t per tonne of the load.

  The amount. oxidized dust returned in con-

  continuous melt is 44.3% by mass relative to the quantity of the filler; the lead level in

dust is 62.1% by mass.

  At the end of the indicated treatment,

  raw lead, in which the lead contained in the con-

  starting center rose to 92.1%, as well as a lai-

  lead-depleted zinciferous tier, in which lead

- 23 -

  contained in the starting concentrate increased to 0.95%.

  In addition, coarsely oxidized and finely divided sublimates are obtained, containing 45.1% by mass of zinc and 34.3% by mass of lead (6.8% by mass of lead contained in the starting concentrate) o

  The above examples show that the realization

  sation of the treatment of sulphidic lead materials according to the process of the invention (examples 1 to 5) allows, compared to the known process (example 6), to increase from 0.9 to 1.1% the extraction rate lead from the starting sulfur materials in the raw lead

  (by mass calculating lead contained in the concentrate

  starting point). In addition, we obtain a reduction in the quantity of zinc returned to smelting together with recycled dust, which amounts to 4.8 to 21.7% absolute (by calculating the mass of lead contained

in the starting concentrate).

  EXAMPLE 7 A sulfur and lead sulphide concentrate is subjected to the treatment, containing 52.3% by mass of lead, 8.6% by mass of zinc, 1.8% by mass of copper, 3.82% by mass of iron, 15.97% by mass of sulfur sulphides, 4.52% by mass of silicon dioxide, 1.28% by mass of calcium oxide, 0.65% by mass

  aluminum oxide and 0.26% by mass of ma-

  gnesium. The processing is carried out as in the example-

  ple 1. The mass ratio between the calcium oxide and the iron present in the flux is in this case equal to 0.60. Said flux is added in proportion to 15% of the mass of the starting concentrate, calculating

  in total amount of calcium oxide and pre-

  smells in the fondant. The merger takes place in a

  vertical torch maintained in an oxygen atmosphere

  technical gene (95% of 02) which is admitted to fusion in proportion to 242 m3A per tonne of load. The quantity of oxidized dust continuously returned to the fusion is 9.4% by mass relative to the

  amount of charge; lead levels in pushers

sières is 61.6% by mass.

- 24 -

  At the end of the indicated treatment, raw lead containing 2.01% by mass of copper is obtained, produced

  wherein the lead in the d6- concentrate

  share rose to 93.0%, as well as a lead-depleted zinc slag, in which the lead contained in the starting concentrate rose to 0.81%, and also a matte containing 20.1% by mass of copper , a product in which the lead in the starting concentrate has increased to 4.3%. In addition, coarsely and finely divided oxidized sublimates are obtained, containing 43.9% by mass of zinc and 32.4% by mass of lead (1.8% of the

  mass of lead contained in the starting concentrate).

  E-xample 8 A sulfur and lead sulphide concentrate is subjected to the treatment, containing 51.12% by mass of lead, 9.11% by mass of zinc, 0.73% by mass of copper, 3.61% by weight. mass of iron, 16.31% by mass of sulfur sulphides, 4.48% by mass of silicon dioxide, 1.49% by mass of calcium oxide, 0.68% by mass

  aluminum oxide and 0.39% by mass of ma-

  gnesium. To do this, we prepare the load by adding

  a fondant with the starting concentrate. As a foundation

  In a mixture of limestone (56% by mass of calcium oxide) with pyrite (42% by mass of iron), the mass ratio between calcium oxide and

  the iron present in the mixture being equal to 0.60. The-

  said fondant is added in proportion to 5% of the mass of the starting concentrate, calculating in total amount

  calcium oxide and iron present in the fungus

  dant. The charge thus obtained contains 47.68% by mass of lead, 8.39% by mass of zinc, 0.67% by mass of copper, 6.21% by mass of iron, 18, 32% by mass of

  sulfur sulfides, 4.13% by mass of si

  silicon, 3.09% by mass of calcium oxide, 0.63% by mass of aluminum oxide and 0.36% by mass of magnesium oxide.

- 25 -

  The charge consisting of the said sulphide concentrate and the flux is dried to a humidity level of 1% by mass and sent to fusion-in a group of fusions together with the oxidized dust recycled through a device provided with a burner whose diameter

  the effective cross-sectional area is 0.095 m.

  The feed rate is 1 t / h. The merger is

  rée in a vertical torch maintained in an att-

  technical oxygen mosphere (95% of 02) that we

  admits in proportion determined according to formula (1).

  Found: Of = 0, t492, Ca = 0.294, b = 0.214, A = 0.825, K = 1.483 (the height H of the fusion zone of the fusion group is equal to 2.0 m), B = 181. We infers that

  the flow rate (D) of the oxygen-containing gas, in calcu-

  lant oxygen, is 221 m3N per ton of the load, which, taking into account the concentration of oxygen in the oxygen-containing gas, that the flow of this

  the latter is 233 m per tonne of load.

  By proceeding in this way, an oxidized melt is obtained, essentially containing metal oxides, and a mixture of oxidized dust recycled with the gases resulting from the fusion. We separate in a

  electrofilter said dust with the resulting gases

  so much of the fusion and we continuously send back this dust

  25. to the merger. The amount of oxidized dust re-

  continuously turned in the fusion is 15.6% by mass relative to the quantity of the filler; the rate of

  lead in the dust is 62.2% by mass.

  The oxidized melt is filtered through a layer of coke which is used in an amount of 50 kg per tonne of the feed. Under these conditions, the metal oxides, mainly lead oxide,

  are reduced to metals.

  At the end of the indicated treatment,

  raw lead, in which the lead contained in the con-

  starting center increased to 93.8%, as well as a lai-

  lead-depleted zinciferous tier, in which lead

  contained in the starting concentrate increased to 0.43%.

  -26- The indicated molten products flow by gravity into the electrothermal zone of the melting group where the zinc slag is left to settle. When

  from decantation, zinc vapors are formed.

  bifers which, together with the gases from the electric zone

  trothermal, are sent to a post-com chamber

  bustion for the oxidation of said vapors. In this same device, air is admitted. The prevailing pressure

  in the afterburner is minus 68.6 Pa.

  Finally, coarsely and finely divided oxidized sublimates are obtained, containing 45.3% by mass of zinc and 35.1% by mass of lead (5.6% by mass of lead

  contained in the starting concentrate).

Example 9

  The treatment of a lead sulphide concentrate,

  holding 67.43% by mass of lead, 2.71% by mass of zinc, 0.48% by mass of copper, 2.84% by mass of iron,, 33% by mass of sulfur sulphides, 4.6 % by mass

  of silicon dioxide, 1.45% by mass of calcium oxide

  cium, 0.07% by mass of magnesium oxide, 0.01% by mass of aluminum oxide, is carried out as in Example 8. The charge prepared on the basis of this concentrate contains 62.10% in mass of lead, 2.50% by mass of zinc, 0.44% by mass of copper, 5.5% by mass of iron, 17.42% by mass of sulfur and sulphides, 4.24% by mass of dioxide silicon, 3.06% by mass of calcium oxide, 0.06% by mass of magnesium oxide,

  0.01% by mass of aluminum oxide. The merger is

  rée in a vertical torch maintained in an atmos-

  air sphere enriched in oxygen (80% of 02) which is admitted in quantity defined by formula (1). Found: r = 0.49, Ca = 0.294, Cb = 0.216, A = 0.824, K = 1.483 (for H = 2 m), B = 164. We deduce that the flow rate (D) of gas containing oxygen, by calculating oxygen, amounts to 200 m3N per tonne of the charge, which makes, taking into account the concentration of oxygen in the oxygen-containing gas, that the consumption of this

  the latter is 250 mON per tonne of load. The quan-

  - 27- oxidized dust returned continuously to the melting is 15.7% by mass relative to the amount of the charge; the lead level in the dust is

62.4% by mass.

  The oxidized melt is filtered through a layer of charcoal which is used in an amount of

86 kg per tonne of load.

  At the end of the indicated treatment,

  raw lead, in which the lead contained in the con-

  starting center rose to 93.9%, as well as a lai-

  lead-depleted zinciferous tier, in which lead

  contained in the starting concentrate increased to 0.41%.

  In addition, coarsely and finely divided oxidized sublimates are obtained, containing 44.2% by mass of zinc and 33.6% by mass of lead (5.6% by mass of lead

  contained in the starting concentrate).

  The above-mentioned examples 1 to 5, 8, 9 for carrying out the proposed process for treating lead-bearing products

  show that the realization of the pro-

  assigned according to examples 8 and 9 increases from 0.5 to

  0.9%, compared to examples 1 to 5, the rate of ex-

  pulling of lead which passes from sulphate products

  starting fumes in raw lead (by calculating in

  mass of lead contained in the starting concentrate).

  In addition, a reduction of 9.1% in mass is obtained in the consumption of the solid carbonaceous reducing agent, and of

  , 4% by mass that of the gas containing oxygen.

EXAMPLE 10 A mixture of a sulphurized concentrate of lead and of

  zinc and a lead sulphide ore, containing 40.39% by mass of lead, 8.24% by mass of zinc, 1.99% by mass of copper, 6.24% by mass of iron, 17.96 % by mass of sulfur of sulphides, 6.15% by mass of silicon dioxide, 2.28% by

  mass of calcium oxide, 2.76% by mass of aluminum oxide.

  minium 'and 2,05% by mass of magnesium oxide.

  To this end, the charge is prepared by adding a flux to the starting mixture, consisting of a concentrate

- 28 -

  and an ore. As a flux, a mixture of limestone (56% by mass of calcium oxide) with pyrite (42% by mass of iron) is used, the mass ratio between the calcium oxide and the iron present in the mixture being equal to 0.60. Said fondant is

  added in proportion to 5% of the mass of the sul-

  starting fume (concentrated mixture - ore), in calcu-

  total amount of calcium oxide and iron

  present in the fondant. The charge thus obtained con-

  holds 37.2% by mass of lead, 7.59% by mass of zinc, 1.83% by mass of copper, 8.63% by mass of iron, 19.84% by mass of sulfur sulphides, 5, 66% by mass of silicon dioxide, 3.82% by mass of calcium oxide, 2.54% by mass of aluminum oxide and

  1.89% by mass of magnesium oxide.

  The charge is dried to a humidity level of 1% by mass and sent to fusion in a group of

  melting, together with oxidized dust re-

  cycled, through a device provided with a burner whose effective diameter of the useful section is equal to 0.06 m. The feed rate is 1 t / h. The fusion is carried out in a vertical torch maintained in

  an atmosphere of technical oxygen (95% 02). We are-

  performs the fusion with a stoichiometric flow rate of gas containing oxygen, by calculating in oxygen, flow rate necessary for a complete oxidation of the lead, iron, zinc contained in the charge, which is equal to 50.4m3N per ton of the charge. The flow (Q) of gas containing

  oxygen, calculating oxygen, per 1 kg of sou-

  fre of the sulphides contained in the feed, is determined by the formula (3) o n = 1.30; Q is then equal to

  09616 m3N. Consumption of gases containing oxy-

  gene, calculating oxygen, reported consumption

  to the total sulfur content of the sulphides (198.4 kg)

  bare in a ton of load, amounts to -

  122.2 m3N. The total consumption of oxygen-containing gas, when calculating oxygen, constitutes 172.6 m3 per tonne of charge, which, taking into account the

- 29 -

  concentration of oxygen in the gas containing oxy-

  gene, that the consumption of the latter is 182 m

  per tonne of load * The height H of the fu-

  Zion of the fusion group is equal to 2.0 m.

  By proceeding in this way, an oxidized molten material is obtained containing essentially metal oxides, and also a mixture of recycled dust oxidized with the gases resulting from the fusion. Said dust is separated in an electrostatic precipitator from the gases resulting from the fusion and these are continuously returned

  fusion dust. The amount of oxy-

  the amount continuously returned to the fusion is 16.5% by mass relative to the quantity of the charge; the lead level in the dust is 62.5% in

mass.

  The oxidized melt is filtered through a layer of coke which is used in proportion to 52 kg per tonne of the feed. Under these conditions, the metal oxides, mainly lead oxide,

found reduced to metals.

  At the end of the indicated treatment, crude lead containing 0.55% by mass of copper is obtained, product in which the lead contained in the initial sulfurized product (concentrated mixture - ore) has increased to 93.1%, thus than a lead-depleted zinc slag in

  which lead contained in the sulfide product of

  share increased to 0.66%, and also a matte containing, 4% by mass of copper, product in which the lead contained in the starting sulfurized product passed to

3.5%.

  Said molten products flow by gravity into the electrothermal zone of the melting group where the lead-depleted zinc slag is abandoned.

  decantation. The lower layer of raw lead, already

  center at the bottom of the melting group, is cooled in

  - continuous by air up to a temperature of 650 C.

  When the slag is decanted, it forms

  fears of lead-bearing zinc which, together with

- 30 -

  gases from the electrothermal zone, are sent to a

  post-combustion chamber for the oxidation of the

  your vapors. In this same device, we also admit

  the air. The pressure in the post-com chamber

  bustion is minus 49 Pa. We finally obtain

  coarsely oxidized and finely divided sublimates,

  holding 45.5% by mass of zinc and 35.0% by mass of

  lead (2.6% of the mass of lead contained in the pro-

sulfur starting material).

  EXAMPLE 11 Treatment of a Mixture Consisting of a Sulfurized Lead and Zinc Ore and a Concentrated Sulfurized Lead Concentrate Containing 46.04% by Weight of Lead, 10.04% by Weight of Zinc, 2.20 % by mass of copper, 6.16% by mass of iron, 20.24% by mass of sulfur sulphides, 6.62% by mass of silicon dioxide, 2.18% by mass of calcium oxide, 2 , 39% by mass of aluminum oxide and 2.18% by mass of magnesium oxide is carried out as in Example 10. The charge prepared on the basis of this mixture contains 42.4% by mass of lead, 9.25% by mass of zinc, 2.03% by mass of copper, 8.56% by mass of iron, 21.94% by mass of sulfur sulphides, 6.1% by mass of silicon dioxide, 3 , 73% by mass of calcium oxide, 2.2% by mass of aluminum oxide and 2.01% by mass of magnesium oxide. The fusion is carried out in a vertical torch maintained in a

  technical oxygen atmosphere (95% 02). We do

  kills the fusion with a stoichiometric consumption of gas containing oxygen, by calculating in oxygen, consumption necessary for a complete oxidation of lead, iron, zinc contained in the charge, which is

  equal to 55.8 m per tonne of load. Consumption

  tion (Q) of oxygen-containing gas, calculating in oxygen, per 1 kg of sulfur sulphides contained in the feed is determined according to formula (3) where n = 1.05; Q is then equal to 0.632 m .; Consumption of oxygen-containing gas, calculating oxygen, related to the total sulfur (219.4 kg) of sulfides

- 31 -

  contained in one ton of the load constitutes 138.7 mN. The total consumption of oxygen-containing gas, when calculating oxygen, amounts to 194.5 m N per tonne of charge, which taking into account the concentration of oxygen in the gas containing l oxygen, that the consumption of the latter constitutes 204 m3N per tonne of the load. The quantity of oxidized dust returned to the fusion is 16.5% by mass relative to the quantity of the feed; the lead level in the dust is 62.0% by mass. By proceeding in this way, raw lead is obtained containing 0.88% by mass of copper, a product in which

  the lead contained in the starting sulfur product (

  lange ore - concentrate) rose to 93.0%, as well as a lead-depleted zinc-bearing slag, in which the lead contained in the starting sulfur product rose to 0.68%, and also a mat containing 26.8 % copper, product in which the lead contained in the

  sulfur starting product increased to 3.41%.

  The lower layer of raw lead, adjacent to the bottom of the melting group, is continuously cooled by

  air up to a temperature of 9000C.

  Besides the products listed above, we also obtain coarsely and finely divided oxidized sublimates, containing 44.1% by mass of zinc and, 6% by mass of lead (2.8% by mass of lead

  contained in the initial sulfurized product).

Example 12

  A mixture consisting of a lead and zinc sulphide mineral and a lead concentrate is subjected to the treatment, a mixture containing 46.04% by mass of lead,. 04% by mass of zinc, 2.20% by mass. of copper, 6.16% by mass of iron, 20.24% by mass of sulfur sulphides, 6.62% by mass of silicon dioxide, 2.18% by mass of calcium oxide, 2.39% en masse

  of aluminum oxide and 2.18% by mass of maize oxide

  gnesium, proceeding as in Example 10. The

- 32 -

  feed prepared from this mixture contains 42.4% by mass of lead, 9.25% by mass of zinc, 2.03% by mass of copper, 8.56% by mass of iron, 21.94% by mass of

  sulfur sulfides, 6.1% by mass of silicon dioxide

  cium, 3.73% by mass of calcium oxide, 2.2% by mass

  aluminum oxide and 2.01% by mass of magnesium oxide

  sium. The fusion is carried out in a vertical torch in-

  maintained in an atmosphere of technical oxygen (95% 02). We perform the fusion with a consumption

  stoichiometric of oxygen-containing gas, calcu-

  oxygen, consumption necessary for an oxidation

  complete lead, iron, zinc content in the

  load, which is equal to 55.8 m .; per tonne of load.

  The consumption (Q) of oxygen-containing gas, in

  calculating in oxygen, related to 1 kg of sulfur

  fures contained in the charge, is determined by the form-

  mule (3) o n = 1.05; Q is then equal to 0.632 m3N. Consumption of oxygen-containing gas, calculating oxygen, based on total sulfur (219.4 kg)

  sulfides contained in one tonne of feed,

  titrates 138.7 mAt. The total consumption of oxygen-containing gas, when calculating oxygen, amounts to 194.5 min per tonne of charge, which, taking into account the concentration of oxygen in the oxygen-containing gas, that the consumption of the latter constitutes 204 m3N per tonne of load. The quantity of oxidized dust returned continuously to melting is 16.4% by mass relative to the quantity of the charge; the lead level in the dust is 62.1% in

mass.

  At the end of the indicated treatment, raw lead is obtained containing 0.56% by mass of copper, produced in

  which lead contained in the sulfide product of

  share (ore-concentrate mixture) increased to 93.2%,

  as well as a lead-depleted zinc-bearing slag, in the-

  which the lead contained in the starting sulfurized product passed to 0.73%, and also a matte containing 25.9% by mass of copper, product in which the lead contained

- 33 -

  in the starting sulfur product increased to 3.55%.

  The inner layer of raw lead, adjacent to the bottom of the fusion unit, is continuously cooled by

  air up to a temperature of 650 C.

  Besides the products previously listed,

  also holds coarsely oxidized and fi-

  divided, containing 44.9% by mass of zinc and

  , 1% by mass of lead (2.4% by mass of lead

  held in the starting sulfur product).

  EXAMPLE 13 A mixture consisting of a sulfur sulphide of lead and zinc and a concentrate of lead is subjected to the treatment, a mixture containing 46.04% by mass of lead,. 04% by mass of zinc, 2.20%. by mass of copper, 6.16% by mass of iron, 20.24% by mass of sulfur sulphides, 6.62% by mass of silicon dioxide, 2.18% by mass of calcium oxide, 2, 39% by mass of aluminum oxide and 2.18% by mass of magnesium oxide, proceeding as in Example 10. The charge prepared on the basis of this mixture contains 42.4% by mass of lead, 9.25% by mass of zinc, 2.03% by mass of copper, 8.56% by mass of iron, 21.94% by mass of sulfur sulphides 6.1% by mass of silicon dioxide, 3, 73%

  by mass of calcium oxide, 2.2% by mass of aluminum oxide

  minimum and 2.01% by mass of magnesium oxide. The fu-

  Zion is operated in a vertical torch maintained in an atmosphere of oxygen-enriched air (70% of

  02) * We perform the fusion with a stoe-

  chiometric of gas containing oxygen, calculating in oxygen, consumption necessary for a complete oxidation of the. lead, iron, zinc contained in the

  load, which is 55.8 mA per tonne of load.

  The consumption (Q) of oxygen-containing gas, in

  calculating in oxygen, related to 1 kg of sulfur

  fures contained in the charge, is determined according to the

  formula (3) o n = 0.65; Q is then equal to 0.658 m3N.

  The consumption of oxygen-containing gases, in calcu-

  oxygen, based on the totality (219.4 kg) of sulfur sulfides contained in one tonne of the feed,

  constitutes 144.3 mN * The total consumption of gas

  oxygen, by calculating oxygen, amounts to, 1 m3N per tonne of the charge, which makes, taking into account the concentration of oxygen in the gas containing oxygen, that the consumption of the latter constitutes 286 m3N. per tonne of load. The quantity of oxidized dust returned continuously to melting is 17.2% by mass relative to the quantity of the charge; the lead level in the dust is 61.7% by mass. At the end of the indicated treatment, raw lead is obtained containing 0.62% by mass of copper, produced in

  which lead contained in the sulfide product of

  share (ore-concentrate mixture) increased to 93.1%,

  as well as a lead-depleted zinc-bearing slag, in the-

  which the lead contained in the starting sulfurized product passed to 0.75%, and also a matte containing 25.5% by mass of copper, product in which the lead contained

  in the starting sulfur product increased to 3.72%.

  The lower layer of raw lead, adjacent to the bottom of the melting group, is continuously cooled by

  air up to a temperature of 650C.

  Besides the products listed above,

  also holds coarsely oxidized and fi-

  divided, containing 45.0% by mass of zinc and

  0.0% by mass of lead (2.3% by mass of lead

  held in the starting sulfur product).

Example 14

  A mixture consisting of a sulphide ore of lead and zinc and a concentrate of lead is subjected to the treatment, a mixture containing 46.04% by mass of lead,. 04% by mass of zinc, 2.20% by mass. of copper, 6.16% by mass of iron, 20.24% by mass of sulfur under

  form of sulphides, 6.62% by mass of silicon dioxide

  cium, 2.18% by mass of calcium oxide, 2.39% by mass of aluminum oxide and 2.18% by mass of magnesium oxide by proceeding as in Example 10. The

26.16446

  Charge prepared from this mixture contains 42.4% by mass of lead, 9.25% by mass of zinc, 2.03% by mass of copper, 8.56% by mass of iron, 21 , 94% by mass of sulfur in the form of sulphides, 6.1% by mass of silicon dioxide, 3.73% by mass of calcium oxide, 2.2% by mass of aluminum oxide and 2 0.01% by mass of oxide

* magnesium. The fusion takes place in a vertical torch.

  hold maintained in an atmosphere of technical oxygen

  (95% of 02) * The fusion is carried out with a consumption

  stoichiometric tion of oxygen-containing gas, calculating in oxygen, consumption necessary for complete oxidation of the lead, iron, zinc contained in the charge, which is equal to 55.8 m per ton of the

  load. * The consumption (Q) of gas containing oxy-

  gene, by calculating in oxygen, related to 1 kg of sulfur

  sulphides contained in the feed, is determined se-

  lon formula (3) where n = 1.05; Q is then equal to 0.632 m3N. The consumption of oxygen-containing gas, by calculating oxygen, related to the totality (219.4 kg) of the sulfur of the sulphides contained in one tonne of the load, constitutes 138.7 m3. The total consumption of oxygen-containing gas, when calculating oxygen, amounts to 194.5 m3N per tonne of charge, which, taking into account the concentration of oxygen in the oxygen-containing gas, that the consumption of the latter constitutes 204 m3q per tonne of the load. The quantity of oxidized dust continuously returned to

  the merger is 15.5% by mass compared to the quan-

  charge charge; the lead level in the dust

is 61.9% by mass.

  At the end of the indicated treatment, raw lead containing 0.33% by mass of copper is obtained, a product in which the lead contained in the starting sulfur product (ore-concentrate mixture) has increased to 93.3%, as well as '' a lead-depleted zinc-bearing slag in which the lead contained in the initial sulfurized product has increased to 0.70%, and also a matte containing 24.1% by mass of copper, product in which the lead contained

  in the starting sulfur product increased to 3.88%.

  -36 - The lower layer of raw lead, adjacent to the bottom of the melting group, is continuously cooled

  by air up to a temperature of 33,000.

  Outside of the previously listed products,

  holds coarsely and finely divided oxidized sublimes, containing 44.7% by mass of zinc and 35.1% by mass

  lead (2.0% of the mass of lead contained in the pro-

sulfur starting material).

  The aforementioned examples 7, 10 to 14 of carrying out the proposed process for treating lead-bearing products

  sulfides show that carrying out the process

  lon examples 10 A 14 allows to significantly improve, compared to example 7, the quality of lead and

  matte. In these examples, we see the need to disappear

  coarse refining of raw lead, which

copper barrasse.

Example 15

  The treatment of the lead and zinc sulphide concentrate, described in Example 1, is carried out as in Example 1. The feed used contains 47.08% by mass of lead, 8.39% by mass of zinc , 0.67% by mass of copper, 6.21% by mass of iron, 18.32% by mass of sulfur sulphides, 4.13% by mass of silicon dioxide, 3.09% by mass of oxide of calcium, 0.63% by mass of aluminum oxide, 0.36% by mass of magnesium oxide. The prepared charge is sent to the fusion in a fusion group, together with the recycled oxidized dust, through a device provided with a burner whose effective diameter of the useful section (de) is determined according to formula (4). The density (?)

  technical oxygen is 1.42 kg / m3, the con-

  summation of the load (M) is equal to 0.278 kg / s, the desulfurization rate (C) is equal to 1.0, the parameter remains equal to 0.2176 s (the calculation of is carried out according to formula 5) . The effective diameter of the useful section (of) of the burner is equal to 0.089 m. The quantity of oxidized dust continuously returned to the fusion is 16.4% by mass relative to the quantity of the

- 37 -

  charge; the lead level in the dust is

59.18% by mass.

  At the end. from the treatment indicated, crude lead is obtained, in which the lead contained in the starting concentrate has increased to 93.4%, as well as a lead-depleted zinc-bearing slag, in which the lead contained in the

  starting concentrate increased to 0.41%. In addition, we ob-

  holds coarsely and finely divided oxidized sublimates

  containing 46.1% by mass of zinc and 33.4% by mass

  lead (6.1% of the mass of lead contained in the

starting center).

  : emle le16 The treatment of the lead and zinc sulphide concentrate, described in Example 8, is carried out as in Example 8. The prepared charge is sent to the fusion in a fusion group, together with the recycled oxidized dust. , through a device provided with a braleur whose effective diameter of the useful section (de) is determined according to formula (4). The density (O) of technical oxygen is 1.42 kg / m3, consumption

  load (M) is 0.278 kg / s, the desulfurization rate

  tion () is 1.0, the parameter _ is equal to

  0.2176 s (the calculation of C 'is carried out according to formula 5).

  The effective diameter of the useful section (of) of the burner is equal to 0.089 m. The quantity of oxidized dust returned continuously to melting is 15.1% by mass relative to the quantity of the charge; lead level

  in dust is 60.87% by mass.

  At the end of the indicated treatment, crude lead is obtained, in which the lead contained in the starting concentrate has increased to 94.0%, as well as a lead-depleted zinc-bearing slag, in which the lead contained in the

  starting concentrate increased to 0.44%. In addition, we ob-

  holds sublimates coarsely oxidized and finely di-

  targeted, containing 45.3% by mass of zinc and 34.1% by mass of lead (5.5% by mass of lead contained in

the starting concentrate).

-38-

Example 17

  Processing the mixture consisting of a sulphide ore

  furé and a sulphide concentrate of lead and zinc,

  lange described in exeMle 10, is carried out as in Example 10. The prepared charge is sent to the fusion in a fusion group, together with the recycled oxidized dust, through a device provided with a burner whose diameter effective of the useful section (of) is determined according to formula (4). The density (ji)

  technical oxygen is 1.42 kg / m3, the consumption

  tion (M) of the load is 0.278 kg / s, the rate of de-

  sulfurization (J) is 0.5, the parameter 'V is equal to

  0.101 s (the calculation of tL is carried out according to formula 5).

  The effective diameter of the useful section (of) of the burner is equal to 0.043 m. The quantity of oxidized dust returned continuously to melting is 16.4% by mass relative to the quantity of the charge; lead level

  in dust is 62.6% by mass.

  At the end of the indicated treatment, lead is obtained

  crude containing 0.5% mg of copper, produced in the-

  which the lead contained in the starting sulfur product (concentrated ore mixture) rose to 93.3%, as well as a zinc-bearing slag depleted in lead, in which the lead contained in the starting sulfur product rose to 0.61 %, and also a matte containing 26.6% by mass of copper, a product in which the lead contained in the initial sulfurized product rose to 3.1%. In addition, coarsely and finely divided oxidized sublimates are obtained, containing 45.5% by mass of zinc and 35.1% by mass of lead (2.9% by mass of lead

  contained in the initial sulfurized product).

  Claim 18B The treatment of the lead and zinc sulphate concentrate, described in example 1, is carried out as in

  Example 1, except that before admitting

  portion of the melting charge through a device fitted with a burner, part of the charge is reduced, in proportion to 8.8% of the mass of the starting charge,

- 39 -

  up to four times the particle size

  higher than that of the particles of the initial charge, after which the reduced fraction of the charge is mixed

  with its remaining part and we send everything to the fusion.

  The quantity of oxidized dust continuously returned

  at merger is 1393% by mass compared to the quan-

  charge charge; the lead level in the dust

is 62.3% by mass.

  The oxidized melt is filtered through a layer of coke which is used in proportion to

48 kg per tonne of load.

  At the end of the indicated treatment, crude lead is obtained, in which the lead contained in the starting concentrate has increased to 93.5%, as well as a lead-depleted zinc-bearing slag, in which the lead contained in the

  starting concentrate increased to 0.7%. In addition, we ob-

  holds sublimes coarsely and finely divided oxidized

  containing 45.6% by mass of zinc and 34.7% by mass of lead (5.8% by mass of the lead contained in

the starting concentrate).

Example 19

  The treatment of the lead and zinc sulphide concentrate, described in Example 1, is carried out as in Example 1, except that before the admission of the charge to fusion through a device provided

  a burner reduces part of the load,

  8.8% portion of the mass of the initial charge,

  up to eight times the particle size

  lower than that of the particles of the starting charge,

  after which the reduced fraction is mixed with the

  remaining part of the charge and we send everything to the fu-

  if we. The amount of oxidized dust returned continuously to melting is 15.3% by mass compared to

  the amount of the charge; lead levels in pushers

sières is 59.9% by mass.

  The oxidized melt is filtered through a layer of coke which is used in proportion to

49 kg per tonne of load.

  -40 - At the end of the indicated treatment, crude lead is obtained, in which the lead contained in the starting concentrate has gone 6 to 93.6%, as well as a lead-depleted zinc-bearing slag, in which the lead contained in the starting concentrate increased to 0.7%. In addition, we ob-

  holds coarsely and finely divided oxidized sublimates

  seeds, containing 45.5% by mass of zinc and 34.8% by mass

  lead (5.6% of the mass of lead in the container

starting center).

  Example 20 The treatment of the lead and zinc sulphide concentrate, described in Example 8, is carried out as in Example 8, with the difference that before the admission of the charge to fusion through a device provided

  a burner reduces part of the load,

  8.8% portion of the mass of the initial charge, Juice-

  that at a particle size six times smaller than that of the particles of the starting charge, after which the reduced part is mixed with the remaining part of the charge and the whole is sent to fusion. The quantity of oxidized dust returned continuously to melting is 16.0% by mass relative to the quantity of the feed; the lead level in the dust is

61.3% by mass.

  The oxidized melt is filtered through a layer of coke which is used in proportion to

43 kg per tonne of load.

  At the end of the indicated treatment, crude lead is obtained, in which the lead contained in the starting concentrate has increased to 94.1%, as well as a lead-depleted zinc slag, in which the lead contained in the

  starting concentrate increased to 0.44%. In addition, we ob-

  holds coarsely and finely divided oxidized sublimates

  containing 45.4% by mass of zinc and 34.3% by mass of lead (5.4% by mass of the lead contained in the con-

starting center).

Example 21

  Treatment of lead sulphide concentrate and

_-41 -

  zinc, described in example 8, is carried out as in example 8, except that before the admission of the charge to the fusion through a device provided with a burner, 13% of the mass is reduced of the feedstock to a particle size six times smaller than that of the particles of the feedstock, after which the reduced fraction is mixed with the portion

  remaining charge and send it all to fusion.

  The quantity of oxidized dust continuously returned

  on merger is 16.3% by mass compared to the quan-

  charge charge; the lead level in the dust

is 61.0% by mass.

  The oxidized melt is filtered through a layer of coke which is used in proportion to

44 kg per tonne of load.

  At the end of the indicated treatment, crude lead is obtained, in which the lead contained in the starting concentrate has passed to 94.1%, as well as a lead-depleted zinc-bearing slag, in which the lead contained in the

  starting concentrate increased to 0.46%. In addition, we ob-

  holds sublimates coarsely oxidized and finely di-

  targeted, containing 45.5% by mass of zinc and 34.5% by mass of lead (5.4% by mass of lead contained in

the starting concentrate).

Example 22

  Processing the mixture consisting of a sulphide ore

  fume of lead and of a sulphide concentrate of lead and zinc, mixture described in Example 10, is carried out as in Example 10, except that before

  admission of the charge to the merger through a provision

  with a burner, part of the load is reduced,

  in proportion to 4.5% of the mass of the

  share, up to a particle size of six times in-

  lower than that of the particles of the starting charge, after which the reduced fraction is mixed with the part

  remaining charge and send it all to fusion.

  The quantity of oxidized dust continuously returned

  on merger is 16.6% by mass compared to the quan-

- 42 -

  charge charge; the lead level in the dust

is 62.2% by mass.

  The oxidized melt is filtered through a layer of coke which is used in proportion to 48 kg per tonne of the feed. At the end of the indicated treatment, raw lead containing 0.56% of copper is obtained, a product in which the lead contained in the starting sulfur product (mixture

  ore - concentrate) increased to 93.4%, as well as

  lead-depleted zinciferous tier, in which lead -

  contained in the initial sulfurized product increased to 0.6%, and also a matte containing 26.2% by mass of

  copper, a product in which the lead contained in the pro-

  sulfur starting material increased to 3.2%. In addition, coarsely and finely divided oxidized sublimates are obtained, containing 45.3% by mass of zinc and 34.4% by mass of lead (2.7% by mass of lead contained in

the starting sulfur product).

  The above examples 1, 8, 10, 18 to 22 of

  tion of the proposed process for processing plom-

  sulfurized bifers show that carrying out the process according to examples 18 to 22 makes it possible to increase from 0.2 to 0.5%, compared to examples 1, 8, 10, the rate of extraction of lead which passes from sulphide starting products in raw lead (by calculating the mass of lead contained in the starting sulphide product). In addition, the

  consumption of the solid carbonaceous reducer is reduced

cloud from 8 to 14% by mass.

Example 23

  The treatment of the lead and zinc sulphide concentrate, described in Example 1, is carried out as in

  Example 1. The amount of oxidized dust returned-

  born continuously from fusion is 16.4% by mass relative to the quantity of the filler; lead level

  in dust is 61.7% by mass.

  At the end of the indicated treatment, raw lead is obtained, in which the lead contained in the

-2616446

- 43 -

  departure increased to 93.2%, as well as a lead-depleted zinc-bearing slag, in which the lead contained in the

  starting concentrate increased to 0.59%.

  The pressure in the afterburner chamber-

  tion during the oxidation by air of the lead zinc vapors formed during the slag settling

zinciferous is minus 19.6 Pa.

  Finally, coarse oxidized sublimates are obtained.

  rely divided, containing 8.13% by mass of lead and 48.2% by mass of zinc, in which the lead contained in the starting concentrate rose to 1.2%. Said coarsely divided oxidized sublimates are deposited in the afterburner. In addition, finely divided oxidized sublimates are obtained, containing 61.2% by mass of lead and 10.75% by mass of zinc, in which the lead contained in the starting concentrate rose to 4.9%. Said finely divided sublimates are isolated in bag filters and then sent to fusion in the

fusion group.

Example 24

  The treatment of the lead and zinc sulphide concentrate, described in Example 8, is carried out as in

  Example 8. The amount of oxidized dust returned-

  born continuously from the merger is 15.6% based on the quantity of the filler; the lead level in

  dust is 62.2% by mass. At the end of the milking

  As indicated, raw lead is obtained, in which the lead contained in the starting concentrate has risen to 93.9%, as well as a lead-depleted zinc-bearing slag, in which the lead contained in the starting concentrate

rose to 0.38%.

  The pressure in the afterburner chamber.

  tion during the oxidation by air of the lead-bearing zinc vapors formed during the slag settling

zinciferous is minus 0.1 Pa.

  Finally, coarse oxidized sublimates are obtained.

  rely divided, containing 8.0% by mass of lead and 4.3% by mass of zinc, in which the lead contained

- 44 -

  in the starting concentrate increased to 1.2%. Said coarsely divided oxidized sublimates are deposited in the afterburner. In addition, finely divided oxidized sublimates are obtained, containing 61.1% by mass of lead and 28.9% by mass of zinc, in which the lead contained in the starting concentrate rose to 4.4%. Said finely divided sublimates are isolated in bag filters and then sent to fusion in the

fusion group.

Example 25

  Processing the mixture consisting of a sulphide ore

  lead fume and a sulfur and lead sulfur concentrate, mixture described in Example 10, is carried out

  as in Example 10. The amount of oxy-

  the amount continuously returned to the fusion is 16.5% by mass relative to the quantity of the charge; the rate of

  lead in the dust is 62.5% by mass.

  At the end of the indicated treatment, raw lead containing 0.55% of copper is obtained, in which the lead

  contained in the initial sulfurized product (mixed

  centered - ore) rose to 93.3%, as well as a lead-depleted zinc-bearing slag, in which the lead contained in the starting sulfur product rose to 0.46%, and also a matte containing 25.4% copper, in which the lead in the starting sulfur product is

increased to 3.5%.

  The pressure in the afterburner chamber-

  tion during the oxidation by air of lead-bearing zinc vapors formed during the settling of slag

zinciferous is more 19.6 Pa.

  Finally, coarse oxidized sublimates are obtained.

  rely divided, containing 9.8% by mass of lead and 56.5% by mass of zinc, in which the lead contained

  in the starting sulfur product increased to 0.5%.

  Said coarsely divided oxidized sublimates are deposited in the afterburner. In addition, finely divided oxidized sublimates are obtained, containing 59.3%.

  by mass of lead and 12.1% by mass of zinc, in the-

  -45- which lead contained in the starting sulfur product

  rose to 2.1%. Said finely divided oxidized sublimates

  are isolated in bag filters and then sent

  to merge into the merge group.

  The aforementioned examples 1, 8, 10, 23 to 25 of realization

  tion of the proposed process for processing plom-

  sulfurized bifers show that carrying out the process according to examples 23 to 25 makes it possible, with respect to examples 1, 8, 10, to enrich the sublimed with lead.

  finely divided oxidized. This is what allows them to

  lead to fusion and, consequently, to increase by 0.1 to 0.2% the rate of extraction of lead passing from

  sulphide starting materials in raw lead (in cal-

  massing lead contained in the sulfurized product

departure).

  Claim 26 The treatment of the sulfurized lead and zinc concentrate, described in Example 8, is carried out as in

  Example 8, except that before admitting

  sion of the charge to fusion through a device fitted with a burner, a part of the charge is reduced, in an amount of 8.8% of the mass of the starting charge, up to a particle size of six times lower than that of the particles of the starting charge, after

  what the reduced fraction is mixed with the res-

  aunt of the charge and we send it all to the fusion in the fusion group, together with the dust

  oxidized recycled through the device with br / l-

  their. The effective diameter of the useful section (of) of the burner is determined according to formula (4). The density

  technical oxygen (jô) is 1.42 kg / m3, the con-

  summation of the charge (M) is 0.278 kIcg / s, the desulfurization rate () is 1.0, the parameter 'is equal

  at 0.2176 s (the calculation of 'V is carried out according to formula 5).

  The effective diameter of the useful section (of) of the burner is equal to 0.089 m. The quantity of oxidized dust continuously returned to the melting is 15.6% by mass relative to the quantity of the charge; lead level

  in dust is 62.20% by mass.

- 46 -

  At the end of the indicated treatment, crude lead is obtained, in which the lead contained in the starting concentrate has increased to 94.4%, as well as a lead-depleted zinc-bearing slag, in which the lead contained in the concentrate of departure increased to 0.38%.

  The pressure in the afterburner chamber-

  tion during the oxidation by air of the lead-bearing zinc vapors formed during the slag settling

zinciferous is minus 0.1 Pa.

  We finally get coarse oxidized sublimates-

  divided, containing 8.0% by mass of lead and 35.6% by mass of zinc, in which the lead contained in the starting concentrate rose to 1.2%. Said coarsely divided oxidized sublimes are deposited in the chamber

  afterburner. In addition, oxy-

  finely divided dice, containing 61.1% by mass of lead

  and 28.9% by mass of zinc, in which the lead con-

  held in the starting concentrate rose to 4.0%. The-

  said finely divided oxidized sublimates are isolated in bag filters and then sent to fusion in the

fusion group.

  The aforementioned examples 8 and 26 of carrying out the

  proposed sale of treatment of sulphurous lead products

  res show that carrying out the process according to

  -example 26 allows, compared to example 8, of hooking-

  the extraction rate of lead passing from 0.6%

  sulphide starting products in raw lead (in calcu-

* by mass of lead contained in the sulfurized product

departure).

  Example 27 The treatment of a mixture consisting of a sulphide of lead ore and a sulphide of lead and zinc concentrate, a mixture described in Example 10, is carried out as in Example 10, except that 'before

  admission of the charge to the merger through a provision

  with a burner, part of the charge is reduced, in an amount of 4.5% of the mass of the initial charge, to a particle size of six times

- 47. -

  inside that of the particles of the initial charge, after which the reduced fraction is mixed with the remaining part of the charge and the whole is sent to fusion, together with the oxidized dust recycled through the device provided with a braleur in the fusion group. The effective diameter of the useful section (of) of the burner is determined according to formula (4). The density

  (J) technical oxygen is 1.42 kg / m3, the consumption

  mation (M) of the load is 0.278 kg / s, the rate of de-

  sulfurization (&) is 0.5, the test parameter equal to

  0.101 s (the calculation of. Is carried out according to formula 5).

  The effective diameter of the useful section (of) of the burner is equal to 0.043 m. The quantity of oxidized dust returned continuously to melting is 16.5% by mass relative to the quantity of the charge; lead level

  in dust is 62.5% by mass.

  At the end of the indicated treatment, raw lead is obtained containing 0.45% by mass of copper, in which the lead contained in the starting sulfur product (mixture

  concentrate - ore) rose to 93.8%, as well as

  lead-depleted zinciferous tier, in which the lead contained in the initial sulfurized product rose to - 0.45%, and also a matte containing 27.1% by mass of copper, in which the lead contained in the product

  sulphide starting material increased to 3.1%.

  The pressure in the afterburner chamber-

  tion during the oxidation by air of the lead-bearing zinc vapors formed during the slag outfall

zinciferous is more 19.6 Pa.

  We finally get coarse oxidized sublimates-

  divided, containing 9.8% by mass of lead and 56.5% by mass of zinc, in which the lead contained in

  sulfur starting product increased to 0.5%. The said

  coarsely divided oxidized oxidized deposits in the

  afterburner. In addition, we obtain

  finely divided oxidized blimés, containing 59.3% by mass of lead and 12.1% by mass of zinc, in which the lead contained in the starting sulfur product is

- 48 -

  increased to 2.1%. Said finely divided oxidized sublimates are isolated in bag filters and then sent to the

fusion in the fusion group.

  The aforementioned examples 10 and 27 of carrying out the proposed process for treating lead-bearing products

  sulfides show that carrying out the process

  lon example 27 allows, compared to example 10,

  increase the lead extraction rate by 0.7%

  health of sulphide starting products in raw lead (by mass calculating lead contained in the product

starting sulfur).

  The proposed mineral processing method

  lead sulfides and lead ores and zinc sulfides

  res and / or concentrates therefore makes it possible to extract efficiently-

  lead from said sulphide products, and no-

  as much to increase from 0.9 to 2.3%, compared to the pro-

  ceded known, the lead extraction rate passing into the raw lead (by calculating by mass of the lead contained in the starting sulfur product). In addition, the process of the invention makes it possible to extract sulfur from the indicated sulfurized products, by virtue of the formation of gases (resulting from fusion) with a high sulfur content (30 to

  % by mass), these gases can be used in the manufacture

  cation of sulfuric acid; it makes it possible to pass the zinc through a zinc-bearing slag depleted in lead and in coarsely divided oxidized sublimates, as well as to pass the copper (in the case where its rate in the initial sulfur-containing products is greater than 1%

  en masse) in a marketable matte.

  Of course, various modifications can be made by those skilled in the art to the process which comes

  d'Otre described only as non-limiting examples

  without departing from the scope of the invention.

-49-

Claims (7)

  1. Process for processing sulphurous lead ores   resides or sulphides of lead and zinc and / or their concentrates, containing metal compounds, including those of iron and copper, silicon dioxide,   aluminum, calcium and magnesium oxides,   assigned including admission to the merger of a charge   consisting of said sulphide products and a flux,   joining with the oxidized dust recycled through a device fitted with a burner, the fusion of said   charge together with recyc- oxidized dust   lées in a vertical torch maintained in an atmos-   sphere of an oxygen-containing gas, obtaining an oxidized melt containing essentially oxides   of metals, and a mixture of oxidized dust recyc-   with gases resulting from fusion, separation   said recycled oxidized dust. with the gases   resulting from the melting and the return of this dust to the melting, the reduction of metal oxides, mainly lead oxide, down to metals by filtration of the oxidized molten material through a layer of a solid carbonaceous material, by obtaining a raw lead and a lead-depleted zinc-bearing slag, the settling of this slag   which gives rise to lead-bearing zinc vapors, the oxy-   donation of said lead-bearing zinc vapors by an oxygen-containing gas which provides coarsely and finely divided oxidized sublimates, said process being characterized in that, as a flux, a   mixture of limestone or lime with a ferri-   fere, the mass ratio between the calcium oxide and the iron present in the mixture being between 0.43 and 0.76, said mixture being used in a proportion of 5 to 22% relative to the mass of ore and / or the starting concentrate, calculating the total amount of   the calcium oxide and iron present in this mixture.   2. Method according to claim 1, -caractérisé in that one carries out the fusion of the load jointly   with recycled oxidized dust with consumption - 50 -   tion of the oxygen-containing gas, calculating in oxy-   gene, less than stoichiometric amount, necessary   for complete oxidation of metals and sulfur   sulfides present in the feed, obtaining final-   apart from raw lead and the zinc zinc slag ap-   poor in lead, a mat enriched with copper.   3. Method according to claim 1, characterized in that the melting of the charge together with the   recycled oxidized dust is operated with a consumption   the oxygen-containing gas determined according to the following formula: P = A'B! K,   o P is the consumption of the oxygen-containing gas, calculating in oxygen gfi m3N per tonne of charge, A = 1.542 - 3.299Ca - 7.972Cb - 4, 285Cf + 28.8510a0b + + 14.657CaCf + 27.370bCf - 88.895CbCfCa, o Ca + Cb + Cf = 1 is the sum of the concentrations in the charge of the acid oxides Ca (SiO2 and A1203),   basic oxides Cb (CaO and MgO) and iron Of (in cal-   culant in FeO), the concentrations being expressed in mass parts B is the stoichiometric consumption of oxygen   being part of the oxygen-containing gas, consumption   tion necessary for complete oxidation of the metals and sulfur of the sulphides present in the m3N loader per tonne of the load,   E --l +, where oH is the height of the fu-   sion, in m 4. Method according to claim 1, characterized in that the melting of the charge together with the   recycled oxidized dust is operated with a consumption   stoichiometric measurement of the oxygen-containing gas, by calculating in oxygen, necessary for a complete oxidation of the lead, iron and zinc contained in the charge, and with a consumption of the oxygen-containing gas, by calculating in oxygen, reported at 1 kg of -51 -   sulfur sulfides contained in the feed, which is de-   terminated according to the following formula: Cou Q - 0.70 (1-ns), where Q is the consumption of the gas containing oxygen, calculating in oxygen, per 1 kg of sulfur in the sulphides contained in the charge, e m3N n is the mass ratio between the sulfur of the sulphides and the copper in the oxidized molten material, between 0.65 and 1.30,   Neck, Os are, respectively, the concentrations of copper   glass and sulfur sulfides in the feed, in% by mass, while the lower layer of raw lead is continuously cooled to a temperature ranging from 330 to 9000C, finally obtaining, apart from raw lead and slag lead-depleted zinc, a matte enriched with copper.   5. Method according to claims 1 to 4, character-   laughed at the fact that the admission to the merger of the charge con-   joint with recycled oxidized dust is reac   read through a device fitted with a burner, the   effective diameter of the useful section is determined se-   lon the formula: e /0.Q H- H o de is the effective diameter of the useful section of the burner, in m,   is the desulfurization rate, defined as the ratio   port of the quantity of sulfur present in the fusion gases to the quantity of sulfur present in charge, -   M is the consumption of the charge, in Kg / s is the density of the oxygen-containing gas, in Kg / m3 H is the height of the melting zone, in m,   T = -0.0703 + 0.3031 & 8 -0.0157. 2 8.17 10-5'S -.OCcao- 3.6410-3. + +3 5C2i2 + 26 1 6446 - 52 -   + 8899.10-4 * .cao + 2,? 68.l0-3C aon s; OS, "CaO, CSi0 being, respectively, the sulfur concentrations of the ulphides, calcium oxide and silicon dioxide in the feed,% by mass.   6. Method according to claims 1 to 5, character-   laughed at the fact that before admitting the charge through a device fitted with a burner, part of the charge is reduced, in an amount of 4.5 to 13% of the   mass of the starting load, up to a size of the   ticles of 4 to 8 laws lower than that of the particles of the starting charge, after which the fraction is mixed   reduced with the remaining part of the load.   7. Method according to claims 1 to 6, character-   laughed at that the oxidation of zinc vapors by the   oxygen-containing gas is carried out under a pres-   sion from minus 19.6 to plus 19.6 Pa, obtaining subli-   coarsely divided oxidized mes, enriched with zinc oxide, and finely divided oxidized sublimates, enriched   in lead oxide, said finely divided oxidized sublimates sés being sent to the merger.