JPH01234A - Process for processing lead sulfide or lead sulfide-zinc ores and/or concentrates - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to non-ferrous metal metallurgy, and in particular to the treatment of sulfide- or lead-sulfide-zinc ores and/or concentrates.
It is about logic and law.

The main trend in the improvement of the pyrometallurgy of heavy non-ferrous metals lies in the development of processes for the extraction of said metals from sulfide raw materials using autogenic techniques. Autogenous technologies have the following common advantages: high dead productivity, sharp reduction in the volume of technological gases, use of heating capacity of sulfide ores and concentrates (which significantly reduces the use of external heat sources), non-ferrous Possibilities for the effective treatment of raw materials with relatively low metal content, various embodiments of autogenous treatment are known.

The use of a highly developed surface of the sulfide feedstock to ensure the autogenous character of the melt process is a common feature of all aspects of the autogenous process.

[Prior art and problems] Iron and copper compounds, silicon dioxide, aluminum oxide,
Lead sulfide or lead-zinc sulfide ores containing calcium oxide, magnesium oxide are also/known in some circles. As a solvent, quartz sand and limestone or lime are used. The melting of the said charge and the oxidized return dust is carried out in a vertical flame in an oxygen-containing gas, producing an oxide melt containing mainly metal oxides and an oxidized melt containing the molten gas. Return dust mixture and form. The oxidized return dust is separated from the melt gas and returned for melting. Metal oxides, primarily lead oxide, are reduced to metal by filtering the oxidized melt through a layer of solid carbon-containing material.

Crude lead and lead-depleted zinc-containing slag are formed. Upon precipitation of the slab, a lead-containing zinc vapor is formed which is oxidized by an oxygen-containing gas to form a coarsely dispersed oxide sublimate and a finely dispersed oxide sublimate (US, A, 4519
836).

The method described above is characterized by the use of refractory components in the solvent, namely quartz sand, so that the amount of lead in the oxidized return dust increases as a result of sublimation of the lead sulphide. Furthermore, the presence of quartz sand in the solvent reduces the degree of reduction of lead oxide by the solid carbon-containing reducing layer, thus increasing the loss of lead with the zinc-containing slag.

Objects and Effects of the Invention The main object of the invention is to improve the melting conditions of the process for processing lead sulfide or lead-sulfide-zinc ores and/or concentrates so as to enable the maximum possible extraction of lead. .

SUMMARY OF THE INVENTION The object is to introduce a charge consisting of a sulfide material and a solvent into a burner for melting together with oxidized return dust; melting together with the return dust in a vertical flame in an oxygen-containing gas to form an oxidized melt containing primarily metal oxides and a mixture of the oxidized return dust and the molten gas; separating the oxidized return dust from the molten gas and returning the dust for melting; and reducing metal oxides, especially lead oxide, to metal by filtering through a layer of solid carbon-containing material, reducing crude lead and lead depletion. precipitating the slag to form a lead-containing zinc vapor; and oxidizing the lead-containing zinc vapor with an oxygen-containing gas to form a sublimate. In a process for the treatment of lead sulfide or lead sulfide-zinc ores and/or concentrates containing metal compounds such as iron and copper compounds, silicon dioxide, aluminum oxide, calcium oxide and magnesium oxide, as a solvent, 1 limestone. Alternatively, a mixture of lime and iron-containing material is used, and the calcium oxide/iron ball ratio in the mixture is 0. No43 to 0.
76 and the total amount of calcium oxide and iron in the mixture is 5 to 22% by weight of the three raw ores and/or concentrates. 5. By using a solvent containing a low melting point component, i.e. an iron-containing material, in the process of the invention, the content of lead in the oxidized return dust is significantly reduced as a result of the reduction in the degree of sublimation of lead chloride. this is,
This is because during melting, the iron-containing components of the solvent form a low melting point eutectic system in which lead sulfide is dissolved. Furthermore, in the oxidized melt that is formed, the silicon dioxide is replaced by iron oxide leaving the solvent used in the invention, so that this melt forms solid carbon on the surface of the material during the reaction process. Easily dissolves ash. As a result, the contact conditions between the oxidized melt and the carbon of the reducing agent are improved, thus increasing the degree of reduction of the lead oxide and reducing its loss to the zinc-containing slag.

As mentioned earlier, the solvent components (limestone or lime, four iron-containing materials) are used in amounts that guarantee an oxidizing power f/iron weight ratio of 0.43:0.76, and the amount used for melting is The combination of calcium oxide and iron in the solvent, calculated as an amount, is equal to 5 to 22% of the weight of the raw ore and/or precisely.

, by using the above calcium oxide/iron ratio and the above amount of solvent, the best conditions for forming a low melting point eutectic system "iron oxide (X) - calcium oxide - iron sulfide" (melting point 880°C) is obtained, and as a result, the initial temperature for strong sublimation of lead (
Lead sulfide enters the melt formed at temperatures below 'r==exooo°C).

The method of the present invention increases the separation efficiency of lead and zinc in the reduction stage with solid carbon-containing materials and reduces the lead content in the oxidized return dust, thereby increasing the lead extraction rate compared to the conventional method. Increase by 0.9-1.1%.

If the copper concentration in the raw sulfide material exceeds 1% by weight, in order to improve the quality of the crude lead obtained, i.e. to reduce the copper content contained in it, the charge and oxidized return No melting with dust.

It is carried out with an oxygen-containing gas flow rate (oxygen calculation) below the stoichiometric amount required for complete oxidation of the metals and sulphides in the charge, and in addition to crude lead and lead-depleted zinc-containing slag, copper-rich It is recommended to form a hardened mat.

If the copper concentration in the raw sulfide material does not exceed 1% by volume,
Melting of the charge and the oxidized return dust is carried out with an oxygen-containing gas flow rate obtained from the equation below.

P=A−B−, (υ where P is the flow rate of oxygen-containing gas calculated as oxygen, Nm3/t charge.

A=1.542-3.299Ca-7,972Cb-4
,28°5Ci+28.851CaCb+14.657
CaCi+27.370CbCi-88, 895CbC
iCa, (2) Here, Ca+Cb+C:i=
1 is the acidic oxide Ca (SiOx and A1
203) - Basic oxide Cb (CaO and MgO)
and the total concentration of iron Ci (calculated as Fees), this concentration is expressed in parts by weight.

B is the stoichiometric oxygen flow rate of the oxygen-containing gas required for complete oxidation of the metal and sulfide sulfur in the charge, Nm''/charge.

K=1+0.965/H, where H is the height of the melting zone;
It is desirable to set it to m.

As is known, the specific reaction rate (more specifically, the reaction rate constant) of a gas-melt reaction is dependent on the composition of the melt, including the composition of components that do not participate in the reaction6, e.g.
Slag forming components (Cart M
gO* Alx 03p Sx O* + Fe O
) is the effect.

P b S + 1, 502--1 → pbo+so.

Z n S + 1, 50 snow--→Z n O+
S Oa First, the dissolution rate of lead sulfide and tin sulfide in the melt.

Second, the tissue-sensitive parameter of the rate constant of the heterogeneous desulfurization reaction is explained by its dependence on the concentration of the slag-forming components in the melt. That is, the rate constant of the desulfurization reaction is completely dependent on the chemical composition of the raw material charge.

Moreover, the degree of desulfurization (ratio between the amount of sulfur in the molten gas and the amount of sulfur in the charge) depends on the residence time of the charge in the melting zone.

This residence time is related to the height of the melting zone by known physical laws. The amount of oxygen actually required to achieve the desired degree of desulfurization therefore depends on the content of the aforementioned slag-forming components in the charge and on the height of the melting zone. The actual requirement of oxygen is due to the matte and excess amount of iron oxide (II
I) is the amount that achieves the desired result of the melting process without forming.

The above dependence relationship (Equation 1) cannot be calculated theoretically; the applicant discovered this experimentally.

The implementation of the melting process at the flow rate of the oxygen-containing gas determined by the formula l yields the required degree of desulphurization, i.e. the maximum possible degree of heat release, and constitutes the best conditions for the melting and reduction processes, resulting in lead Increases the extraction degree of O,S ~0.9%.

If the copper concentration in the raw sulfide material exceeds 1% by volume, the melting of the charge and the oxidized return dust will occur.

At the stoichiometric flow rate of oxygen-containing gas (calculated as oxygen) required for complete oxidation of lead, iron and zinc in the charge,
Also, the consumption of oxygen-containing gas per kg of sulfide sulfur in the charge (calculated as oxygen) determined by the following formula:
carried out at C1, where Q is the flow rate of oxygen-containing gas (calculated as oxygen) per ton of sulphide sulfur in the charge, Nm3n is 0.65
The weight ratio of sulfide sulfur to copper in the oxide melt equal to ~1.30.

Cc, and C, are the concentrations of copper and sulfide sulfur in the charge.

It is also recommended that the bottom layer of crude lead be continuously cooled to 330-900°C to form a feed-enriched mat in addition to the crude lead and lead-depleted zinc-containing slag.

With such a flow rate of oxygen to melt the bottom layer of blister copper and cool it to the temperature range mentioned above, it is possible to prepare a blister lead with minimal grain and sulfur content (most of the copper and sulfur are matte). ).

If the sulfide sulfur/copper ratio in the oxidized melt is less than 0.65, the extraction of copper from Il lead to matte is incomplete. If this ratio exceeds 1.30, an excess amount of sulfur appears in the crude lead, which produces lead sulfide. This is undesirable because it requires a special purification process to remove sulfur from the crude lead particles.

When the bottom layer of crude lead is cooled to the above temperature, the solubility of copper sulfide in the crude lead decreases, the copper content in the ship decreases as the lead moves downwards, and the matte droplets become slag-crude lead. Move upward to the interface.

As the bottom layer of crude lead cools down, the lead refined from the copper and the copper removed from the lead move in opposite directions.

Continuous purification of crude lead from copper is achieved with the formation of matte.

If the bottom layer of lead is cooled to a temperature of over 900°C,
The quality of refining lead from S rapidly deteriorates.

Even if the bottom layer of crude lead is cooled to below 330°C.

If the quality of shipping made from copper is not improved,
Along with this, the height of the bath of molten crude lead gradually decreases, which increases the energy consumption to maintain the required slag temperature, and also creates difficulties in removing refined lead from copper. It is from.

As is clear from the above, upon cooling of the bottom layer of crude lead, if this step is carried out at the flow rate of the oxygen-containing gas determined by equation (3) above.

It improves the quality of crude lead and ultimately reduces lead losses during the refining process of the process.

The optimum degree of desulphurization of the charge and the maximum degree of heat release during the melting stage,
In order to improve the oxidation of the charge and the reduction conditions of the oxidized melt and to achieve maximum lead extraction degree, the charge, together with the oxidized return dust for melting, is combined with the effective passed through a burner having a cross-sectional diameter.

where d is the effective cross-sectional diameter of the burner 1 m, δ is the degree of desulfurization determined as the ratio of the amount of sulfur in the molten gas to the amount of sulfur in the charge, M is the charge consumption rate, kg/s .

ρ is the density of oxygen-containing gas, kg/m''.

H is the height of the melting zone, m.

τ=-0,0703+0. 3031 ・δ−0
゜0157・6m-8,17・10 bow・δ・
ce,.

-3,64・10゛1・Cm,. ! +1.83
・104・C21,. , +8.899 ・10
°4・C5゜+2゜768・10-co-c
' c, , , S, (5) Here,
Cs, Cc-0, C1,. , respectively, are the concentrations of sulfide sulfide, calcium oxide, and silicon dioxide in the charge, and are preferably expressed as percentages.

If the effective cross-sectional diameter of the burner differs from the value calculated by equation (4), the following undesirable phenomena will be observed. If the cross-sectional diameter of the burner is smaller than the calculated diameter (high flow rate of sulfide material), the residence time of the material in the melting zone is short;
The desired degree of desulfurization is not achieved, which increases the amount of lead in the matte and reduces the extraction of lead into the crude metal, thus increasing lead losses. If the effective cross-sectional diameter of the burner is larger than the calculated value, the residence time of the material in the melting zone will be longer than the required time (the flow rate of the sulfide material exceeds the required flow rate);
As a result, reoxidation of the charge occurs.

The reducing conditions for lead oxide are worsened and lead loss through the zinc-containing slag is therefore increased.

Before sending the charge through the burner for melting.

It is preferable to grind 4.5 to 13% of the ffi amount of the raw material charge to a particle size of 1/4 to 1/8 of the particle size of the raw material charge, and mix the pulverized portion with the remaining portion. .

When sulfide ores and/or concentrates are oxidized by heat radiation under their heating conditions, the increase in the rate of the heterogeneous reaction after crushing depends on the ratio of the particle sizes of the raw and crushed parts of the charge. They found that it was 50-80% higher than expected.

Due to the significant increase in the oxidation rate of the crushed charge relative to the oxidation rate of the raw charge, the crushed charge portion is completely oxidized in the upper part of the melting zone, and the heat released during its oxidation is transferred to the It is used to heat and melt the coarse particles of most of the materials, resulting in the intense oxidation of the large particles of sulfide materials and the expansion of the high temperature zone of the melting zone. This expansion of the high-temperature zone increases the residence time of the material therein by a factor of 2.1 to 3.6,
Significantly increases the rate of reaction between sulfides and gas phase oxygen and between high iron oxides and sulfides.

Increasing the residence time of the charge at elevated temperatures results in increased utilization of gas phase oxygen, particularly oxygen bound to high iron oxides. As a result of the reduction in the content of iron-rich iron oxide in the prepared oxidized melt, the consumption of solid carbon-containing material for the reduction of the iron-rich iron oxide is reduced during the subsequent reduction of the melt.

In order to obtain a temperature at which the amount of heat released during one reaction when adding a grinding fraction in an amount of up to 4.5% by weight of the raw material charge results in a strong oxidation of the charge in the upper part of the melting zone. It becomes insufficient. Similarly, addition of material with a grindness of less than 4 does not result in a sufficiently high oxidation rate necessary to initiate oxidation of the main coarse portion of the charge.

If the grinding fraction is added at more than 13% by weight of the raw material charge, or at a very high degree of grinding of the sulfide material (above 8), the amount of oxidized return dust increases rapidly. , and the additional cost of grinding the material becomes large.

As is clear from the foregoing, the comminution of a portion of the charge increases the efficiency of oxygen use, i.e. completely converts the metal from the sulfide form to the oxide form, so that the lead in the i1 primary stage The degree of extraction increases by 0.2-0.5%. Furthermore, such technology can reduce the consumption of solid carbon-containing materials.

The lead-containing zinc vapor formed during the precipitation of the lead-depleted zinc-containing slag is oxidized with an oxygen-containing gas under a pressure of -19.6 to +19.6 Pa to produce copper-enriched coarsely dispersed oxidation. Preferably, a finely dispersed oxidized sublimate enriched with lead oxide is formed with the sublimate and said finely dispersed oxidized sublimate is provided for melting.

During precipitation of the zinc-containing slag, the lead and zinc partially pass into the vapor state. During the oxidation of said steam at a pressure of -1,9,6 to +19°8 Pa, an effective separation of lead and zinc occurs in the oxidized sublimate obtained, and! Lead is concentrated in the coarsely dispersed sublimate;

It is concentrated in the finely dispersed sublimate that is sent to the melting process.

As a result of the higher lead content in the finely dispersed sublimate than in the charge, it is preferable to return the sublimate to the melt stage to increase the extraction rate of the vessel.

Lead content at pressures outside the above range! [The oxidation of lead vapor is
the possibility of enriching coarse fraction oxidized sublimate with zinc;
This eliminates the possibility of enriching the finely dispersed sublimate with lead, thus making it impossible to use the finely dispersed oxidized sublimate as return material during the melting process.

Therefore, during the oxidation of lead-containing zinc vapor at a pressure of -19.6~+19.6 Pa, the finely dispersed sublimate fraction can be enriched with lead and the lead extraction rate can be increased by 0.3~0.4%. .

[Action of the invention] Iron and lead compounds, silicon dioxide aluminum pentoxide,
Lead sulfide and lead sulfide-zinc ores and/or lead sulfide containing any metal compounds such as calcium oxide, aluminum oxide and magnesium oxide.
Alternatively, the method of the present invention for treating concentrate is carried out as follows.

To carry out the process of the invention, a melting plant is used ("Nonferrous Metals", No. 8, 1977°A, P.
"Oxygen-electrothermal treatment process of concentrate", pp. 8-15).

drying a charge consisting of lead sulfide or lead-zinc ore and/or concentrate and a solvent to a moisture content of less than 1% by weight;
It was passed along with the atomized return dust into the burner of the melting plant for melting. A mixture of 1 lime or limestone and an iron-containing material is used as a solvent, the calcium oxide/shear volume ratio in the mixture is 0.43-0.76, and this mixture is combined with the above-mentioned charge and oxidized return material. Melting of the mixture with dust is carried out in a vertical flame of oxygen-containing gas.

As the oxygen-containing gas, commercially available oxygen or oxygen-enriched air can be used.

If the copper content in the raw sulfide material exceeds 1% by weight, the oxygen-containing gas (oxygen calculation) flow rate is less than the stoichiometric amount required for complete oxidation of the metal and sulfide sulfur in the charge. It is preferable to carry out a melting process (i.e. it is preferable to carry out a melting process so as to form a bronze matte), if the copper content in the raw sulfide material is less than 1ffi%, It is desirable to carry out the melting process without matte formation at a flow rate of oxygen-containing gas (oxygen calculation) that is greater than or equal to the stoichiometric amount required for complete oxidation of the metal and sulfide sulfur.

The oxidized melt obtained after melting mainly contains a mixture of metal oxides, a-oxidized return dust, and molten gas. This mixture is passed through the gas discharge standpipe of the melting plant into a device which separates the oxidized return dust from the melt gas, for example into an electric filter. The oxidized return dust is again sent to the melting plant for melting.

The resulting oxidized melt is filtered through a solid carbon-containing bed (for example a coke or coal bed), with the result that the metal oxides, primarily lead oxide, are reduced to metal. As a result, crude lead and lead-depleted zinc-containing slags are obtained, or these products and bronze-plated mats are obtained. Said molten product enters the electrical heating section of the melting plant, the bottom of the furnace being common for the electrical heating section and the melting section. In electric heating areas.

The zinc-containing slag is precipitated and the following layers are formed. J
A lower layer of 11 lead and an upper layer of lead-depleted zinc-containing slag, if a copper-enriched matte is present, this forms an intermediate layer between the crude lead and the slag. During the precipitation of the slag, a lead-containing zinc vapor is formed which, together with the gas of the electric heating section, is sent to the oxidizer of said vapor (for example an afterburner). An oxygen-containing gas (eg, oxygen-enriched air) is also fed into the device. The result is a large and finely dispersed oxide sublimate containing almost equal amounts of lead oxide and zinc oxide. A coarsely dispersed oxidized sublimate is produced in the apparatus.

Condensed due to steam oxidation. The finely dispersed oxidized sublimate in the mixture with the gas in the electric field area is passed for separation into a sleeve-like filter, for example. These coarse and finely dispersed oxidized sublimate are sent to the next processing step for further extraction of zinc and lead.

As a result of the sulfide material treatment described above, crude lead, tIa-depleted zinc-containing slag, copper matte (if required) and gas are obtained from the melting process. Crude lead is sent for purification of feed and other impurities, lead-depleted zinc-containing slag is sent for zinc extraction, copper-enriched matte is sent for copper production, and the gases from the melting process are Sent for the production of sulfuric acid.

When the copper content in the raw material sulfide material is less than lit% 1
a! determined by equation (1). ! It is desirable to carry out the melting process at a flow rate of the containing gas, so that the stoichiometric flow of oxygen ffi (B) is equal to the lead in the feedstock.

SiO, Alto3゜CaOe in the zero-order charge determined from the content of zinc, iron, copper and sulfide sulfur
Parameter A is determined from the contents of M g O and Fe (calculated as FaO) according to equation (2) (assuming the total content as 1). Since the height H of the melting zone is known, the parameter K is determined. After determining the values A, B and K, the required flow rate of oxygen-containing gas (calculated as oxygen) per ton of charge is determined from equation (1) and the melting is then carried out at this flow rate.

If the copper content in the sulfide raw material is 1% by weight or more, melting is carried out at the flow rate of the oxygen-containing gas determined by equation 1 (3), and at the same time the coarse gas near the bottom of the melting plant is It is desirable to cool the lead layer to a temperature of 330 to 900°C (for example, by air cooling).As a result of processing the sulfide raw material with the aforementioned oxygen-containing gas flow rate and cooling the crude lead layer, the crude lead and lead-depleted zinc-containing In addition to slag, copper-rich matte is also obtained.

In order to ensure the best conditions for the melting process, it is desirable to determine the effective cross-sectional diameter of the burner according to equation (4).

Before sending the charge to the burner for melting, a 4.5 to 13 wt.
It is preferable to grind to a particle size of .8 and mix the ground charge portion with the other portions.

The lead-containing zinc vapor formed during the precipitation of the lead-depleted zinc-containing slag, for example in an afterburner.

It is preferable to oxidize from an oxygen-containing gas (commercially available oxygen or oxygen-enriched air) under a pressure of -19.6 to +19.6 Pa, resulting in a coarsely dispersed oxidation sublimation enriched with zinc alumide. A finely dispersed oxide sublimate enriched with lead oxide is obtained.

The coarsely dispersed oxidized sublimate is condensed in a steam oxidizing device and separated from the finely dispersed sublimate.

The coarse molecule 11 oxidized sublimate is then used for the extraction of zinc. The lead-enriched finely dispersed oxidized sublimate is sent into a melting plant for melting.

[Example] The present invention will be explained below with reference to Examples.

Example 1 51.121i% by weight of lead, 9.11% by weight of zinc,
0.73% by weight copper, 3.61% by weight iron, 16.
31% by weight sulfur sulfide, 4.48% by weight silicon dioxide, 1.49% by weight calcium oxide, 0.68% by weight
A lead-zinc sulfide concentrate containing % by weight aluminum oxide and 0.39% by weight magnesium oxide is treated.

The charge is made by adding a solvent to the raw concentrate. As a solvent (56% by weight of limestone calcium oxide)
A mixture of pyrite and pyrite (iron content: 42% by weight) was used, and the calcium oxide/iron amount ratio lt was 0.60. The above-mentioned solvent is added in an amount of about 51i weight percent of the 1M raw concentrate, calculated as the total amount of calcium oxide and iron content.

A charge consisting of sulfide concentrate and solvent is dried to fil% moisture with oxidized return dust.

It is passed into a burner with an effective cross-sectional diameter of 0.095 m for melting. The flow rate of this charge is 1 ton/hour. Melting is carried out in a vertical flame of commercially available oxygen (95% Os) at a rate of 26 ONm" per tonne of charge. The height of the melting zone in the melting plant (I() is 2.0 m. The result is an oxidized melt containing primarily metal oxides and a mixture of oxidized return dust and molten gas.

The dust is separated from the molten gas in an electric filter and the dust is returned continuously for melting, the amount of this returned dust being 16.4% by weight of the charge. The lead content in the dust is 61.7% by weight.

The oxidized melt is filtered through a bed of coke in an amount of 55 g per tonne of charge. Metal oxides, primarily lead oxide, are reduced to metals.

After said treatment, the molten product containing 93.degree. of the total amount of lead in the raw concentrate flows into the electrothermal section of the melting plant where zinc-containing slabs are precipitated.

During precipitation of the slag, a lead-containing zinc vapor is formed which, together with the gas from the electric heating section, is sent to the 7th pan for oxidation. Air is supplied to this afterburner. As a result, 45 Ili amount % zinc and 35 weight %
An oxidized coarsely and finely dispersed oxidized sublimate containing lead (6.1% of the total lead content of the raw concentrate) is obtained.

' Example 2 The 11th sulfide lead-zinc concentrate described in Example 1 was treated in the same manner as in Example 1. Calcium oxide/iron amount ratio is 0.
A solvent consisting of a mixture of limestone (calcium a oxide 56% by weight) and pyrite cinder (iron content 51% by weight) equal to 60 was used. This solvent was added in an amount of 22% by weight of the raw material, calculated based on the total amount of calcium oxide and iron. Melting is.

a17 delivered at a rate of 301 N m' per tonne of charge! It is carried out in a vertical flame of enriched air (0.270%). The amount of dust continuously returned for melting is 14.1% by weight of the charge. The lead content in the dust is 6
It is 2.3% by weight.

i "As a result of the treatment described above, the total lead content of the raw material concentrate was 93.1
% crude lead was obtained. In addition, oxidized coarse and finely dispersed sublimate are formed containing 0.75% of the total lead content of the raw concentrate (6.05% of the lead depletion).

Example 3 The sulfide lead-zinc concentrate described in Example 1 was treated in the same manner as in Example 1. Calcium oxide/iron weight ratio is 0.6
A solvent consisting of a mixture of limestone (calcium a oxide 70% by weight) and pyrite cinder (iron content 42% by weight) equal to 0 was used. This solvent was added in an amount of 15% by weight of the raw material, calculated based on the total amount of calcium oxide and iron.

Melting is.

It is carried out in a vertical flame of oxygen-enriched air (Oz 95%) fed at a rate of 360 Nm'' per tonne of charge.

The amount of dust continuously returned for 111 melting is 9.3% by weight of the charge. Lead content in dust is 62.7
Weight%.

As a result of the above treatment, 93.2% of the total lead content of 1g raw concentrate
Crude lead containing . In addition, oxidized coarse and finely dispersed sublimate are formed containing 0.81% of the total lead content of the raw concentrate (5.9% of the lead depletion).

Example 4 The lead-zinc sulfide concentrate described in Example 1 is treated in the same manner as in Example 1. The weight ratio of calcium oxide to iron in the solvent is 0.43. The solvent is added in an amount of 15Ii weight % of the raw concentrate, calculated on its total calcium oxide and iron content. Melting is carried out in a vertical flame of commercially available oxygen (85% 02) delivered at a flow rate of 370 Nm'' per tonne of charge.

The amount of oxidized return dust that is continuously returned for melting is 36.4% by weight of the amount of charge.

The lead content in the dust is 62.3% by weight. The oxidized melt is filtered through a coal seam, the amount of coal being 71.5 Kg per tonne of charge.

By the above treatment, the total lead content of the yK feed concentrate was reduced to 93%.
Crude lead containing 0% and [0.69% of the total amount of lead in the feed concentrate]
A lead-depleted zinc-containing slag was produced. Further +
An oxidized coarsely and finely dispersed sublimate containing 44.4% by weight of zinc and 35.1% by weight of lead (6.2% of the lead content of the raw concentrate) was obtained.

Example 5 The lead-zinc sulfide concentrate described in Example 1 is treated in the same manner as in Example 1. The weight ratio of calcium oxide to iron in the solvent is 0.76. The solvent is added in an amount of 15% by weight of the raw concentrate, calculated on its total calcium oxide and iron content. Melting is carried out in a vertical flame of commercially available oxygen (95% Ox) delivered at a flow rate of 352 Nm' per ton of charge.

The amount of oxidized return dust that is continuously returned for melting is LL,0ii% by weight of the amount of charge.

The lead content in the dust is 61.9% by mass.

By the above treatment, the total lead content of the raw concentrate was reduced to 93.1%.
% crude lead and a lead-depleted zinc-containing slag containing 0.72% of the total lead content of the 1M feed concentrate. Furthermore, 4
5. An oxidized coarsely and finely dispersed sublimate containing 35.1% by weight of zinc and 35.1% by weight of lead (6.1% of the lead content of the raw concentrate) was obtained.

Example 6 (Comparative Example) The lead-zinc sulfide concentrate described in Example 1 was processed according to known methods (US Pat. No. 4,519,836) in a IIi-like melting plant under similar processing conditions.

As a solvent, a mixture of limestone (56% by weight of calcium oxide) and quartz sand (93% by weight of silicon dioxide) is used.
:Fe0 weight ratio is 0.8. Also, Ca in the charge
The O+ M g O: F a O weight ratio is 0.51.

Melting was carried out in a vertical flame of commercial a-element (95% Oa) delivered at a flow rate of 220 Nm” per tonne of charge. The amount of oxidized return dust continuously returned for melting. is 44.3% by weight of the charge.The lead content in the dust is 62.1% by weight.

After the above treatment, a crude lead containing 92.1% of the total lead content of the raw concentrate and a lead-depleted zinc-containing slag containing 0.95% of the lead content of the raw concentrate were obtained. . Furthermore, 45
．． An oxidized coarsely and finely dispersed sublimate was obtained containing 1% by weight of zinc and 34.3% by weight of lead (6.8% of the lead content of the d-feed concentrate).

As can be seen from the above examples, one method of the invention (Example 1)
Compared to the known method (Example 6), the processing method according to ~5) has a lead extraction rate of 0.9 to 1 from the raw sulfide material to crude lead.
．． Increase by 1%. (Calculated for the lead content in the raw concentrate) Furthermore, the amount of lead returned to the melting process by oxidized return dust is 4°8 to 21.7% (calculated for the lead content in the raw concentrate). absolute) is reduced.

Example 7 52.31% by weight lead and 8.6% by weight zinc.

1.8% by weight copper, 3.82% by weight iron, 15.9% by weight
Contains 7% by weight sulfur sulfide, 4.52% by weight silicon dioxide, 1.28% by weight calcium oxide, 0.65% by weight aluminum oxide, and 0.26% by weight magnesium oxide. Process lead-zinc sulfide concentrate. This process is performed in the same manner as in the first embodiment. The weight ratio of calcium oxide to iron in the solvent is 0.60. Solvents are calculated for their total calcium oxide and iron content.

15% by weight of the raw concentrate is added. Melting is carried out in a vertical flame in commercial oxygen (0*95%). This oxygen is delivered at a flow rate of 242 Nm'' per tonne of charge.The amount of oxidized return dust that is continuously returned for melting is 9.4% by weight of the charge.Return Dust The lead content in it is 61.6% by weight.

As a result of the above treatment, crude lead containing 2.01% by weight of copper and 93.0% of the amount of lead in the raw concentrate, and lead containing 0.81% by weight of the amount of lead in the yX material concentrate. Depletion plate lead-containing slag with 20.1% by weight of copper and 4.3% of the amount of lead in the raw concentrate
A mat containing % was obtained. Furthermore, an oxidized coarse and finely dispersed sublimate was obtained containing 43.9% by weight of zinc and 32.4% by weight of lead (1.8% of the weight in the M feed concentrate).

Example 8 51.12% by weight lead, 9.11% by weight zinc,
0.73% by weight copper, 3.61% by weight iron, 16.
31% by weight sulfur sulfide, 4.48% by weight silicon dioxide, 1.49% by weight calcium oxide, 0.68% by weight
A lead-zinc sulfide concentrate containing 0.39% by weight of aluminum oxide and 0.39% by weight of magnesium oxide is treated.

By adding a solvent to the concentrate.

Prepare the charge. A mixture of limestone (56% by weight of calcium oxide) and pyrite (4211% by weight of iron) is used as a solvent, and the weight ratio of calcium oxide to iron in this mixture is 0.60. The solvent is added in an amount of 5% by weight of the raw concentrate, calculated on the sum of its calcium oxide and iron. The charge thus prepared contained 47.68% by weight of lead.

8.39% by weight zinc and 0.67% by weight copper.

6.21% by weight iron, 18.32% by weight sulfur sulfide, 4.13% by weight silicon dioxide, 3.09% by weight
of calcium oxide, 0.63% by weight of aluminum oxide, and 0.36% by weight of magnesium oxide.

The charge consisting of the sulfide concentrate and solvent was dried to 1% moisture by weight and, together with the oxidized and reconstituted dust, was passed through a burner with an effective cross-sectional diameter of 0.095 m in the melting plant. The flow rate of the charge is 1 ton/hour. One set of melting (
1) amount of commercially available oxygen (95 wt% 02) determined from
It was carried out in a vertical flame. Actual value: Ci g 0
, 492, Ca=0.294. Cb=0.214.
A=0.823, N=1.483 (height H of the melting zone of the melting plant is 2.0 m), B=IJ11. Therefore, the flow rate (P) of oxygen-containing gas calculated for oxygen is 2
21 Nm3/tonne of charge or, taking into account the oxygen in the oxygen-containing gas, 233Nm''/tonne of charge.

As a result, an oxidized melt containing mainly metal oxides and a mixture of oxidized return dust and molten gas was expected. The dust was separated from the melt gas by an electric filter and continuously returned for melting. The amount of return dust that is continuously returned for melting is 15.
It is 6% by weight. Lead content in dust is 62.2% by weight
It is.

The oxidized melt was filtered through a bed of coke of 50 kg per tonne of charge. Metal oxides, primarily lead, were reduced to metals.

As a result of the above treatment, a crude lead containing 93.8% by weight of the lead content of the raw concentrate and a lead-depleted zinc-containing slag containing 0.43% by weight of the lead content of the 1M raw concentrate were obtained. It was done.

The molten product flowed into the electrothermal section of the melting plant where the zinc-containing slag was precipitated.

Lead-bearing zinc vapor was generated during the precipitation process, and this vapor was sent to the afterburner along with the gas from the electric heating section for its oxidation. Air was supplied to the device.

The result was an oxidized coarse and finely dispersed sublimate containing 45.3% by weight of zinc and 35.1% by weight of lead (5.6% of the lead content of the raw concentrate).

Example 9 67.43% by weight lead, 2.71% by weight zinc, 0
．． 48% by weight copper, 2.84% by weight iron, 15.3
Contains 3% by weight sulfur sulfide, 4.6% by weight silicon dioxide, 1.45% by weight calcium oxide, 0.07% by weight magnesium oxide, and 0.01% by weight aluminum oxide. A lead-zinc sulfide concentrate was treated according to the procedure of Example 8. The charge thus amended contained 62°10% by weight lead, 2.50% zinc and 0°44% by weight.
1! weight% of feed, 5.5% of weight of iron, 17°42il
% of sulfide sulfide, 4.24% by weight of silicon dioxide, 3.06% by weight of calcium oxide, 0.06% by weight of magnesium oxide, and 0.01% by weight of aluminum oxide. Melting is.

Commercially available oxygen (80% by weight 0
2) was carried out in a vertical flame. Actual value 20i=0.4
9. Ca=0.294. Cb=0°216, A=0.8
24. = 1.483 (height H of the melting zone of the melting plant is 2.On), B = 164, so the flow rate of oxygen-containing gas (P) calculated for oxygen is 20ONm”/ton of charge; or 25 ONm''/ton of charge, taking into account the oxygen in the oxygen-containing gas. The amount of return dust that is continuously returned for melting is 15% of the charge
．． It is 7% by weight. The lead content in the dust is 62.4% by weight.

The oxidized melt was filtered through a layer of coke weighing 86 kg per tonne of charge.

As a result of the above treatment, crude lead containing 93.9% by weight of the lead content of the raw concentrate and lead-depleted zinc-containing slag containing 0.41% by weight of the lead content of the 1M raw concentrate were obtained. It was done. Furthermore, an oxidized coarsely and finely dispersed sublimate containing 44.2% by weight of zinc and 33.6% by weight of lead (5.6% of the lead content of the raw concentrate) was obtained.

As is clear from Examples 1 to 5 and 8.9 in which the method of treating lead sulfide-containing materials according to the present invention is carried out, the methods of Examples 8 and 9 are more effective in reducing raw material sulfide than the methods of Examples 1 to 5. The lead extraction rate from raw materials to crude lead is 0.5 to 0.9 of the amount of lead in the raw material concentrate.
Increase in weight %. In addition, the consumption rate of solid carbon-containing reducing agent decreased by 9.1% by weight, and the consumption rate of oxygen-containing gas decreased by 10%.
．． It has decreased by 4% by weight.

Example 10 40.39% by weight lead, 8.24% by weight zinc, 1
．． 99% by weight copper, 6.24% iron, 17.9% by weight
Contains 6% by weight sulfur sulfide, 6.15% by weight silicon dioxide, 2.28% by weight calcium oxide, 2.76% by weight aluminum oxide, and 2.05% by weight magnesium oxide. A mixture of lead-zinc sulfide concentrate and lead sulfide ore is processed.

A charge is prepared by adding a solvent to this mixture. Using a mixture of limestone (calcium oxide 56% by weight) and pyrite (iron content 42% by weight) as a solvent,
In this mixture, the weight ratio of calcium oxide to iron is 0.
60. The solvent is added in an amount of 5% by weight of the raw concentrate, calculated on the sum of its calcium oxide and iron. The charge thus prepared contained 37.2% by weight of lead and 7% by weight of lead.
゜59% by weight of zinc, 1.83% by weight of feed, 8゜6
3 wt% iron, 19.84 wt% sulfur sulfur, 5
．． 66% by weight silicon dioxide, 3.82% by weight calcium oxide, 2.54% by weight aluminum oxide,
Contains 1.89 weight + 1% magnesium oxide.

The charge consisting of sulfide concentrate and solvent was dried to 1% moisture by weight and passed together with the oxidized return dust through a burner with an effective cross-sectional diameter of 0.06 m in the melting plant. The flow rate of the charge is 1 ton/hour. Melting is commercially available M
# (95% zero) in a vertical flame. Lead and iron in the charge.

and the amount of oxygen required for complete oxidation of zinc was carried out with an oxygen-containing gas stoichiometric flow rate of 50.4 Nm”/ton of charge. The flow rate of oxygen-containing gas (Q) calculated for
is calculated from Equation 1 (3), and in this equation n=1.3
It is 0. Q was 0°616 Nm”, charge 1
The flow rate of oxygen-containing gas (calculated as oxygen) for the amount of sulfide sulfur in a ton (198.4 kg) is 122.2 Nm
'is. The total flow rate of oxygen-containing gas, calculated as oxygen per ton of charge, is 172.6 Nm'' and, taking into account the oxygen concentration in the oxygen-containing gas, 182 Nm'. The height (H) is 2.0m.

The result was an oxidized melt containing mainly metal oxides and a mixture of oxidized return dust and molten gas. Dust was separated from the melt gas by an electric filter and continuously returned for melting. The amount of return dust that is continuously returned for melting is 16-
,．． It is 5% by weight. The lead content in the dust is 62.5% by weight.

The oxidized melt was filtered through a layer of coke weighing 352 kg per tonne of charge. metal oxide.

Mainly lead oxide was reduced to metal.

After the above treatment, 0.55! ! 93, lf of lead content in feed and raw sulfide materials (mixture of concentrate and ore) in l amount%
Crude lead containing i amount % and 0.6 of the lead content of H feed concentrate
lead-depleted zinc-containing slag containing 6111% by mass;
．． 4g amount% of the amount of lead in steel and raw sulfide materials 3.5
A mat containing % by weight was obtained.

The molten product flowed into the electrothermal section of the melting plant where a lead-depleted zinc-containing slag was precipitated. The crude lead layer adjacent to the furnace bottom was continuously cooled to 650° C. with air. Lead-bearing zinc vapor was generated during the precipitation process, and this vapor was sent to the afterburner along with the gas from the electric heating section for its oxidation. Air was supplied to the device. As a result, 4
An oxidized coarsely and finely dispersed sublimate containing 5.5% by weight zinc and 35.0% by weight lead (2.6% of the lead content of the M concentrate) was obtained.

Example 11 46.04% by weight lead, 10.04% by weight zinc,
2.20% by weight of feed, 6.16% by weight of iron, 20.
24% by weight sulfur sulfide, 6.62% by weight silicon dioxide, 2.18% by weight calcium oxide, 2.39% by weight
A mixture of lead-zinc sulfide ore and lead sulfide concentrate containing % aluminum oxide and 2.18% magnesium oxide by weight is processed by the procedure of Example 10. The prepared charge contained 42.4% by weight lead, 9.25% zinc, 2.03% by weight feed, 8.56% by weight iron, and 21.94% by weight. Sulfide sulfur and 6.1% by weight
of silicon dioxide, 3.73% by weight of calcium oxide, 2.2% by weight of aluminum oxide, and 2.01% by weight of
Contains magnesium oxide. Melting is done using commercially available oxygen (
Calculate the amount of oxygen required for complete oxidation of lead, iron and zinc in the charge in a vertical flame in 95%02).
It was carried out with a stoichiometric flow rate of oxygen-containing gas of 55.8% m'/ton of charge. The flow rate of oxygen-containing gas (Q) calculated for oxygen per kg of sulfur sulfide in the charge is calculated from equation 9 (3), in which n-1,03
It is. Q was 0.632Nm3. The flow rate of oxygen-containing gas (calculated as oxygen) for the amount of sulfide sulfur (219.4 kg) in 1 ton of charge is 138.7% m'. The total flow rate of oxygen-containing gas, calculated as oxygen per ton of charge, is 194.5% m" and, taking into account the oxygen concentration in the oxygen-containing gas, 204 Nm3. Continuously for melting The amount of oxidized return dust returned is 16.5% by weight of the amount of charge.The lead content in the return dust is 62.0% by weight.

After the above treatment, 0.88% by weight copper and 93.0% by weight lead content in the raw sulfide material (mixture of concentrate and ore)
crude lead containing 0.68% by weight of the lead content of the raw concentrate and lead-depleted zinc-containing slag containing + 26.8% by weight of copper and 3.4% of the amount of lead in the raw sulfide material A mat containing % by weight was obtained.

The crude lead layer adjacent to the bottom of the melting plant was continuously cooled to 900° C. by air.

In addition to the above products, 44.1% by weight of zinc and 35.6%
ffi amount% lead (2.8% of the lead content of the raw sulfide material
) oxidized coarsely and finely dispersed sublimate were obtained.

Example 12 46.04% by weight lead, 10.04% by weight zinc,
2.20% by weight of feed, 6.16% by weight of iron, 20.
24% by weight sulfur sulfide, 6.62% by weight silicon dioxide, 2.18% by weight calcium oxide, 2.39% by weight
A mixture of lead-zinc sulfide ore and lead sulfide concentrate containing % aluminum oxide and 2.18% magnesium oxide by weight is processed by the procedure of Example 10. The prepared charge was 42.41! % lead, 9.25% zinc, 2.03% copper, 8°56% by weight
of iron, 21.94% by weight sulfur sulfide, 6.1% by weight silicon dioxide, 3.73% by weight calcium oxide, 2.2% by weight aluminum oxide, 2.01% by weight Contains magnesium oxide. Melting was carried out in a vertical flame in commercially available oxygen (95% 02) to remove the lead, iron and
and the amount of oxygen required for complete oxidation of zinc, the flow rate (Q) of the element-containing gas containing 55.8% m'/ton of charge is calculated from Equation 1 (3), and this In the equation, n==1.05. Q is 0°632 Nm3
It became. Amount of sulfide sulfur in 1 ton of charge (219,
The flow rate of oxygen-containing gas (calculated as oxygen) for 4 kg) is 138.7% m'', the total flow rate of oxygen-containing gas calculated as oxygen per ton of charge is 194.5
%m' and, taking into account the oxygen concentration in the oxygen-containing gas, 204 N m'', the amount of oxidized return dust continuously returned for melting is 16° of the amount of charge. 4
Weight%. The lead content in the returned dust is 62.1% by weight.

The above treatment resulted in crude lead containing 0.56% by weight of copper and 93.2% by weight of the lead content in the raw sulfide material (mixture of concentrate and ore), and the lead content in the raw concentrate. 0.731 of
A lead-depleted zinc-containing slag containing 1% by weight and a mat containing 25.9% by weight of copper and 3.55% by weight of the amount of lead in the raw sulphide material were obtained.

The crude lead layer adjacent to the bottom of the melting plant was continuously cooled to 650° C. with air.

In addition to the above products, 44.9% by weight of zinc and 35.1
An oxidized coarse and finely dispersed sublimate containing % lead by weight (2.4% of the lead content of the sulfide material) was obtained.

Example 13 46.04% by weight lead, 10.04% by weight zinc,
2.20% by weight copper, 6.16% by weight iron + 20
．． 24% by weight of sulfur sulfide, 6.62% by weight of silicon dioxide, 2.18% by weight of calcium oxide, 2.
．． 39% by weight aluminum oxide and 2.18ii% by weight
A mixture of lead-zinc sulfide ore containing magnesium oxide and lead sulfide concentrate is processed by the procedure of Example 1O. The prepared charge contained 42.4% lead by weight and 9.
25% by weight zinc, 2.03% by weight feed, 8°56
6. wt% iron, 21.94 wt% sulfide sulfur;
1% by weight silicon dioxide, 3.73% by weight calcium oxide, 2.2% by weight aluminum oxide, 2.0% by weight
1% by weight of magnesium oxide. Melting was carried out in a vertical flame in oxygen-enriched air (70% 02) at a rate of 55.8 Nm”/charge, calculated for the amount of oxygen required for complete oxidation of the lead, iron and zinc in the charge. The flow rate of the oxygen-containing gas (Q) calculated for oxygen per kg of sulfur sulfide in the charge was calculated from Eq. , in this equation n==0.65. Q is the amount of sulfide sulfur in 1 ton of charge (219,4
Flow rate of oxygen-containing gas (calculated as oxygen) per kg)
is 144.3Nm3. The total flow rate of oxygen-containing gas calculated as oxygen per ton of charge is 200.1N
m”, and considering the oxygen concentration in the oxygen-containing gas, it is 2
The amount of oxidized return dust continuously returned for melting is 17.2% by weight of the amount of the charge. The lead content in the return dust is 61.7% by weight. It is.

Through the above treatment, crude lead containing 0.62% by weight of lead and 93.1% by weight of the lead content in the raw sulfide material (mixture of concentrate and ore) and the lead content of the raw sulfide material were obtained. amount of 0.
25. a lead-depleted zinc-containing slag containing 75% by weight;
3.72 of the amount of lead in feed and feedstock sulfide materials at 5% by weight
A mat containing % by weight was obtained.

The crude lead layer adjacent to the bottom of the melting plant was continuously cooled to 650° C. with air.

In addition to the above products, 45.0% by weight of zinc and 35.0%
An oxidized coarsely and finely dispersed sublimate containing % lead by weight (2.3% of the lead content of the sulfide material) was obtained.

Example 14 46.04% by weight lead, 10.04% by weight zinc,
2.20% by weight of feed, 6.16% by weight of iron, 20.
24% by weight sulfur sulfide, 6.62% by weight silicon dioxide, 2.18% by weight calcium oxide, 2.39% by weight
A mixture of lead-zinc sulfide ore and lead sulfide concentrate containing % aluminum oxide and 2.18% magnesium oxide by weight is processed by the procedure of Example 1O. The prepared charge contained 42.4% by weight lead, 9.25% by weight zinc, 2.03% by weight copper, 8.56% by weight iron, and 21.94% by weight. Sulfide sulfur and 6.1% by weight
of silicon dioxide, 3.73% by weight of calcium oxide, 2.2% by weight of aluminum oxide, and 2.01% by weight of
Contains magnesium oxide. Melting is done using commercially available oxygen (
In a vertical flame in 95% 01M), lead, iron,
Calculations were made for the amount of oxygen required for complete oxidation of zinc and carried out at a gas stoichiometric flow rate containing 55.8 Nm"/tonne of charge. 1k of sulfur sulfide in charge.
The flow rate (Q) of oxygen-containing gas calculated in terms of oxygen per gram is calculated from equation 1 (3), where n=
It is 1.05. The flow rate of oxygen-containing gas (calculated as oxygen) for the amount of sulfide sulfur (219.4 kg) in 1 ton of charge was 138,
7 Nm", the total flow rate of oxygen-containing gas calculated as oxygen per ton of charge is 194.5 Nm3, and 204 Nm if the oxygen concentration in the oxygen-containing gas is taken into account.
”, the amount of oxidized return dust continuously returned for melting is 15°5% by weight of the amount of charge.The lead content in the return dust is 61°9% by weight. be.

By the above treatment, the lead content of crude lead and 1M raw sulfide material containing 0.33% by weight of copper and 93.3% by weight of the lead content in the raw sulfide material (mixture of concentrate and ore) was obtained. amount of 0.
24. lead-depleted lead-containing slag containing 70% by weight;
3.88 of the amount of lead in 1% by weight copper and raw sulfide material
A mat containing % by weight was obtained.

The crude lead layer adjacent to the bottom of the melting plant was continuously cooled to 330° C. by air.

In addition to the above products, 44.7% by weight of zinc and 35.1
An oxidized coarse and finely dispersed sublimate containing % lead by weight (2.0% of the lead content of the sulfide material) was obtained.

As is evident from Examples 7, 10 to 14, in which the method of the present invention was carried out for treating materials containing lead sulfide.

The embodiments according to Examples 10-14 have significantly improved lead and matte quality compared to Example 7.

In this case, the crude lead copper tfI step is unnecessary.

Example 15 The lead-zinc sulfide concentrate described in Example 1 was treated according to the procedure of Example 1. The prepared charge is.

47.08% lead by weight, 8.39% zinc, 0
．． 67% by weight feed, 6.21% by weight iron, 18.3% by weight
2% by weight of sulfur sulfide, 4.13% by weight of silicon dioxide, 3.09% by weight of calcium oxide, and 0.6% by weight of calcium oxide.
Contains 3% by weight aluminum oxide and 0.36% by weight magnesium oxide. For melting, the charge together with the oxidized return dust was passed through a burner with an effective cross-sectional diameter (d,) determined by equation (4) of the melting plant. In this equation, the density (ρ) of commercially available oxygen is 1.
42kg/m3. The flow rate (M) of the charge is 0°278kg
/s, desulfurization degree (δ) is 1.0. The parameter (τ) is 0.2176s (τ was calculated from equation (5))
, the effective cross-sectional diameter (d,) of the burner is Q, QB9m. The amount of oxidized return dust that is continuously returned for melting is 16.4% by weight of the charge. The lead content in the dust is 59.18% by weight.

As a result of the above treatment, the amount of lead in the raw concentrate was 93.4% by weight.
Crude lead containing 0.41% by weight of the amount of lead in the raw material concentrate
A lead-depleted zinc-containing slag was obtained. In addition, an oxidized coarsely and finely dispersed sublimate containing 46.1% by weight of zinc and 33.4% by weight of lead (6.1% of the amount of lead in the raw concentrate) was obtained.

Example 16 The lead-zinc sulfide concentrate described in Example 8 was treated according to the procedure of Example 8. The prepared charge is.

For melting, along with the oxidized return dust, the effective cross-sectional diameter (d,) of the melting plant is determined by equation (4)
passed through a burner with a In this formula, the density of commercially available oxygen! (p) is 1.42 kg/m3, charge flow rate (M)
is 0.278 kg/m, m sulfurity (δ) is 1.0, and parameter (τ) is 0.2176 s (τ was calculated from equation (5)).

The effective cross-sectional diameter (d,) of the burner is 0.089 m,
The amount of oxidized return dust that is continuously returned for melting is 15.1% by weight of the charge.

The lead content in the dust is 60.87% by weight.

As a result of the above treatment, the amount of lead in the raw concentrate was 94.0% by weight.
0.44 weight ff of the amount of lead in the raw material concentrate, such as crude lead containing
A lead-depleted zinc-containing slag containing i% was obtained. In addition, an oxidized coarsely and finely dispersed sublimate containing 45.3 i% by weight of zinc and 34.1% by weight of lead (5.5% of the lead content of the raw concentrate) was obtained.

Example 17 A mixture of the sulfide ore described in Example 10 and a sulfide lead-zinc concentrate was treated according to the procedure of Example 10. The prepared charge was passed for melting together with the oxidized return dust through a burner with an effective cross-sectional diameter (d,) determined by equation (4) of the melting plant. In this equation, the density (p) of commercial oxygen is 1.42 kg/m'', the flow rate (M) of the charge is 0.278 kg/s, and the degree of desulfurization (δ) is 0.
．． The 5° parameter (τ) is O, IOIg (calculated from equation (5)), the effective cross-sectional diameter of the burner (d
, ) is 0.043m. The amount of oxidized return dust that is continuously returned for melting is 16.4% by weight of the charge. The lead content in the dust is 62.6% by weight.

As a result of the above treatment, 93.3% by weight of the amount of lead in the feed and raw sulfide material (mixture of ore and concentrate)
Crude lead containing 0.61% by weight of the amount of lead in the raw material sulfide
A lead-depleted zinc-containing slag containing 26.6% by weight of copper and a mat containing 3.1% by weight of the amount of lead in the raw sulfide material was obtained. In addition, 45.5% by weight of zinc and 35.1% by weight of lead (2.9% of the lead content in the M-based sulfide material)
%) of oxidized coarsely and finely dispersed sublimate were obtained.

Example 18' The lead-zinc sulfide concentrate described in Example 1 was treated according to the procedure of Example 1. Before passing the charge through the burner for melting, an 8.8% by weight portion of the raw charge is reduced to 1% of the grain size of the raw charge.
The pulverized portion was mixed with the remaining portion and sent to the melting process.

The amount of oxidized return dust continuously returned for melting is 13.3% by weight of the charge. The lead content in the dust is 62.3% by weight.

Oxidized melt at 48k per tonne charge.

of coke.

As a result of the above treatment, crude lead containing 93.5% by weight of the lead content of the raw concentrate and lead-depleted zinc-containing slag containing 0.7ffi% by weight of the lead content of the 1M raw concentrate were obtained. . moreover,
An oxidized coarsely and finely dispersed sublimate containing 45.6% by weight of zinc and 34.7% by weight of lead (5.8% of the amount of lead in the raw concentrate) was obtained.

Example 19 The lead-zinc sulfide concentrate described in Example 1 was treated according to the procedure of Example 1. 1M before passing the charge through the burner for melting.
A portion of 8.8% by weight of the raw material charge is 1% of the particle size of the raw material charge.
The crushed portion was mixed with the remaining portion and sent to the melting process.

The amount of oxidized return dust continuously returned for melting is 15.3% by weight of the charge. The lead content in the dust is 59.9% by weight.

The oxidized melt was filtered through a bed of coke in an amount of 49 kg per tonne of charge.

As a result of the above treatment, 98.6% by weight of the lead content of the yi feed concentrate
A lead-depleted zinc-containing slag containing 0.7% by weight of lead in the raw concentrate was obtained. Furthermore, 4
An oxidized coarsely and finely dispersed sublimate containing 5.5% by weight of zinc and 34.8% by weight of lead (5.6% of the amount of lead in the raw concentrate) was obtained.

Example 20 The lead-zinc sulfide concentrate described in Example 8 was treated according to the procedure of Example 8. Before passing the charge through the burner for melting, an 8.8% by weight portion of the raw charge is reduced to 1% of the grain size of the raw charge.
The pulverized portion was mixed with the remaining portion and sent to the melting process.

The amount of oxidized return dust continuously returned for melting is 16.0% by weight of the charge. The lead content in the dust is 61.3% by weight.

The oxidized melt was filtered through a bed of coke in an amount of 43 kg per tonne of charge.

As a result of the above treatment, crude lead containing 94.1% by weight of the lead content of the raw material concentrate and lead-depleted zinc-containing slag containing 0.44% by weight of the lead content of the raw material concentrate were obtained. . Furthermore, 4
An oxidized coarsely and finely dispersed sublimate containing 5.5% by weight of zinc and 34.3% by weight of lead (5.4% of the amount of lead in the M concentrate) was obtained.

Example 21 The lead-zinc sulfide concentrate described in Example 8 was treated according to the procedure of Example 8. Before passing the charge through the burner for melting, a 13% by weight portion of the raw charge is reduced to 1/1/2 of the grain size of the raw charge.
The crushed portion was mixed with the remaining portion and sent to the melting process.

The amount of oxidized return dust continuously returned for melting is 16.3% by weight of the charge. The lead content in the dust is 61.0% by weight.

The oxidized melt was filtered through a bed of coke in an amount of 44 kg per tonne of charge.

As a result of the above treatment, crude lead containing 94.1% by weight of the lead content of the raw concentrate and lead-depleted zinc-containing slag containing 0.46% by weight of the lead content of the 1M raw concentrate were obtained. . Furthermore, 4
An oxidized coarsely and finely dispersed sublimate containing 5.5% by weight of zinc and 34.5% by weight of lead (5.4% of the amount of lead in the raw concentrate) was obtained.

Example 22 The mixture of lead sulfide ore and lead-zinc sulfide concentrate described in Example 10 was treated according to the procedure of Example 10. Before passing the charge through the burner for melting, a 4.5% by weight portion of the raw material charge is ground to a particle size of 1/6 of the particle size of the raw material charge, and this ground portion is The mixture was mixed with the parts and sent to the melting process. The amount of oxidized return dust continuously returned for melting is 16.6% by weight of the charge. The lead content in the dust is 6
It is 2.2% by weight.

Oxidized melt at 48k per tonne charge.

of coke.

As a result of the above treatment, crude lead containing 0.56% copper and 93.4% by weight of the lead content of the raw material sulfide material (mixture of ore and concentrate), and A lead-depleted zinc-containing slag containing 0.6% by weight was obtained. A mat was also obtained containing 3.2% by weight of lead in the raw sulfide material. moreover.

Oxidized 8.10.1 containing 45.3% by weight zinc and 34.4% lead (2.7% of the amount of lead in the raw concentrate)
8-22, according to Examples 18-22, Example 1,
It is clear that compared to 8.10, the lead extraction rate from the raw sulfide material to crude lead is increased by 0.2 to 0.5% (calculated for the amount of lead in the raw sulfide material), and , the consumption rate of solid carbon-containing reducing agent is reduced by 8-14% by weight.

Example 23 The lead-zinc sulfide concentrate described in Example 1 was treated according to the procedure of Example 1. The amount of oxidized return dust continuously returned for melting is 16.4% by weight of the charge. The lead content in the dust is 61.7% by weight.

As a result of the above treatment, crude lead containing 93.2% by weight of the lead content of the raw material concentrate and lead-depleted zinc-containing slag containing 0.59% by weight of the lead content of the raw material concentrate were obtained. .

The pressure in the 7-lid burner for the oxidation of the lead-containing zinc vapor formed during the precipitation of the zinc-containing slag was -19,6 Pa.
It is.

As a result, 48.2% by weight of zinc and 8.13% by weight of Ilj
An oxidized coarsely dispersed sublimate containing lead (1.2% of the amount of lead in the raw concentrate) was obtained. This coarsely dispersed sublimate was precipitated in an afterburner. Furthermore, 61.2
An oxidized finely dispersed sublimate containing % by weight lead and 10.75% by weight zinc (4.9% of the lead in the feed concentrate) was obtained.

This finely dispersed sublimate was separated on a sleeve filter and passed into a melting plant for melting.

Example 24 The lead-zinc sulfide concentrate described in Example 8 was treated according to the procedure of Example 8. The amount of oxidized return dust continuously returned for melting is 15.6% by weight of the charge. The lead content in the dust is 62.2% by weight. As a result of the above treatment, crude lead containing 93.9% by weight of the lead content of the raw material concentrate and lead-depleted zinc-containing slag containing 0.38% by weight of the lead content of the raw material concentrate were obtained. .

The pressure in the seven-bar burner for the oxidation of the lead-containing zinc vapor formed during the precipitation of the zinc-containing slag is -0.1 Pa.

As a result, 34.3% by weight of zinc and 8.0% by weight of lead (
An oxidized coarsely dispersed sublimate containing [1.2% of the amount of lead in the feed concentrate] was obtained. This coarsely dispersed sublimate was condensed in a 7-tube burner. Furthermore, 61.1% by weight
An oxidized finely dispersed sublimate was obtained containing lead.

This finely dispersed sublimate was separated on a sleeve filter and passed into a melting plant for melting.

Example 25 The four-compound mixture of lead sulfide ore and lead sulfide-zinc concentrate described in Example 10 was treated according to the procedure of Example 10.

The amount of oxidized return dust continuously returned for melting is 16.5% by weight of the charge. The lead content in the dust is 62.5% by weight.

As a result of the above treatment, crude lead containing 0.55% by weight of feedstock and 93.3% by weight of the lead content in the raw sulfide material (mixture of concentrate and ore) and 0% of the lead content in the 1M chemical concentrate. .46% lead-depleted zinc-containing slag.

25.4% by weight of the lead content of feedstock and feedstock sulfide materials.
5! A mat containing % of It was obtained.

The pressure in the afterburner for the oxidation of the lead-containing zinc vapor formed during the precipitation of the zinc-containing slag is +19.6 Pa.
It is.

As a result, 56.5% by weight of zinc and 9.8% by weight of lead (
An oxidized coarsely dispersed sublimate containing 0.5% of the amount of lead in the raw sulfide material was obtained.

This coarsely dispersed sublimate was condensed in a 7-tube burner. Furthermore, an oxidized finely dispersed sublimate containing 59.3% by weight of lead and 12% by weight of zinc (2% by weight of the amount of lead in the M-based sulfide material) was obtained. This finely dispersed sublimate is separated on a sleeve-like filter and for melting into a melting plant, as evident from 8.10.23-25, the embodiments of Examples 1, 8 .1
0 embodiment promotes enrichment of oxidized finely dispersed sublimate containing lead. Due to this.

The above-mentioned sublimate is fed into a melting plant for melting, and the lead extraction rate from raw sulfide material to crude lead can be increased by 0.1-0.2% of the amount of lead in the raw material. .

Example 26 The lead-zinc sulfide concentrate described in Example 8 was treated according to the procedure of Example 8. Before feeding the charge into the burner for melting, an 8.8% by weight portion of the raw charge is reduced to 1% of the grain size of the charge.
It was ground to a particle size of /6. The pulverized portion was then mixed with the remaining portion and sent together with the oxidized return dust to the burner of the melting plant. The effective cross-sectional diameter (d, ) of the burner is determined by equation (4), where the density of commercial oxygen (p) is 1.42 kg/m3. Charge flow rate (
M) is 0.278 kg/g, and the desulfurization bottom (δ) is 1. o.

The parameter τ was determined by equation (5). The effective cross-sectional diameter (d,) of the burner is 0.089 m. The amount of oxidized recycle dust continuously returned for melting is 15.6% by weight of the charge.

The lead content in the dust is 62.2% by weight.

As a result of the above treatment, 94.4% by weight of the lead content of JI feed concentrate
A lead-depleted zinc-containing slag containing 0.38% by weight of lead in the raw concentrate was obtained.

The pressure in the seven-door burner for the oxidation of the lead-containing zinc vapor formed during the precipitation of the zinc-containing rag is -O, LP'a.
It is.

As a result, 8.0% by weight of lead and 35.6% by weight of zinc (
An oxidized coarsely dispersed sublimate containing 1.2% of the lead content of the raw material concentrate was obtained. This coarsely dispersed sublimate was condensed in an afterburner. Furthermore, 61.1% by weight
An oxidized finely dispersed sublimate was obtained containing 50% of lead and 28.9% by weight of zinc (4.0% of the amount of lead in the M-based sulfide material).

This finely dispersed sublimate was separated on a sleeve-like filter and fed into a melting plant for melting, as seen in Figures 8 and 26, in the practice of Example 26.

The embodiment increases the lead extraction rate from the raw sulfide material to crude lead by 0.6% of the lead content of the material compared to the embodiment of Example 8.

Example 27 A mixture of lead sulfide ore and lead-zinc sulfide concentrate described in Example 10 was treated according to the procedure of Example 10. 4.5% by weight of the raw material charge before feeding the charge into the burner for melting
This portion was ground to a particle size of 1/6 of the particle size of the charge. The pulverized portion was then mixed with the remaining portion and sent together with the oxidized return dust to the burner of the melting plant. The effective cross-sectional diameter (d,) of the burner is determined by equation (4),
In this equation, the density (p) of commercially available oxygen is 1.42 kg
/ m”, the flow rate (M) of the charge is 0.278 kg/
S, desulfurization bottom (δ) is 0.5. The parameter τ is determined by equation (5) and is O,molg. The effective cross-sectional diameter (d,) of the burner is 0.043 m. The amount of oxidized return dust continuously returned for melting is 1
It is 6.5% by weight.

The lead content in the dust is 62.5% by weight.

As a result of the above treatment, 0.45% by weight of copper and 93.8% by weight of lead in the raw sulfide material (mixture of concentrate and ore)
A lead-depleted zinc-containing slag containing 0.45% by weight of the lead content of the 1M raw concentrate, and a mat containing 3.1% of the lead content of the raw sulfide material were obtained. .

The pressure in the 7-lid burner for the oxidation of the lead-containing zinc vapor formed during the precipitation of the zinc-containing slag is +19.6 Pa.
It is.

As a result, 9.8% by weight of lead and 56.5% by weight of zinc (
An oxidized coarsely dispersed sublimate containing 0.5% of the lead content of the M feed concentrate was obtained. This coarsely dispersed sublimate was condensed in a 7-tube burner. Furthermore, 59.3% by weight
An oxidized finely dispersed sublimate was obtained containing 12.1% by weight of lead and 12.1% by weight of zinc (2.1% of the amount of lead in the raw sulfide material).

This finely dispersed sublimate was separated on a sleeve filter and passed into a melting plant for melting.

Examples 10 and 27 of the treatment of lead sulfide-containing materials according to the invention
As is clear from the above, the embodiment of Example 27 is similar to that of Example 1.
The lead extraction rate from the 1M sulfide material to crude lead was compared to the embodiment with 0.0% of the lead content of the material. .

Increases by 7%.

[Effects of the Invention] Thus, the method of treating lead sulfide and lead sulfide-zinc ores and/or concentrates according to the invention can efficiently extract lead from said sulfide materials, i.e. The method compared the extraction rate to crude lead by 0.9 of the amount of lead in the sulfide raw material.
It is possible to increase by ~2.3%. Furthermore, the present invention
From the sulfide material mentioned above, the sulfur is extracted into a molten gas with a high sulfur content (30-50% by weight) suitable for the production of sulfuric acid, and the zinc is also oxidized into a lead-depleted zinc-containing slag. It is possible to transfer the copper content (if the copper content in the sulfide feedstock exceeds 1%) into the conditional matte by transferring it into the dispersed sublimate.

[Phase] Inventors Elena, Pyotrov Sobi: Su, Semashko m:: 0 Inventors Tsuyacheslav, Pyonbi: -Trowitsch, Kurataha.

[Federal Forces Menokorsk, Prospect, Shif
, 3/1, Carvey, 1

Claims (1)

[Claims] 1. Feeding a charge consisting of a sulfide material and a solvent into a burner for melting together with oxidized return dust; melting in a vertical flame in an oxygen-containing gas together with the oxidized melt to form an oxidized melt containing primarily metal oxides and a mixture of oxidized return dust and molten gas; separating the dust from the molten gas and returning the dust for melting; and reducing metal oxides, especially lead oxide, to metal by filtering through a layer of solid carbon-containing material, including crude lead and lead-depleted zinc. forming a slag;
a compound of iron and copper; silicon dioxide; A process for the treatment of lead sulphide or lead sulphide-zinc ores and/or concentrates containing metal compounds such as aluminum oxide, calcium oxide and magnesium oxide, using limestone or a mixture of lime and iron-containing materials as a solvent, The calcium oxide/iron weight ratio in the mixture is in the range of 0.43 to 0.76, and the mixture contains 5 to 22% of the raw ore and/or concentrate as the total amount of calcium oxide and iron in the mixture. % by weight. 2. The melting of the charge and the oxidized return dust is carried out at an oxygen-containing gas flow rate (oxygen calculation) below the stoichiometric amount required for complete oxidation of the metal and sulfide sulfur in the charge. 2. A method according to claim 1, characterized in that, in addition to crude lead and lead-depleted zinc-containing slag, a copper-enriched mat is formed. 3. The melting of the charge and the oxidized return dust is carried out at an oxygen-containing gas flow rate obtained from the following formula:
The method described in. P: A・B・K, where P is the flow rate of oxygen-containing gas calculated as oxygen, Nm^3/t charge, A=1.542-3.299Ca-7.972Cb-4
．． 285Ci+28.851CaCb+14.657C
aCi+27.370CbCi-88.895CbCi
Ca, where Ca+Cb+Ci=1 is the acidic oxide Ca (SiO_2 and Al_2O_3), basic oxide Cb (CaO and MgO) and iron Ci (FeO
B is the stoichiometric oxygen flow rate of the oxygen-containing gas required for complete oxidation of the metal and sulfide sulfur in the charge, Nm^3/ t charge, K=1+0.965/H, where H is the height of the melting zone,
m. 4. The melting of the charge and the oxidized return dust is carried out at the stoichiometric flow rate of oxygen-containing gas (calculated as oxygen) required for complete oxidation of lead, iron and zinc in the charge, and at: carried out at the oxygen-containing gas consumption (calculated as oxygen) per ton of sulfide sulfur in the charge determined by the formula: Q=0.70·(1-nC_C_■/C_S
) where Q is the flow rate of oxygen-containing gas (calculated as oxygen) per ton of sulfide sulfur in the charge, and Nm^3n is 0.
The weight ratio of sulfide sulfur to copper in the oxide melt equal to 65 to 1.30. C_C_■ and C_S are the concentrations of copper and sulfide sulfur in the charge, weight percent; 2. The method of claim 1, further comprising forming a copper-enriched matte. 5. Because the charge is melted together with oxidized return dust,
5. A method according to claim 1, wherein the method is passed through a burner having an effective cross-sectional diameter determined by the formula: ▲There are mathematical formulas, chemical formulas, tables, etc.▼ Here, d_■ is the effective cross-sectional diameter of the burner, m, and δ are the degree of desulfurization determined as the ratio of the amount of sulfur in the molten gas to the amount of sulfur in the charge. M is charge consumption rate, kg/s, p is density of oxygen-containing gas, kg/m^3, H is height of melting zone, m, τ=-0.0703+0.3031・δ-0.0157
・δ＾2−8.17・10＾−＾■・δ・C＿C＿■＿
■-3.64・10^-^3・C_S_i_O_2+1
．． 83.10^-^5.C^2_S_i_O_2+8.
899・10＾−＾4・C_C＿■＿■+2.768・
10^-^3・C^2_C_■＿■, s, here, C_
S, C_C_a_O, and C_S_i_O_2 are the concentrations of sulfide sulfur, calcium oxide, and silicon dioxide in the charge, respectively, in weight percent. 6. Before sending the charge to the burner, a portion of 4.5 to 13% by weight of the raw charge is 1/4 to 1 of the particle size of the raw charge.
6. Process according to claim 1, characterized in that the milled portion of the charge is mixed with the remaining portion of the charge. 7. Oxidation of lead-containing zinc vapor by oxygen-containing gas is -1
carried out at a pressure of 9.6 to +19.6 Pa to form a coarsely dispersed sublimate enriched with zinc oxide and a finely dispersed sublimate enriched with lead oxide, and melt the finely dispersed sublimate. The method according to any one of claims 1 to 5, characterized in that the method is performed for: