CN101195857A - Solvent extraction method for acquiring alloy with magnetic separation copper bessemer matte - Google Patents
Solvent extraction method for acquiring alloy with magnetic separation copper bessemer matte Download PDFInfo
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Abstract
The invention relates to a leaching method for alloy obtained by magnetic separation nickel-copper bessemer matte. The invention is characterized in that two-stage atmospheric pressure leaching, pressurized leaching, pressurized deferrization and bluestone evaporation and crystal processes are adopted to obtain pressurized slag with higher noble metal concentration ratio, and the pressurized slag is delivered in the noble metal system directly. The method of the invention belongs to the metallurgical technology for treating the alloy (coarse grain alloy) material obtained by magnetic separation nickel-copper bessemer matte. Nickel, iron, and copper are leached out stage by stage, and the leached slag concentrated with noble metal can be sent for the noble metal processing. Leached lixivium solution including iron is pressurized for deferrization, and after the deferrization, the solution is nickel solution with less foreign impurities, which can be delivered in the nickel system. The lixivium solution including copper is evaporated and crystallized, to obtain bluestone to form the open circuit of copper, and crystallized mother solution is circularly used in the leaching system. The process has the advantages that the process is simple, highly efficient and environment friendly. The invention is suitable for the treatment of copper nickel alloy, and through adjusting the relative technical parameter, the invention is suitable for selectively leaching and segregating nickel, copper and noble metal from alloy mineral with various grades.
Description
Technical field
The present invention relates to the leaching method of the alloy that a kind of magnetic separation copper Bessemer matte obtains.
Background technology
Since in the nickel mineral symbiosis palladium family and precious metal, in the nickel production process, can reclaim platinum metals (platinum, palladium, osmium, iridium, ruthenium, rhodium) simultaneously.The existing method of extracting the platinum metals is, select coarse grain alloy from smelting intermediates copper Bessemer matte, with enrichment the coarse grain alloy of platinum metals, allocate sulphur (anode sludge desulfurization residue) refuse again into, generate secondary copper Bessemer matte, again secondary copper Bessemer matte is pulverized, magneticly elected the secondary cupronickel, enter between the precious metal recovery vehicle as the raw material that extracts the platinum metals.This recovery technique process is many, energy consumption big, the platinum metals rate of recovery is low, and labor condition is abominable, the SO of generation
2The severe contamination atmosphere.
Under the condition that the production capacity of nickel improves, the treatment capacity of the alloy that the main raw material magnetic separation copper Bessemer matte of production precious metal obtains also can increase, if adopting existing alloy sulfuration process handles, the recovery of precious metal and problem of environmental pollution can senior general increase on total amount, with the pollution that increases environment.
Seek and a kind ofly can effectively handle the alloy method that magnetic separation copper Bessemer matte obtains, make ambrose alloy and precious metal in the alloy obtain enrichment respectively, significant in order to follow-up recovery.
Summary of the invention
The objective of the invention is the deficiency that exists in the above-mentioned technology, the leaching method of the alloy that the magnetic separation copper Bessemer matte that can obtain enrichment ambrose alloy and noble metal materials respectively and can effectively reduce the dirt of production process environment obtains is provided.
The objective of the invention is to be achieved through the following technical solutions.
The leaching method of the alloy that a kind of magnetic separation copper Bessemer matte obtains is characterized in that adopting two sections normal pressures to leach, pressurization is leached, the technology of pressurization deironing and copper sulfate evaporative crystallization, obtains concentration of precious metal and directly enters noble metal systems than high pressurization slag.
The leaching method of the alloy that a kind of magnetic separation copper Bessemer matte of the present invention obtains is characterized in that its leaching process comprises:
A) the mineral acid-containing solution is carried out one section normal pressure pulp control pulp liquid-solid ratio 10-14: 1m
3/ ton, initial sulfuric acid concentration is 45-70g/l, and ore pulp carries out one section normal pressure leaching oxidation panel after the pulp, and controlled oxidation section temperature of reaction is 80-90 ℃, and the reaction times is 1-2h;
B) the displacement section reaction times is 4h～5h, and temperature of reaction is 80-90 ℃, and terminal point contains Cu＜0.5g/l, Ni≤110g/l;
C) two sections normal pressures of control leach: pulp liquid-solid ratio 7-9: 1m
3/ ton, initial sulfuric acid concentration is 100-160g/l, temperature of reaction is 80-90 ℃;
D) the control pressurization is leached: pulp liquid-solid ratio 6-8: 1m
3/ ton, temperature of reaction is 150-160 ℃, and the leaching oxygen partial pressure is 0.20-0.25Mpa, and the reaction times is 3h-4h;
E) control pressurization deironing: temperature of reaction is 165-180 ℃, and the leaching oxygen partial pressure is 0.3MPa, and the reaction times is 2-4h;
F) control copper sulfate evaporative crystallization: 85 ℃～90 ℃ of vaporization temperatures, heating steam pressure 0.2MPa～0.3Mpa, the evaporation terminal point contains Cu 100-120g/l, 25～28 ℃ of temperature of cooling water, crystallizing cycle 4h.
Method of the present invention, being divided into oxidation in one section normal pressure leaches leaches and replaces and leach two stages, oxidation leaching stage aerating oxygen mainly leaches nickel and the iron in the alloy, the displacement leaching stage mainly is the nickel of the cupric ion substitutional alloy phase in the preceding liquid, reaction end keeps lower pH value, prevents the hydrolytic precipitation of iron.Reaction slag major ingredient be to get copper after the nickel that do not leach and the displacement, and copper nickel is than higher.
Method of the present invention, one section leach liquor are adjusted and are sent into the autoclave deironing of pressurizeing after the pH value, and liquid can directly enter the nickel production system after the deironing, and nickeliferous the hanging down of scum can be abandoned.
Method of the present invention, carry out two sections leachings after the pulp of one section pressurization leached mud, this section will obtain copper nickel than two sections higher leach liquors, can carry out evaporative crystallization copper sulfate, with most copper open circuit, the remaining amount of copper of crystalline mother solution is returned one section and is leached the preceding liquid of preparation leaching.
The present invention further improves the accumulation rate of precious metal in order to reduce the slag rate, with the leaching of pressurizeing of two sections normal pressure leached muds, leaches wherein nickel and copper as much as possible, to reduce the burden that noble metal systems is handled.The pressurization leach liquor returns one section normal pressure and leaches at system's internal recycle.
Method of the present invention is a kind of metallurgical technology of handling alloy (coarse grain alloy) material that is obtained by magnetic separation copper Bessemer matte.By segmentation leaching nickel, iron, copper wherein, the leached mud that obtains enriching noble metals can be sent to precious metal and handle.The iron content leach liquor that the leaches deironing of pressurizeing, liquid is the less nickel solution of impurity after the deironing, can directly enter the nickel system.The cupric leach liquor carries out evaporative crystallization, obtains the open circuit that copper sulfate forms copper, and crystalline mother solution recycles in the leaching system.Simply efficient, the eco-friendly flow process of technology.Be fit to handle cupronickel, also can be by adjusting the correlation technique parameter, the alloy mineral selectivity that can be suitable for various grades leaches separating nickel, copper and precious metal.
Description of drawings
Fig. 1 is a principle flow chart of the present invention.
Embodiment
The leaching method of the alloy that a kind of magnetic separation copper Bessemer matte obtains, the technology that adopts two sections normal pressures to leach, pressurize and leach, pressurize deironing and copper sulfate evaporative crystallization obtains concentration of precious metal and directly enters noble metal systems than high pressurization slag.Each section flow process condition is:
1, one section normal pressure leaches oxidation panel control pulp liquid-solid ratio 10-14: 1m
3/ ton, initial sulfuric acid concentration is 45-70g/l, and temperature of reaction is 80-90 ℃, and the reaction times is 1-2h.
2, one period normal pressure leaching displacement section reaction times is 4h～5h, and temperature of reaction is 80-90 ℃, and terminal point contains Cu＜0.5g/l, Ni≤110g/l.
3, two sections normal pressures of control leach: pulp liquid-solid ratio 7-9: 1m
3/ ton, initial sulfuric acid concentration is 100-160g/l, temperature of reaction is 80-90 ℃.
4, the control pressurization is leached: liquid-solid ratio 6-8: 1m
3/ ton, temperature of reaction is 150-160 ℃, and the leaching oxygen partial pressure is 0.20-0.25Mpa, and the reaction times is 3h-4h.
5, control pressurization deironing: temperature of reaction is 165-180 ℃, and the leaching oxygen partial pressure is 0.3MPa, and the reaction times is 2-4h;
6, control copper sulfate evaporative crystallization: 85 ℃～90 ℃ of vaporization temperatures, heating steam pressure 0.2MPa～0.3Mpa, the evaporation terminal point contains Cu 100-120g/l, 25～28 ℃ of temperature of cooling water, crystallizing cycle 4h.
The coarse grain alloy quantitative and even of sending here from the floating workshop of high sulfonium mill adds the pulp groove of preparing burden, and adds the pressurization leaching simultaneously in batching pulp groove and returns liquid, crystalline mother solution, a certain amount of water and sulfuric acid.The slurry for preparing pumps into one section atmospheric pressure oxidation groove, carries out oxidation and leach under the situation of logical oxygen, and the oxidation leaching is replaced heavy copper leaching after medial launder pumps into one section normal pressure displacement slot.Ore pulp after the leaching directly enters thickener and carries out liquid-solid separation.The thickener overflow enters overflow groove, through pumping pressure oxidation deironing.
Thickener underflow filters through underflow pumping pressure filter, and filter residue is discharged into one section slag pulp groove, and a certain amount of water of adding and sulfuric acid are prepared burden in the pulp groove simultaneously.The slurry for preparing pumps into two sections normal pressure leaching vat, carries out two sections normal pressures and leach under the situation of logical oxygen.
Leach the back ore pulp and be pumped to the pressure filter filtration through medial launder.Filtrate is through pumping copper sulfate evaporative crystallization.Filter residue is discharged into two sections slag pulp dosing vessels, adds a certain amount of water and sulfuric acid and carries out the pulp batching, and the pumping pressurization is leached then.Leach two sections leached mud slurries of alloy of sending here from two sections normal pressures and after ore pulp force (forcing) pump, the preheating of ore pulp well heater, enter horizontal pressurization leaching still, the leaching copper and mickel that pressurizes under the situation of logical oxygen, the ore pulp after the leaching carries out liquid-solid separation through decompression cooling groove decompression back inflow thickener.The thickener overflow is promptly pressurizeed leach liquor from flowing into pressurization leach liquor storage tank, returns one section normal pressure through pump and leaches; Thickener underflow is pumped to the band filter and carries out filtration washing.Filtrate is from flowing into pressurization leach liquor storage tank, and washing lotion concentrates on the washing lotion storage tank, from then on returns normal pressure or pressurization leaching batching.Filter residue after the washing is that the precious metal slag is discharged into the slag case, is sent to the precious metal workshop.
Two sections normal pressure leach liquors are through the transferpump well heater, add vaporizer continuously, and the solution after the evaporation concentration successively enters crystallizer tank continuously, puts into whizzer behind the cupric sulphate crystal and separates, and is sent to other workshops after the packing and makes with extra care; Nickeliferous after the crystallization, copper mother liquor leaches batching through one section normal pressure of mother liquid tank blowback.The water vapor that vaporizer is separated enters condenser, and water of condensation returns and is used for leaching batching.
One section normal pressure leaches the leach liquor of sending here and is rich in nickel and iron, after force (forcing) pump, ore pulp well heater, preheating, enter horizontal pressure oxidation and remove iron still, ferrous ion is hydrolyzed into the trivalent ferric oxide and folds under the high temperature that leads to oxygen, condition of high voltage, the ore pulp of autoclave flows into thickener and carries out liquid-solid separation after the decompression of decompression cooling groove.The thickener overflow is liquid liquid storage tank after flowing into deironing after the deironing, through the past nickel electrowinning workshop of pumping.Thickener underflow pumping band filter carries out filtration washing.Filtrate is the liquid storage tank after flowing into deironing, and washing lotion concentrates on the washing lotion storage tank, returns one section normal pressure and leaches batching.Filter residue after the washing is that scum is discharged into the slag case, transports the slag field to.
Embodiment 1
Alloying constituent sees Table 1
The raw material composition sees Table 1:
Table 1 coarse grain alloy composition following (%, g/t):
| Ni(％) | Co | Cu | Fe | S | Si0 2 | Pt(g/t) | Pd | Au |
| 69 | 1.28 | 14.23 | 8.5 | 3.5 | 1.36 | 123.22 | 56.19 | 48.8 |
The coarse grain alloy quantitative and even adds batching pulp groove, and the adding pressurization is leached and returned liquid, crystalline mother solution, a certain amount of water and sulfuric acid in batching pulp groove simultaneously, control pulp liquid-solid ratio 11: 1m
3/ ton, initial sulfuric acid concentration is 60g/l, and ore pulp carries out one section normal pressure leaching oxidation panel after the pulp, and controlled oxidation section temperature of reaction is 80 ℃, and the reaction times is 1h; The slurry for preparing pumps into one section atmospheric pressure oxidation groove, carries out oxidation and leach under the situation of logical oxygen, and the oxidation leaching is replaced heavy copper leaching after medial launder pumps into one section normal pressure displacement slot, the displacement section reaction times is 4h, temperature of reaction is 80 ℃, and terminal point contains Cu＜0.5g/l, Ni≤110g/l.Ore pulp after the leaching directly enters thickener and carries out liquid-solid separation.The thickener overflow enters overflow groove, through pumping pressure oxidation deironing.
Thickener underflow filters through underflow pumping pressure filter, and filter residue is discharged into one section slag pulp groove, and a certain amount of water of adding and sulfuric acid are prepared burden in the pulp groove simultaneously, control pulp liquid-solid ratio 7: 1m
3/ ton, initial sulfuric acid concentration is 150g/l.The slurry for preparing pumps into two sections normal pressure leaching vat, and temperature of reaction is 80 ℃.
Leach the back ore pulp and be pumped to the pressure filter filtration through medial launder.Filtrate is through pumping copper sulfate evaporative crystallization.Filter residue is discharged into two sections slag pulp dosing vessels, adds a certain amount of water and sulfuric acid and carries out pulp batching, pulp liquid-solid ratio 6: 1m
3/ ton, the pumping pressurization is leached then, and it is 160 ℃ that temperature of reaction is leached in the control pressurization, and the leaching oxygen partial pressure is 0.25Mpa, and the reaction times is 4h.Ore pulp after the leaching flows into thickener and carries out liquid-solid separation after the decompression of decompression cooling groove.The thickener overflow is promptly pressurizeed leach liquor from flowing into pressurization leach liquor storage tank, returns one section normal pressure through pump and leaches; Thickener underflow is pumped to the band filter and carries out filtration washing.Filtrate is from flowing into pressurization leach liquor storage tank, and washing lotion concentrates on the washing lotion storage tank, from then on returns normal pressure or pressurization leaching batching.Filter residue after the washing is that the precious metal slag is discharged into the slag case, is sent to the precious metal workshop.
Two sections normal pressure leach liquors are through the transferpump well heater, add vaporizer continuously, and the solution after the evaporation concentration successively enters crystallizer tank continuously, 90 ℃ of control vaporization temperatures, heating steam pressure 0.3Mpa, the evaporation terminal point contains Cu120g/l, 25 ℃ of temperature of cooling water, crystallizing cycle 4h.Put into whizzer behind the cupric sulphate crystal and separate, be sent to other workshops after the packing and make with extra care; Nickeliferous after the crystallization, copper mother liquor leaches batching through one section normal pressure of mother liquid tank blowback.
One section normal pressure leaches the leach liquor of sending here and is rich in nickel and iron, enters horizontal pressure oxidation and remove iron still after force (forcing) pump, ore pulp well heater, preheating, and temperature of reaction is 180 ℃, and the leaching oxygen partial pressure is 0.3MPa, and the reaction times is 2h; Ferrous ion is hydrolyzed into the trivalent ferric oxide and folds under the high temperature that leads to oxygen, condition of high voltage, the ore pulp of autoclave flows into thickener and carries out liquid-solid separation after the decompression of decompression cooling groove.The thickener overflow is liquid liquid storage tank after flowing into deironing after the deironing, through the past nickel electrowinning workshop of pumping.
Embodiment 2
The coarse grain alloy composition sees Table 1
The coarse grain alloy quantitative and even adds batching pulp groove, and the adding pressurization is leached and returned liquid, crystalline mother solution, a certain amount of water and sulfuric acid in batching pulp groove simultaneously, control pulp liquid-solid ratio 12: 1m
3/ ton, initial sulfuric acid concentration is 55g/l, and ore pulp carries out one section normal pressure leaching oxidation panel after the pulp, and controlled oxidation section temperature of reaction is 85 ℃, and the reaction times is 1.5h; The slurry for preparing pumps into one section atmospheric pressure oxidation groove, carries out oxidation and leach under the situation of logical oxygen, and the oxidation leaching is replaced heavy copper leaching after medial launder pumps into one section normal pressure displacement slot, the displacement section reaction times is 4h, temperature of reaction is 85 ℃, and terminal point contains Cu＜0.5g/l, Ni≤110g/l.Ore pulp after the leaching directly enters thickener and carries out liquid-solid separation.The thickener overflow enters overflow groove, through pumping pressure oxidation deironing.
Thickener underflow filters through underflow pumping pressure filter, and filter residue is discharged into one section slag pulp groove, and a certain amount of water of adding and sulfuric acid are prepared burden in the pulp groove simultaneously, control pulp liquid-solid ratio 8: 1m
3/ ton, initial sulfuric acid concentration is 135g/l.The slurry for preparing pumps into two sections normal pressure leaching vat, and temperature of reaction is 85 ℃.
Leach the back ore pulp and be pumped to the pressure filter filtration through medial launder.Filtrate is through pumping copper sulfate evaporative crystallization.Filter residue is discharged into two sections slag pulp dosing vessels, adds a certain amount of water and sulfuric acid and carries out pulp batching, pulp liquid-solid ratio 7: 1m
3/ ton, the pumping pressurization is leached then, and it is 155 ℃ that temperature of reaction is leached in the control pressurization, and the leaching oxygen partial pressure is 0.23Mpa, and the reaction times is 3.5h.Ore pulp after the leaching flows into thickener and carries out liquid-solid separation after the decompression of decompression cooling groove.The thickener overflow is promptly pressurizeed leach liquor from flowing into pressurization leach liquor storage tank, returns one section normal pressure through pump and leaches; Thickener underflow is pumped to the band filter and carries out filtration washing.Filtrate is from flowing into pressurization leach liquor storage tank, and washing lotion concentrates on the washing lotion storage tank, from then on returns normal pressure or pressurization leaching batching.Filter residue after the washing is that the precious metal slag is discharged into the slag case, is sent to the precious metal workshop.
Two sections normal pressure leach liquors are through the transferpump well heater, add vaporizer continuously, and the solution after the evaporation concentration successively enters crystallizer tank continuously, 85 ℃ ℃ of control vaporization temperatures, heating steam pressure 0.25MPa, the evaporation terminal point contains Cu 110g/l, 27 ℃ of temperature of cooling water, crystallizing cycle 4h.Put into whizzer behind the cupric sulphate crystal and separate, be sent to other workshops after the packing and make with extra care; Nickeliferous after the crystallization, copper mother liquor leaches batching through one section normal pressure of mother liquid tank blowback.
One section normal pressure leaches the leach liquor of sending here and is rich in nickel and iron, enters horizontal pressure oxidation and remove iron still after force (forcing) pump, ore pulp well heater, preheating, and temperature of reaction is 275 ℃, and the leaching oxygen partial pressure is 0.3MPa, and the reaction times is 3h; Ferrous ion is hydrolyzed into the trivalent ferric oxide and folds under the high temperature that leads to oxygen, condition of high voltage, the ore pulp of autoclave flows into thickener and carries out liquid-solid separation after the decompression of decompression cooling groove.The thickener overflow is liquid liquid storage tank after flowing into deironing after the deironing, through the past nickel electrowinning workshop of pumping.
Embodiment 3
The coarse grain alloy composition sees Table 1
The coarse grain alloy quantitative and even adds batching pulp groove, and the adding pressurization is leached and returned liquid, crystalline mother solution, a certain amount of water and sulfuric acid in batching pulp groove simultaneously, control pulp liquid-solid ratio 13: 1m
3/ ton, initial sulfuric acid concentration is 50g/l, and ore pulp carries out one section normal pressure leaching oxidation panel after the pulp, and controlled oxidation section temperature of reaction is 85 ℃, and the reaction times is 2h; The slurry for preparing pumps into one section atmospheric pressure oxidation groove, carries out oxidation and leach under the situation of logical oxygen, and the oxidation leaching is replaced heavy copper leaching after medial launder pumps into one section normal pressure displacement slot, the displacement section reaction times is 4h, temperature of reaction is 85 ℃, and terminal point contains Cu＜0.5g/l, Ni≤110g/l.Ore pulp after the leaching directly enters thickener and carries out liquid-solid separation.The thickener overflow enters overflow groove, through pumping pressure oxidation deironing.
Thickener underflow filters through underflow pumping pressure filter, and filter residue is discharged into one section slag pulp groove, and a certain amount of water of adding and sulfuric acid are prepared burden in the pulp groove simultaneously, control pulp liquid-solid ratio 9: 1m
3/ ton, initial sulfuric acid concentration is 120g/l.The slurry for preparing pumps into two sections normal pressure leaching vat, and temperature of reaction is 90 ℃.
Leach the back ore pulp and be pumped to the pressure filter filtration through medial launder.Filtrate is through pumping copper sulfate evaporative crystallization.Filter residue is discharged into two sections slag pulp dosing vessels, adds a certain amount of water and sulfuric acid and carries out pulp batching, pulp liquid-solid ratio 8: 1m
3/ ton, the pumping pressurization is leached then, and it is 150 ℃ that temperature of reaction is leached in the control pressurization, and the leaching oxygen partial pressure is 0.20Mpa, and the reaction times is 3h.Ore pulp after the leaching flows into thickener and carries out liquid-solid separation after the decompression of decompression cooling groove.The thickener overflow is promptly pressurizeed leach liquor from flowing into pressurization leach liquor storage tank, returns one section normal pressure through pump and leaches; Thickener underflow is pumped to the band filter and carries out filtration washing.Filtrate is from flowing into pressurization leach liquor storage tank, and washing lotion concentrates on the washing lotion storage tank, from then on returns normal pressure or pressurization leaching batching.Filter residue after the washing is that the precious metal slag is discharged into the slag case, is sent to the precious metal workshop.
Two sections normal pressure leach liquors are through the transferpump well heater, add vaporizer continuously, and the solution after the evaporation concentration successively enters crystallizer tank continuously, 85 ℃ of control vaporization temperatures, heating steam pressure 0.2MPa, the evaporation terminal point contains Cu100g/l, 25 ℃ of temperature of cooling water, crystallizing cycle 4h.Put into whizzer behind the cupric sulphate crystal and separate, be sent to other workshops after the packing and make with extra care; Nickeliferous after the crystallization, copper mother liquor leaches batching through one section normal pressure of mother liquid tank blowback.
One section normal pressure leaches the leach liquor of sending here and is rich in nickel and iron, enters horizontal pressure oxidation and remove iron still after force (forcing) pump, ore pulp well heater, preheating, and temperature of reaction is 170 ℃, and the leaching oxygen partial pressure is 0.3MPa, and the reaction times is 4h; Ferrous ion is hydrolyzed into the trivalent ferric oxide and folds under the high temperature that leads to oxygen, condition of high voltage, the ore pulp of autoclave flows into thickener and carries out liquid-solid separation after the decompression of decompression cooling groove.The thickener overflow is liquid liquid storage tank after flowing into deironing after the deironing, through the past nickel electrowinning workshop of pumping.
Claims (2)
1. the leaching method of the alloy that obtains of a magnetic separation copper Bessemer matte is characterized in that adopting two sections normal pressures to leach, pressurization is leached, the technology of pressurization deironing and copper sulfate evaporative crystallization, obtains concentration of precious metal and directly enters noble metal systems than high pressurization slag.
2. the leaching method of the alloy that a kind of magnetic separation copper Bessemer matte according to claim 1 obtains is characterized in that its leaching process comprises:
A) the mineral acid-containing solution is carried out one section normal pressure pulp control pulp liquid-solid ratio 10-14: 1m
3/ ton, initial sulfuric acid concentration is 45-70g/l, and ore pulp carries out one section normal pressure leaching oxidation panel after the pulp, and controlled oxidation section temperature of reaction is 80-90 ℃, and the reaction times is 1-2h;
B) the displacement section reaction times is 4h～5h, and temperature of reaction is 80-90 ℃, and terminal point contains Cu＜0.5g/l, Ni≤110g/l;
C) two sections normal pressures of control leach: pulp liquid-solid ratio 7-9: 1m
3/ ton, initial sulfuric acid concentration is 100-160g/l, temperature of reaction is 80-90 ℃;
D) the control pressurization is leached: pulp liquid-solid ratio 6-8: 1m
3/ ton, temperature of reaction is 150-160 ℃, and the leaching oxygen partial pressure is 0.20-0.25Mpa, and the reaction times is 3h-4h;
E) control pressurization deironing: temperature of reaction is 165-180 ℃, and the leaching oxygen partial pressure is 0.3MPa, and the reaction times is 2-4h;
F) control copper sulfate evaporative crystallization: 85 ℃～90 ℃ of vaporization temperatures, heating steam pressure 0.2MPa～0.3Mpa, the evaporation terminal point contains Cu 100-120g/l, 25～28 ℃ of temperature of cooling water, crystallizing cycle 4h.
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