CN116254410A - Leaching method of sulfide minerals - Google Patents
Leaching method of sulfide minerals Download PDFInfo
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- CN116254410A CN116254410A CN202211737833.7A CN202211737833A CN116254410A CN 116254410 A CN116254410 A CN 116254410A CN 202211737833 A CN202211737833 A CN 202211737833A CN 116254410 A CN116254410 A CN 116254410A
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- sulfuric acid
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- 238000002386 leaching Methods 0.000 title claims abstract description 266
- 229910052569 sulfide mineral Inorganic materials 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 47
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 124
- 238000000227 grinding Methods 0.000 claims abstract description 73
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 61
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 61
- 239000001301 oxygen Substances 0.000 claims abstract description 61
- 238000006243 chemical reaction Methods 0.000 claims abstract description 56
- 239000000463 material Substances 0.000 claims abstract description 39
- 229910052500 inorganic mineral Inorganic materials 0.000 claims abstract description 31
- 239000011707 mineral Substances 0.000 claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 21
- 239000002002 slurry Substances 0.000 claims abstract description 20
- 238000001914 filtration Methods 0.000 claims abstract description 19
- 239000002893 slag Substances 0.000 claims abstract description 19
- 238000003756 stirring Methods 0.000 claims abstract description 13
- 238000004537 pulping Methods 0.000 claims abstract description 7
- 230000004913 activation Effects 0.000 claims abstract description 5
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 124
- 229910052759 nickel Inorganic materials 0.000 claims description 62
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 37
- 238000000605 extraction Methods 0.000 claims description 29
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 26
- 239000010949 copper Substances 0.000 claims description 26
- 229910052802 copper Inorganic materials 0.000 claims description 25
- 239000007800 oxidant agent Substances 0.000 claims description 18
- 239000012535 impurity Substances 0.000 claims description 10
- WWNBZGLDODTKEM-UHFFFAOYSA-N sulfanylidenenickel Chemical compound [Ni]=S WWNBZGLDODTKEM-UHFFFAOYSA-N 0.000 claims description 9
- NHPHQYDQKATMFU-UHFFFAOYSA-N [Cu]=S.[Co] Chemical compound [Cu]=S.[Co] NHPHQYDQKATMFU-UHFFFAOYSA-N 0.000 claims description 6
- RYTYSMSQNNBZDP-UHFFFAOYSA-N cobalt copper Chemical compound [Co].[Cu] RYTYSMSQNNBZDP-UHFFFAOYSA-N 0.000 claims description 6
- 238000005507 spraying Methods 0.000 claims description 5
- 238000010907 mechanical stirring Methods 0.000 claims description 4
- 239000002904 solvent Substances 0.000 claims description 4
- 229910000881 Cu alloy Inorganic materials 0.000 claims description 3
- 238000012545 processing Methods 0.000 claims description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims 1
- 239000003795 chemical substances by application Substances 0.000 claims 1
- 229910001882 dioxygen Inorganic materials 0.000 claims 1
- 230000001105 regulatory effect Effects 0.000 claims 1
- 239000002184 metal Substances 0.000 abstract description 33
- 229910052751 metal Inorganic materials 0.000 abstract description 33
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 239000000243 solution Substances 0.000 description 55
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 36
- 229910052742 iron Inorganic materials 0.000 description 18
- 239000010941 cobalt Substances 0.000 description 13
- 229910017052 cobalt Inorganic materials 0.000 description 13
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 13
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 12
- 238000007254 oxidation reaction Methods 0.000 description 12
- 238000013461 design Methods 0.000 description 11
- 229910052717 sulfur Inorganic materials 0.000 description 8
- 239000011593 sulfur Substances 0.000 description 8
- 150000002739 metals Chemical class 0.000 description 7
- 239000002245 particle Substances 0.000 description 7
- 238000001514 detection method Methods 0.000 description 6
- 238000000746 purification Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 239000001117 sulphuric acid Substances 0.000 description 5
- 235000011149 sulphuric acid Nutrition 0.000 description 5
- 239000005864 Sulphur Substances 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 230000001590 oxidative effect Effects 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 229910000531 Co alloy Inorganic materials 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000009854 hydrometallurgy Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 239000003082 abrasive agent Substances 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- LGQLOGILCSXPEA-UHFFFAOYSA-L nickel sulfate Chemical compound [Ni+2].[O-]S([O-])(=O)=O LGQLOGILCSXPEA-UHFFFAOYSA-L 0.000 description 2
- 229910000363 nickel(II) sulfate Inorganic materials 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 229910000361 cobalt sulfate Inorganic materials 0.000 description 1
- 229940044175 cobalt sulfate Drugs 0.000 description 1
- KTVIXTQDYHMGHF-UHFFFAOYSA-L cobalt(2+) sulfate Chemical compound [Co+2].[O-]S([O-])(=O)=O KTVIXTQDYHMGHF-UHFFFAOYSA-L 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229910000365 copper sulfate Inorganic materials 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- -1 hydrogen ions Chemical class 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 150000002815 nickel Chemical class 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 150000004763 sulfides Chemical class 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/06—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
- C22B3/08—Sulfuric acid, other sulfurated acids or salts thereof
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0002—Preliminary treatment
- C22B15/0004—Preliminary treatment without modification of the copper constituent
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/005—Preliminary treatment of ores, e.g. by roasting or by the Krupp-Renn process
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
- C22B3/30—Oximes
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Metallurgy (AREA)
- Mechanical Engineering (AREA)
- Materials Engineering (AREA)
- Manufacturing & Machinery (AREA)
- Environmental & Geological Engineering (AREA)
- Geology (AREA)
- Geochemistry & Mineralogy (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention provides a method for leaching sulfide minerals, which comprises the following steps: secondary grinding is carried out on the vulcanized minerals, concentrated sulfuric acid is added in the secondary grinding, and pre-activation is carried out, so that materials after secondary grinding are obtained; adding the materials subjected to secondary grinding into sulfuric acid solution, and carrying out normal pressure leaching to obtain normal pressure leaching slurry; wherein at least one of stirring, introducing oxygen, and maintaining an atmospheric leaching temperature is performed during the atmospheric leaching; filtering the normal pressure leaching slurry to obtain normal pressure leaching slag and normal pressure leaching liquid; and pulping the normal pressure leaching slag by using sulfuric acid solution, performing pressure leaching, and performing at least one operation of introducing oxygen, adjusting the air pressure and adjusting the initial temperature of the pressure leaching in the pressure leaching process, and filtering after the reaction is completed to obtain pressure leaching liquid and pressure leaching slag. The leaching rate of target metal in the normal pressure leaching stage can be improved, the treatment capacity of sulfide minerals in the pressure leaching stage is reduced, and the energy consumption, the cost and the potential safety hazard are reduced.
Description
Technical Field
The invention relates to the field of nonferrous metal hydrometallurgy, in particular to a leaching method of sulfide minerals.
Background
Hydrometallurgy is one of two technologies for extracting metallurgy, namely a process of contacting ore or other raw materials with an aqueous solution or other liquid, leaching by chemical reaction or the like, and separating solid from liquid to extract target metals or compounds thereof. In the hydrometallurgical industry, the target metal extracted from copper and cobalt raw materials represented by copper cobalt sulfide ore and copper cobalt alloy and nickel raw materials represented by nickel sulfide ore, high nickel matte and low nickel matte has a considerable specific gravity. It is therefore necessary to study the leaching process in hydrometallurgical processes of sulphide minerals for modern metallurgical development.
Taking nickel extraction from high nickel matte as an example, the conventional extraction process is to grind the high nickel matte to 200 meshes by a ball mill, then leach the high nickel matte under normal pressure in a dilute sulfuric acid solution, leach a large amount of elemental nickel by acid in an normal pressure leaching stage, then pump the slurry after normal pressure leaching into an oxygen pressure leaching kettle, leach the unleached nickel continuously under the high-pressure high-temperature oxygen-enriched condition, leach more than 90% of impurity copper in the high nickel matte, and leach about 20% of iron at the same time of extracting the nickel. Then adding sodium carbonate into the solution containing the impurities such as nickel, iron, copper and the like after the reaction to neutralize, hydrolyze and remove iron and copper to achieve the aim of purification, and extracting the purified solution to deeply purify other impurities to finally produce a high-purity nickel sulfate solution which can be directly used for producing high-purity nickel series products.
The process of hydrometallurgical extraction of target metals from other sulphide minerals is similar to that of nickel in high grade nickel matte.
However, in the above process, the step of grinding the high nickel matte to 200 meshes by using the ball mill only reduces the size of the vulcanized mineral so as to carry out subsequent normal pressure leaching and pressure leaching, so that the leaching rate of the target metal in the normal pressure leaching stage is lower, more than 70% of leaching reaction needs to be leached under the condition of pressure oxygen enrichment, and the high leaching rate of the target metal can be ensured by utilizing multi-stage pressure leaching in the high pressure oxygen enrichment leaching stage, so that a large amount of high pressure oxygen enrichment reaction equipment is required to be configured in the process of extracting the target metal, the equipment investment is large, the required electric energy is huge, and meanwhile, the configuration of a large amount of high pressure oxygen enrichment equipment greatly increases the potential safety hazard in the production process.
Therefore, how to improve the grinding process to increase the leaching rate of target metals in the normal pressure leaching stage, thereby reducing the treatment capacity of sulphide minerals in the pressure oxygen-enriched leaching stage, simplifying the extraction equipment, reducing the energy consumption and the cost, and reducing the potential safety hazard in the production process has become a technical problem to be solved.
Disclosure of Invention
Aiming at the technical problems that in the prior art, the leaching rate of target metal is low in the normal pressure leaching stage, so that the high leaching rate of the target metal can be ensured only by utilizing multi-stage pressure leaching in the high pressure oxygen-enriched leaching stage.
The invention provides a method for leaching sulfide minerals, which comprises the following steps:
s1, secondary grinding is carried out on sulfide minerals, concentrated sulfuric acid is added in the secondary grinding, and pre-activation is carried out, so that materials after secondary grinding are obtained;
s2, adding the materials subjected to secondary grinding into sulfuric acid solution, and performing normal pressure leaching to obtain normal pressure leached pulp; wherein at least one of stirring, introducing oxygen, and maintaining an atmospheric leaching temperature is performed during the atmospheric leaching;
s3, filtering the normal pressure leaching slurry to obtain normal pressure leaching slag and normal pressure leaching liquid;
s4, adding the normal pressure leaching slag into sulfuric acid solution for pulping, performing pressure leaching, and performing at least one of the operations of introducing oxygen, adjusting the air pressure and adjusting the initial temperature of the pressure leaching in the pressure leaching process, and filtering after full reaction to obtain the pressure leaching slag and the pressure leaching liquid.
Preferably, after S4, the leaching method further comprises:
s5, carrying out impurity removal treatment on the pressurized leaching solution, and filtering to obtain impurity-removed leaching solution.
Preferably, in S1, the second grinding is first grinding and then second grinding; adding concentrated sulfuric acid into the second-stage grinding to perform preactivation; the particle size of the materials after secondary grinding is required to be satisfied, the particle size D90 of the materials after the first section of grinding is less than 80 microns, and the particle size D90 of the materials after secondary grinding is less than 40 microns; the concentration of sulfuric acid in the concentrated sulfuric acid in S1 is 1400-1800g/L, and the addition amount of the concentrated sulfuric acid is 1.0-5.5% of the weight of the sulfide mineral; the adding speed of the concentrated sulfuric acid is 0.1-0.5t/h; concentrated sulfuric acid is added in a pipeline conveying and spraying mode; preferably, the first stage of grinding is coarse grinding by a ball mill or a Raymond mill, and the second stage of grinding is fine grinding by a tube mill, a vibration mill or a mechanical stirring mill.
Preferably, in S2, the concentration of sulfuric acid in the sulfuric acid solution is 100g/L-160g/L; in S4, the concentration of sulfuric acid in the sulfuric acid solution is 10g/L-100g/L. The material consumption is determined according to the quality of sulfide minerals in the material, and the quality of sulfide minerals is determined according to the quality of sulfuric acid; wherein the sulphide mineral mass= (mass of total sulphuric acid x molar mass of metal element to be leached/molar mass of sulphuric acid) x 1.05/[ 1- (mass% of sulphur in sulphide mineral x molar mass of metal element to be leached/molar mass of sulphur element)/percentage of metal element to be leached in sulphide mineral ].
Preferably, in S2, the device for atmospheric leaching reaction is an atmospheric leaching device; the oxygen inlet speed is 10-60Nm 3 /h, and the purity of the oxygen is more than 90 percent;
the device for introducing oxygen is an ultrasonic super-energy oxidizer, and the ultrasonic super-energy oxidizer is connected with an oxygen source and is communicated with the bottom of the atmospheric leaching device;
the mode of the introduced oxygen is as follows: the ultrasonic super-energy oxidizer mixes the slurry of the secondary ground material flowing out of the upper part of the normal pressure leaching device with sulfuric acid solution and introduced oxygen, and then the mixture is pumped into the normal pressure leaching device from the bottom of the normal pressure leaching device.
Preferably, the stirring speed is 50-120r/min;
preferably, the atmospheric leaching temperature is maintained at 60-90 ℃;
preferably, the atmospheric leaching time is 2-13h.
Preferably, in S4, the slurrying time is 0.5-2 hours; pressurizing with oxygen and maintaining the air pressure at 1.4-1.8Mpa, wherein the purity of the oxygen is more than 90%; the initial temperature of the pressure leaching was adjusted to 120-140 ℃.
Preferably, the pressure leaching time is 2-5 hours.
Preferably, the sulfide mineral is at least one or more of nickel sulfide mineral, copper cobalt sulfide mineral, cobalt copper alloy, high nickel matte and low nickel matte.
Preferably, when the sulfide mineral is at least one or more of nickel sulfide mineral, high nickel matte, and low nickel matte, S5 is specifically: adjusting the pH and temperature of the pressurized leaching solution, adding an LIX extractant, adopting a 4-stage centrifugal extraction method to remove copper and purify, and filtering to obtain the impurity-removed leaching solution.
Preferably, in S5, the pH of the pressurized leach solution is maintained at 1-2; the temperature of the pressurized leaching solution is maintained to be less than or equal to 55 ℃; the organic proportion of the 4-stage centrifugal extraction method is LIX extractant: solvent oil= (20% -30%): (70% -80%).
In summary, the invention provides a method for leaching sulfide minerals, which comprises the steps of pre-activating sulfide minerals by using concentrated sulfuric acid in a grinding stage, so that oxidation reaction of sulfide in the sulfide minerals and leaching reaction of elemental metal in the sulfide minerals are accelerated; further, oxygen is fully dispersed by utilizing an ultrasonic super-energy oxidizer, and the granularity of the grinded sulfide mineral needs to meet the requirement of D90<40 microns, so that the specific surface area of the material and the contact area with the oxygen are greatly increased, and the reaction rate of oxidizing sulfide at normal pressure and the leaching rate of target metal are further increased. Thereby reducing the treatment capacity of the sulphide minerals in the pressure leaching stage, and achieving the purposes of simplifying the extraction equipment of the pressure leaching, reducing the energy consumption and the cost and reducing the potential safety hazard in the production process.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings that are needed in the description of the embodiments or the prior art will be briefly described, and it is obvious that the drawings in the description below are some embodiments of the present invention, and other drawings can be obtained according to the drawings without inventive effort for a person skilled in the art.
Fig. 1: the embodiment of the invention provides a flow chart of a method for leaching sulfide minerals;
fig. 2: the embodiment of the invention provides a flow chart of a method for leaching sulfide minerals.
Detailed Description
To further clarify the above and other features and advantages of the present invention, a further description of the invention will be rendered by reference to the appended drawings. It should be understood that the specific embodiments presented herein are for purposes of explanation to those skilled in the art and are intended to be illustrative only and not limiting.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present invention. It will be apparent, however, to one skilled in the art that the specific details need not be employed to practice the present invention. In other instances, well-known steps or operations have not been described in detail in order to avoid obscuring the invention.
In order to improve the leaching rate of target metal in the normal pressure leaching stage, thereby reducing the treatment capacity of sulfide minerals in the pressure oxygen-enriched leaching stage, simplifying extraction equipment, reducing energy consumption and cost and reducing potential safety hazard in the production process. As shown in fig. 1, the present invention provides a method for leaching a sulphide mineral, the method comprising:
s1, secondary grinding is carried out on sulfide minerals, concentrated sulfuric acid is added in the secondary grinding, and pre-activation is carried out, so that materials after secondary grinding are obtained; .
In the application, the sulfide mineral is at least one or more of nickel sulfide mineral, copper cobalt sulfide mineral, cobalt copper alloy, high nickel matte and low nickel matte.
The secondary grinding is first section grinding and then second section grinding; adding concentrated sulfuric acid into the second-stage grinding to perform preactivation;
more specifically, the first stage of grinding in the secondary grinding is ball mill coarse grinding, and the second stage of grinding is sand mill fine grinding; in a further preferred embodiment, the first stage of grinding is performed by a ball mill or a Raymond mill, and the second stage of grinding is performed by a tube mill, a vibration mill or a mechanical stirring mill.
The granularity of the vulcanized mineral after the first-stage grinding is required to reach the abrasive material with the granularity D90 smaller than 80 microns, and the granularity of the vulcanized mineral after the second-stage grinding is required to reach the abrasive material with the granularity D90 smaller than 40 microns. So as to ensure that the material can be fully contacted with oxygen in the subsequent leaching process.
Further, adding concentrated sulfuric acid into the second-stage grinding, wherein the concentration of sulfuric acid in the concentrated sulfuric acid is 1400-1800g/L, and the adding amount of the concentrated sulfuric acid is 1.0-5.5% of the weight of the sulfide minerals; the adding speed of the concentrated sulfuric acid is 0.1-0.5t/h; concentrated sulfuric acid is added in a pipeline conveying and spraying mode; the oxidizing property of the concentrated sulfuric acid and the mechanical strength and friction heat in the grinding process are utilized for preactivation. On one hand, the oxidation reaction of sulfide in sulfide minerals can be accelerated, and on the other hand, the leaching reaction of elemental metal in sulfide minerals can be accelerated.
S2, adding the materials subjected to secondary grinding into sulfuric acid solution, and performing normal pressure leaching to obtain normal pressure leached pulp; wherein at least one of stirring, introducing oxygen, and maintaining an atmospheric leaching temperature is performed during the atmospheric leaching.
In this step, the concentration of the sulfuric acid solution is 100g/L to 160g/L to oxidize part of the metal sulfide by the strong oxidizing property of the sulfuric acid of relatively high concentration. The quality of the sulphide mineral is determined on the basis of the quality of the sulphuric acid, in particular the quality of the sulphide mineral= (total sulphuric acid mass x molar mass of the metal element to be leached/molar mass of the sulphuric acid) ×1.05/[ 1- (mass% of sulphur in the sulphide mineral x molar mass of the metal element to be leached/molar mass of the sulphur element)/percentage of the metal element to be leached in the sulphide mineral ].
The device for normal pressure leaching reaction is a normal pressure leaching device; the oxygen inlet speed is 10-60Nm 3 /h, and the purity of the oxygen is more than 90 percent; specifically, the slurry obtained by mixing the vulcanized mineral with the sulfuric acid solution and the introduced oxygen are mixed by using an ultrasonic super-energy oxidizer communicated with the upper part of the atmospheric pressure leaching device, and then the mixture is pumped into the atmospheric pressure leaching device from the bottom of the atmospheric pressure leaching device. The dispersing effect of oxygen is greatly increased by ultrasonic wave, and meanwhile, the material is ground to have the D90 granularity of 40 microns in the second-stage grinding, so that the specific surface area of the material and the contact area with oxygen are greatly increased, and the reaction rate of normal-pressure oxidized sulfide and the leaching rate of target metal can be greatly increased.
The stirring speed is 50-120r/min, the oxygen introduced into the atmospheric leaching device is further dispersed, the atmospheric leaching temperature is maintained at 60-90 ℃, and the proper temperature of the atmospheric leaching reaction is ensured; the atmospheric leaching time is 2-13h, so that the atmospheric leaching reaction is sufficient.
S3, filtering the normal pressure leaching slurry to obtain normal pressure leaching slag and normal pressure leaching liquid.
In the application, after normal pressure leaching, normal pressure leaching slurry is filtered to obtain normal pressure leaching slag and normal pressure leaching liquid. The normal pressure leaching liquid is sulfate solution of target metal, and can be directly used for producing high-purity target metal series products, and the normal pressure leaching slag contains sulfide of the target metal and can be used for subsequent extraction operation.
S4, adding the normal pressure leaching slag into sulfuric acid solution for pulping, performing pressure leaching, and performing at least one of the operations of introducing oxygen, adjusting the air pressure and adjusting the initial temperature of the pressure leaching in the pressure leaching process, and filtering after full reaction to obtain the pressure leaching slag and the pressure leaching liquid.
In the application, after normal pressure leaching slag is added into sulfuric acid solution to slurry for 0.5-2h, wherein the concentration of sulfuric acid in the sulfuric acid solution is 10g/L-100g/L, the sulfuric acid solution is conveyed into a pressure leaching device, the gas pressure in the pressure leaching device is pressurized and maintained at 1.4-1.8Mpa by utilizing oxygen, meanwhile, the temperature in the pressure leaching device is raised to 120-140 ℃, the pressure oxidation reaction starts violent reaction, and the reaction temperature is maintained by the self-heat release of the reaction until the pressure oxidation reaction is ended. Wherein the pressure leaching time is 2-5h, and the reaction temperature can reach more than 160 ℃ by self-heat release of the reaction.
As shown in fig. 2, in some preferred embodiments, the leaching method further comprises:
s5, when the sulfide mineral is at least one or more of nickel sulfide mineral, high nickel matte and low nickel matte,
s5 specifically comprises the following steps: adjusting the pH and temperature of the pressurized leaching solution, adding an LIX extractant, adopting a 4-stage centrifugal extraction method to remove copper and purify, and filtering to obtain the impurity-removed leaching solution.
In the application, after the pressure leaching reaction is sufficient, the filtered pressure leaching solution is conveyed to a impurity removing device, the PH of the pressure leaching solution is adjusted to be 1-2, the temperature is less than or equal to 55 ℃, an LIX extractant is added, copper removal purification is carried out by adopting a 4-stage centrifugal extraction method, and the impurity removing leaching solution, namely the sulfate solution of target metal, is obtained through filtration and solid-liquid separation. Wherein, the organic proportion of the 4-stage centrifugal extraction method is LIX extractant: solvent oil= (20% -30%): (70% -80%).
In summary, the method provided by the invention has the following advantages:
1) The oxidation reaction of sulfides in the sulfide ores can be accelerated and the leaching of target metals in the subsequent sulfide ores can be accelerated by adding quantitative concentrated sulfuric acid for preactivation at the second stage of grinding nodes and using the oxidizing property of the concentrated sulfuric acid and the mechanical strength and friction heat in the grinding process for preactivation.
2) In normal pressure leaching, the material subjected to secondary grinding is leached at normal pressure by utilizing a sulfuric acid solution with relatively high concentration, so that the oxidation reaction of sulfide in sulfide minerals and the leaching reaction efficiency of elemental metal in sulfide minerals are accelerated.
3) The method is provided with an ultrasonic super-energy oxidizer for performing normal pressure leaching on oxygen in a dispersing way, the ultrasonic wave of the ultrasonic super-energy oxidizer is utilized to greatly increase the dispersing effect of the oxygen, the oxygen with higher purity is introduced, and the material is ground to about 40 microns in granularity by secondary grinding, so that the specific surface area of the material and the contact area with the oxygen are increased, and the reaction rate of normal pressure oxidation sulfide and the leaching rate of target metal can be greatly increased.
4) The method realizes accurate batching in the batching process of normal pressure leaching reaction, utilizes the alkaline characteristic of consuming hydrogen ions of the materials, utilizes the materials as a neutralizing reagent to carry out neutralization hydrolysis iron removal purification reaction, has extremely low content of impurities such as iron in normal pressure leaching liquid, shortens the process flow, reduces the addition of auxiliary materials, and reduces the processing cost of sulphide ores.
5) Compared with the conventional method, the pressure leaching equipment adopts the horizontal belt stirring equipment to carry out pressure leaching, and the scheme greatly increases the reaction rate of normal-pressure oxidized sulfide and the leaching rate of target metal, so that the configuration quantity of high-pressure reaction equipment in the pressure leaching stage can be reduced, and the leaching purification cost of sulfide minerals is reduced. Compared with the conventional method, the method provided by the invention has the advantage that the configuration quantity of high-pressure reaction equipment can be reduced by more than 60%. And the pressurizing oxidation leaching purification process flow for sulphide ore treatment is greatly compressed, the consumption of auxiliary materials is greatly reduced, and the processing cost of sulphide ores is reduced.
In order to embody the advantages of the method provided by the present invention, the following description is made in connection with specific examples.
Example 1
The sulphide mineral is copper-cobalt sulphide ore containing 13.7% of copper, 6% of cobalt, 15.2% of iron and 12.6% of sulfur.
1) Firstly, carrying out first-stage grinding on vulcanized mineral particles 4.05t by using a ball mill, wherein the granularity D90 of the materials subjected to the first-stage grinding is 80 microns, and then carrying out second-stage grinding by using a tube mill, so that the granularity D90 of the materials subjected to the second-stage grinding is 40 microns; and adding concentrated sulfuric acid which is 1.0 percent of the weight of the copper-cobalt sulfide ore into the second section of grinding node in a pipeline conveying and spraying mode. Wherein the concentration of the concentrated sulfuric acid is 1800g/L, and the adding speed of the concentrated sulfuric acid is 0.2t/h.
2) Conveying the material after secondary grinding to a solution containing sulfuric acid with the concentration of 100g/L for 6.5m 3 In the reaction vessel, the reaction temperature was maintained at 60℃and stirring was carried out at a stirring rate of 50r/min and at a stirring rate of 10Nm 3 And introducing oxygen (purity is more than 90%) at the rate of/h for normal pressure leaching reaction for 4h, so as to obtain normal pressure leaching slurry.
The device for introducing oxygen is an ultrasonic super-energy oxidizer, and the ultrasonic super-energy oxidizer is connected with an oxygen source and is communicated with the bottom of the atmospheric leaching device;
the mode of the introduced oxygen is as follows: the ultrasonic super-energy oxidizer mixes the slurry of the secondary ground material flowing out of the upper part of the normal pressure leaching device with sulfuric acid solution and introduced oxygen, and the mixture is pumped into the normal pressure leaching device from the bottom of the normal pressure leaching device so as to make the oxygen fully contact with the material.
3) After the atmospheric leaching reaction is finished, the atmospheric leaching slurry is conveyed to an atmospheric leaching slurry filtering device for solid-liquid separation to obtain an atmospheric leaching solution of 5m 3 And leaching residues at normal pressure. Wherein the normal pressure leaching solution is a copper and cobalt sulfate solution, the pH value is 5.0, the copper concentration is 17.95g/L, the iron concentration is 0.012g/L, the cobalt concentration is 8.10g/L, the normal pressure copper leaching rate is 62.3%, and the normal pressure cobalt leaching rate is 64.2%.
4) The normal pressure leaching slag is utilized to use sulfuric acid solution with the concentration of 50g/L for 6.5m 3 Pulping and then conveying to a pressure leaching reaction kettle; the gas pressure in the pressure oxidation leaching reaction kettle is raised and maintained at 1.4Mpa by high-pressure oxygen (purity > 90%), the initial temperature of the pressure leaching reaction is raised to 120 ℃, the pressure leaching reaction starts violent reaction, and the reaction temperature is maintained by the self-heat of the reaction until the pressure oxidation reaction is ended. After 5 hours of reaction, filtering to obtain the pressurized leaching solution and the pressurized leaching slag. Wherein the pressure leaching liquid is 5m 3 The copper concentration is 10.61g/L, the cobalt concentration is 4.29g/L, the pressurized copper leaching rate is 36.9%, and the pressurized cobalt leaching rate is 34.1%. The leaching rate of the normal-pressure and pressurized comprehensive copper is 99.2 percent, and the leaching rate of the normal-pressure and pressurized comprehensive cobalt is 98.3 percent.
Example 2
The sulphide mineral is high nickel matte containing 71% of nickel, 1% of iron and 20% of sulfur.
1) Carrying out first-stage grinding on vulcanized mineral particles 4.05t by using a Raymond mill, wherein the granularity D90 of the materials subjected to the first-stage grinding is 70 microns, and carrying out second-stage grinding by using a vibration mill, so that the granularity D90 of the materials subjected to the second-stage grinding is 30 microns; and adding 5% concentrated sulfuric acid with the weight of high nickel matte into the second section of grinding node in a pipeline conveying and spraying mode, wherein the concentration of the concentrated sulfuric acid is 1800g/L, and the adding speed of the concentrated sulfuric acid is 0.3t/h.
2) Conveying the material after secondary grinding to a solution containing sulfuric acid with the concentration of 120g/L for 24m 3 Maintaining the reaction temperature at 85℃and stirring at a stirring rate of 120r/min, and at 60Nm 3 And introducing oxygen (purity is more than 90%) at the rate of/h for normal pressure leaching reaction for 4h, so as to obtain normal pressure leaching slurry.
The device for introducing oxygen is an ultrasonic super-energy oxidizer, and the ultrasonic super-energy oxidizer is connected with an oxygen source and is communicated with the bottom of the atmospheric leaching device;
the mode of the introduced oxygen is as follows: the ultrasonic super-energy oxidizer mixes the slurry of the secondary ground material flowing out of the upper part of the normal pressure leaching device with sulfuric acid solution and introduced oxygen, and the mixture is pumped into the normal pressure leaching device from the bottom of the normal pressure leaching device so as to make the oxygen fully contact with the material.
3) After the atmospheric leaching reaction is finished, the atmospheric leaching slurry is conveyed to an atmospheric leaching slurry filtering device for solid-liquid separation to obtain an atmospheric leaching solution of 20m 3 And leaching residues at normal pressure. Wherein the normal pressure leaching liquid is nickel sulfate solution, the pH value is 5.1, the nickel concentration is 91.81g/L, the iron concentration is 0.011g/L, and the normal pressure nickel leaching rate is 64.0%.
4) The normal pressure leaching slag is utilized to be 18m of sulfuric acid solution with the concentration of 80g/L 3 Pulping and then conveying to a pressure leaching reaction kettle; the gas pressure in the pressure oxidation leaching reaction kettle is raised and maintained at 1.8Mpa by high-pressure oxygen (purity > 90%), the initial temperature of the pressure leaching reaction is raised to 140 ℃, the pressure leaching reaction starts violent reaction, and the reaction temperature is maintained by the self-heat of the reaction until the pressure oxidation reaction is ended. After the pressure leaching time is 2 hours, passingFiltering to obtain pressurized leaching liquid and pressurized leaching residue. And after the reaction is finished, filtering to obtain the pressurized leaching solution and the pressurized leaching slag. Wherein the pressure leaching liquid is 15m 3 The nickel concentration is 68.99g/L, the iron concentration is 0.007g/L, and the normal pressure nickel leaching rate is 35.4%. The leaching rate of the comprehensive nickel under normal pressure and pressure is 99.4 percent.
5) And (3) conveying the pressurized leaching solution into a impurity removal reaction kettle, maintaining the reaction pH at 1.2 and the reaction temperature at 50 ℃, adding an LIX extractant, performing copper removal purification by a 4-stage centrifugal extraction method, filtering, and performing solid-liquid separation to obtain the impurity removal leaching solution. Wherein, the organic proportion in the 4-stage centrifugal extraction method is as follows: 30%; solvent oil: 70%. The concentration of copper in the impurity-removed leaching solution is 0.01g/L.
Example 3
Sulfide minerals: copper-cobalt alloy containing 65% of copper, 2.5% of cobalt, 24.66% of iron and 3% of sulfur.
Extraction equipment: as in example 1.
The extraction step: as in example 1.
Design parameters: the addition amount of the concentrated sulfuric acid is 5 percent of the weight of the copper-cobalt alloy, the concentration of the normal pressure leaching sulfuric acid solution is 170g/L, and the addition amount is 25m 3 The atmospheric leaching time was 2h and other design parameters were the same as in example 1.
Detection result: atmospheric leachate 20m 3 Copper is 118.56g/L, cobalt is 4.54g/L, the leaching rate of copper is about 90.1% under normal pressure, and the leaching rate of cobalt is 89.8% under normal pressure.
Detecting the pressurized leach liquor 20m 3 Copper content is 12.24g/L, cobalt content is 0.47g/L, pressure copper leaching rate is 9.3%, and pressure cobalt leaching rate is 9.3%. The leaching rate of copper is 99.4% at normal pressure and pressure, and the leaching rate of cobalt is 99.1%.
Example 4
Sulfide minerals: nickel sulfide ore containing 53% of nickel, 0.5% of copper, 4% of iron and 28% of sulfur.
Extraction equipment: as in example 2.
The extraction step: as in example 2.
Design parameters: the addition amount of the concentrated sulfuric acid is 5 percent of the weight of the nickel sulfide ore, the concentration of the normal pressure leaching sulfuric acid solution is 100g/L, and the method comprises the following steps ofThe input is 21m 3 The atmospheric leaching time was 13h, and other design parameters were the same as in example 2.
Detection result: atmospheric leachate 15m 3 87.59g/L of nickel and about 61.2% of normal pressure nickel leaching rate, and 0.008g/L of iron concentration.
Pressurized leach liquor 15m 3 55.53g/L of nickel and 37.0 percent of pressurized nickel leaching rate. The leaching rate of the comprehensive nickel under normal pressure and pressure is 98.2 percent.
The concentration of copper in the impurity-removed leaching solution is detected to be 0.01g/L.
Example 5
Sulfide minerals: 31.08 percent of nickel, 35 percent of iron and 27 percent of low nickel matte containing sulfur.
Extraction equipment: as in example 2.
The extraction step: as in example 2.
Design parameters: the addition amount of the concentrated sulfuric acid is 5% of the weight of the low nickel matte, the concentration of the normal pressure leaching sulfuric acid solution is 102g/L, and the addition amount is 19m 3 The atmospheric leaching time was 2h and other design parameters were the same as in example 2.
Detection result: atmospheric leachate 15m 3 The nickel content is 52.31g/L, the leaching rate of normal pressure nickel is about 62.4%, and the iron concentration is 0.009g/L.
Pressurized leach liquor 15m 3 31.46g/L of nickel and 35.1 percent of pressurized nickel leaching rate. The leaching rate of the normal pressure and pressurized comprehensive nickel is 97.5 percent.
The concentration of copper in the impurity-removed leaching solution is detected to be 0.01g/L.
Comparative example 1
Sulfide minerals: 71% of nickel, 1% of iron and 20% of high nickel matte containing sulfur.
Extraction equipment: as in example 2.
The extraction step: the second stage of grinding was performed without adding concentrated sulfuric acid for pre-activation, and the other steps were the same as in example 2.
Design parameters: the concentration of the sulfuric acid solution leached under normal pressure was adjusted to 204g/L so that the total sulfuric acid concentration added was consistent, and other design parameters were the same as in example 2.
Detection result: atmospheric leachate 20m 3 73.48g/L of nickel and 51.1 percent of normal-pressure nickel leaching rate. Compared with example 2, the same asThe ratio was reduced by 12.9%.
Comparative example 2
Sulfide minerals: 71% of nickel, 1% of iron and 20% of high nickel matte containing sulfur.
Extraction equipment: as in example 2.
The extraction step: as in example 2.
Design parameters: the particle size of the high nickel matte after secondary grinding was satisfactory with a particle size D90 of 80 microns and other design parameters as in example 2.
Detection result: atmospheric leachate 20m 3 69.01g/L of nickel and 48.0 percent of normal-pressure nickel leaching rate. The homonymy was reduced by 16.0% compared to example 2.
Comparative example 3
Sulfide minerals: 71% of nickel, 1% of iron and 20% of high nickel matte containing sulfur.
Extraction equipment: the normal pressure leaching device is not provided with an ultrasonic super-energy oxidizer, but is a conventional mechanical stirring leaching device.
The extraction step: as in example 2.
Design parameters: as in example 2.
Detection result: atmospheric leachate 20m 3 The leaching rate of the nickel is about 43.3 percent under normal pressure, and the nickel content is 62.24 g/L. The same ratio was reduced by 20.7% as compared to example 2.
Table 1 leaching rates of target metals in examples and comparative examples
As can be seen from the description of the table 1, in the method of the present application, the grinding stage uses the concentrated sulfuric acid solution for preactivation, grinds the granularity of the sulfide minerals to D90<40 μm, and the atmospheric leaching stage uses the ultrasonic super-energy oxidizer to sufficiently scatter oxygen, so that the leaching rate of the target leaching in the atmospheric leaching stage can be effectively improved, and the comprehensive leaching rate of the target metals in the sulfide minerals can be ensured under the condition of simplifying the pressure leaching equipment. Thereby reducing the energy consumption and the cost in the extraction process and the potential safety hazard in the production process. Further, as can be seen from examples 1 to 5, the method is suitable for extracting target metals from various sulphide minerals, the leaching rate in the atmospheric leaching stage can reach more than 62%, and the comprehensive leaching rate can reach more than 97.8%.
Finally, it should be noted that the above embodiments are merely illustrative of the technical solution of the present invention, and not limiting thereof; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention.
Claims (10)
1. A method of leaching sulphide minerals, the method comprising:
s1, secondary grinding is carried out on sulfide minerals, concentrated sulfuric acid is added into the secondary grinding, and pre-activation is carried out, so that materials after secondary grinding are obtained;
s2, adding the material subjected to secondary grinding into sulfuric acid solution, and performing normal pressure leaching to obtain normal pressure leaching slurry; wherein at least one of stirring, introducing oxygen, and maintaining an atmospheric leaching temperature is performed during the atmospheric leaching;
s3, filtering the normal pressure leaching slurry to obtain normal pressure leaching slag and normal pressure leaching liquid;
s4, adding the normal pressure leaching slag into sulfuric acid solution for pulping, performing pressure leaching, and performing at least one operation of introducing oxygen, adjusting air pressure and adjusting the initial temperature of the pressure leaching in the pressure leaching process, and filtering after full reaction to obtain the pressure leaching slag and the pressure leaching liquid.
2. The method of leaching a sulphide mineral according to claim 1, wherein after S4, the method further comprises:
s5, carrying out impurity removal treatment on the pressurized leaching solution, and filtering to obtain impurity-removed leaching solution.
3. A method for leaching sulphide minerals according to claim 1 or 2,
in the step S1, the step of,
the secondary grinding is first section grinding and then second section grinding; adding concentrated sulfuric acid into the second-stage grinding to perform preactivation;
the granularity D90 of the materials after the first section of grinding is smaller than 80 microns, and the granularity D90 of the materials after the second section of grinding is smaller than 40 microns;
the concentration of sulfuric acid in the concentrated sulfuric acid in the S1 is 1400-1800g/L, and the addition amount of the concentrated sulfuric acid is 1.0-5.5% of the weight of the sulfide minerals; the adding speed of the concentrated sulfuric acid is 0.1-0.5t/h; the concentrated sulfuric acid is added in a pipeline conveying and spraying mode;
preferably, the first stage grinding is performed by a ball mill or a Raymond mill, and the second stage grinding is performed by a tube mill, a vibration mill or a mechanical stirring mill.
4. A method for leaching sulphide minerals according to claim 1 or 2,
s2, the concentration of sulfuric acid in the sulfuric acid solution is 100g/L-160g/L;
in S4, the concentration of sulfuric acid in the sulfuric acid solution is 10g/L-100g/L.
5. A method for leaching sulphide minerals according to claim 4,
in the step S2, the step of,
the device for the atmospheric leaching reaction is an atmospheric leaching device;
the oxygen gas is introduced at a rate of 10-60Nm 3 /h, and the purity of the oxygen is > 90%;
the device for introducing oxygen is an ultrasonic super-energy oxidizer, and the ultrasonic super-energy oxidizer is connected with an oxygen source and is communicated with the bottom of the atmospheric leaching device;
the mode of the introduced oxygen is as follows: the ultrasonic super-energy oxidizer mixes the secondary ground material flowing out of the upper part of the normal pressure leaching device with the slurry mixed by the sulfuric acid solution and the introduced oxygen, and then the mixed material is pumped into the normal pressure leaching device from the bottom of the normal pressure leaching device.
6. A method for leaching sulfide minerals according to claim 5,
in the step S2, the step of,
the stirring speed is 50-120r/min;
the atmospheric leaching temperature is maintained at 60-90 ℃;
the time of the atmospheric leaching is 2-13h.
7. A method for leaching sulphide minerals according to claim 1 or 2,
in S4, the processing unit is configured to,
the pulping time is 0.5-2h;
pressurizing and maintaining the air pressure at 1.4-1.8Mpa by using the oxygen, wherein the purity of the oxygen is more than 90%;
adjusting the initial temperature of the pressure leaching to 120-140 ℃;
the pressure leaching time is 2-5h.
8. A method for leaching sulphide minerals according to any one of claims 1, 2, 5 or 6,
the sulfide mineral is at least one or more of nickel sulfide mineral, copper cobalt sulfide mineral, cobalt copper alloy, high nickel matte and low nickel matte.
9. A method for leaching sulphide minerals according to claim 8,
when the sulfide mineral is at least one or more of nickel sulfide mineral, high nickel matte and low nickel matte,
s5 specifically comprises the following steps: and regulating the pH value and the temperature of the pressurized leaching solution, adding an LIX extracting agent, adopting a 4-stage centrifugal extraction method to remove copper and purify, and filtering to obtain the impurity-removed leaching solution.
10. A method for leaching sulphide minerals according to claim 9,
s5, maintaining the pH of the pressurized leaching solution at 1-2;
the temperature of the pressurized leaching solution is maintained to be less than or equal to 55 ℃;
the organic proportion of the 4-stage centrifugal extraction method is LIX extractant: solvent oil= (20% -30%): (70% -80%).
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