CN1087387A - Method and device that mineral reclaim - Google Patents
Method and device that mineral reclaim Download PDFInfo
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- CN1087387A CN1087387A CN93118331.6A CN93118331A CN1087387A CN 1087387 A CN1087387 A CN 1087387A CN 93118331 A CN93118331 A CN 93118331A CN 1087387 A CN1087387 A CN 1087387A
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- 229910052500 inorganic mineral Inorganic materials 0.000 title claims abstract description 100
- 239000011707 mineral Substances 0.000 title claims abstract description 100
- 238000000034 method Methods 0.000 title claims abstract description 58
- 238000000605 extraction Methods 0.000 claims abstract description 57
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 54
- 239000008151 electrolyte solution Substances 0.000 claims abstract description 52
- 238000004519 manufacturing process Methods 0.000 claims abstract description 36
- 239000002904 solvent Substances 0.000 claims abstract description 34
- 238000002386 leaching Methods 0.000 claims abstract description 20
- 238000000638 solvent extraction Methods 0.000 claims abstract description 15
- 238000011282 treatment Methods 0.000 claims abstract description 13
- 239000012530 fluid Substances 0.000 claims description 72
- 229910052751 metal Inorganic materials 0.000 claims description 49
- 239000002184 metal Substances 0.000 claims description 49
- 239000007788 liquid Substances 0.000 claims description 33
- 239000000463 material Substances 0.000 claims description 25
- 230000008569 process Effects 0.000 claims description 22
- 239000000284 extract Substances 0.000 claims description 9
- 150000002500 ions Chemical class 0.000 claims description 9
- 239000012528 membrane Substances 0.000 claims description 9
- 239000000243 solution Substances 0.000 claims description 9
- 238000000151 deposition Methods 0.000 claims description 8
- 230000008021 deposition Effects 0.000 claims description 8
- 239000003792 electrolyte Substances 0.000 claims description 8
- 238000005363 electrowinning Methods 0.000 claims description 8
- 230000004888 barrier function Effects 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 4
- 150000001768 cations Chemical class 0.000 claims description 3
- 238000011109 contamination Methods 0.000 claims description 3
- 208000035126 Facies Diseases 0.000 claims description 2
- 125000000129 anionic group Chemical group 0.000 claims 1
- 239000003978 infusion fluid Substances 0.000 abstract description 2
- 239000010949 copper Substances 0.000 description 35
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 33
- 229910052802 copper Inorganic materials 0.000 description 33
- 239000007789 gas Substances 0.000 description 13
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 11
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 11
- 238000005516 engineering process Methods 0.000 description 11
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 10
- 238000000926 separation method Methods 0.000 description 10
- 239000005864 Sulphur Substances 0.000 description 8
- ORTQZVOHEJQUHG-UHFFFAOYSA-L copper(II) chloride Chemical compound Cl[Cu]Cl ORTQZVOHEJQUHG-UHFFFAOYSA-L 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 6
- 229910000365 copper sulfate Inorganic materials 0.000 description 6
- ARUVKPQLZAKDPS-UHFFFAOYSA-L copper(II) sulfate Chemical compound [Cu+2].[O-][S+2]([O-])([O-])[O-] ARUVKPQLZAKDPS-UHFFFAOYSA-L 0.000 description 6
- 229910052742 iron Inorganic materials 0.000 description 6
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- 150000002739 metals Chemical class 0.000 description 6
- 238000013022 venting Methods 0.000 description 6
- 238000003723 Smelting Methods 0.000 description 5
- 238000009924 canning Methods 0.000 description 5
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 4
- 239000000460 chlorine Substances 0.000 description 4
- 229910052801 chlorine Inorganic materials 0.000 description 4
- 229960003280 cupric chloride Drugs 0.000 description 4
- 238000001914 filtration Methods 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- 239000003082 abrasive agent Substances 0.000 description 3
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- 239000007864 aqueous solution Substances 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000004020 conductor Substances 0.000 description 3
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- 150000001457 metallic cations Chemical class 0.000 description 3
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- 238000011084 recovery Methods 0.000 description 3
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- 241000370738 Chlorion Species 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
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- 230000008859 change Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
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- 230000007246 mechanism Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 229910052759 nickel Inorganic materials 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 238000002161 passivation Methods 0.000 description 2
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- 229920003023 plastic Polymers 0.000 description 2
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- 239000000047 product Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000002893 slag Substances 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 238000004381 surface treatment Methods 0.000 description 2
- 238000000108 ultra-filtration Methods 0.000 description 2
- 229910021591 Copper(I) chloride Inorganic materials 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 229910001245 Sb alloy Inorganic materials 0.000 description 1
- 241001417490 Sillaginidae Species 0.000 description 1
- FKNQFGJONOIPTF-UHFFFAOYSA-N Sodium cation Chemical compound [Na+] FKNQFGJONOIPTF-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 241001062472 Stokellia anisodon Species 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 239000002140 antimony alloy Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
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- 239000006227 byproduct Substances 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000010406 cathode material Substances 0.000 description 1
- 238000010349 cathodic reaction Methods 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 150000003841 chloride salts Chemical class 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- OXBLHERUFWYNTN-UHFFFAOYSA-M copper(I) chloride Chemical compound [Cu]Cl OXBLHERUFWYNTN-UHFFFAOYSA-M 0.000 description 1
- OMZSGWSJDCOLKM-UHFFFAOYSA-N copper(II) sulfide Chemical compound [S-2].[Cu+2] OMZSGWSJDCOLKM-UHFFFAOYSA-N 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 229940045803 cuprous chloride Drugs 0.000 description 1
- 125000004093 cyano group Chemical group *C#N 0.000 description 1
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- 238000010790 dilution Methods 0.000 description 1
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- 238000004090 dissolution Methods 0.000 description 1
- 239000002659 electrodeposit Substances 0.000 description 1
- 238000004070 electrodeposition Methods 0.000 description 1
- 238000000909 electrodialysis Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- NMCUIPGRVMDVDB-UHFFFAOYSA-L iron dichloride Chemical compound Cl[Fe]Cl NMCUIPGRVMDVDB-UHFFFAOYSA-L 0.000 description 1
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000002923 metal particle Substances 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- LVIYYTJTOKJJOC-UHFFFAOYSA-N nickel phthalocyanine Chemical compound [Ni+2].C12=CC=CC=C2C(N=C2[N-]C(C3=CC=CC=C32)=N2)=NC1=NC([C]1C=CC=CC1=1)=NC=1N=C1[C]3C=CC=CC3=C2[N-]1 LVIYYTJTOKJJOC-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229960001866 silicon dioxide Drugs 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000011882 ultra-fine particle Substances 0.000 description 1
- 239000010913 used oil Substances 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C1/00—Electrolytic production, recovery or refining of metals by electrolysis of solutions
- C25C1/12—Electrolytic production, recovery or refining of metals by electrolysis of solutions of copper
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C5/00—Electrolytic production, recovery or refining of metal powders or porous metal masses
- C25C5/02—Electrolytic production, recovery or refining of metal powders or porous metal masses from solutions
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C7/00—Constructional parts, or assemblies thereof, of cells; Servicing or operating of cells
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Electrolytic Production Of Metals (AREA)
Abstract
Disclose the method for electrolysis for production mineral, comprised, soluble mineral is leached by leaching and solvent extraction circuit processing infusion solution; By extraction and back extraction circular treatment solvent the mineral of selecting leaching are come together in the solvent; By back extraction and mineral extraction tank circular treatment electrolytic solution, use and select soluble mineral to go into the electrolytic solution from the solvent back extraction, switch on to extraction tank, wherein extraction tank comprises the elongate housing with electrically conductive inner surface, the tightness system at shell two ends penetrates the electrode of shell, stream socket, and the electric terminals of electric current between continuous electrode and conductive surface, the soluble mineral galvanic deposit that makes selection is on conductive surface.
Description
The present invention relates to method and device that a kind of mineral reclaim.
The present invention's special (but not being uniquely) is applicable to the electrolysis for production and/or the electrorefining of copper.However, it should be understood that the present invention can also be used for other field, for example preparation of the electrolysis for production of other metal or refining or gas.
A lot of methods of extracting metal from ore still have a small amount of in the ore after extracting but constitute a certain proportion of metal.Other method can not be used for low grade ore in less expensive ground.A kind of definite method of extracting remaining metal or extract metal from the ore of handling from low grade ore is exactly well-known lixiviation process.Lixiviation process is by a kind of fluid, and leach liquor is collected in the i.e. stripping from ore of metal to be extracted, and this metal is separated from leach liquor.The leaching method is extracted copper, and leach liquor commonly used is a dilute sulphuric acid, and it and copper reaction generate copper sulfate.
But the vitriol leach liquor is not suitable for many metals, perhaps to usually by some physical aspect and/or the mineral form and inapplicable of the metal of vitriol leach liquor leaching.Thereby the dissolving of these class mineral realizes by adopting chlorination, iron(ic) chloride or cupric chloride leaching or hydrochloric acid leaching to form chloride salt usually.Chloride system still is in the initial stage developmental stage and only obtains limited commercial applications, and this is not only because of technical difficulty with by height and corrodes and/or the caused construction costs of high reducing atmosphere, goes back the difficulty because of electrolysis for production aspect from chloride soln.Therefore, vitriol leaching system becomes striving direction always.
For vitriol leaching liquid system, allow copper sulfate contact with metallic iron or steel, generate ferric sulfate and metallic copper, copper can be from by separating in the copper sulfate of discharging the ore.Regrettably, the copper of producing like this contains significant impurity component, and sour completely consumed used in this flow process is fallen, and this just makes that the economy of this technology is relatively poor.
On the other hand, the electrolyzer of copper-bath can being flowed through reclaims copper and sulfuric acid simultaneously.Yet the conventional electrolysis groove can not be used for direct extracting metals from the lower concentration leach liquor that the ore of exploitation obtains economically, needs further enrichment before the leach liquor electrolysis.
The existing method of further enriched in metals from solution comprises two solvent extraction, and in a first step, the metal part extracts from leaching liquid and enters and the not miscible solvent of leaching liquid; Second step, again the extraction from solvent of this metal part is entered with the not miscible electrolytic solution of this solvent in.Leach liquor, solvent and electrolytic solution can be recycled.
Leach circulation and comprise a leaching stage, in this stage, metal dissolves from ore and enters in the leach liquor; With a solvent extraction stage, in this stage, with desire metal to be refined from leach liquor come together according to qualifications (being generally organic solvent) in a kind of solvent.Solvent extraction circuit comprises extraction and two stages of back extraction, and in extraction stages, metal extracts from leach liquor and enters solvent; In second stage, metal is stripped from solvent and is entered in the electrolytic solution.Electrolytic solution and leaching agent all are the aqueous solution usually.
Electrolytic solution can recycle in a recycle system.This recycle system comprises solvent stripping stage (metal is stripped and entered electrolytic solution) and electrolysis stage from solvent, in electrolysis stage, feed electric current in electrolytic solution, thereby metal is separated with electrolytic solution.
In this flow process, must strictly control each round-robin behavior in above-mentioned three recycle systems.Especially only allow to exist the organic solvent of minute quantity in the electrolytic solution, surpass the consequence allow to limit the quantity of and be, the electrolysis for production process poor efficiency and/or impossible that becomes.Therefore need a filtration unit to remove the solvent of unnecessary amount from electrolytic solution, this has increased the complicacy and the cost of this technology again.
In electrolyte circulation system, for the concentration of metal in electrolytic solution is maintained on the certain level, allow feed back in the electric smelting process through the electrolytic solution short cut that electrolysis for production is crossed, this is the common practice.When from solvent, obtaining metal, need from electrolytic solution, remove all solvents substantially with a filtration unit in the reextraction stage.Electrolytic solution also need be emptied completely, filling again after also need being emptied completely by fresh electrolyte and the occupied whole spaces of leaching fluid, and this is owing to foreign metal concentration in the electrolytic process constantly increases, as the existence of iron in electrolytic copper.The complicacy of these and other this class increases running cost in this system, and the design and installation cost of an electrolysis for production factory is increased.
Usually make the electrolysis for production groove that contains electrolytic solution keep laminar flow regime fully, so that restriction adds the size of the current density on all electrolytic tank electrodes.A reason of doing like this is exactly to make that the metal of galvanic deposit does not come off from electrode.In addition, because the susceptibility of the present electrolysis for production groove that uses, the concentration of electrolytic solution and flow velocity must maintain in the narrow range.In the high place of chloride amount, the corrosion of water pipeline also may be a problem.
In general, owing to the use of electrorefining technology is developed the technology of electrolysis for production metal from ore, in this technology, metal through comprising fusion and two steps of electrolysis for production extractive process and be refined into high pure metal.Since the electrorefining process be from the electrolysis for production process produce metal in the distinct raw material of employed character.So from ore, during the electrolysis for production metal, need make overall plans and pay attention to adopting electrorefining technology.
The electrolysis for production method of metal has directly applied to the matte phase in the production of nickel particularly.But this technology is applied to during copper smelts always with failing, mainly be since on the electrode surface due to the influence of sedimentary free sulfur.This or cause being coated with the electrode passivation of sulphur, or owing to selective copper ground never passive area remove and make the anode completely destroy.
The present invention is intended to alleviate one or more above-mentioned defectives and use mineral extraction element reliably and efficiently is provided.
Based on above-mentioned viewpoint, an aspect of of the present present invention mainly is the method by following technology certain mineral of electrolysis for production from ore:
By leaching and solvent extraction plant circular treatment one infusion solution, wherein, soluble mineral leaches from ore body, dissolves in leach liquor;
By solvent extraction plant and reextraction device circular treatment solvent, thereby selectivity is dissolved in soluble mineral in the leach liquor and is extracted from leach liquor and enter this solvent;
By reextraction and a mineral extraction tank circular treatment electrolytic solution, thereby selected soluble mineral is stripped from solvent enters electrolytic solution, and
In mineral extraction tank device, feed electric current, and wherein said mineral extraction tank device comprises:
The fixed case extension that internal surface can conduct electricity;
Be installed in the tightness system on each end of shell movably;
Insert the electrode that stretches out shell and the tightness system from least one end, so that between electrode and shell, form the ring-type cave;
Be arranged in the fluid intake that a tightness system leads to the ring-type cave, the fluid that forms when using like this can depart from the long axis direction of stationary, enters the mineral extraction tank by this inlet,
The fluid outlet of the slot device that in another tightness system, constitutes and
The electric terminals of electric current between connection electrode and conductive surface makes selected soluble mineral galvanic deposit on conductive surface.
Preferably, this extraction tank device can such as among our unsettled jointly " the international patent application NO.PCT/AU92/00052 " announcement, perhaps it can comprise tripping device, this tripping device is divided into an electrolysis liquid pool (realizing that by its fluid intake and outlet fluid contacts) and a treat fluid pond with the ring-type cave, the inlet that leads to the treat fluid pond, the outlet of leading to the treat fluid pond, and treated entrance and exit circular treatment fluidic method.
In order not influence the deposition of mineral at conductive surface, electrolytic solution should be with the relative stationary stream mode mineral extraction tank of flowing through, yet, preferably electrolytic solution is circulated in shell, feeding electrolytic solution between fluid intake and fluid outlet in the mineral extraction tank, thereby electrolytic solution is closely contacted with conductive surface.Adapt therewith, closely contact at conductive surface in order to strengthen electrolytic solution, electrode need carry out surface treatment, and/or improves or guide needed fluid-flow mode.Fluid can be laminar flow regime, but turbulence state preferably, and no matter whether turbulent flow produces, sets up or fully, the galvanic deposit mineral all are present in the electrolytic solution with suspension.
Conductive surface can be with the different material of sedimentary mineral, galvanic deposit mineral are from the teeth outwards removed regularly.This process can be changed a new shell and realizes by removing shell.Yet the conductive surface material is preferably same with a sedimentary mineral facies, can save like this from conductive surface the sedimentary mineral of institute are peeled off this step.In addition, use out of phase fluid to help to alleviate the contamination of tripping device.
Remain the zone of suspension at the galvanic deposit mineral, collect with particle collection device, in addition, can open the electrolysis liquid pool, shift out conductive surface to the galvanic deposit mineral that small part is deposited on the electrode.
Preferably this electrode is used as anode, conductive surface is made negative electrode, thereby the logical electric current mineral of going up are promptly by the galvanic deposit of conductor institute.
On the other hand, the present invention mainly comprises the mineral extraction tank device that extracts mineral from the fluent solution that contains mineral, and this extraction tank device comprises:
Fixed extension housing with electrically conductive inner surface;
Be installed in the tightness system at stationary two ends movably;
Insert the electrode that stretches out shell and the tightness system from least one end, so that between shell and electrode, form the ring-type cave;
Be positioned at the fluid intake that leads to the ring-type cave on the tightness system, the fluid that forms when using like this departs from the long axis direction of stationary, enters the mineral extraction tank by this inlet,
The fluid outlet that leads to extraction tank that on another tightness system, forms,
Tripping device, it is divided into an electrolysis liquid pool (realizing that by its fluid intake and outlet fluid contacts) and a treat fluid pond with the ring-type cave;
The inlet that leads to the treat fluid pond;
The outlet of leading to the treat fluid pond, wherein, present method comprise by the inlet in treat fluid pond and the outlet convection cell carry out circular treatment and
The circuit terminal of electric current between connection electrode and conductive surface is so that the mineral galvanic deposit is on conductive surface.Adopt suitable separation means (as ion-selective membrane) to allow selected material pass through.Can also cooperate the ion back-and-forth method to use together with other separation means when needing, as means such as dialysis, ultrafiltration, micro-filtrations.Adapt with it, for example for electrolysis for production one positively charged ion (as metal), tripping device promptly is a cation selective membrane, and the positively charged ion mineral are smelted in corresponding negatively charged ion electrolysis from solution.
In a preferred embodiment, tripping device can be collected the electrolysis for production mineral near cathode compartment, and is that two ends are by tightness system supported tubular film.
This extension housing preferably is installed between two end walls and electrode also is placed in the shell between end wall.Electrode can be arbitrary shape, but preferably has a kind of like this shape or configuration, comprises such as becoming projection or rib-loop shape with the surface treatment of the tight contact that is increased in conductive surface and/or promote fluidic proper flow flowing mode.Electrode also be preferably used as anode and conductive surface as negative electrode, be deposited on the conductive surface with the mineral material that electrolytic solution produced that the anode of this electrolyzer contacts with negative electrode like this.Yet, also can make mineral deposition on electrode as negative electrode at this electrode.
The applicant believes that turbulent flow and the combination of non-stationary stream flow pattern make electrolytic solution closely contact with conductive surface in the electrolytic solution, thereby makes the current density that is added on the conductive surface can increase to the current density that is higher than on the conventional electrolysis pond.In addition, in the further preferred embodiment, be used for keeping the electrolysis for production material in conjunction with the turbulent flow mode in the electrolytic solution and in electrolytic solution, be suspension, to reclaim raw mineral materials by means such as filtration, sedimentation, heart separation, the isolating chemical treatments of spinning liquid or with the arbitrary combination of these means.Chemical treatment can comprise the impurity that optionally dissolves again such as sulphur, unwanted metal etc.
Should note, by the operational condition (these operational conditions comprise rate of flow of fluid and cathode current density) that electrolyzer is set in requiring limit, can adopt this electrolytic tank electrolysis to smelt mineral in granular form, so that to small part electrolysis for production mineral be not to be deposited on the negative electrode, but bring into by electrolyzer with fluid, therefore can collect at bleeding point easily away from the shell cylindrical portion.Electrolyzer is loaded onto the metallic particles collection device, can particulate state collect from electrolyzer to small part electrolysis for production material like this, influences the electrolysis for production process less as far as possible.
This particle collection device can additionally or alternately insert between the electrolyzer of serial connection, or is assembled on the gas separation unit.This particle collection device can comprise gravitational effect and centrifugal effect are used for isolating tripping device and collecting chamber or funnel.The latter can be joined with a collected outside zone selectively by the external valve device, adopt other valve system that collecting chamber itself is optionally isolated with electrolyzer, so that allow granular material enter collecting chamber (this moment, external valve was closed) by open other valve, shut other valve then, open the external valve device, can extract granular material like this.
In another embodiment, this collection device is with below being positioned at electrolyzer or pod at a collecting region) and discharge region (away from this electrolyzer or pod) between free active collecting chamber, a plurality of collecting chambers suitably are provided, and rotate the storehouse around one and lay, the latter need be rotatable so that can move these collecting chambers between collecting region and discharge region.
No matter be that electrolytic solution closely contacts with conductive surface and removed to small part electrolysis for production material, or nearly all electrolysis for production material still rests on the conductive surface, the material of conductive surface all should select its surface properties with the electrolysis for production mineralogical property to a certain degree different materials to be arranged, and one deck mineral material that gathers at this conductive surface can be removed from this easily like this.Separated mineral material can be a thin-walled tubulose, when it with after conducting material separates, the same layer mineral that itself can be used as one " trigger mechanism " to be formed after handling.For example, when electrolysis for production copper, available stainless steel tube is produced a large amount of copper that is used for other electrolyzer " trigger mechanism " pipes from less relatively electrolyzer.
This shell preferably includes the elongated cylinder part that forms with electro-conductive material so that conductive surface becomes one with it.The cathode material especially material of conductive surface can be selected mineral identical materials with required galvanic deposit.During for example electric copper metallurgy, cylindrical portions may can be a thin-wall copper pipe shape, and a thick-layer copper film can be deposited on the copper pipe inwall, replaces this cylindrical portions may with a new copper pipe then, can save like this from pipe and peel off institute's this operation of sedimentary material.
Stream socket can place any direction with respect to shell such as the direction parallel with the shell major axis.Yet, fluid intake preferably is positioned at adjacent housings first end, make it vertical with the axle of case extension, and/or and the ring-type cave that between shell and electrode, forms tangent, so that the liquid eddy flow is entered in the annular cave, we think that this cyclone mode can promote the uniform deposition of electric smelting material.Suitably, fluid outlet should adopt with enter the mouth similar configuration and needing away from the ingress, so that further strengthen the eddy flow of liquid of fluid.
Fluid intake can be connected with the fluid outlet of second mineral extraction tank, like this fluid can Continuous Flow through two grooves, thereby realize from this fluid, extracting continuously mineral.A plurality of extraction tanks are connected in series form an extraction tank group, can in continuing for some time, from volume of fluid, carry out mineral like this and extract, thereby the considerable part of total starting point concentration of required mineral is extracted out.
When leaching process produces gaseous by-product, can between extraction tank, insert gas separation unit, the gas that in the said extracted groove, produces like this, before entering the downstream extraction groove, available differential density technology or similar techniques are removed from liquid.Can be randomly or additionally load onto ventilating pit in the upper end of extraction tank, like this before liquid enters the downstream extraction groove, and the i.e. emptying from extraction tank of the gas that is produced.The liquid exit top is adorned a gas delivery cabin and can be strengthened gas separation effect.Suitably, in order to obtain needed separating effect, the pod diameter should approximately equate with ring-type cave outside dimension, and its minimum altitude equals this diameter half.
One embodiment of the invention comprise the ion-selective membrane that can select anolyte and catholyte.Especially from chloride soln during the electrolysis for production metal, a suitable available cation selective membrane.With this film the electrolysis for production groove is divided into two chambers, anodic reaction and impregnable the carrying out of cathodic reaction energy only are that selected material can pass through this film.The effect of film is can open path to cathode compartment to collect the metal that plates.Film stops the chlorine that forms at anode to enter the cathodic area of electrolyzer; The selection class shape of film also makes sodium ion can see through this film, to form complete circuit and to keep stoichiometry.Only remove chlorine from the anolyte compartment.
The exhausted catholyte can use to keep the chlorion balance as anolyte to the circulating anode chamber from cathode compartment, and it can directly re-use in leaching operation, or is made into leach liquor again.Can become leach liquor by respectively cuprous chloride and/or iron protochloride being reoxidized the way reprovision that becomes cupric chloride and iron(ic) chloride and form hydrochloric acid.
On the other hand, the present invention mainly comprises a mineral extraction tank device, and this device comprises:
Extended pattern shell (this conductive surface is positioned at the axial medial surface of cylinder) with conductive surface;
Electrode with this conductive surface insulation and insertion shell;
The fluid intake that leads to shell;
Draw and away from the fluid outlet of fluid intake from shell;
The electric terminals of electric current between connection electrode and conductive surface, and the disrupter between insertion electrode and the conductive surface.This disrupter can be sheet or similar other shape, but barrier film preferably.In another preferred embodiment, this barrier film is an ion-exchange membrane, and the fluid that flows into electrolyzer has at least part closely to contact with conductive surface.The combination of also available other membrane separation technique or these membrane separation techniques is as dialysis, ultrafiltration electrodialysis etc.
This mineral extraction tank is preferably in ionogen and does not use with one or more barrier films in the solution.But this barrier film tubular film, its bottom is supported on the end cap of electrolyzer.Barrier film preferably separates anode 2 or 3mm.The use of flow pattern (comprising out of phase use) and/or membrane sepn means helps to alleviate membranous contamination degree.
In another embodiment of the present invention, when in alkaline aqueous solution, during from precious metal cyano complex electrowinning precious metal, adopting chlorion electrolytic solution in the mineral extraction tank.
In the another embodiment of the present invention, mineral extraction tank of the present invention has alleviated the deposition of sulphur on electrode, and therefore available this extraction tank is from the direct mutually extracting metals of matte.In addition, can adopt the allotropic substance of this systems produce crystal sulphur or other sulphur that needs, and/or in this circulation process, add a kind of abrasive material, with the flow effect of enhance fluid in extraction tank.The mineral that shift out from this system can be a kind of Powdered or sheets, adopt filtration or other separating step can remove desulfuration, and abrasive material still keeps wherein and recycles.
On the other hand, the present invention relates generally to the method for a kind of mineral of electrowinning, comprising:
The mineral extraction element is provided, this device comprises the elongated shape shell (this surface is positioned at the inner peripheral of shell) with a conductive surface, be placed in the slender electrode in this shell, feed the fluid intake of shell, the fluid outlet away from fluid intake of drawing from shell is with a pair of electric terminals that is used for telegraph circuit is connected with the conductive surface circuit;
Power supply between conductive surface and the electrode is connected;
Feed the fluid that contains this mineral dissolution salt by the shell between fluid intake and outlet.
Present method further comprises, increases by one and leach operation in the electrowinning operation, and fluid contains the ore suitable in small, broken bits for the treatment of extracting metals, and two processes of dissolving metal and electric smelting can be carried out simultaneously like this, and need not leachings and electric the refining are divided into two and go on foot and carry out.For example, during electrolysis for production copper, with ore input dilution heat of sulfuric acid in small, broken bits, this solution is by an electrolyzer or electrolyzer group from copper mine.In the copper vitriolization, there promptly from solution by electrolytic deposition, with free metal form precipitation, sulfuric acid is preferably regenerated in this course.Undissolved slag can be removed from liquid in separating step, and separation can be adopted sedimentation, filters centrifugation or other similar means.
As previously mentioned, further enrichment process generally includes two solvent extraction.In first solvent extraction, metallic cation be adsorbed enter with the not miscible substantially liquid solvent of leach liquor in; Second step, metallic cation from solvent, strip enter with the not miscible substantially a kind of electrolytic solution of this solvent in.Leach liquor and electrolytic solution is the aqueous solution preferably, and solvent non-water-soluble liquid preferably.The electrolysis for production stage of the present invention is preferably used in electrowinning metal from electrolytic solution.
In order more easily to understand the present invention and to make the present invention bring into play actual effect, see also accompanying drawing, these accompanying drawings have specifically at length been explained the preferred embodiments of the invention.Wherein:
Fig. 1 is with solvent-extracted electrowinning flow process diagram;
Fig. 2 is to use the cross sectional side view of the employed electrolyzer of method of the present invention;
Fig. 3 is the profile view of electrolyzer shown in Figure 2;
Fig. 4 is the cross sectional side view of electrolyzer in another embodiment of the present invention;
Fig. 5 is a tripping device cross sectional side view of the present invention;
Fig. 6 is to use the electrowinning groove diagram of a separating diaphragm;
Fig. 7 is the metal smelting method diagram that comprises from matte phase electrolysis for production.
Referring to Fig. 1, mineral recovery method (35) comprises three circulation loops that are used for leaching from ore body (18) mineral.This mineral recovery method (35) comprises that one leaches circulation (36), a solvent extraction circuit (37) and electrolysis cycle (38).Treat from ore body (18) mineral that extract when electrolysis cycle (38) from electrolytic bath (10) by electrolysis.
Around leaching circulation loop (36) circulation, mineral are full of in the leach liquor leach liquor whereby by ore body.For example when copper metallurgy, be full of in the leach liquor of mineral and contain the copper of 3g/l level and the sulfuric acid of 5g/l level.Leach liquor flows through adsorption step (58) then, and at this moment these mineral promptly are extracted from leach liquor and enter a solvent, and this solvent is by solvent extraction circuit loop (37) circulation.Its concentration of leach liquor of coming out from adsorption step (58) is reduced to mineral concentration usually, copper for example, and its concentration is reduced to 0.3g/l.Consider the reduction of leach liquor intensity, adopt a leach liquor compensation system (59), to keep acid concentration on 15g/l level vitriolic level.
Solvent extraction circuits (37) comprises an adsorption step (58) and a desorption procedure (57).In adsorption step (58), solvent contacts with leach liquor and mineral are adsorbed from leach liquor and enter around in the round-robin solvent of solvent extraction circuit loop (37).In desorption procedure (57), solvent with contact around electrolysis cycle loop (38) round-robin electrolytic solution.
Mineral extract from solvent and enter electrolytic solution and reach higher concentration, and for example the concentration by desorption procedure (57) back copper can reach 50g/l, and circulation fluid circulates to remove any solvent and/or other unwanted material by a strainer (56).This electrolyte stream is through an electrolyzer (10) then, is extracted out to the small part mineral in electrolyzer, thereby produced the old electrolytic solution of a certain concentration, for example contains 35g/l copper and 180g/l vitriolic electrolytic solution.
In the typically used of using the copper sulfate system, in electrolytic bath (10), copper sulfate is soluble in water, and a water molecules is participated in electrolytic reaction by following equation:
Cu
2++SO
2-
4+H
2O→H
2SO
4+1/2O
2+Cu
o
Metallic copper is deposited on the negative electrode generating half oxygen molecule on the anode like this.On negative electrode, water is pressed following formula generation ionization:
H
2O→H
++OH
-
Perhaps, also can use a standard cupric chloride system, like this in the copper deposition on the negative electrode and main be to discharge chlorine on the anode.During with the cupric chloride system, the oxidation state that electrodeposition process also can adopt cuprous salt or mantoquita is to provide a stoicheiometry easily.
Usually an electrolytic solution arm (39) is connected on the electrolysis cycle loop (38), a part that comes from the spent solvent of electrolyzer (10) like this can be at strainer (56) afterwards, and electrolyzer (10) returns in the electrolysis cycle loop (38) before again.
The author believes that applying the present invention to mineral recovery process (35) (Fig. 1 has done sufficient description) can also simplify, and for example, strainer (56) and/or electrolytic solution arm (39) can save.The author thinks, the present invention is used for the described flow process of Fig. 1, and conditional request is not really harsh.The mineral concentration for the treatment of galvanic deposit from electrolysis cycle loop (38) is approaching as far as possible to be had in the desired concentration range of technology earlier although keep; The author believes, uses the present invention to reduce or eliminate the loss of solvent in the electrolyzer, does not therefore need to filter dense electrolytic solution.
Fig. 2 and electrolyzer (10) shown in Figure 3 comprise the canning (11) that is made of a metal tube (12), settle a upper end block (13) and a lower end cover cap (14) with the sealing-ring sealing on the outer side of metal tube.Canning (11) is fixed together with tie-bolt (16), and tie-bolt is fixed on the edge of pipe cap (13,14) formation.
Seal cartridge (20) is centrally placed in the pipe cap (13,14), and a cylindrical electrode (21) therefrom passes.If necessary, can be only with a seal cartridge, the other end of electrode (21) is received on the axle sleeve or is received from the inner socket connected in star that protrudes of an end cap cap, hollow edged electrode (21) is received on axle sleeve or the groove with the tightness system sealing, otherwise or, it is blocked to reduce the loss of feeding electrode (21) fluidic.Form a liquid exit (22) in upper end block (13), lower end block (14) locates to form a liquid inlet (23).This outlet (22) and this inlet (23) axially with canning (11) spool should be vertical and and canning (11) and electrode (21) between formed ring-type cave (24) tangent.The upwards flowing fluid that makes inlet (23) be positioned at lower end block (14) and introduce can be flushed in the gas that (21) are produced on the electrode, gas is moved on the venting hole (32) that is positioned on the upper end block (13), this air-flow plays air pump, can quicken liquid-flow, reduce needs external pump.Certainly, in case of necessity, also inlet (23) can be driveed at upper end block (13), outlet (22) is positioned at lower end block (14), and liquid flows from top to bottom like this.
Zone between inlet (22) and cylindrical duct (12) lower end, the internal diameter of lower end block (14) should cooperate with the internal diameter of cylindrical duct (12) closely, can form a level and smooth relatively drum surface infeeds liquid with enhancing eddy flow like this.The diameter of upper end block (13) and cylindrical duct (12) also should mate, with the steady eddy flow effect of further enhance fluid in annular cave (24).
Each pipe end-cap (13,14) all is to be combined by PVC plastics tubing parts, comprises a flange coupling connector (25), one section pipe fitting (26), a pipe cap (27), pullover (30) of compression and the less pipe (31) of another section internal diameter are with all these parts welding or bond together.Certainly, if necessary, pipe cap also can adopt the die casting of plastic mold casting process to make integral body.If desired, can adorn a float valve or similar parts on the venting hole (32), in gas accumulated in upper end block (13), float valve can be opened; After gas was discharged, float valve can cut out.
In the time need from the liquid that contains sulfuric acid and copper sulfate, refining electrolytic copper, this metallic cylinder (12) is an available copper pipe, pipe electrode (21) usable surface is coated with the metal titanium of metal oxide containing precious metals and makes (being famous dimensional stable anode), or other is insoluble to material (as the lead-antimony alloy) preparation of acid and not passivation under operational condition.On the other hand, the also available inert material of round metal bobbin (12) (as stainless steel) is made, and the material of galvanic deposit can easily be removed above it like this.
During use, a direct current power supply is received (10) on the electrolyzer, the positive pole of power supply is received on the pipe electrode (21), and this moment, pipe electrode became anode; Negative pole is received round metal bobbin (12), this moment metallic cylinder (12) negative electrode, for the ease of installation and removal (especially removing and change canning (12)), the most handy wire connection clamp connects.When electric current circulated between electrode (21) and cylindrical duct (12), during copper promptly deposits on the cylindrical duct (12), and the oxygen that solution discharged in this process fed in the atmosphere via venting hole (32).When the copper on being deposited on cylindrical duct (12) inwall reaches required thickness, just can take out as smart copper and sell, or, change a new cylinder again as bus-bar.
If necessary, can form row's electrolyzer (10), liquid pumps into one group of placed in-line electrolyzer, and the concentration of copper descends one by one in the liquid like this.Certainly, one group of electrolyzer is arranged with the flow configuration of required serial or parallel connection, to optimize the flow condition of liquid in electrolyzer.Similarly, also can be arranged to series, parallel or series connection/parallel way arbitrarily, so that the current/voltage of electrolyzer and power supply coupling to the electrolyzer with electricity mode.
Electrolyzer shown in Figure 4 (40) and Fig. 2, cell construction shown in Figure 3 are similar, but on upper end block (41), between fluid outlet (43) top and venting hole (44), reserve a vertical gap greater than cylindrical duct (42) internal diameter 1/2, like this, the gas that upwards carries in the mobile fluid along cylindrical duct (42), fluid flow out electrolyzer (40) before can with fluid separation.Lower end block (45) is also reserved a vertical gap greater than cylindrical duct (42) internal diameter 1/2, and this gap is positioned between fluid intake (46) bottom and lower end block (45) bottom.Anode (50) terminates at liquid inlet (46) top, but its drum extends beyond liquid inlet (46) downwards with the form of the non-conductive anode assembly (51) that is connected in substrate (47), so can remarkably influenced ingress fluidic flow pattern.When these characteristics have guaranteed that the metal particle of uniform deposition deposits to electrolyzer (40) bottom, neither hinder fluid to flow into inlet (46), can between anode (50) and cylindrical duct, not cause short circuit again.
Ring joint between the bottom of lower end pipe cap (45) and cylindrical duct (42) at least also should be positioned at inlet (46) top upwards apart from being cylindrical duct (42) internal diameter 1/2 part, can alleviate like this under turbulent-flow conditions near the erosion of ingress to cylindrical duct (42) end.Ring joint between upper end pipe cap (41) and cylindrical duct (42) top also should be done similar arrangement, thereby strengthens the stationarity that spiral goes out stream, alleviates the erosion on cylindrical duct (42) top.
Tripping device shown in Figure 5 (60) is used for being recovered in electrolyzer (10) and forms but do not deposit to mineral grain on the negative electrode, for reaching this purpose, this device comprises the tubular separate chamber of a vertical (61), this top, separate chamber be sealing and be divided into two portions by a vertical clapboard (62), this dividing plate separates inlet tube (63) and outlet pipe (64).Venting hole (65) is positioned at (can have float valve in case of necessity) top of separate chamber (61).Separate chamber bottom shortens taper shape gradually into and is terminated at a upper valve (66), and valve (66) lower surface connects a tubular collecting chamber (67) again, collecting chamber (67) bottom again with a lower valve (70) termination.
During use, the liquid and the metallic particles that have bubble can enter tripping device (60) through inlet pipe (63) from the liquid exit (22) of electrolyzer (10), the volume of separate chamber (61) should be electrolyzer (a 10) volumetrical manyfold, and liquid can have the relatively long residence time in separate chamber (61) like this.Dividing plate (62) has prevented that liquid stream from directly flowing to outlet (64) short cut from inlet (63).Go up emersion in the gas from liquid (71) and discharge, and metallic particles falls into collecting chamber (67) by mother liquor (71) and the last valve (66) opened, and rest on the lower valve (70) of closing through venting hole (65).
When the metallic particles that needs balling-up to get up, will go up valve (66) and close, in operating process, allow the liquid flow of pressurization continue to circulate, open lower valve (70) simultaneously with the discharging metallic particles.In case of necessity, can settle sensing electrode at interval, and monitor with sensoring (as ohmer) when metallic particles reaches the needed scope of collecting along collecting chamber (67) side.
From the above, the invention provides as can be seen simplification usually with matching used oil tank factory of common electrolysis smelting device institute, about the layout of pipework and equipment etc. and/or the benefit of operation.In addition, also may save the needs that reclaim the heat exchanger of heat energy in the circulation of elecrolyte loop, this is because compare not really important with the conventional electrolysis groove by the electrolyte temperature of this electrolyzer.
Because the electrolyzer among the present invention is not really harsh to the requirement of ore grade and flow pattern, therefore can loosen the requirement of solvent extraction control, and the concentration of electrolytic solution also can be different and can not reduce extraction efficiency.The author thinks that also available chip mixing subsider is made the ultrafine particle powder retrieving arrangement.From the above, as can be seen, adopt the present invention, there is not water piping (this can cause erosion) in the electrolyzer, product of the present invention and technology are not very sensitive to the aggressiveness impurity such as chlorine.In addition, the author believes, this recycle system is lost the speed ratio conventional system to flowing molten iron and required lowly, and this just makes that the composition of acid is less in the electrolytic solution, and can use the lower and/or cheap extraction agent of selectivity.
Referring to Fig. 6, one comprises the method for electrolysis for production groove (28), and this groove has an anode (19), a negative electrode (29) and a circulation loop (33).Abrasive material and/or sulphur crystal catalyst are injected into this circulation loop through inlet (34).Add positive voltage at positive terminal (48), cathode terminal (49) adds negative voltage so that metallic cation becomes the free metal along migration of direction shown in the arrow (52) and galvanic deposit on negative electrode (29).The electrolyte flow mode that can regulate by electrolyzer (28) makes the free metal break away from negative electrode (29), and removes from the electrolysis flow process in separating step (not expressing among the figure).Sulphur is discharged with the 53a of free sulfur from this system in desulfurizer (53).
Referring to Fig. 7.Fusion flow process (54) comprises a concentrating unit (75), and the ore after this device will be pulverized is imported a reverberatory furnace (72), and ore is melted in the reverberatory furnace, to remove the impurity such as silicon-dioxide that exist with slag (76) form.Fused matte phase materials (55) advances converting furnace (73) and adds oxygen (78) blowing further to remove impurity (77) such as de-iron and sulphur then.In the process of production of copper, matte phase (55) mainly is a cupric sulfide.By an anode furnace (74) and refinement step (69), just produced metallic copper.
An application of the present invention is, with an electrolysis for production groove (68) directly from matte phase (55) electrodeposit metals.Although be used for producing nickel certain limit is arranged, will have more high-level efficiency from matte phase electrowinning metal product with electrolysis for production groove of the present invention from nickelous sulfide.
Certainly, must understand, when providing foregoing with illustrative example of the present invention, modification that all are such or such and modification are conspicuous to being proficient in this professional person, belong to category of the present invention so all regard as.This declares in following claim.
Claims (16)
1, a kind of method by following flow process electrolysis for production metal from ore body:
Leach liquor is circulated by leaching device and solvent extraction plant, thereby soluble mineral leach and dissolve in the said leach liquor from said ore body;
Make solvent pass through the circulation of described solvent extraction plant and back extraction device, thereby make the soluble mineral in the described leach liquor of dissolving in of selection from this leach liquor, extract and enter this solvent;
Make electrolytic solution pass through described back extraction device and the circulation of mineral extraction tank device, thereby, this soluble mineral from described solvent back extraction enter described electrolytic solution and
To the logical electric current of going up of this mineral extraction tank device, wherein said mineral extraction tank device comprises:
Fixed elongate housing with electrically conductive inner surface;
The removable tightness system that is installed on each end of said stationary;
Electrode stretches out from least one described tightness system and inserts in the shell, forms the ring-type cave between described shell and described electrode;
Be positioned at the fluid intake that leads to described ring-type cave on the described tightness system, the long axis direction that the fluid that forms during use departs from this stationary enters in the said mineral extraction tank device;
Be positioned at the fluid outlet that leads to described extraction tank on another described tightness system and
The electric terminals that connects electric current between described electrode and the conductive surface makes selected soluble mineral galvanic deposit on conductive surface.
2, the method for claim 1, wherein said extraction tank device comprises:
Tripping device, it is divided into an electrolyte liquor chamber (utilizing it can realize that described fluid intake contacts with fluid between fluid outlet) and a treat fluid chamber with said ring-type cave;
The inlet of said treat fluid chamber;
The outlet of said treat fluid chamber, wherein this method comprises by said entrance and exit convection cell and carries out circular treatment.
3, as claim 1 or the described method of claim 2, wherein, between described stream socket, electrolytic solution is passed through described shell, make electrolytic solution recirculation in described mineral extraction tank device, thereby described electrolytic solution is closely contacted with described conductive surface.
4, the method described in preceding arbitrary claim wherein, in order to strengthen tight contact the between described electrolytic solution and described conductive surface, and/or is improved the fluidic flow pattern, and described electrode surface will be handled.
5, the method described in preceding arbitrary claim, wherein the liquid stream by electrolyzer is the turbulent flows mode, thereby is describedly kept suspended state by the mineral of galvanic deposit in electrolytic solution.
6, as the described method of preceding arbitrary claim, wherein said conductive surface material is same with the institute sedimentary mineral facies of wanting, thus can save from conductive surface peel off this step of sedimentary mineral.
7, as the described method of preceding arbitrary claim, wherein with said electrode as anode and described conductive surface as negative electrode, described mineral are promptly by galvanic deposit after the current lead-through.
8,, also comprise and utilize particle collection device to be collected into the step that the small part electrode produces sedimentary deposition mineral as the described method of preceding arbitrary claim.
9, as each described method of claim 2-8, wherein said electrolyte liquor chamber can be opened, to shift out described conductive surface.
10, as each described method of claim 2-9, wherein liquid stream can use out of phase fluid, helps to alleviate the contamination of tripping device.
11, be used for extracting from the fluent solution that contains mineral the mineral extraction tank device of mineral, said device comprises:
Fixed elongate housing with electrically conductive inner surface;
Be installed in the tightness system on each end of this stationary movably;
From at least one described tightness system, stretch out and insert electrode in the described shell, between described electrode and described shell, form the ring-type cave like this;
Be positioned at the fluid intake that leads to described ring-type cave on the described tightness system, the long axis direction that the fluid that forms during use departs from this stationary enters in the described mineral extraction tank device;
Be positioned at the fluid outlet that leads to described slot device on another described tightness system;
Tripping device is divided into an electrolyte liquor chamber (utilizing it can realize that fluid intake contacts with fluid between fluid outlet) and a treat fluid chamber with described ring-type cave;
The inlet of treat fluid chamber;
The outlet of treat fluid chamber, and wherein this method comprise by said entrance and exit convection cell carry out circular treatment and
The electric terminals that connects electric current between described electrode and the described conductive surface is so that the mineral galvanic deposit is on described conductive surface.
12, the mineral extraction tank device described in claim 11, wherein the configuration of said tripping device can make selected material wear itself and mistake.
13, as claim 11 or 12 described mineral extraction tank devices, tripping device wherein comprises an ion-selective membrane.
14, as each the described mineral extraction tank device in the claim 11～13, tripping device wherein is a cation selective membrane, is used for from solution respective anionic electrowinning positively charged ion mineral.
15, as each described mineral extraction tank device in the claim 11～14, wherein said ion selects tripping device to allow to feed cathode compartment to collect the galvanic deposit mineral.
16, as each described mineral extraction tank device in the claim 11～15, wherein said tripping device is the round shape barrier film that its each end is supported by said tightness system.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AUPL4296 | 1992-08-25 | ||
| AUPL429692 | 1992-08-25 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1087387A true CN1087387A (en) | 1994-06-01 |
Family
ID=3776377
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN93118331.6A Pending CN1087387A (en) | 1992-08-25 | 1993-08-24 | Method and device that mineral reclaim |
Country Status (3)
| Country | Link |
|---|---|
| CN (1) | CN1087387A (en) |
| AP (1) | AP422A (en) |
| MY (1) | MY109831A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103849903A (en) * | 2014-03-25 | 2014-06-11 | 金隆铜业有限公司 | System for recovering antimony and bismuth in copper electrolyte |
| CN104152947A (en) * | 2014-07-14 | 2014-11-19 | 红板（江西）有限公司 | Suspended electrolyzing device for separating and recovering metals in waste circuit board |
| CN104775138A (en) * | 2015-04-01 | 2015-07-15 | 马恩高 | Electrolytic triple unit module for purifying noble metal |
| CN107208180A (en) * | 2014-11-28 | 2017-09-26 | 普罗特股份有限公司 | EWTECH LED process |
| CN108842171A (en) * | 2018-09-13 | 2018-11-20 | 陕西瑞凯环保科技有限公司 | A kind of method and apparatus that turbulent flow electrodeposition prepares metal-powder |
| CN117965884A (en) * | 2024-04-01 | 2024-05-03 | 烟台昌久智能科技有限公司 | Metal ore pretreatment processing device and processing method |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NO156724C (en) * | 1983-07-08 | 1987-11-11 | Elkem As | PROCEDURE FOR EXPLOITING THE COPPER CONTENT IN SULPHIDIC ORE AND CONCENTRATES. |
-
1993
- 1993-08-24 CN CN93118331.6A patent/CN1087387A/en active Pending
- 1993-08-24 MY MYPI93001693A patent/MY109831A/en unknown
- 1993-08-24 AP APAP/P/1993/000571A patent/AP422A/en active
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103849903A (en) * | 2014-03-25 | 2014-06-11 | 金隆铜业有限公司 | System for recovering antimony and bismuth in copper electrolyte |
| CN103849903B (en) * | 2014-03-25 | 2016-08-24 | 金隆铜业有限公司 | Antimony and the recovery system of bismuth in copper electrolyte |
| CN104152947A (en) * | 2014-07-14 | 2014-11-19 | 红板（江西）有限公司 | Suspended electrolyzing device for separating and recovering metals in waste circuit board |
| CN107208180A (en) * | 2014-11-28 | 2017-09-26 | 普罗特股份有限公司 | EWTECH LED process |
| CN104775138A (en) * | 2015-04-01 | 2015-07-15 | 马恩高 | Electrolytic triple unit module for purifying noble metal |
| CN104775138B (en) * | 2015-04-01 | 2017-03-22 | 马恩高 | Electrolytic triple unit module for purifying noble metal |
| CN108842171A (en) * | 2018-09-13 | 2018-11-20 | 陕西瑞凯环保科技有限公司 | A kind of method and apparatus that turbulent flow electrodeposition prepares metal-powder |
| CN117965884A (en) * | 2024-04-01 | 2024-05-03 | 烟台昌久智能科技有限公司 | Metal ore pretreatment processing device and processing method |
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Also Published As
| Publication number | Publication date |
|---|---|
| MY109831A (en) | 1997-08-30 |
| AP9300571A0 (en) | 1993-10-31 |
| AP422A (en) | 1995-10-26 |
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