WO2023243827A1 - 니켈 또는 코발트 수용액 제조 방법 - Google Patents
니켈 또는 코발트 수용액 제조 방법 Download PDFInfo
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- WO2023243827A1 WO2023243827A1 PCT/KR2023/004100 KR2023004100W WO2023243827A1 WO 2023243827 A1 WO2023243827 A1 WO 2023243827A1 KR 2023004100 W KR2023004100 W KR 2023004100W WO 2023243827 A1 WO2023243827 A1 WO 2023243827A1
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- Prior art keywords
- cobalt
- nickel
- aqueous solution
- filtrate
- producing
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- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 title claims abstract description 220
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 title claims abstract description 143
- 229910017052 cobalt Inorganic materials 0.000 title claims abstract description 141
- 239000010941 cobalt Substances 0.000 title claims abstract description 141
- 229910052759 nickel Inorganic materials 0.000 title claims abstract description 110
- 239000007864 aqueous solution Substances 0.000 title claims abstract description 72
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 61
- 238000000034 method Methods 0.000 claims abstract description 145
- 238000002386 leaching Methods 0.000 claims abstract description 82
- 239000000706 filtrate Substances 0.000 claims abstract description 68
- 239000012535 impurity Substances 0.000 claims abstract description 63
- 238000001556 precipitation Methods 0.000 claims abstract description 52
- 239000011777 magnesium Substances 0.000 claims abstract description 36
- 229910052749 magnesium Inorganic materials 0.000 claims abstract description 35
- 238000000605 extraction Methods 0.000 claims abstract description 30
- 239000002904 solvent Substances 0.000 claims abstract description 30
- 239000012044 organic layer Substances 0.000 claims abstract description 29
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000002994 raw material Substances 0.000 claims abstract description 22
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 20
- 230000003472 neutralizing effect Effects 0.000 claims abstract description 20
- 239000011575 calcium Substances 0.000 claims abstract description 19
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 18
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000000203 mixture Substances 0.000 claims abstract description 10
- 230000001376 precipitating effect Effects 0.000 claims abstract description 8
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 50
- 239000010949 copper Substances 0.000 claims description 38
- 229910052802 copper Inorganic materials 0.000 claims description 36
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 35
- 239000000243 solution Substances 0.000 claims description 35
- 239000011701 zinc Substances 0.000 claims description 26
- 239000011734 sodium Substances 0.000 claims description 23
- 238000010792 warming Methods 0.000 claims description 23
- 229910052725 zinc Inorganic materials 0.000 claims description 20
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical group [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 claims description 18
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 16
- 239000002244 precipitate Substances 0.000 claims description 16
- 238000000746 purification Methods 0.000 claims description 14
- PUZPDOWCWNUUKD-UHFFFAOYSA-M sodium fluoride Chemical group [F-].[Na+] PUZPDOWCWNUUKD-UHFFFAOYSA-M 0.000 claims description 14
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims description 12
- 229910052708 sodium Inorganic materials 0.000 claims description 12
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 11
- 238000005406 washing Methods 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- QUXFOKCUIZCKGS-UHFFFAOYSA-N bis(2,4,4-trimethylpentyl)phosphinic acid Chemical group CC(C)(C)CC(C)CP(O)(=O)CC(C)CC(C)(C)C QUXFOKCUIZCKGS-UHFFFAOYSA-N 0.000 claims description 7
- 239000011775 sodium fluoride Substances 0.000 claims description 5
- 235000013024 sodium fluoride Nutrition 0.000 claims description 5
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 claims description 4
- 239000000463 material Substances 0.000 claims description 4
- SEGLCEQVOFDUPX-UHFFFAOYSA-N di-(2-ethylhexyl)phosphoric acid Chemical compound CCCCC(CC)COP(O)(=O)OCC(CC)CCCC SEGLCEQVOFDUPX-UHFFFAOYSA-N 0.000 claims description 3
- 239000013077 target material Substances 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 27
- 238000010438 heat treatment Methods 0.000 description 14
- 239000007788 liquid Substances 0.000 description 13
- 238000011068 loading method Methods 0.000 description 13
- 229910052751 metal Inorganic materials 0.000 description 11
- 239000002184 metal Substances 0.000 description 11
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 8
- 229910052748 manganese Inorganic materials 0.000 description 8
- 239000011572 manganese Substances 0.000 description 8
- 150000002739 metals Chemical class 0.000 description 7
- 238000010586 diagram Methods 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- OMZSGWSJDCOLKM-UHFFFAOYSA-N copper(II) sulfide Chemical compound [S-2].[Cu+2] OMZSGWSJDCOLKM-UHFFFAOYSA-N 0.000 description 5
- 238000004880 explosion Methods 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- 239000013049 sediment Substances 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 238000000638 solvent extraction Methods 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 4
- 239000003960 organic solvent Substances 0.000 description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 3
- 229910017709 Ni Co Inorganic materials 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 150000004679 hydroxides Chemical class 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000007774 positive electrode material Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OAOABCKPVCUNKO-UHFFFAOYSA-N 8-methyl Nonanoic acid Chemical compound CC(C)CCCCCCC(O)=O OAOABCKPVCUNKO-UHFFFAOYSA-N 0.000 description 1
- 229910020634 Co Mg Inorganic materials 0.000 description 1
- 229910017518 Cu Zn Inorganic materials 0.000 description 1
- WHXSMMKQMYFTQS-UHFFFAOYSA-N Lithium Chemical compound [Li] WHXSMMKQMYFTQS-UHFFFAOYSA-N 0.000 description 1
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 1
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 1
- 229910001634 calcium fluoride Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052744 lithium Inorganic materials 0.000 description 1
- 229910001416 lithium ion Inorganic materials 0.000 description 1
- ORUIBWPALBXDOA-UHFFFAOYSA-L magnesium fluoride Chemical compound [F-].[F-].[Mg+2] ORUIBWPALBXDOA-UHFFFAOYSA-L 0.000 description 1
- 229910001635 magnesium fluoride Inorganic materials 0.000 description 1
- LGQLOGILCSXPEA-UHFFFAOYSA-L nickel sulfate Chemical compound [Ni+2].[O-]S([O-])(=O)=O LGQLOGILCSXPEA-UHFFFAOYSA-L 0.000 description 1
- 229910000363 nickel(II) sulfate Inorganic materials 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000036967 uncompetitive effect Effects 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G53/00—Compounds of nickel
-
- 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
-
- 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
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M4/00—Electrodes
- H01M4/02—Electrodes composed of, or comprising, active material
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M4/00—Electrodes
- H01M4/02—Electrodes composed of, or comprising, active material
- H01M4/36—Selection of substances as active materials, active masses, active liquids
- H01M4/48—Selection of substances as active materials, active masses, active liquids of inorganic oxides or hydroxides
- H01M4/52—Selection of substances as active materials, active masses, active liquids of inorganic oxides or hydroxides of nickel, cobalt or iron
- H01M4/525—Selection of substances as active materials, active masses, active liquids of inorganic oxides or hydroxides of nickel, cobalt or iron of mixed oxides or hydroxides containing iron, cobalt or nickel for inserting or intercalating light metals, e.g. LiNiO2, LiCoO2 or LiCoOxFy
-
- 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
Definitions
- the present invention relates to a method for producing an aqueous solution of nickel or cobalt. More specifically, the present invention relates to a method of recovering nickel and cobalt from raw materials and then producing a nickel or cobalt aqueous solution that can be used to manufacture positive electrode active materials for lithium ion secondary batteries.
- MHP Mixed Hydroxide Precipitate
- nickel and cobalt were selectively recovered from the ionized nickel and cobalt aqueous solution using solvent extractants such as Ion quest 801, Cyanex 272, Versatic Acid 10, and LIX 84I.
- solvent extractants such as Ion quest 801, Cyanex 272, Versatic Acid 10, and LIX 84I.
- the purpose of the present invention is to recover nickel and cobalt from MHP cake raw materials containing nickel and cobalt mixed hydroxides and prepare a high purity aqueous solution.
- the purpose of the present invention is to improve nickel and cobalt recovery and reduce energy usage by ionizing nickel and cobalt using a two-stage atmospheric pressure warming leaching process.
- the present invention uses sodium fluoride (NaF), a precipitant, to separate magnesium and calcium in the high-purity nickel aqueous solution production process, and uses sodium hydrogen sulfide (NaSH) in the high-purity cobalt aqueous solution production process to separate magnesium and manganese through solubility differences.
- NaF sodium fluoride
- NaSH sodium hydrogen sulfide
- the purpose is to reduce the solvent extraction process by additionally separating impurities such as copper, magnesium, and manganese through the use of sodium hydrogen sulfide (NaSH) and sodium fluoride (NaF).
- the purpose of the present invention is to minimize the solvent extraction process so that it is not only suitable for the operating environment but also reduces the cost of manufacturing the final product.
- One aspect of the present invention includes (A) a leaching process comprising a first atmospheric pressure warming leaching process and a second atmospheric pressure warming leaching process for leaching raw materials under normal pressure to form a leachate containing nickel, cobalt, and impurities; (B) a first extraction process of adding a first solvent extractant to the leachate to separate it into a first filtrate containing nickel and impurities and a first organic layer containing cobalt and impurities; and (C-i) a precipitation removal step of adding a precipitant to the first filtrate to precipitate and remove impurities including magnesium, calcium, or a mixture thereof; and (D-i) a target precipitation step of selectively precipitating a nickel cake containing nickel by adding a neutralizing agent to the first filtrate from which the impurities have been precipitated and removed. .
- Another aspect of the present invention includes (A) a leaching process comprising a first atmospheric pressure warming leaching process and a second atmospheric pressure warming leaching process for leaching raw materials under normal pressure to form a leachate containing nickel, cobalt, and impurities; (B) a first extraction process of adding a first solvent extractant to the leachate to separate it into a first filtrate containing nickel and impurities and a first organic layer containing cobalt and impurities; and (C-ii) preparing a second filtrate by adding a sulfuric acid solution to the first organic layer, and adding sulfide to the second filtrate to precipitate and recover the cobalt precipitate to produce magnesium, manganese, zinc, copper, or a mixture thereof. It relates to a method for producing an aqueous solution of nickel or cobalt, including a purification process for purifying impurities contained therein.
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution in which the pH of the filtrate from the second atmospheric pressure warming leaching process is lower than the pH of the filtrate from the first atmospheric pressure warming leaching process.
- One embodiment of the present invention can provide a method for producing a nickel or cobalt aqueous solution in which the filtrate from the second atmospheric pressure warming leaching process is sent to the first atmospheric pressure warming leaching process.
- One embodiment of the present invention may provide a method for producing an aqueous nickel or cobalt solution in which the first solvent extractant is Bis(2,4,4-trimethylpentyl) phosphinic acid.
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution in which the first extraction process is performed at 40° C. and under pH conditions of more than 5.0 and less than 5.4.
- One embodiment of the present invention may provide a method for producing an aqueous solution of nickel or cobalt, wherein the precipitant is sodium fluoride.
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution in which the precipitant is added in an amount greater than 2.0 equivalents but less than 2.4 equivalents of magnesium, calcium, or a mixture thereof.
- One embodiment of the present invention may provide a method for producing an aqueous solution of nickel or cobalt, wherein the neutralizing agent is a basic material containing sodium.
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution in which the pH of the first filtrate is 8 or higher at 85°C after the neutralizing agent is added.
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution, further comprising (E-i) a washing process of washing the nickel cake with pure water.
- One embodiment of the present invention can provide a method for producing an aqueous solution of nickel or cobalt, wherein the sulfide is sodium hydrogen sulfide (NaSH).
- NaSH sodium hydrogen sulfide
- One embodiment of the present invention can provide a method for producing a nickel or cobalt aqueous solution in which the sulfide is added in an amount greater than 1.0 equivalent but less than 1.6 equivalent of the cobalt and zinc content.
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution, further comprising the step (D-ii) of dissolving the cobalt precipitate in a sulfuric acid solution and then removing copper.
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution in which the copper removal process is performed by adding sodium hydrogen sulfide (NaSH) in an amount of more than 4.5 equivalents but less than 5.5 equivalents of the copper content.
- NaSH sodium hydrogen sulfide
- (E-ii) adding a second solvent extractant to the aqueous solution from which the copper has been removed is separated into a third filtrate containing cobalt and impurities and a second organic layer containing zinc and impurities.
- a method for producing an aqueous nickel or cobalt solution may be provided, further comprising a second extraction process.
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution in which the second solvent extractant is D2EHPA (Di-(2-ethylhexyl)phosphoric acid).
- D2EHPA Di-(2-ethylhexyl)phosphoric acid
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution in which the second extraction process is performed at 40° C. and under pH conditions of more than 2.4 and less than 3.2.
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution, further comprising (F) a precipitation removal step of adding a precipitant to the third filtrate to remove impurities including magnesium by precipitation.
- One embodiment of the present invention includes (G) a target precipitation process of selectively precipitating a cobalt cake containing cobalt by adding a neutralizing agent to the third filtrate from which the impurities have been precipitated and removed; including, nickel or A method for producing an aqueous cobalt solution can be provided.
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution in which the pH of the third filtrate is 8 or more at 85°C after the neutralizing agent is added.
- One embodiment of the present invention may provide a method for producing a nickel or cobalt aqueous solution, further comprising (H) a washing process of washing the cobalt cake using pure water.
- nickel and cobalt recovery rates can be improved and energy consumption can be reduced by using a two-stage atmospheric pressure heating process.
- Figure 1 is a diagram showing a two-stage leaching process and a first extraction process for producing a nickel or cobalt aqueous solution according to an embodiment of the present invention.
- Figure 2 is a diagram showing a precipitation removal process and a target precipitation process for producing an aqueous nickel solution according to an embodiment of the present invention.
- Figure 3 is a diagram showing an impurity purification process, a copper removal process, a second extraction process, a precipitation removal process, and a target precipitation process for producing an aqueous cobalt solution according to an embodiment of the present invention.
- Embodiments of the present invention are illustrated for the purpose of explaining the technical idea of the present invention.
- the scope of rights according to the present invention is not limited to the embodiments presented below or the specific description of these embodiments.
- Figure 1 is a diagram showing a two-stage leaching process (S10) and a first extraction process (S20) for producing a nickel or cobalt aqueous solution according to an embodiment of the present invention.
- Figure 2 is a diagram showing a precipitation removal process (S31) and a target precipitation process (S32) for producing an aqueous nickel solution according to an embodiment of the present invention.
- Figure 3 shows an impurity purification process (S32, S42), a copper removal process (S62), a second extraction process (S72), a precipitation removal process (S82), and a target product for producing an aqueous cobalt solution according to an embodiment of the present invention.
- This is a diagram showing the precipitation process (S92).
- a method of producing a nickel or cobalt aqueous solution that can be used to manufacture a positive electrode active material for a lithium secondary battery from a mixed hydroxide precipitate (MHP cake) through a series of processes can be provided. According to this method, operational stability and purity can be improved, and manufacturing costs can be reduced. Below, each process will be described in detail with reference to each drawing.
- a first extraction process (S20) of separating into a first organic layer may be performed.
- the leaching process (S10) is a process of forming a leachate by dissolving the hydroxide-type MHP cake in an acid solution such as sulfuric acid to ionize it.
- the leaching process (S10) includes a first atmospheric pressure warming leaching process (S11) and a second atmospheric pressure warming leaching process (S12).
- the normal pressure heating leaching process is a process of preparing an acid solution in an open reactor at a temperature of 100°C or lower, introducing raw materials into the reactor, and leaching valuable metals through a reaction according to Scheme 1 below.
- the raw material introduced here may be an MHP cake in the form of a hydroxide containing 40% by weight of nickel.
- the first atmospheric pressure warming leaching process (S11) and the second atmospheric pressure warming leaching process (S12) are each performed in a two-stage device, or are performed in a single pressurizing device under process conditions (e.g., temperature, pressure, or acidity). ) can be performed differently.
- Valuable metals may be leached from raw materials through the first atmospheric pressure heating leaching process (S11).
- valuable metals such as nickel, cobalt, and manganese in raw materials may be leached.
- elements such as iron, copper, aluminum, zinc, or magnesium in the raw materials may also be leached.
- the first atmospheric pressure leaching process (S11) may be performed for about 2 hours at a temperature ranging from 50°C to 70°C and a pH ranging from 2.7 to 3.3. By satisfying the temperature and pH range, high leaching efficiency can be obtained under optimal conditions.
- the solid density of the raw material introduced into the reactor may be 100 g/L or more.
- the solid density of the raw material may range from 100 g/L to 200 g/L.
- solid density is defined as the ratio of the mass of the raw material introduced into the pressurizing device to the volume of the acid solution previously introduced into the reactor.
- the solid density may be the ratio of the mass of the raw material introduced per unit solvent, and may be the mass of the raw material per 1 L of solvent.
- the filtrate is input into the first extraction process (S20), and the residue may be subsequently treated in the second atmospheric pressure warming leaching process (S12).
- leaching of the leaching residue from the first atmospheric pressure leaching process (S11) may be performed at a temperature ranging from 80°C to 100°C for about 3 hours.
- Other conditions of the second atmospheric pressure warming leaching process (S12) may be the same as the conditions of the first atmospheric pressure warming leaching process (S11).
- the pH of the filtrate from the second atmospheric pressure leaching process (S12) may be lower than the pH of the filtrate from the first atmospheric pressure leaching process (S11).
- the leaching rate in each atmospheric pressure heating process can be increased. Accordingly, the entire amount of valuable metals contained in the raw materials may be leached. For example, all of the nickel, cobalt, manganese, iron, copper, aluminum, zinc, or magnesium contained in the raw materials may be leached.
- the filtrate formed in the second atmospheric pressure leaching process (S12) may be sent to the first atmospheric pressure leaching process (S11) as shown in FIG.
- the reaction time must be continued for more than 18 hours to increase the leaching rate of valuable metals.
- additional costs were incurred due to increased fuel and steam usage, and productivity was low due to the small amount of raw materials processed per day.
- nickel and cobalt recovery rates can be improved and energy consumption can be reduced by using a two-stage atmospheric pressure heating leaching method. Therefore, manufacturing costs can be reduced and productivity can be improved.
- the residue generated in the second atmospheric pressure leaching process (S12) can be discarded, as shown in FIG. 1.
- the first extraction process (S20) is a process of selectively separating or extracting nickel from the ionized nickel and cobalt aqueous solution (leach solution) through a two-stage atmospheric pressure leaching process using a first solvent extractant.
- the first solvent extractant is not particularly limited as long as it has a low nickel loading rate, but may be, for example, Bis(2,4,4-trimethylpentyl) phosphinic acid (Cyanex272).
- the first extraction process may be performed at 40°C under conditions of pH greater than 5.0 and less than 5.4.
- the loading rate of cobalt and impurities can be increased, and nickel can be efficiently separated into the filtrate.
- the ratio of the first solvent extractant (O) and the aqueous solution (A) can be adjusted depending on the concentration of the component to be extracted in the solution.
- the ratio (O:A) of the first solvent extractant (O) and the aqueous solution (A) may range from 0.5:1 to 2:1.
- O:A can be 1.5:1.
- a target precipitation process (S41) and a final leaching process to prepare a high-purity nickel aqueous solution can be performed.
- the precipitation removal process (S31) may be performed to remove impurities such as magnesium, calcium, or mixtures thereof remaining in the first filtrate. After the precipitation removal process (S31), the first filtrate may be sent to the target object precipitation process (S41).
- the sediment removal process (S31) may include adding a removal agent into the liquid.
- the remover is not particularly limited as long as it can react with magnesium or calcium to form a precipitate, but may be, for example, sodium fluoride (NaF).
- magnesium and calcium may be precipitated into magnesium fluoride or calcium fluoride through a reaction as shown in Scheme 4 below.
- nickel precipitation in the filtrate can be reduced and only magnesium and calcium can be separated through selective precipitation.
- sodium fluoride may be added in an amount exceeding 2.0 equivalents (eq) of the magnesium, calcium, or mixture thereof. In another example, sodium fluoride may be added in an amount less than 2.4 equivalents (eq) of magnesium, calcium, or a mixture thereof.
- a neutralizing agent may be added to the first filtrate after the precipitation removal process (S31).
- the neutralizing agent may be a basic substance containing sodium.
- the neutralizing agent may be sodium carbonate (Na 2 CO 3 ).
- nickel After removing impurities such as magnesium and calcium, nickel can be precipitated in the form of a cake through a reaction as shown in Scheme 5 below in the target precipitation process (S41).
- the target precipitation process (S41) may be performed for more than 4 hours at a pH of 8 or more and a temperature in the range of 80°C to 90°C.
- sodium components may be present in the precipitated nickel cake, so the water-soluble sodium component can be removed by using a washing process using pure water at a later stage.
- manufacturing costs can be reduced by reusing the removed sodium component to manufacture sodium carbonate (Na 2 CO 3 ), a neutralizing agent.
- the final leaching process (S51) is a process in which components such as sodium in the produced nickel cake are washed with water and then dissolved in a sulfuric acid solution to produce a high-purity nickel aqueous solution.
- the nickel cake can be added to a solution of pure water mixed with sulfuric acid at an acidity of 150 g/L to 200 g/L. Nickel, cobalt, and trace impurities contained in the nickel cake will be dissolved in the sulfuric acid solution. The aqueous sulfuric acid solution and the nickel cake are reacted until the pH is 2.0.
- the temperature is 4 to 1.0 to 3.0 and a temperature range is 50°C to 70°C. The reaction may proceed over time.
- a second filtrate production process in which a sulfuric acid solution is added to the first organic layer that has undergone the first extraction process (S11), cobalt precipitate in the second filtrate is precipitated and recovered, and impurities are purified.
- a purification process S42
- a process of dissolving the recovered cobalt precipitate again in a sulfuric acid solution S52
- a copper removal process S62
- a target precipitation process (S92) to selectively precipitate cake) and a final leaching process (S102) to produce a high-purity cobalt aqueous solution can be performed.
- the second filtrate production process (S32) is a process of adding a sulfuric acid solution to the first organic layer containing cobalt and impurities and stripping the cobalt from the sulfuric acid solution.
- Stripping is a process in which sulfuric acid and loaded cobalt are reacted to produce a stripping filtrate containing cobalt, and the loaded impurities are recovered as an aqueous solution.
- the purification process (S32) is a process for selectively recovering only cobalt from the stripped second filtrate. What is different from the precipitation removal process (31) is that in the purification process (S32), the target cobalt can be recovered in the form of a precipitate.
- the purification process (S32) may generate cobalt precipitate by adding sulfide into the liquid.
- the sulfide may be sodium hydrogen sulfide (NaSH), and cobalt may be recovered by precipitation in the form of sulfide through reactions according to Schemes 6 and 7 below.
- the purification process (S32) can be performed for about 3 hours or more while maintaining a pH of 4.5 to 5.0 at a reaction temperature in the range of 70°C to 90°C.
- the solubility of CoS and ZnS is very low at less than 0.1 mg/L, and the solubility of MgS and MnS is very low. Therefore, by adjusting the pH range, only cobalt and zinc are separated through selective precipitation, and magnesium and manganese are separated. can be purified.
- sulfide may be added in an amount greater than 1.0 equivalent but less than 1.6 equivalent of the cobalt and zinc content.
- the sulfuric acid solution manufacturing process (S52) is to prepare an aqueous solution by dissolving a precipitate containing cobalt in a sulfuric acid solution.
- the sulfuric acid solution preparation process (S52) can be performed by a reaction according to Scheme 8 below.
- the solid density (S/D) of the precipitate in the sulfuric acid solution when preparing the aqueous solution may be 100 g/L or more.
- the sulfuric acid solution preparation process (S52) may be performed at a reaction temperature in the range of 80°C to 100°C for about 20 hours or more.
- the copper removal process (S62) is a process of removing copper (Cu) in the liquid by adding sodium hydrogen sulfide (NaSH) into the liquid. Copper can be precipitated as a copper sulfide (CuS) compound through a reaction shown in Scheme 9 below.
- Copper sulfide (CuS) can precipitate above pH 1.0.
- the pH in the liquid may be maintained at 1.0 to 2.5 in the copper removal process (S62). In one embodiment, the pH in the liquid may be maintained at 1.0 to 1.5 in the copper removal process (S62). If the pH of the liquid is less than 1.0, it is difficult to remove copper in the liquid below 20 mg/L, and if the pH is higher than 2.5, the solubility of cobalt in sulfuric acid may decrease, resulting in loss of cobalt.
- sodium hydrogen sulfide can be added slowly so that the pH in the liquid does not change suddenly.
- sodium hydrogen sulfide NaSH
- NaSH sodium hydrogen sulfide
- sodium hydrogen sulfide (NaSH) may be added in an amount greater than 4.5 equivalents (eq) to less than 5.5 equivalents (eq) of the copper content.
- the amount of sodium hydrogen sulfide (NaSH) added is 4.5 equivalents (eq) or less, the copper removal rate is 95% or less, making it difficult to sufficiently remove copper in the liquid.
- the input amount of sodium hydrogen sulfide (NaSH) is more than 5.5 equivalents (eq)
- the cobalt recovery rate may decrease because the cobalt removal rate is more than 0.05%.
- the second extraction process (S72) is a process of adding a second solvent extractant into the liquid and separating it into a third filtrate containing cobalt and impurities and a second organic layer containing zinc and impurities.
- the second solvent extractant is not particularly limited as long as it has a low cobalt loading rate, but may be, for example, D2EHPA (Di-(2-ethylhexyl)phosphoric acid).
- the second extraction process (S72) may be performed for about 10 minutes or more at 40°C under conditions of pH greater than 2.4 and less than 3.2.
- the loading rate of impurities such as zinc can be increased and the loading rate of cobalt can be lowered, and cobalt can be efficiently separated into the filtrate.
- the ratio of the second solvent extractant (O) and the aqueous solution (A) can be adjusted depending on the concentration of the component to be extracted in the solution.
- the ratio (O:A) of the second solvent extractant (O) and the aqueous solution (A) may range from 0.5:1 to 2:1.
- O:A can be 1.5:1.
- the precipitation removal process (S82) may be performed to remove impurities such as magnesium remaining in the third filtrate. After the precipitation removal process (82), the third filtrate may be sent to the target object precipitation process (S92).
- a neutralizing agent may be added to the third filtrate after the precipitation removal process (S82).
- the neutralizing agent may be a basic substance containing sodium.
- the neutralizing agent may be sodium carbonate (Na 2 CO 3 ).
- nickel After removing impurities such as magnesium, nickel can be precipitated in the form of a cake through a reaction shown in Scheme 11 below in the target precipitation process (S41).
- the target precipitation process (S92) may be performed for more than 4 hours at a pH of 8 or more and a temperature in the range of 80°C to 90°C.
- sodium components may be present in the precipitated cobalt cake, so the water-soluble sodium component can be removed by using a washing process using pure water at a later stage.
- manufacturing costs can be reduced by reusing the removed sodium component to manufacture sodium carbonate (Na 2 CO 3 ), a neutralizing agent.
- the final leaching process (S102) is a process in which components such as sodium in the produced cobalt cake are washed with water and then dissolved in a sulfuric acid solution to produce a high-purity cobalt aqueous solution.
- the cobalt loaded in the organic layer by Cyanex272 was washed with a sulfuric acid solution and then used sodium hydrogen sulfide (NaSH) to precipitate and recover the cobalt in the form of sulfide.
- NaSH sodium hydrogen sulfide
- the input amount of NaSH was adjusted to the cobalt and zinc contents.
- the content of the precipitated cake was compared by adding 1.0, 1.3, and 1.6 equivalents. The reaction was performed for 3 hours at 85°C and pH 4.5 to 5.0.
- the copper removal rate was determined by adding NaSH at 4.5, 5.0, and 5.5 equivalents of the copper content. compared. The reaction was conducted for 3 hours at 60°C and pH 1.0 conditions. The removal rate was expressed by comparing the content of each component in the aqueous solution before and after adding NaSH.
- Ni(g/L) Co Mg Mn Zn Content 131.3 17.9 18.9 2.87 2.88
Abstract
Description
Ni | Co | Mg | Mn | Zn | |
함량(wt%) | 38.0 | 3.80 | 1.40 | 6.15 | 0.90 |
Ni | Co | Mg | Mn | Zn | |
함량(g/L) | 100.1 | 10.3 | 5.11 | 9.87 | 2.33 |
여액 원액 | 2.0당량 투입 | 2.2당량 투입 | 2.4당량 투입 | ||||||
Mg | Ca | Mg | Ca | Mg | Ca | Mg | Ca | ||
함량 | mg/L | 1,024 | 184 | 252.2 | 68.2 | 204.8 | 55.1 | 205.0 | 54.9 |
Ni(g/L) | Co | Mg | Mn | Zn | |
함량(mg/L) | 131.3 | 17.9 | 18.9 | 2.87 | 2.88 |
Co(g/L) | Cu | Zn | Mn | Mg | |
함량(mg/L) | 110.6 | 3.63 | 3.38 | 12.0 | 11.4 |
Claims (22)
- (A) 원료를 상압 가온 침출하여 니켈, 코발트, 및 불순물을 포함하는 침출액을 형성하는 제1 상압 가온 침출 공정 및 제2 상압 가온 침출 공정을 포함하는 침출 공정;(B) 상기 침출액에 제1 용매 추출제를 투입하여 니켈 및 불순물을 포함하는 제1 여액 및 코발트 및 불순물을 포함하는 제1 유기층으로 분리하는 제1 추출 공정; 및(C-i) 상기 제1 여액에 침전제를 투입하여, 마그네슘, 칼슘 또는 이들의 혼합물을 포함하는 불순물을 침전 제거하는 침전 제거 공정; 및(D-i) 상기 불순물이 침전 제거된 제1 여액에 중화제를 투입하여, 니켈을 포함하는 니켈 케이크(Cake)를 선택적으로 침전하는 목적물 침전 공정;을 포함하는, 니켈 또는 코발트 수용액 제조 방법.
- (A) 원료를 상압 가온 침출하여 니켈, 코발트, 및 불순물을 포함하는 침출액을 형성하는 제1 상압 가온 침출 공정 및 제2 상압 가온 침출 공정을 포함하는 침출 공정;(B) 상기 침출액에 제1 용매 추출제를 투입하여 니켈 및 불순물을 포함하는 제1 여액 및 코발트 및 불순물을 포함하는 제1 유기층으로 분리하는 제1 추출 공정; 및(C-ii) 상기 제1 유기층에 황산 용액을 투입하여 제2 여액을 제조하고, 제2 여액에 황화물을 투입하여 코발트 침전물을 침전 회수함으로써 마그네슘, 망간, 아연, 구리, 또는 이들의 혼합물을 포함하는 불순물을 정제하는 정제 공정;을 포함하는, 니켈 또는 코발트 수용액 제조 방법.
- 제1항 또는 제2항에 있어서,상기 제2 상압 가온 침출 공정의 여액의 pH는, 상기 제1 상압 가온 침출 공정의 여액의 pH보다 낮은, 니켈 또는 코발트 수용액 제조 방법.
- 제1항 또는 제2항에 있어서,상기 제2 상압 가온 침출 공정의 여액은, 상기 제1 상압 가온 침출 공정으로 송액되는, 니켈 또는 코발트 수용액 제조 방법.
- 제1항 또는 제2항에 있어서,상기 제1 용매 추출제는 Bis(2,4,4-trimethylpentyl) phosphinic acid인, 니켈 또는 코발트 수용액 제조 방법.
- 제1항 또는 제2항에 있어서,상기 제1 추출 공정은 40℃에서 pH 5.0 초과 5.4 미만의 조건에서 수행되는, 니켈 또는 코발트 수용액 제조 방법.
- 제1항에 있어서,상기 침전제는 플루오린화 나트륨인, 니켈 또는 코발트 수용액 제조 방법.
- 제1항에 있어서,상기 침전제는 마그네슘, 칼슘 또는 이들의 혼합물 함량의 2.0 당량 초과 2.4 당량 미만의 함량으로 투입되는, 니켈 또는 코발트 수용액 제조 방법.
- 제1항에 있어서,상기 중화제는 소듐을 포함하는 염기성 물질인, 니켈 또는 코발트 수용액 제조 방법.
- 제1항에 있어서,상기 중화제가 투입된 후 제1 여액의 85℃에서 pH는 8 이상인, 니켈 또는 코발트 수용액 제조 방법.
- 제1항에 있어서,(E-i) 상기 니켈 케이크를 순수를 이용하여 세척하는 수세 공정을 더 포함하는, 니켈 또는 코발트 수용액 제조 방법.
- 제2항에 있어서,상기 황화물은 황화수소나트륨(NaSH)인, 니켈 또는 코발트 수용액 제조 방법.
- 제2항에 있어서,상기 황화물은 코발트 및 아연 함량의 1.0 당량 초과 1.6 당량 미만의 함량으로 투입되는, 니켈 또는 코발트 수용액 제조 방법.
- 제2항에 있어서,(D-ii) 상기 코발트 침전물을 황산 용액에 용해시킨 후, 구리를 제거하는 공정을 더 포함하는, 니켈 또는 코발트 수용액 제조 방법.
- 제13항에 있어서,상기 구리를 제거하는 공정은 황화수소나트륨(NaSH)을 구리 함량의 4.5 당량 초과 5.5 당량 미만의 함량으로 투입하여 수행되는, 니켈 또는 코발트 수용액 제조 방법.
- 제14항에 있어서,(E-ii) 상기 구리가 제거된 수용액에 제2 용매 추출제를 투입하여 코발트 및 불순물을 포함하는 제3 여액 및 아연 및 불순물을 포함하는 제2 유기층으로 분리하는 제2 추출 공정을 더 포함하는, 니켈 또는 코발트 수용액 제조 방법.
- 제16항에 있어서,상기 제2 용매 추출제는 D2EHPA(Di-(2-ethylhexyl)phosphoric acid)인, 니켈 또는 코발트 수용액 제조 방법.
- 제16항에 있어서,상기 제2 추출 공정은 40℃에서 pH 2.4 초과 3.2 미만의 조건에서 수행되는, 니켈 또는 코발트 수용액 제조 방법.
- 제16항에 있어서,(F) 상기 제3 여액에 침전제를 투입하여, 마그네슘을 포함하는 불순물을 침전 제거하는 침전 제거 공정을 더 포함하는, 니켈 또는 코발트 수용액 제조 방법.
- 제19항에 있어서,(G) 상기 불순물이 침전 제거된 제3 여액에 중화제를 투입하여, 코발트를 포함하는 코발트 케이크(Cake)를 선택적으로 침전하는 목적물 침전 공정;을 포함하는, 니켈 또는 코발트 수용액 제조 방법.
- 제20항에 있어서,상기 중화제가 투입된 후 제3 여액의 85℃에서 pH는 8 이상인, 니켈 또는 코발트 수용액 제조 방법.
- 제20항에 있어서,(H) 상기 코발트 케이크를 순수를 이용하여 세척하는 수세 공정을 더 포함하는, 니켈 또는 코발트 수용액 제조 방법.
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Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR101535250B1 (ko) * | 2015-02-02 | 2015-07-08 | 주식회사 에너텍 | 니켈 및 코발트 혼합 수산화물을 포함한 원료로 사용하여 상압침출을 통해 제조되는 고순도 황산니켈 및 그 제조방법 |
KR101979419B1 (ko) * | 2017-12-26 | 2019-08-28 | 케이지에너켐(주) | 칼슘 고함량의 니켈, 코발트 및 망간 혼합 수산화물 원료로 제조되는 고순도 황산니켈의 제조방법 |
KR20210079709A (ko) * | 2019-12-20 | 2021-06-30 | 주식회사 포스코 | 고농도 니켈 케이크 제조방법 |
KR102451443B1 (ko) * | 2020-06-08 | 2022-10-07 | 재단법인 포항산업과학연구원 | 이차전지 양극재용 니켈 전구체 제조방법 |
KR102471399B1 (ko) * | 2022-02-17 | 2022-11-28 | (주)에코프로머티리얼즈 | 니켈, 코발트 및 망간의 분리 회수를 위한 2단 추출을 이용한 용매추출방법 |
KR102509344B1 (ko) * | 2023-01-27 | 2023-03-14 | 고려아연 주식회사 | 니켈 또는 코발트 수용액 제조 방법 |
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Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR101535250B1 (ko) * | 2015-02-02 | 2015-07-08 | 주식회사 에너텍 | 니켈 및 코발트 혼합 수산화물을 포함한 원료로 사용하여 상압침출을 통해 제조되는 고순도 황산니켈 및 그 제조방법 |
KR101979419B1 (ko) * | 2017-12-26 | 2019-08-28 | 케이지에너켐(주) | 칼슘 고함량의 니켈, 코발트 및 망간 혼합 수산화물 원료로 제조되는 고순도 황산니켈의 제조방법 |
KR20210079709A (ko) * | 2019-12-20 | 2021-06-30 | 주식회사 포스코 | 고농도 니켈 케이크 제조방법 |
KR102451443B1 (ko) * | 2020-06-08 | 2022-10-07 | 재단법인 포항산업과학연구원 | 이차전지 양극재용 니켈 전구체 제조방법 |
KR102471399B1 (ko) * | 2022-02-17 | 2022-11-28 | (주)에코프로머티리얼즈 | 니켈, 코발트 및 망간의 분리 회수를 위한 2단 추출을 이용한 용매추출방법 |
KR102509344B1 (ko) * | 2023-01-27 | 2023-03-14 | 고려아연 주식회사 | 니켈 또는 코발트 수용액 제조 방법 |
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