CN116590524A - Method for separating and extracting molybdenum and nickel from carbon-containing nickel-molybdenum ore - Google Patents
Method for separating and extracting molybdenum and nickel from carbon-containing nickel-molybdenum ore Download PDFInfo
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- CN116590524A CN116590524A CN202310576460.8A CN202310576460A CN116590524A CN 116590524 A CN116590524 A CN 116590524A CN 202310576460 A CN202310576460 A CN 202310576460A CN 116590524 A CN116590524 A CN 116590524A
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- nickel
- molybdenum
- leaching
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- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 title claims abstract description 200
- 229910052759 nickel Inorganic materials 0.000 title claims abstract description 100
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 title claims abstract description 75
- 229910052750 molybdenum Inorganic materials 0.000 title claims abstract description 75
- 239000011733 molybdenum Substances 0.000 title claims abstract description 75
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 title claims abstract description 58
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 48
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 47
- 238000002386 leaching Methods 0.000 claims abstract description 92
- 239000002893 slag Substances 0.000 claims abstract description 57
- 239000011684 sodium molybdate Substances 0.000 claims abstract description 42
- 235000015393 sodium molybdate Nutrition 0.000 claims abstract description 42
- TVXXNOYZHKPKGW-UHFFFAOYSA-N sodium molybdate (anhydrous) Chemical compound [Na+].[Na+].[O-][Mo]([O-])(=O)=O TVXXNOYZHKPKGW-UHFFFAOYSA-N 0.000 claims abstract description 42
- 238000003723 Smelting Methods 0.000 claims abstract description 32
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 27
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 27
- 239000001301 oxygen Substances 0.000 claims abstract description 27
- 238000001914 filtration Methods 0.000 claims abstract description 25
- 239000007788 liquid Substances 0.000 claims abstract description 21
- 238000005406 washing Methods 0.000 claims abstract description 20
- 239000012535 impurity Substances 0.000 claims abstract description 18
- 238000002156 mixing Methods 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 238000001035 drying Methods 0.000 claims abstract description 13
- 239000011734 sodium Substances 0.000 claims abstract description 12
- 239000003513 alkali Substances 0.000 claims abstract description 11
- 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 abstract description 9
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 9
- 230000035484 reaction time Effects 0.000 claims abstract description 7
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 63
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 38
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 28
- 239000000047 product Substances 0.000 claims description 24
- 229910052742 iron Inorganic materials 0.000 claims description 19
- 239000012452 mother liquor Substances 0.000 claims description 15
- 238000006243 chemical reaction Methods 0.000 claims description 14
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 14
- 230000009467 reduction Effects 0.000 claims description 13
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 11
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 11
- 239000011777 magnesium Substances 0.000 claims description 11
- 229910052749 magnesium Inorganic materials 0.000 claims description 11
- 239000010703 silicon Substances 0.000 claims description 11
- 229910052710 silicon Inorganic materials 0.000 claims description 11
- 239000002002 slurry Substances 0.000 claims description 11
- 239000011593 sulfur Substances 0.000 claims description 11
- 229910052717 sulfur Inorganic materials 0.000 claims description 11
- 239000000706 filtrate Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 8
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 7
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 7
- RQPZNWPYLFFXCP-UHFFFAOYSA-L barium dihydroxide Chemical compound [OH-].[OH-].[Ba+2] RQPZNWPYLFFXCP-UHFFFAOYSA-L 0.000 claims description 7
- 229910001863 barium hydroxide Inorganic materials 0.000 claims description 7
- TZCXTZWJZNENPQ-UHFFFAOYSA-L barium sulfate Chemical compound [Ba+2].[O-]S([O-])(=O)=O TZCXTZWJZNENPQ-UHFFFAOYSA-L 0.000 claims description 6
- 230000005484 gravity Effects 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 6
- 238000004537 pulping Methods 0.000 claims description 6
- 229910052979 sodium sulfide Inorganic materials 0.000 claims description 6
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 claims description 6
- 239000002244 precipitate Substances 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 5
- 229910019142 PO4 Inorganic materials 0.000 claims description 3
- 150000001768 cations Chemical class 0.000 claims description 3
- 229910001385 heavy metal Inorganic materials 0.000 claims description 3
- 239000010452 phosphate Substances 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 239000012141 concentrate Substances 0.000 claims description 2
- 230000002401 inhibitory effect Effects 0.000 claims description 2
- 230000008569 process Effects 0.000 abstract description 19
- 238000000926 separation method Methods 0.000 abstract description 7
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 62
- 239000002994 raw material Substances 0.000 description 12
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 10
- 238000011084 recovery Methods 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 8
- 239000003153 chemical reaction reagent Substances 0.000 description 7
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 7
- 229910052683 pyrite Inorganic materials 0.000 description 7
- 239000011028 pyrite Substances 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 6
- 235000011941 Tilia x europaea Nutrition 0.000 description 6
- 239000000571 coke Substances 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 6
- 239000004571 lime Substances 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 5
- 229910052751 metal Inorganic materials 0.000 description 5
- 239000002184 metal Substances 0.000 description 5
- 229910052500 inorganic mineral Inorganic materials 0.000 description 4
- 235000010755 mineral Nutrition 0.000 description 4
- 239000011707 mineral Substances 0.000 description 4
- 230000001590 oxidative effect Effects 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 230000002829 reductive effect Effects 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 239000002585 base Substances 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 239000013590 bulk material Substances 0.000 description 3
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 3
- 239000000292 calcium oxide Substances 0.000 description 3
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000012047 saturated solution Substances 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- APUPEJJSWDHEBO-UHFFFAOYSA-P ammonium molybdate Chemical compound [NH4+].[NH4+].[O-][Mo]([O-])(=O)=O APUPEJJSWDHEBO-UHFFFAOYSA-P 0.000 description 2
- 239000011609 ammonium molybdate Substances 0.000 description 2
- 235000018660 ammonium molybdate Nutrition 0.000 description 2
- 229940010552 ammonium molybdate Drugs 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 230000004907 flux Effects 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Inorganic materials O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 description 2
- LGQLOGILCSXPEA-UHFFFAOYSA-L nickel sulfate Chemical compound [Ni+2].[O-]S([O-])(=O)=O LGQLOGILCSXPEA-UHFFFAOYSA-L 0.000 description 2
- 229910000363 nickel(II) sulfate Inorganic materials 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 229910000851 Alloy steel Inorganic materials 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 1
- NBFQLHGCEMEQFN-UHFFFAOYSA-N N.[Ni] Chemical compound N.[Ni] NBFQLHGCEMEQFN-UHFFFAOYSA-N 0.000 description 1
- 239000005708 Sodium hypochlorite Substances 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
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 238000000498 ball milling Methods 0.000 description 1
- 229910052788 barium Inorganic materials 0.000 description 1
- DSAJWYNOEDNPEQ-UHFFFAOYSA-N barium atom Chemical compound [Ba] DSAJWYNOEDNPEQ-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 229910052748 manganese Inorganic materials 0.000 description 1
- 239000011572 manganese Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 1
- MEFBJEMVZONFCJ-UHFFFAOYSA-N molybdate Chemical compound [O-][Mo]([O-])(=O)=O MEFBJEMVZONFCJ-UHFFFAOYSA-N 0.000 description 1
- -1 molybdate ions Chemical class 0.000 description 1
- CWQXQMHSOZUFJS-UHFFFAOYSA-N molybdenum disulfide Chemical compound S=[Mo]=S CWQXQMHSOZUFJS-UHFFFAOYSA-N 0.000 description 1
- 229910052982 molybdenum disulfide Inorganic materials 0.000 description 1
- NKHCNALJONDGSY-UHFFFAOYSA-N nickel disulfide Chemical compound [Ni+2].[S-][S-] NKHCNALJONDGSY-UHFFFAOYSA-N 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- PTISTKLWEJDJID-UHFFFAOYSA-N sulfanylidenemolybdenum Chemical compound [Mo]=S PTISTKLWEJDJID-UHFFFAOYSA-N 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- LEONUFNNVUYDNQ-UHFFFAOYSA-N vanadium atom Chemical compound [V] LEONUFNNVUYDNQ-UHFFFAOYSA-N 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/04—Extraction of metal compounds from ores or concentrates by wet processes by leaching
- C22B3/12—Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic alkaline solutions
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G39/00—Compounds of molybdenum
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B23/00—Obtaining nickel or cobalt
- C22B23/02—Obtaining nickel or cobalt by dry 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
- C22B23/00—Obtaining nickel or cobalt
- C22B23/04—Obtaining nickel or cobalt by wet processes
- C22B23/0407—Leaching processes
- C22B23/0446—Leaching processes with an ammoniacal liquor or with a hydroxide of an alkali or alkaline-earth metal
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical 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
- C22B34/00—Obtaining refractory metals
- C22B34/30—Obtaining chromium, molybdenum or tungsten
- C22B34/34—Obtaining molybdenum
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Environmental & Geological Engineering (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Inorganic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
A method for separating and extracting molybdenum and nickel from carbon-containing nickel-molybdenum ore comprises the steps of adding water into the ground carbon-containing nickel-molybdenum ore for size mixing, adding sodium alkali, adjusting the initial alkalinity to 130-180 g/L, and adding into a pressure kettle for oxygen pressure leaching to enable molybdenum to enter a solution and inhibit nickel in slag; filtering to obtain leaching liquid and leaching slag, wherein the leaching liquid is sodium molybdate solution, and the leaching slag is nickel-containing slag; washing the leached slag with water to obtain washing slag, drying the washing slag, and then reducing and smelting to obtain a low nickel matte product; and removing impurities from the leaching solution, purifying to obtain a pure sodium molybdate solution, concentrating, crystallizing, filtering and drying to obtain a sodium molybdate product. The invention efficiently realizes the separation of molybdenum and nickel, realizes the separation of nickel and molybdenum in one step by applying an oxygen pressure alkaline leaching process, ensures that the nickel slag rate is more than 99 percent and the molybdenum leaching rate is more than 96 percent, and has the advantages of environmental friendliness, short reaction time and the like.
Description
Technical Field
The invention belongs to the technical field of metallurgical chemical industry. In particular to a process for separating molybdenum and nickel by oxygen pressure alkaline leaching for carbon-containing nickel-molybdenum ore, a method for producing sodium molybdate by removing impurities from leaching liquid and purifying, and a method for producing low nickel matte by reducing and smelting leaching slag.
Background
Nickel and molybdenum are important strategic resources in China, and have wide application in the fields of nonferrous steel alloys, chemical industry, aerospace and the like, and along with the rapid development of economy in China, the demand of nickel and molybdenum resources is continuously increased. The nickel-molybdenum resources are rich, but most of the nickel-molybdenum resources are associated with molybdenum ores, and the beneficiation pressure is high. Meanwhile, along with continuous exploitation and utilization of traditional nickel-molybdenum resources, the grade of ores is lower and lower, and the ores are seriously depleted.
The carbon-containing nickel-molybdenum ore is used as a multi-metal complex refractory mineral resource and is mainly distributed in sedimentary minerals in black shale layers of the systems of the West North Hunan and the Guanzhong Wu systems of Guizhou, and has the advantages of rich reserves and high grade. The nickel-molybdenum ore contains a great amount of carbon and sulfur, the molybdenum and the nickel mainly exist in the form of sulfide, and the molybdenum ore is mainly sulfur-molybdenum ore (MoS 2 ) The nickel mineral is needle nickel ore, nickel disulfide, and arsenical nickel ore. The ore is distributed in the carbon granules in the symbiotic way of ultrafine granularity and pyrite, and molybdenum and nickel are difficult to be effectively separated and extracted by the traditional physical mineral separation and metallurgical technology.
The disclosures of similar carbonaceous nickel molybdenum ore treatment processes are mainly as follows:
the Chinese patent publication No. CN101086034A discloses a process for extracting molybdenum by decomposing nickel-molybdenum ore by wet method. And (3) using an alkaline solution as a leaching solution to leach the finely ground nickel-molybdenum ore, and adding air, oxygen-enriched air or oxygen into the ore pulp in the leaching process. In the leaching process, molybdenum disulfide gradually reacts with oxygen to be converted into sodium molybdate to enter solution, vanadium, tungsten and the like contained in nickel-molybdenum ore also enter solution at the same time, sulfur is converted into sulfur-containing anions such as sulfate radical, sulfite radical, valuable metals such as nickel, copper and the like and iron are remained in slag, and the method can be further used for extracting nickel and copper.
The Chinese patent publication No. CN1267740A discloses a process for preparing molybdenum-nickel salt by directly leaching molybdenum-nickel symbiotic raw ore by weak base and oxidant. The technological process includes crushing and ball milling raw ore of molybdenum-nickel paragenetic ore, leaching with weak base and oxidant, filtering, evaporating ammonia, extracting solution to obtain ammonium molybdate, evaporating and concentrating the extracted solution to obtain nickel sulfate. The grade of raw ore molybdenum is 4.0% -8.0%, and nickel product is 2.5% -4.0% and sulfur is 23%. The total recovery rate of molybdenum and nickel prepared by the method is 80% and 88% respectively.
The Chinese patent with publication number of CN110643811A discloses a clean smelting process of nickel-molybdenum ore by a full wet method, which comprises the steps of potential-controlled ammonia activated leaching, leaching liquid extraction of molybdenum, nickel and the like. The nickel-molybdenum ore is leached by controlled potential ammonia activation to obtain leaching solution and leaching slag, the leaching solution adopts an ion exchange or induced crystallization mode to extract molybdenum, then adopts an ion exchange or solvent extraction mode to extract nickel, and respectively obtains ammonium molybdate and nickel sulfate products meeting national standard requirements, and the liquid is evaporated and crystallized after the extraction to obtain ammonium sulfate.
The Chinese patent publication No. CN109055727A discloses a method for comprehensively recovering nickel and molybdenum in nickel-molybdenum ore, which comprises the following steps: (1) Uniformly mixing nickel-molybdenum ore and pyrolusite, and then carrying out oxidizing roasting to obtain roasting clinker; (2) And adding the roasting clinker into an ammonia water solution for stirring reaction, and carrying out solid-liquid separation to obtain leaching solution containing nickel ammonia complex ions and molybdate ions and leaching slag containing manganese. Can solve SO 2 The problem of smoke pollution and the problem of high reduction cost of low-grade pyrolusite.
The traditional process for extracting the carbon-containing nickel-molybdenum ore is an oxidizing roasting-water leaching method, and has the problems of simple equipment, metal recovery rate, environmental pollution and the like, and the problems are eliminated. The oxygen pressure acid leaching technology, the sodium hypochlorite method and the like have the problems of large reagent consumption, long reaction time, long flow, environmental pollution and the like. The technical methods disclosed in the patent documents generally have the problems that nickel and molybdenum enter the leaching solution simultaneously, the production flow is long, the leaching solution contains high iron, magnesium and silicon as impurities, the purification difficulty is high, and the intermediate slag output in the smelting flow can be piled up only by carrying out innocent treatment.
Disclosure of Invention
The invention aims to solve the defects of the prior art and provide the method for separating and extracting the molybdenum and the nickel from the carbon-containing nickel-molybdenum ore, which can effectively separate the molybdenum and the nickel in the carbon-containing nickel-molybdenum ore under the condition of oxygen pressure alkaline leaching, has high recovery rate of the whole process of the molybdenum and the nickel, short reaction time and is environment-friendly.
In order to achieve the aim of the invention, the technical scheme adopted by the invention is as follows:
the method for separating and extracting molybdenum and nickel from the carbon-containing nickel-molybdenum ore comprises the following steps:
(1) Size mixing: mixing water and ground carbon-containing nickel-molybdenum ore, pulping to obtain ore pulp, adding sodium alkali into the ore pulp, and regulating the initial alkalinity to 130-180 g/L to obtain a pulp-blended liquid;
(2) Oxygen pressure alkaline leaching: adding the slurry into an autoclave, introducing oxygen to perform oxygen pressure leaching to enable molybdenum to enter the solution, and inhibiting nickel in slag; filtering to obtain leaching liquid and leaching slag, wherein the leaching liquid is sodium molybdate solution, and the leaching slag is nickel-containing slag;
(3) Washing leaching residues: washing the leached residues with water and then filtering to obtain washing residues and filtrate;
(4) Reduction smelting: drying the washing slag and then carrying out reduction smelting to obtain a low nickel matte product;
(5) Impurity removal and purification of leaching liquid: removing impurities from the leaching solution, and purifying to obtain a pure sodium molybdate solution;
(6) Concentrating and crystallizing: concentrating the pure sodium molybdate solution, cooling, crystallizing, filtering and drying to obtain sodium molybdate products and mother liquor.
Further, in the step (1), the finely ground carbon-containing nickel-molybdenum ore is-100 mesh carbon-containing nickel-molybdenum ore; the sodium alkali is sodium hydroxide or a mixture of sodium hydroxide and sodium carbonate; the mass ratio of the sodium alkali solution to the carbon-containing nickel-molybdenum ore is 4 ml-8 ml to 1g.
Further, the sodium hydroxide is industrial sodium hydroxide, and the main content of the sodium hydroxide is more than 99%; the sodium carbonate is industrial sodium carbonate, and the main content of the sodium carbonate is more than 99%.
Further, the carbon-containing nickel-molybdenum ore contains 2-6wt% of nickel, 2-7wt% of molybdenum, 19-21wt% of sulfur, 20-21.5wt% of silicon, 9.5-10.5wt% of carbon, 9.5-10.5wt% of iron and 3.2-3.5wt% of magnesium.
Further, in the step (2), the reaction temperature of the oxygen pressure alkaline leaching is 110-150 ℃, the reaction time is 3-6 hours, and the reaction pressure is 1.0-1.6 MP.
Further, in the step (3), the filtrate obtained by washing and filtering the leached residues is returned to the step (1) for size mixing.
Further, in the step (4), the smelting temperature of the reduction smelting washing slag is 1450-1650 ℃ and the smelting time is 2-6 h.
Further, in the step (5), the leaching solution is purified by adding a sodium sulfide solution into the leaching solution to remove heavy metal cation impurities in the sodium molybdate solution; then adding barium hydroxide to generate barium sulfate precipitate, and removing sulfate radical in the sodium molybdate solution; adding MgCl again 2 And (3) generating double salt precipitate by the solution and ammonia water, and removing phosphate radicals.
Further, in the step (6), the pure sodium molybdate solution concentrate is concentrated to a specific gravity of 1.4 to 1.6g/cm 3 Cooling and crystallizing, filtering and drying to obtain a sodium molybdate product and mother liquor, and returning the mother liquor to the step (1) for pulping.
The invention has the following beneficial effects:
(1) The oxygen pressure alkaline leaching realizes the high-efficiency separation of nickel and molybdenum in the carbon-containing nickel-molybdenum ore, nickel enters slag and molybdenum enters liquid, the whole process is simple and easy to implement, the flow is short, the leaching rate of molybdenum is more than 96%, the molybdenum content in slag is less than 0.25%, and the slag entering rate of nickel is more than 99%;
(2) The amount of waste gas generated in the reaction process of the oxygen pressure alkaline leaching process is small, and standard emission can be realized only by configuring a conventional waste gas absorbing device, so that the environment is basically not adversely affected;
(3) By adopting the oxygen pressure alkaline leaching process, the pressure kettle can use common carbon steel with lower manufacturing cost, and compared with the titanium and zirconium pressure kettle used in the oxygen pressure alkaline leaching process, the equipment investment can be reduced by more than 60 percent;
(4) In the oxygen pressure alkaline leaching process, more than 98% of silicon and iron and about 60% of magnesium enter slag, so that the difficulty of solution purification is reduced;
(5) In the process of adding barium hydroxide into the leaching solution to remove sulfate radical, generating barium sulfate precipitate to remove sulfate radical, and generating NaOH, so that the investment of sodium hydroxide can be reduced when the concentrated mother liquor returns to the pulp mixing;
(6) The low nickel matte is produced by adopting electric furnace reduction smelting, and the low nickel matte product containing about 23% nickel and about 55% iron can be produced, thereby meeting the quality requirements of the general low nickel matte product. The nickel content in the slag is less than or equal to 0.4 percent, and the nickel direct yield is more than or equal to 88.04 percent. The production flow is simple, and the smelting slag does not need to be subjected to harmless treatment.
According to the invention, by strictly controlling the process conditions, molybdenum is selectively oxidized into soluble molybdate to enter the liquid phase, nickel and the like are retained in the slag phase, and the separation of molybdenum and nickel is efficiently realized. The invention adopts the oxygen pressure alkali leaching technology to realize the separation of nickel and molybdenum in one step, the nickel slag entering rate is more than 99 percent, the molybdenum leaching rate is more than 96 percent, and the invention has the advantages of environmental protection, short reaction time and the like. The method effectively solves the problems that nickel and molybdenum in the existing process for extracting nickel and molybdenum from the carbon-containing nickel-molybdenum ore enter the leaching solution simultaneously, the production flow is long, the leaching solution contains iron, magnesium and silicon which are impurities, the purification difficulty is high, and the intermediate slag in the smelting flow is produced and can be piled up only by carrying out innocuous treatment.
Drawings
Fig. 1 is a process flow diagram of the present invention.
Detailed Description
The invention is further illustrated below in conjunction with examples.
A method for separating and extracting molybdenum and nickel from carbon-containing nickel-molybdenum ore, as shown in fig. 1, comprising the following steps:
(1) Mixing-100 mesh carbon-containing nickel-molybdenum ore and water according to the mass ratio of liquid to solid of 4-8 ml to 1g, and mixing to obtain ore pulp, adding sodium alkali into the ore pulp to adjust the initial alkalinity to 130-180 g/L, and obtaining the pulp-mixed liquid.
The carbon-containing nickel-molybdenum ore comprises 2-6wt% of nickel, 2-7wt% of molybdenum, 20.76wt% of sulfur, 21.18wt% of silicon, 9.51wt% of carbon, 9.62wt% of iron and 3.28wt% of magnesium.
The sodium base is sodium hydroxide or a mixture of sodium hydroxide and sodium carbonate. The sodium hydroxide is industrial sodium hydroxide, and the main content of the sodium hydroxide is more than 99%. The sodium carbonate is industrial sodium carbonate, and the main content of the sodium carbonate is more than 99%.
(2) Adding the slurry into an autoclave, introducing industrial oxygen to perform oxygen pressure alkaline leaching, controlling the reaction temperature to be 110-150 ℃ and the reaction time to be 3-6 hours, wherein the reaction pressure is 1.0-1.6 MPa, so that molybdenum enters the solution, nickel is inhibited in slag, and filtering to obtain leaching liquid and leaching slag, wherein the leaching liquid is mainly sodium molybdate solution, and the leaching slag is nickel-containing slag.
(3) Washing the leached slag with water, filtering to obtain washing slag and washing water, and returning the washing water to the step (1) for pulp mixing.
(4) And (5) after the washing slag is dried, feeding the ingredients into reduction smelting. During reduction smelting, the characteristics of silicon, iron, magnesium and calcium in leaching slag can be utilized to carry out reduction smelting production, and a large amount of flux can be saved. And (3) taking carbon remained in leaching slag as a partial reducing agent, taking silicon and magnesium as smelting flux, taking iron and sulfur as a nickel collector, and smelting at 1450-1650 ℃ for 2-6 h to obtain a low nickel matte product. The nickel content of the smelting slag is less than or equal to 0.4 percent, and the smelting slag can be piled up without innocent treatment.
(5) And removing impurities and purifying the leaching solution. Firstly, adding a sodium sulfide solution, and removing heavy metal cation impurities in the sodium molybdate solution; then adding barium hydroxide to generate barium sulfateRemoving sulfate radical in the sodium molybdate solution by precipitation; adding MgCl again 2 The solution and ammonia water are used for generating double salt precipitation, phosphate radical is removed, and pure sodium molybdate solution is obtained.
(6) Concentrating the pure sodium molybdate solution until the specific gravity of the concentrated solution is 1.4-1.6 g/cm 3 Cooling, crystallizing, filtering and drying to obtain a sodium molybdate product and mother liquor, wherein the mother liquor can be returned to the step (1) for pulping.
Example 1
The carbonaceous nickel-molybdenum ore used in this example was sampled from a location in Guizhou province, and bulk material was obtained. The materials are ground and sieved, and the total materials are sieved by a 100-mesh sieve. The reagent lime contains 80% of calcium oxide, 80% of coke grain carbon, 42% of iron in pyrite, and the rest of reagents are analytically pure.
The method for separating and extracting molybdenum and nickel from the carbon-containing nickel-molybdenum ore comprises the following steps:
(1) 400g of-100 mesh nickel-molybdenum ore containing 5.2wt percent of nickel, 4.52wt percent of molybdenum, 20.76wt percent of sulfur, 21.18wt percent of silicon, 9.51wt percent of carbon, 9.62wt percent of iron and 3.28wt percent of magnesium are added with water to pulp according to the liquid-solid volume mass ratio of 4:1 (ml/g), and sodium hydroxide is added to adjust the initial alkali concentration to 150g/L;
(2) Adding the slurry into a 3L autoclave, introducing oxygen for leaching, and leaching under the conditions of: the reaction pressure is 1.2Mpa, the reaction temperature is 120 ℃, the leaching time is 4 hours, leaching slurry is filtered to obtain leaching slag and filtrate, the leaching slag is washed to obtain 345g of nickel raw material containing 5.98% of nickel and 0.15% of molybdenum, the nickel slag rate is 99.18%, the molybdenum leaching rate is 97.13%, and the filtrate is sodium molybdate solution;
(3) After the nickel raw material is dried, 200g of the raw material is added with 12g of lime, 20g of coke particles and 26g of pyrite, and the mixture is evenly mixed and placed in a crucible for reduction smelting in a muffle furnace, wherein the smelting temperature is 1550 ℃ and the smelting time is 4 hours, 45.6g of low nickel matte product containing 23.08% of nickel and 55.95% of iron is obtained after smelting, the nickel content of slag is 0.40% and the nickel direct yield is 88.04%;
(4) Heating 1.575L of sodium molybdate solution to 80 ℃, adding sodium sulfide saturated solution, heating and boiling for 10 minutes, fully reacting, standing for 3 hours, filtering to obtain a solution after impurity removal, and purifying;
(5) Adding barium hydroxide, ba into the solution after impurity removal 2+ Is added with (a)The input is controlled according to 0.98 times of the sulfate content in the raw materials; adding MgCl again 2 The solution and ammonia water, the addition amount is 1.1 times of the theoretical amount, the pH value of the solution is about 9.5, the standing time is 5 hours, and 1.26L of pure sodium molybdate solution containing 13.52g/L of molybdenum is obtained after filtration;
(6) Concentrating 1.26L pure sodium molybdate solution to a specific gravity of 1.48g/cm 3 Cooling, crystallizing, filtering and drying to obtain Na containing 39.25% of molybdenum 2 MoO 4 .2H 2 75.8g of O product and mother liquor. The recovery rate of molybdenum is 99%. And (5) returning the mother liquor to the step (1) for size mixing.
The total recovery rate of molybdenum in the embodiment reaches 94.22%, and the quality of sodium molybdate products reaches the non-ferrous metal industry standard YS/T1311-2019 secondary standard, as shown in Table 1.
Table 1 non-ferrous industry Standard compares with example 1 product (unit: mass fraction/%)
Example 2
The carbonaceous nickel-molybdenum ore used in this example was sampled from a location in Guizhou province, and bulk material was obtained. The materials are ground and sieved, and the total materials are sieved by a 100-mesh sieve. The reagent lime contains 80% of calcium oxide, 80% of coke grain carbon, 42% of iron in pyrite, and the rest of reagents are analytically pure.
The method for separating and extracting molybdenum and nickel from the carbon-containing nickel-molybdenum ore comprises the following steps:
(1) 400g of nickel molybdenum ore with the particle size of minus 100 meshes, which contains 5.98 weight percent of nickel, 6.95 weight percent of molybdenum, 19.36 weight percent of sulfur, 20.45 weight percent of silicon, 10.35 weight percent of carbon, 9.62 weight percent of iron and 3.46 weight percent of magnesium, is added with water to be slurried according to the liquid-solid volume mass ratio of 8:1 (ml/g), and mixed alkali (sodium hydroxide: sodium carbonate=7:3) of sodium hydroxide and sodium carbonate is added, and the initial alkalinity is regulated to 180g/L, so as to obtain a slurry-mixed liquid;
(2) Adding the slurry after the slurry mixing into a 3L autoclave, and introducing industrial oxygen for leaching under the conditions of: the reaction pressure is 1.5Mpa, the reaction temperature is 150 ℃, the leaching time is 6 hours, leaching slurry is filtered to obtain leaching slag and filtrate, the leaching slag is washed to obtain 351g of nickel raw material containing 6.76% nickel and 0.18% molybdenum, the nickel slag rate is 99.20%, the molybdenum leaching rate is 97.73%, and the filtrate is sodium molybdate solution;
(3) Drying a nickel raw material, taking 200g of the dried nickel raw material, adding 10g of lime, 22g of coke particles and 30g of pyrite, uniformly mixing, placing the mixture into a crucible, and carrying out reduction smelting in a muffle furnace at 1650 ℃ for 2 hours to obtain 42.1g of a low nickel matte product containing 28.47% nickel and 53.67% iron, wherein the nickel content of slag is 0.38% and the nickel direct yield is 88.44%;
(4) Adding 3.16L of sodium molybdate solution, heating to 80 ℃, adding sodium sulfide saturated solution, heating and boiling for 10 minutes, fully reacting, standing for 5 hours, filtering to obtain a solution after impurity removal, and purifying;
(5) Adding barium hydroxide and Ba into the solution after impurity removal 2+ The addition amount of the catalyst is controlled according to 0.98 times of the sulfate content in the raw materials; adding MgCl 2 The solution and ammonia water, the addition amount is 1.1 times of the theoretical amount, the pH value of the solution is about 9.5, the standing time is 6 hours, and 2.45L of pure sodium molybdate solution containing 11.10g/L of molybdenum is obtained after filtration;
(6) Concentrating the 2.45L pure sodium molybdate solution to a specific gravity of 1.58g/cm 3 Cooling, crystallizing, filtering and drying to obtain Na containing 39.46% of molybdenum 2 MoO 4 .2H 2 120g of O product and mother liquor, and returning the mother liquor to the step (1) for size mixing. The recovery rate of molybdenum is 98.76%.
The total recovery rate of molybdenum in the embodiment is 94.17%, and the quality of sodium molybdate products reaches the non-ferrous metal industry standard YS/T1311-2019 secondary standard, as shown in Table 2.
Table 2 non-ferrous industry Standard example 2 product comparison (Unit: mass fraction/%)
Example 3
The carbonaceous nickel-molybdenum ore used in this example was sampled from a location in Guizhou province, and bulk material was obtained. The materials are ground and sieved, and the total materials are sieved by a 100-mesh sieve. The reagent lime contains 80% of calcium oxide, 80% of coke grain carbon, 42% of iron in pyrite, and the rest of reagents are analytically pure.
The method for separating and extracting molybdenum and nickel from the carbon-containing nickel-molybdenum ore comprises the following treatment method:
(1) 400g of-100 mesh nickel-molybdenum ore containing 2.52wt% of nickel, 2.45wt% of molybdenum, 19.87wt% of sulfur, 20.36wt% of silicon, 9.78wt% of carbon, 10.24wt% of iron and 3.45wt% of magnesium is added with water to pulp according to a liquid-solid volume mass ratio of 4:1 (ml/g), and sodium hydroxide is added to adjust the initial alkalinity to 130g/L, so as to obtain pulp-mixed liquid;
(2) Adding the slurry after the slurry mixing into a 3L autoclave, introducing oxygen for leaching, wherein the leaching conditions are as follows: the reaction pressure is 1.0Mpa, the reaction temperature is 110 ℃, the leaching time is 3 hours, leaching slurry is filtered to obtain leaching slag and filtrate, the leaching slag is washed to obtain 348g of nickel raw material containing 2.88% of nickel and 0.11% of molybdenum, the nickel slag rate is 99.43%, the molybdenum leaching rate is 97%, and the filtrate is sodium molybdate solution;
(3) After the nickel raw material is dried, 200g of the raw material is added with 12g of lime, 15g of coke particles and 12g of pyrite, and the mixture is evenly mixed and placed in a crucible to be reduced and smelted in a muffle furnace, wherein the smelting temperature is 1450 ℃, the smelting time is 6 hours, and 24.80g of low nickel matte product containing 20.53% of nickel and 52.35% of iron is obtained after smelting, the nickel content in slag is 0.15% and the nickel direct yield is 88.39%;
(4) Adding 1.56L of sodium molybdate solution, heating to 80 ℃, adding sodium sulfide saturated solution, heating and boiling for 10 minutes, fully reacting, standing for 4 hours, filtering to obtain a solution after impurity removal, and purifying;
(5) Adding barium hydroxide and Ba into the solution after impurity removal 2+ The addition amount of the catalyst is controlled according to 0.98 times of the sulfate content in the raw materials; adding MgCl 2 The solution and ammonia water, the addition amount is 1.1 times of the theoretical amount, the pH value of the solution is about 9.5, the standing time is 4 hours, and 1.21L of pure sodium molybdate solution containing 7.8g/L of molybdenum is obtained after filtration;
(6) Concentrating 1.21L pure sodium molybdate solution to a specific gravity of 1.6g/cm 3 Cooling, crystallizing, filtering and drying to obtain Na containing 39.05% of molybdenum 2 MoO 4 .2H 2 44.17g of O product and mother liquor, and returning the mother liquor to the step (1) for pulping. The recovery rate of molybdenum is 98.68 percent.
The total recovery rate of molybdenum in the embodiment is 93.85%, and the quality of sodium molybdate products reaches the non-ferrous metal industry standard YS/T1311-2019 secondary standard, as shown in Table 3.
Table 3 comparison of nonferrous industry Standard with example 3 product (Unit: mass fraction/%)
The percentage values of the components present in the present invention are mass percentages unless otherwise indicated.
Claims (9)
1. The method for separating and extracting molybdenum and nickel from the carbon-containing nickel-molybdenum ore is characterized by comprising the following steps of:
(1) Size mixing: mixing water and ground carbon-containing nickel-molybdenum ore, pulping to obtain ore pulp, adding sodium alkali into the ore pulp, and regulating the initial alkalinity to 130-180 g/L to obtain a pulp-blended liquid;
(2) Oxygen pressure alkaline leaching: adding the slurry into an autoclave, introducing oxygen to perform oxygen pressure leaching to enable molybdenum to enter the solution, and inhibiting nickel in slag; filtering to obtain leaching liquid and leaching slag, wherein the leaching liquid is sodium molybdate solution, and the leaching slag is nickel-containing slag;
(3) Washing leaching residues: washing the leached residues with water and then filtering to obtain washing residues and filtrate;
(4) Reduction smelting: drying the washing slag and then carrying out reduction smelting to obtain a low nickel matte product;
(5) Impurity removal and purification of leaching liquid: removing impurities from the leaching solution, and purifying to obtain a pure sodium molybdate solution;
(6) Concentrating and crystallizing: concentrating the pure sodium molybdate solution, cooling, crystallizing, filtering and drying to obtain sodium molybdate products and mother liquor.
2. The method for separating and extracting molybdenum and nickel from carbon-containing nickel-molybdenum ore according to claim 1, wherein in the step (1), the finely ground carbon-containing nickel-molybdenum ore is-100 mesh carbon-containing nickel-molybdenum ore; the sodium alkali is sodium hydroxide or a mixture of sodium hydroxide and sodium carbonate; the mass ratio of the sodium alkali solution to the carbon-containing nickel-molybdenum ore is 4 ml-8 ml to 1g.
3. The method for separating and extracting molybdenum and nickel from carbon-containing nickel-molybdenum ore according to claim 2, wherein the sodium hydroxide is industrial sodium hydroxide, and the main content of the sodium hydroxide is more than 99%; the sodium carbonate is industrial sodium carbonate, and the main content of the sodium carbonate is more than 99%.
4. The method for separating and extracting molybdenum and nickel from carbon-containing nickel-molybdenum ore according to claim 1, 2 or 3, wherein the carbon-containing nickel-molybdenum ore contains 2-6wt% of nickel, 2-7wt% of molybdenum, 19-21wt% of sulfur, 20-21.5wt% of silicon, 9.5-10.5wt% of carbon, 9.5-10.5wt% of iron and 3.2-3.5wt% of magnesium.
5. The method for separating and extracting molybdenum and nickel from carbon-containing nickel-molybdenum ore according to claim 1, wherein in the step (2), the reaction temperature of the oxygen pressure alkaline leaching is 110-150 ℃, the reaction time is 3-6 hours, and the reaction pressure is 1.0-1.6 MP.
6. The method for separating and extracting molybdenum and nickel from a carbon-containing nickel-molybdenum ore according to claim 1, wherein in the step (3), the leaching residue washing and filtering filtrate is returned to the step (1) for size mixing.
7. The method for separating and extracting molybdenum and nickel from carbon-containing nickel-molybdenum ore according to claim 1, wherein in the step (4), the smelting temperature of the reduction smelting washing slag is 1450-1650 ℃ and the smelting time is 2-6 h.
8. The method for separating and extracting molybdenum and nickel from carbon-containing nickel-molybdenum ore according to claim 1, wherein in the step (5), the leaching solution is purified by adding sodium sulfide solution into the leaching solution to remove heavy metal cation impurities in the sodium molybdate solution; then adding barium hydroxide to generate barium sulfate precipitate, and removing sulfate radical in the sodium molybdate solution; adding MgCl again 2 And (3) generating double salt precipitate by the solution and ammonia water, and removing phosphate radicals.
9. The method for separating and extracting molybdenum and nickel from a carbon-containing nickel-molybdenum ore according to claim 1, wherein in the step (6), the pure sodium molybdate solution concentrate is concentrated to a specific gravity of 1.4 to 1.6g/cm 3 Cooling and crystallizing, filtering and drying to obtain a sodium molybdate product and mother liquor, and returning the mother liquor to the step (1) for pulping.
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