CN110117721B - Method for extracting valuable metals from sulfuric acid residue by phosphoric acid leaching-extraction - Google Patents
Method for extracting valuable metals from sulfuric acid residue by phosphoric acid leaching-extraction Download PDFInfo
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- CN110117721B CN110117721B CN201910413894.XA CN201910413894A CN110117721B CN 110117721 B CN110117721 B CN 110117721B CN 201910413894 A CN201910413894 A CN 201910413894A CN 110117721 B CN110117721 B CN 110117721B
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- sulfuric acid
- phosphoric acid
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- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid group Chemical group S(O)(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 67
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 title claims abstract description 58
- 238000000605 extraction Methods 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 31
- 229910000147 aluminium phosphate Inorganic materials 0.000 title claims abstract description 29
- 229910052751 metal Inorganic materials 0.000 title claims abstract description 25
- 239000002184 metal Substances 0.000 title claims abstract description 21
- 150000002739 metals Chemical class 0.000 title claims abstract description 18
- 238000002386 leaching Methods 0.000 claims abstract description 55
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims abstract description 52
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims abstract description 32
- 229910052802 copper Inorganic materials 0.000 claims abstract description 32
- 239000010949 copper Substances 0.000 claims abstract description 32
- 239000010941 cobalt Substances 0.000 claims abstract description 28
- 229910017052 cobalt Inorganic materials 0.000 claims abstract description 28
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims abstract description 28
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 26
- 238000000926 separation method Methods 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 17
- 238000000498 ball milling Methods 0.000 claims abstract description 14
- 239000002253 acid Substances 0.000 claims abstract description 8
- FQKMRXHEIPOETF-UHFFFAOYSA-N F.OP(O)(O)=O Chemical compound F.OP(O)(O)=O FQKMRXHEIPOETF-UHFFFAOYSA-N 0.000 claims abstract description 6
- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical compound [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 claims description 31
- 239000005955 Ferric phosphate Substances 0.000 claims description 27
- 229940032958 ferric phosphate Drugs 0.000 claims description 27
- 229910000399 iron(III) phosphate Inorganic materials 0.000 claims description 27
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims description 18
- 239000012071 phase Substances 0.000 claims description 17
- 239000003818 cinder Substances 0.000 claims description 14
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 claims description 14
- 229910052683 pyrite Inorganic materials 0.000 claims description 14
- 239000011028 pyrite Substances 0.000 claims description 14
- 239000003085 diluting agent Substances 0.000 claims description 8
- 239000003350 kerosene Substances 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 8
- 238000005406 washing Methods 0.000 claims description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 239000012074 organic phase Substances 0.000 claims description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 abstract description 43
- 229910052742 iron Inorganic materials 0.000 abstract description 22
- 238000011084 recovery Methods 0.000 abstract description 18
- 239000002893 slag Substances 0.000 abstract description 17
- 238000009776 industrial production Methods 0.000 abstract description 2
- 230000002378 acidificating effect Effects 0.000 abstract 1
- BMTOKWDUYJKSCN-UHFFFAOYSA-K iron(3+);phosphate;dihydrate Chemical compound O.O.[Fe+3].[O-]P([O-])([O-])=O BMTOKWDUYJKSCN-UHFFFAOYSA-K 0.000 abstract 1
- 238000004519 manufacturing process Methods 0.000 abstract 1
- 229910021645 metal ion Inorganic materials 0.000 description 14
- 239000000047 product Substances 0.000 description 14
- 239000002994 raw material Substances 0.000 description 11
- 239000007788 liquid Substances 0.000 description 8
- 239000003921 oil Substances 0.000 description 7
- 239000002245 particle Substances 0.000 description 7
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 6
- 235000011114 ammonium hydroxide Nutrition 0.000 description 6
- 239000012153 distilled water Substances 0.000 description 6
- 239000000706 filtrate Substances 0.000 description 6
- 238000001914 filtration Methods 0.000 description 6
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 5
- 229910052500 inorganic mineral Inorganic materials 0.000 description 5
- 239000011707 mineral Substances 0.000 description 5
- 229910000398 iron phosphate Inorganic materials 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000010494 dissociation reaction Methods 0.000 description 2
- 230000005593 dissociations Effects 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- -1 hydrogen ions Chemical class 0.000 description 2
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical group O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 2
- 229910052604 silicate mineral Inorganic materials 0.000 description 2
- 229910052710 silicon Inorganic materials 0.000 description 2
- 239000010703 silicon Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000002441 X-ray diffraction Methods 0.000 description 1
- RAOSIAYCXKBGFE-UHFFFAOYSA-K [Cu+3].[O-]P([O-])([O-])=O Chemical compound [Cu+3].[O-]P([O-])([O-])=O RAOSIAYCXKBGFE-UHFFFAOYSA-K 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 150000004645 aluminates Chemical class 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 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
- 229910000152 cobalt phosphate Inorganic materials 0.000 description 1
- ZBDSFTZNNQNSQM-UHFFFAOYSA-H cobalt(2+);diphosphate Chemical compound [Co+2].[Co+2].[Co+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O ZBDSFTZNNQNSQM-UHFFFAOYSA-H 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 229910052595 hematite Inorganic materials 0.000 description 1
- 239000011019 hematite Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 238000009854 hydrometallurgy Methods 0.000 description 1
- GPRLSGONYQIRFK-UHFFFAOYSA-N hydron Chemical compound [H+] GPRLSGONYQIRFK-UHFFFAOYSA-N 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 150000002500 ions Chemical group 0.000 description 1
- 150000002505 iron Chemical class 0.000 description 1
- LIKBJVNGSGBSGK-UHFFFAOYSA-N iron(3+);oxygen(2-) Chemical compound [O-2].[O-2].[O-2].[Fe+3].[Fe+3] LIKBJVNGSGBSGK-UHFFFAOYSA-N 0.000 description 1
- GELKBWJHTRAYNV-UHFFFAOYSA-K lithium iron phosphate Chemical compound [Li+].[Fe+2].[O-]P([O-])([O-])=O GELKBWJHTRAYNV-UHFFFAOYSA-K 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910000159 nickel phosphate Inorganic materials 0.000 description 1
- JOCJYBPHESYFOK-UHFFFAOYSA-K nickel(3+);phosphate Chemical compound [Ni+3].[O-]P([O-])([O-])=O JOCJYBPHESYFOK-UHFFFAOYSA-K 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/37—Phosphates of heavy metals
- C01B25/375—Phosphates of heavy metals of iron
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B15/00—Obtaining copper
- C22B15/0063—Hydrometallurgy
- C22B15/0065—Leaching or slurrying
- C22B15/0067—Leaching or slurrying with acids or salts thereof
- C22B15/0069—Leaching or slurrying with acids or salts thereof containing halogen
-
- 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
- C22B23/0415—Leaching processes with acids or salt solutions except ammonium salts solutions
- C22B23/0423—Halogenated acids or salts thereof
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
- C22B3/38—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds containing phosphorus
- C22B3/384—Pentavalent phosphorus oxyacids, esters thereof
- C22B3/3846—Phosphoric acid, e.g. (O)P(OH)3
-
- 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
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/006—Wet processes
- C22B7/007—Wet processes by acid leaching
-
- 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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- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Geochemistry & Mineralogy (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
本发明公开了一种硫酸渣磷酸浸出‑萃取提取有价金属的方法，该方法是将硫酸渣经过球磨处理后，采用磷酸‑氢氟酸混合酸浸出，所得浸出渣经过水洗得到二水磷酸铁，所得浸出液调节pH值至弱酸性后，萃取分离回收铜、钴和镍；该方法实现了硫酸渣中铁、镍、钴、铜等有价金属元素的高效综合回收利用，且该方法操作简单、生产成本低、环境友好，满足工业化生产要求。The invention discloses a method for extracting valuable metals by phosphoric acid leaching-extraction from sulfuric acid residues. The method is that after ball milling the sulfuric acid residues, the mixed acid of phosphoric acid-hydrofluoric acid is used for leaching, and the obtained leaching residues are washed with water to obtain iron phosphate dihydrate. , after the obtained leachate is adjusted to weakly acidic pH value, extraction, separation and recovery of copper, cobalt and nickel; the method realizes the efficient and comprehensive recovery and utilization of valuable metal elements such as iron, nickel, cobalt, copper and the like in the sulfuric acid slag, and the method is simple to operate, The production cost is low, the environment is friendly, and it meets the requirements of industrial production.
Description
Technical Field
The invention relates to a method for treating sulfuric acid residue, in particular to a method for efficiently extracting and separating valuable metals from sulfuric acid residue by adopting phosphoric acid leaching-extraction, belonging to the field of mineral processing and hydrometallurgy.
Background
The sulfuric acid residue, also called pyrite cinder, is industrial waste residue produced in the process of producing sulfuric acid. The pyrite cinder contains rich iron and partial elements such as calcium, silicon, copper, sulfur and the like, but the pyrite cinder has low content of nonferrous metals, and metal minerals and gangue minerals are mutually wrapped, so that the comprehensive utilization of the pyrite cinder is limited. About 8000 million tons of sulfuric acid residues are discharged in China every year, and the national accumulated reserves are over hundred million tons. The accumulation of a large amount of sulfate slag wastes land resources and causes serious pollution to the environment. In addition, the utilization rate of the sulfate slag in some developed countries is close to 100%, but the utilization rate of the sulfate slag in China is less than 50%. At present, the comprehensive utilization approach of the pyrite cinder is mainly used as a raw material of sintered pellets.
However, the pyrite cinder contains a large amount of iron elements, and also contains valuable metals such as nickel, cobalt, copper and the like, for example, in the copper hilly area of Anhui, the copper content in part of the pyrite cinder is higher than 0.6%, the cobalt content is higher than 0.3%, and the pyrite cinder has extremely high recovery value. On the other hand, the pyrite cinder is directly used as a blast furnace ironmaking raw material, wherein the copper content is far higher than the requirement of blast furnace ironmaking furnace burden, and a small amount of copper element enters molten iron to influence the mechanical property of subsequent processed steel.
The lithium iron phosphate battery has the advantages of excellent charge and discharge performance, long service life, good thermal stability and the like, thereby having important market share in the market. The iron phosphate is one of the most important raw materials for preparing the iron phosphate, and the preparation method mainly comprises a solution synthesis method, wherein iron salt and phosphoric acid are used as raw materials to react to obtain a ferric phosphate dihydrate product. However, the existing iron phosphate preparation process has high cost and needs high-quality iron raw materials.
Disclosure of Invention
Aiming at the problems of comprehensive utilization of the sulfuric acid residues, low economic value of a value-added processing technology and the like in the prior art, the invention aims to provide the method for efficiently separating and extracting the valuable metals such as iron, copper, cobalt, nickel and the like in the sulfuric acid residues by adopting phosphoric acid leaching-extraction.
In order to realize the technical purpose, the invention provides a method for extracting valuable metals from sulfuric acid residues by phosphoric acid leaching-extraction.
In the preferable scheme, the sulfuric acid residue is ball-milled until the fineness meets the requirement that the mass percentage content of the fraction smaller than 0.037mm is larger than 80%. The ball milling and leaching process can adopt a common ball milling process in the prior art, such as wet ball milling, the sulfuric acid residue is subjected to ball milling mechanical action to destroy the close embedding relationship among different components in the sulfuric acid residue, and the ball milling to a proper particle size is favorable for the subsequent leaching process, so that the metal leaching rate is improved.
In the preferable scheme, the concentration of phosphoric acid in the phosphoric acid-hydrofluoric acid mixed acid is 1.5-3.8 mol/L, and the concentration of hydrofluoric acid is 0.01-0.03 mol/L. The concentration of phosphoric acid and the concentration of hydrogen ions in the whole system are controlled to ensure that iron oxide is dissolved and then converted into ferric phosphate dihydrate in the leaching process, the ferric phosphate dihydrate precipitates and is enriched in a slag phase, and other metal ions still exist in a leachate in the form of metal ions, so that the separation of the ferric phosphate and other metal ions can be realized through simple solid-liquid separation; a small amount of hydrofluoric acid is doped into phosphoric acid, so that on one hand, the effect of destroying silicate minerals in the sulfuric acid slag can be achieved, the dissociation and dissolution of metals wrapped by gangue minerals such as silicate and the like can be promoted, the leaching rate is improved, and on the other hand, partial hydrogen ion concentration is provided, and the pH value of a leaching system is maintained.
In a preferred embodiment, the leaching conditions are as follows: the liquid-solid ratio is 8-16 mL/g, the leaching temperature is 80-145 ℃, and the leaching time is 4-12 h. Higher metal leaching rates can be achieved under the preferred leaching conditions.
Preferably, the leaching residue is washed by water until the pH value is more than 6.
In a preferable scheme, the pH value of the leachate is adjusted to 4.5-6. The pH is adjusted using a common alkaline solution, such as ammonia.
Preferably, the extractant used in the extraction separation process comprises at least one of P204 and P507.
In a preferred embodiment, the extraction separation conditions are as follows: the volume percentage concentration of the extracting agent in the organic phase is 2-5%, and the diluting agent is kerosene; the volume ratio of the water phase to the oil phase is 1-3.5: 1, the extraction temperature is room temperature, and the extraction time is 30-60 min.
The sulfuric acid residue is waste residue after high-temperature oxidation roasting treatment, wherein iron mainly exists in a hematite (ferric oxide) form, other valuable metals such as copper, nickel, cobalt and the like mostly enter an iron oxide crystal lattice in an oxide form or a doping form, and silicon and aluminum elements mainly form silicate, aluminate and the like and are in a close embedding and mutual wrapping relationship. In order to realize extraction of valuable metal elements and separation of the valuable metal elements from impurity elements in the sulfuric acid slag, firstly, ball milling is carried out, mechanical energy is adopted to destroy the close embedding relationship among different components in the sulfuric acid slag, on the basis, phosphoric acid-hydrofluoric acid mixed acid is adopted for leaching, and by utilizing the solubility difference of ferric phosphate, copper phosphate, nickel phosphate and cobalt phosphate under different phosphoric acid concentrations and pH conditions, ferric oxide and other metal oxides can be promoted to be dissolved by controlling the adjustment of the phosphoric acid concentration and the pH value in the leaching process, metal ions are dissolved into a solution, iron ions are selectively precipitated in a ferric phosphate dihydrate form, and other metals still exist in a metal ion form, so that the separation of the ferric phosphate and other metal ions can be realized; a small amount of hydrofluoric acid is added into the mixed acid to destroy silicate minerals in the sulfuric acid residue, further promote dissociation and dissolution of valuable metal ions wrapped in gangue minerals, and improve the leaching rate. After leaching, the iron phosphate and other metal ions can be separated by a physical means of solid-liquid separation, and the separation, extraction and recovery of valuable metal elements are realized by subsequent combination of extraction. Therefore, the valuable metals in the pyrite cinder are separated and recovered.
Compared with the prior art, the technical scheme of the invention has the following beneficial effects:
1) according to the method, the sulfuric acid residues containing valuable metals such as copper, nickel and cobalt are taken as treatment objects, the sulfuric acid residues are subjected to acid leaching by using phosphoric acid-hydrofluoric acid mixture, the acid concentration and the pH value are regulated, the separation and recovery of the valuable metals such as iron, copper, cobalt and nickel in the sulfuric acid residues are realized, the ferric phosphate material is synchronously prepared, the comprehensive utilization and value-added processing of the sulfuric acid residues are realized, the recovery rates of the iron, the copper, the cobalt and the nickel are all higher than 90%, and the method has higher economic value compared with the traditional method.
2) The preparation method for the comprehensive utilization of the pyrite cinder, provided by the invention, has the advantages of simple operation, low energy consumption and low cost, and is easy to realize industrial production.
Drawings
FIG. 1 is a process flow diagram of the present invention;
fig. 2 is the XRD pattern of the product prepared in example 1.
Detailed Description
The following examples are intended to further illustrate the present disclosure, but not to limit the scope of the claims.
Comparative example 1
Sulfuric acid slag (iron grade 57.3%, copper, cobalt and nickel contents of 0.6%, 0.3% and 0.5% respectively) of a certain sulfuric acid plant is used as a raw material to carry out phosphoric acid leaching, and leaching conditions are as follows: the concentration of phosphoric acid is 1.5mol/L, the concentration of hydrofluoric acid is 0.03mol/L, the liquid-solid ratio is 16ml/g, the leaching temperature is 80 ℃, the leaching time is 12 hours, and after the leaching is finished, the solid-liquid separation is carried out by filtering; washing the synthesized product with distilled water until the pH value of the filtrate is more than 6, and obtaining a product, namely battery-grade ferric phosphate dihydrate, wherein the purity of the ferric phosphate is 98.3%, the median particle size is 4.95 mu m, the recovery rate of the iron is 92.9%, and the content of copper and cobalt in the ferric phosphate exceeds 0.1%; adjusting the pH value of the leachate to 4.5 by using ammonia water, and then extracting valuable metal ions in the leachate by using an organic extractant, wherein the extraction conditions are as follows: the concentration of the extractant P204 is 2.0 percent, the diluent is kerosene, the water phase/oil phase ratio is 1:1, the extraction temperature is room temperature, the extraction time is 30min, and the recovery rates of valuable elements of copper, cobalt and nickel in the whole process flow are 78.2 percent, 65.3 percent and 83.9 percent respectively.
Comparative example 2
The method comprises the following steps of taking sulfuric acid residues (the iron grade is 57.3%, the contents of copper, cobalt and nickel are respectively 0.6%, 0.3% and 0.5%) of a certain sulfuric acid plant as raw materials, firstly carrying out ball milling on the sulfuric acid residues until the proportion of minus 0.037mm is higher than 80%, and carrying out phosphoric acid leaching under the leaching conditions that: the concentration of phosphoric acid is 1.5mol/L, the liquid-solid ratio is 16ml/g, the leaching temperature is 120 ℃, the leaching time is 8 hours, and after the leaching is finished, solid-liquid separation is carried out by filtering; washing the synthesized product with distilled water until the pH value of the filtrate is more than 6, and obtaining a product, namely battery-grade ferric phosphate dihydrate, wherein the purity of the ferric phosphate is 99.3%, the median particle size is 4.86 mu m, the recovery rate of the iron is 93.3%, and the content of copper, cobalt and nickel in the ferric phosphate exceeds 0.1%; adjusting the pH value of the leachate to 4.5 by using ammonia water, and then extracting valuable metal ions in the leachate by using an organic extractant, wherein the extraction conditions are as follows: the concentration of the extractant P507 is 2.0 percent, the diluent is kerosene, the water phase/oil phase ratio is 2:1, the extraction temperature is room temperature, the extraction time is 60min, and the recovery rates of valuable elements of copper, cobalt and nickel in the whole process flow are 73.2 percent, 70.3 percent and 83.3 percent respectively.
Example 1:
taking sulfuric acid slag (iron grade 57.3%, copper, cobalt and nickel contents are respectively 0.6%, 0.3% and 0.5%) of a certain sulfuric acid plant as a raw material, firstly, ball-milling the sulfuric acid slag until the proportion of-0.037 mm is higher than 80%, and the concentration of ball-milled ore pulp is 40%; then phosphoric acid leaching is carried out, and leaching conditions are as follows: the concentration of phosphoric acid is 1.5mol/L, the concentration of hydrofluoric acid is 0.03mol/L, the liquid-solid ratio is 16ml/g, the leaching temperature is 80 ℃, the leaching time is 12 hours, and after the leaching is finished, the solid-liquid separation is carried out by filtering; washing the synthesized product with distilled water until the pH value of the filtrate is more than 6, and obtaining a product, namely battery-grade ferric phosphate dihydrate, wherein the purity of the ferric phosphate is 99.3%, the median particle size is 4.86 mu m, the recovery rate of the iron is 93.3%, and the contents of copper, cobalt and nickel in the ferric phosphate are all lower than 0.005%; adjusting the pH value of the leachate to 4.5 by using ammonia water, and then extracting valuable metal ions in the leachate by using an organic extractant, wherein the extraction conditions are as follows: the concentration of the extractant P204 is 2.0 percent, the diluent is kerosene, the water phase/oil phase ratio is 1:1, the extraction temperature is room temperature, the extraction time is 30min, and the recovery rates of the valuable elements of copper, cobalt and nickel in the whole process flow are 93.2 percent, 95.3 percent and 91.9 percent respectively.
Example 2:
taking sulfuric acid slag (iron grade 57.3%, copper, cobalt and nickel contents are respectively 0.6%, 0.3% and 0.5%) of a certain sulfuric acid plant as a raw material, firstly, ball-milling the sulfuric acid slag until the proportion of-0.037 mm is higher than 80%, and the concentration of ball-milled ore pulp is 50%; then phosphoric acid leaching is carried out, and leaching conditions are as follows: the concentration of phosphoric acid is 3.8mol/L, the concentration of hydrofluoric acid is 0.01mol/L, the liquid-solid ratio is 8ml/g, the leaching temperature is 100 ℃, the leaching time is 4 hours, and after the leaching is finished, the solid-liquid separation is carried out by filtering; washing the synthesized product with distilled water until the pH value of the filtrate is more than 6, and obtaining a product, namely battery-grade ferric phosphate dihydrate, wherein the purity of the ferric phosphate is 99.2%, the median particle size is 5.03 mu m, the recovery rate of the iron is 94.1%, and the contents of copper, cobalt and nickel in the ferric phosphate are all lower than 0.003%; adjusting the pH value of the leachate to 6 by using ammonia water, and then extracting valuable metal ions in the leachate by using an organic extracting agent, wherein the extraction conditions are as follows: the concentration of the extractant P507 is 5 percent, the diluent is kerosene, the water phase/oil phase ratio is 3.5:1, the extraction temperature is room temperature, the extraction time is 60min, and the recovery rates of the valuable elements of copper, cobalt and nickel in the whole process flow are 95.1 percent, 96.2 percent and 93.8 percent respectively.
Example 3:
taking sulfuric acid slag (iron grade 54.2%, copper, cobalt and nickel contents are respectively 0.7%, 0.2% and 0.2%) of a certain sulfuric acid plant as a raw material, firstly, ball-milling the sulfuric acid slag until the proportion of-0.037 mm is higher than 80%, and the concentration of ball-milled ore pulp is 55%; then phosphoric acid leaching is carried out, and leaching conditions are as follows: the concentration of phosphoric acid is 2.6mol/L, the concentration of hydrofluoric acid is 0.02mol/L, the liquid-solid ratio is 16ml/g, the leaching temperature is 145 ℃, the leaching time is 6 hours, and after the leaching is finished, the solid-liquid separation is carried out by filtering; washing the synthesized product with distilled water until the pH value of the filtrate is more than 6, and obtaining a product, namely battery-grade ferric phosphate dihydrate, wherein the purity of the ferric phosphate is 99.2%, the median particle size is 5.32 mu m, the recovery rate of the iron is 92.1%, and the contents of copper, cobalt and nickel in the ferric phosphate are all lower than 0.003%; adjusting the pH value of the leachate to 4.5 by using ammonia water, and then extracting valuable metal ions in the leachate by using an organic extractant, wherein the extraction conditions are as follows: the concentration of the extracting agent (the proportion of P204 to P507 is 1:1) is 2.0 percent, the diluting agent is kerosene, the water phase/oil phase ratio is 2:1, the extraction temperature is room temperature, the extraction time is 30min, and the recovery rates of the valuable elements of copper, cobalt and nickel in the whole process flow are 93.2 percent, 95.3 percent and 91.9 percent respectively.
Example 4:
taking sulfuric acid slag (iron grade 54.2%, copper, cobalt and nickel contents are respectively 0.7%, 0.2% and 0.2%) of a certain sulfuric acid plant as a raw material, firstly, ball-milling the sulfuric acid slag until the proportion of-0.037 mm is higher than 80%, and the concentration of ball-milled ore pulp is 55%; then phosphoric acid leaching is carried out, and leaching conditions are as follows: the concentration of phosphoric acid is 2.6mol/L, the concentration of hydrofluoric acid is 0.02mol/L, the liquid-solid ratio is 10ml/g, the leaching temperature is 145 ℃, the leaching time is 6 hours, and after the leaching is finished, the solid-liquid separation is carried out by filtering; washing the synthesized product with distilled water until the pH value of the filtrate is more than 6, and obtaining a product, namely battery-grade ferric phosphate dihydrate, wherein the purity of the ferric phosphate is 99.2%, the median particle size is 5.32 mu m, the recovery rate of the iron is 92.1%, and the contents of copper, cobalt and nickel in the ferric phosphate are all lower than 0.003%; adjusting the pH value of the leachate to 4.5 by using ammonia water, and then extracting valuable metal ions in the leachate by using an organic extractant, wherein the extraction conditions are as follows: the concentration of the extractant P204 is 5.0 percent, the diluent is kerosene, the water phase/oil phase ratio is 3:1, the extraction temperature is room temperature, the extraction time is 45min, and the recovery rates of the valuable elements of copper, cobalt and nickel in the whole process flow are respectively 92.9 percent, 93.8 percent and 90.8 percent.
Claims (4)
1. A method for extracting valuable metals from sulfuric acid residue by phosphoric acid leaching-extraction is characterized by comprising the following steps: ball-milling sulfuric acid residues, leaching with phosphoric acid-hydrofluoric acid mixed acid, washing the obtained leaching residues with water to obtain ferric phosphate dihydrate, adjusting the pH value of the obtained leaching solution to weak acidity, and extracting, separating and recovering copper, cobalt and nickel;
the concentration of phosphoric acid in the phosphoric acid-hydrofluoric acid mixed acid is 1.5-3.8 mol/L, and the concentration of hydrofluoric acid is 0.01-0.03 mol/L;
the leaching conditions are as follows: the liquid-solid ratio is 8-16 mL/g, the leaching temperature is 80-145 ℃, and the leaching time is 4-12 h;
the extraction agent adopted in the extraction separation process comprises at least one of P204 and P507;
the extraction and separation conditions are as follows: the volume percentage concentration of the extracting agent in the organic phase is 2-5%, and the diluting agent is kerosene; the volume ratio of the water phase to the oil phase is 1-3.5: 1, the extraction temperature is room temperature, and the extraction time is 30-60 min.
2. The method for extracting valuable metals by phosphoric acid leaching-extraction of sulfuric acid residue according to claim 1, is characterized in that: and ball-milling the pyrite cinder until the fineness of the pyrite cinder meets the requirement that the mass percentage content of the pyrite cinder in the size fraction smaller than 0.037mm is larger than 80%.
3. The method for extracting valuable metals by phosphoric acid leaching-extraction of sulfuric acid residue according to claim 1, is characterized in that: and washing the leached residues until the pH value is more than 6.
4. The method for extracting valuable metals by phosphoric acid leaching-extraction of sulfuric acid residue according to claim 1, is characterized in that: and adjusting the pH value of the leachate to 4.5-6.
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