CN106622671A - Direct flotation desiliconization and acid leaching magnesium removal combination treatment technology for phosphate ores - Google Patents
Direct flotation desiliconization and acid leaching magnesium removal combination treatment technology for phosphate ores Download PDFInfo
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- CN106622671A CN106622671A CN201611228859.3A CN201611228859A CN106622671A CN 106622671 A CN106622671 A CN 106622671A CN 201611228859 A CN201611228859 A CN 201611228859A CN 106622671 A CN106622671 A CN 106622671A
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- flotation
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- acidleach
- powder
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- 238000005188 flotation Methods 0.000 title claims abstract description 109
- 239000002253 acid Substances 0.000 title claims abstract description 54
- 238000002386 leaching Methods 0.000 title claims abstract description 22
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 title claims abstract description 15
- 239000011777 magnesium Substances 0.000 title claims abstract description 15
- 229910052749 magnesium Inorganic materials 0.000 title claims abstract description 15
- 238000005516 engineering process Methods 0.000 title abstract description 5
- 229910019142 PO4 Inorganic materials 0.000 title abstract 9
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 title abstract 9
- 239000010452 phosphate Substances 0.000 title abstract 9
- 238000011284 combination treatment Methods 0.000 title abstract 2
- 238000000034 method Methods 0.000 claims abstract description 63
- 239000012141 concentrate Substances 0.000 claims abstract description 40
- 238000011282 treatment Methods 0.000 claims abstract description 36
- 238000002156 mixing Methods 0.000 claims abstract description 33
- 239000000126 substance Substances 0.000 claims abstract description 11
- 238000001914 filtration Methods 0.000 claims abstract description 6
- 238000000227 grinding Methods 0.000 claims abstract description 6
- 239000002367 phosphate rock Substances 0.000 claims description 39
- 239000000843 powder Substances 0.000 claims description 38
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 37
- 239000011574 phosphorus Substances 0.000 claims description 37
- 229910052698 phosphorus Inorganic materials 0.000 claims description 37
- 239000003795 chemical substances by application Substances 0.000 claims description 20
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims description 18
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 claims description 18
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 18
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 claims description 18
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 16
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 14
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 14
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 12
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 12
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 claims description 12
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 claims description 12
- 239000000344 soap Substances 0.000 claims description 12
- 235000014113 dietary fatty acids Nutrition 0.000 claims description 10
- 238000000605 extraction Methods 0.000 claims description 10
- 239000000194 fatty acid Substances 0.000 claims description 10
- 229930195729 fatty acid Natural products 0.000 claims description 10
- 239000007787 solid Substances 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 8
- 235000019353 potassium silicate Nutrition 0.000 claims description 8
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical group [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 claims description 8
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 7
- -1 hydrogen Potassium oxide Chemical class 0.000 claims description 7
- 238000010926 purge Methods 0.000 claims description 7
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 7
- MPPQGYCZBNURDG-UHFFFAOYSA-N 2-propionyl-6-dimethylaminonaphthalene Chemical compound C1=C(N(C)C)C=CC2=CC(C(=O)CC)=CC=C21 MPPQGYCZBNURDG-UHFFFAOYSA-N 0.000 claims description 6
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 claims description 6
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 claims description 6
- 229920001732 Lignosulfonate Polymers 0.000 claims description 6
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims description 6
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 6
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 6
- 235000011054 acetic acid Nutrition 0.000 claims description 6
- 235000019253 formic acid Nutrition 0.000 claims description 6
- 239000004310 lactic acid Substances 0.000 claims description 6
- 235000014655 lactic acid Nutrition 0.000 claims description 6
- 229920005610 lignin Polymers 0.000 claims description 6
- 229910017604 nitric acid Inorganic materials 0.000 claims description 6
- 235000006408 oxalic acid Nutrition 0.000 claims description 6
- 150000003839 salts Chemical class 0.000 claims description 6
- 238000004513 sizing Methods 0.000 claims description 6
- 235000015165 citric acid Nutrition 0.000 claims description 5
- 125000005313 fatty acid group Chemical group 0.000 claims description 5
- 150000004665 fatty acids Chemical class 0.000 claims description 5
- GCLGEJMYGQKIIW-UHFFFAOYSA-H sodium hexametaphosphate Chemical compound [Na]OP1(=O)OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])OP(=O)(O[Na])O1 GCLGEJMYGQKIIW-UHFFFAOYSA-H 0.000 claims description 5
- 229910001748 carbonate mineral Inorganic materials 0.000 claims description 4
- 229910052585 phosphate mineral Inorganic materials 0.000 claims description 4
- 229910052739 hydrogen Inorganic materials 0.000 claims 1
- 239000001257 hydrogen Substances 0.000 claims 1
- 229910001950 potassium oxide Inorganic materials 0.000 claims 1
- 238000004064 recycling Methods 0.000 claims 1
- 239000002699 waste material Substances 0.000 abstract description 6
- 239000002002 slurry Substances 0.000 abstract 3
- 239000007788 liquid Substances 0.000 abstract 2
- 230000007613 environmental effect Effects 0.000 abstract 1
- 230000008719 thickening Effects 0.000 abstract 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 8
- 239000011707 mineral Substances 0.000 description 8
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 7
- 229910052604 silicate mineral Inorganic materials 0.000 description 4
- 239000004575 stone Substances 0.000 description 4
- ZLNQQNXFFQJAID-UHFFFAOYSA-L magnesium carbonate Chemical compound [Mg+2].[O-]C([O-])=O ZLNQQNXFFQJAID-UHFFFAOYSA-L 0.000 description 3
- 239000001095 magnesium carbonate Substances 0.000 description 3
- 229910000021 magnesium carbonate Inorganic materials 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 238000003672 processing method Methods 0.000 description 2
- MOMKYJPSVWEWPM-UHFFFAOYSA-N 4-(chloromethyl)-2-(4-methylphenyl)-1,3-thiazole Chemical compound C1=CC(C)=CC=C1C1=NC(CCl)=CS1 MOMKYJPSVWEWPM-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- BPQQTUXANYXVAA-UHFFFAOYSA-N Orthosilicate Chemical compound [O-][Si]([O-])([O-])[O-] BPQQTUXANYXVAA-UHFFFAOYSA-N 0.000 description 1
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 125000001931 aliphatic group Chemical group 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 235000019983 sodium metaphosphate Nutrition 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/001—Flotation agents
- B03D1/004—Organic compounds
- B03D1/008—Organic compounds containing oxygen
-
- 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
- C01B25/01—Treating phosphate ores or other raw phosphate materials to obtain phosphorus or phosphorus compounds
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F5/00—Compounds of magnesium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/02—Collectors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2203/00—Specified materials treated by the flotation agents; Specified applications
- B03D2203/02—Ores
- B03D2203/04—Non-sulfide ores
- B03D2203/06—Phosphate ores
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The invention provides a direct flotation desiliconization and acid leaching magnesium removal combination treatment technology for phosphate ores. During the treatment of the phosphate ores, phosphate concentrates are obtained by adopting a direct flotation and acid chemical leaching combination method, and acid chemical leaching optimally adopts waste acid. The technology specifically comprises the following steps: blending phosphate ore slurry which is obtained by ore grinding, and then adding a direct flotation collector to blend the slurry; enabling the phosphate ore slurry to enter a direct flotation system, carrying out flotation, and after the flotation of the direct flotation system, obtaining direct flotation concentrates; and after carrying out thickening and filtering on the direct flotation concentrates, adding acid liquid or waste acid liquid to carry out leaching, and obtaining final phosphate concentrates. The method not only can achieve the purposes of improving the grade of the phosphate concentrates and reducing magnesium content in the phosphate concentrates, but also can dispose part of waste acid solution and realize environmental protection and benefit increase.
Description
Technical field
The invention belongs to flotation of phosphate rock technical field, more particularly to a kind of direct-flotation desiliconisation and acidleach demagging Combined Treatment
The technique of rock phosphate in powder.
Background technology
Impure mineral in most of collophane is silicate mineral and mineral containing magnesium carbonate.Silicate mineral does not have
Evil impurity, its presence is mainly reduction of phosphorus concentrate grade, and the method for removing of silicate mineral mainly has direct flotation to suppress silicon
Hydrochlorate mineral and reverse flotation direct flotation go out silicate mineral.Magnesium is the objectionable impurities in the processing of phosphorus concentrate phosphoric acid by wet process, in choosing
The content of magnesium in phosphorus concentrate must be down to certain value in ore deposit.At present, the processing method of magnesium-containing mineral has floatation in phosphorus ore
Leach method with chemistry.Chemical Leaching method is applied to the phosphorus ore that phosphorus content is higher and content of magnesium is relatively low, and the method is due to acid consumption
It is larger, it is relatively costly if available without waste acid liquor.Floatation is the mineral containing magnesium carbonate for generally adopting at present
Processing method, with extensive adaptability, floatation remove mineral containing magnesium carbonate mainly have direct flotation Phosphate minerals suppression carbon
Hydrochlorate mineral and reverse flotation direct flotation go out carbonate mineral.
The report that existing data or patented technology also do not combine top-up choosing method and the Chemical Leaching method of phosphorus ore
Road.
The content of the invention
The technical problem to be solved be for the deficiencies in the prior art part, there is provided a kind of direct-flotation desiliconisation with
The technique of acidleach demagging Combined Treatment rock phosphate in powder, the technique can improve phosphorus concentrate grade, reduce the purpose of content of magnesium in phosphorus concentrate,
Again can process part waste acid liquor, realize environmentally friendly income.
The technical problem to be solved is realized by following technical scheme.The present invention is that one kind is top-uped
The technique for selecting desiliconization and acidleach demagging Combined Treatment rock phosphate in powder, is characterized in：In the process of rock phosphate in powder, using direct flotation and acid
The united method of Chemical Leaching obtains phosphorus concentrate.
The technique of a kind of direct-flotation desiliconisation of the present invention and acidleach demagging Combined Treatment rock phosphate in powder, its is further preferred
Technical scheme or technical characteristic be：
1st, described sour Chemical Leaching（Acidleach）It is preferred that adopting spent acid, it is also possible to which common acid, the species of acid is selected from：Acidleach operation
Acid selected from sulfuric acid, magnesium bisulfate, phosphoric acid, hydrochloric acid, nitric acid, fluosilicic acid, organic phospho acid, organic sulfonic acid, oxalic acid, acetic acid, formic acid,
One or more mixed acid in lactic acid, citric acid；The spent acid that further preferably aforementioned various acid recoverys are recycled.
2nd, the technique of a kind of direct-flotation desiliconisation of the present invention and acidleach demagging Combined Treatment rock phosphate in powder, it is further excellent
The step of selecting is as follows：
（1）Phosphorus ore ore pulp after ore grinding adds regulator to be sized mixing；
（2）Phosphorus ore ore pulp Jing after sizing mixing adds direct flotation collecting agent to be sized mixing；
（3）After direct flotation collecting agent is sized mixing, phosphorus ore ore pulp enters direct flotation system carries out flotation, sorts through direct flotation system
After obtain the concentrate selection that top-ups, the concentrate be froth pulp, the carbonate mineral containing Phosphate minerals and containing magnesium；
（4）Concentrate selection top-up through dense, the laggard acidleach agitating device of filtration, adds acid solution leaching, the concentrate after acidleach to pass through
Filter obtains final phosphorus concentrate.
3rd, above-mentioned steps（1）Described direct flotation regulator preferably is selected from：Waterglass, prodan, sodium carbonate, bicarbonate
Sodium, NaOH, potassium hydroxide, calgon, lignin, lignosulfonates, naphthalene sulfonic salt one or two with
Upper mixture.The preferable amount of wherein single regulator be 0.10kg/t-10kg/t raw ores, further preferred 1kg/t-5kg/
T raw ores.Described direct flotation regulator sizes mixing the time for 1min-15min, preferably sizes mixing the time for 5min-10min.
4th, above-mentioned steps（2）Described direct flotation collecting agent is fatty acid soaps, and the time of sizing mixing is 1min-15min, preferably
The time size mixing for 5min-10min.The consumption of the direct flotation collecting agent fatty acid soaps is 0.5 kg/t-6kg/t raw ores, excellent
Elect 1 kg/t-3kg/t raw ores as.
5th, step（3）The flow process of described direct flotation system preferably is selected from：One roughing, or one roughing once purging selection group
Close, or one roughing and 1-4 selected combinations, or one roughing, once purging selection and 1-4 selected combinations；Work as presence
Selected and when scanning, chats that is selected and scanning generation returns successively a flotation operation.
6th, the pH value of acidleach operation is 1-4, and preferred pH value is 2-3.The temperature of acidleach operation is 10-60 degree Celsius,
Preferable temperature is 15-40 degree Celsius.The liquid-solid ratio of acidleach operation is 1:1—4:1, preferred liquid-solid ratio is 2:1-3:1.Acidleach is made
The extraction time of industry is 0.25-3.0 hours, and preferred extraction time is 1-2 hours.
The technique of a kind of direct-flotation desiliconisation of the present invention and acidleach demagging Combined Treatment rock phosphate in powder, it is adaptable to any phosphorus
Ore, is preferably applied to P2O5Content is 12-25%, and content of MgO is 0.5-3.5% rock phosphate in powder.
Present invention process in the ore dressing of rock phosphate in powder, when silicate is excluded using direct flotation, phosphorus ore containing and ore deposit containing magnesium
Thing is flotated together, and top-uping, concentrate selection phosphorus content is higher, and content of magnesium does not reach quality requirement, by acid solution or waste acid liquor
The magnesium-containing mineral top-uped in concentrate selection is further removed, so as to obtain qualified phosphorus concentrate.
Compared with prior art, it is an advantage of the invention that the present invention leaches united side using direct flotation and spent acid chemical
Method process rock phosphate in powder, can reach raising phosphorus concentrate grade, reduce phosphorus concentrate in content of magnesium purpose, again can process part give up
Acid solution, realizes environmentally friendly income.
Specific embodiment
The concrete technical scheme of the present invention described further below, in order to those skilled in the art this is further understood
Invention, and do not constitute the restriction to its right.
The technique of embodiment 1, a kind of direct-flotation desiliconisation and acidleach demagging Combined Treatment rock phosphate in powder, in the process of rock phosphate in powder
In, phosphorus concentrate is obtained with the united method of sour Chemical Leaching using direct flotation.
The technique of embodiment 2, a kind of direct-flotation desiliconisation described in claim 1 and acidleach demagging Combined Treatment rock phosphate in powder
In：Described sour Chemical Leaching adopts spent acid.
The technique of embodiment 3, a kind of direct-flotation desiliconisation described in embodiment 1 or 2 and acidleach demagging Combined Treatment rock phosphate in powder,
Its step is as follows：
（1）Phosphorus ore ore pulp after ore grinding adds regulator to be sized mixing；
（2）Phosphorus ore ore pulp Jing after sizing mixing adds direct flotation collecting agent to be sized mixing；
（3）After direct flotation collecting agent is sized mixing, phosphorus ore ore pulp enters direct flotation system carries out flotation, sorts through direct flotation system
After obtain the concentrate selection that top-ups, the concentrate be froth pulp, the carbonate mineral containing Phosphate minerals and containing magnesium；
（4）Concentrate selection top-up through dense, the laggard acidleach agitating device of filtration, adds acid solution leaching, the concentrate after acidleach to pass through
Filter obtains final phosphorus concentrate.
Embodiment 4, a kind of direct-flotation desiliconisation described in embodiment 3 and the technique of acidleach demagging Combined Treatment rock phosphate in powder, walk
Suddenly（1）In：Described direct flotation regulator is selected from waterglass, prodan, sodium carbonate, sodium acid carbonate, NaOH, hydroxide
Potassium, calgon, lignin, lignosulfonates or naphthalene sulfonic salt, the consumption of single regulator is 0.10kg/t raw ores,
Described direct flotation regulator sizes mixing the time for 1min；
Step（2）In：Described direct flotation collecting agent is fatty acid soaps, sizes mixing the time for 1min, direct flotation collecting agent aliphatic acid
The consumption of soap is 6kg/t raw ores；
Step（3）In：The flow process of described direct flotation system is：One roughing.
Embodiment 5, a kind of direct-flotation desiliconisation described in embodiment 3 and the technique of acidleach demagging Combined Treatment rock phosphate in powder, walk
Suddenly（1）In：Described direct flotation regulator is selected from waterglass, prodan, sodium carbonate, sodium acid carbonate, NaOH, hydroxide
The mixture of any two kinds of compositions in potassium, calgon, lignin, lignosulfonates, naphthalene sulfonic salt, single adjustment
The consumption of agent is 10kg/t raw ores, and described direct flotation regulator sizes mixing the time for 1min.
Step（2）In：Described direct flotation collecting agent is fatty acid soaps, sizes mixing the time for 15min, preferred direct flotation collecting
The consumption of agent fatty acid soaps is 0.5 kg/t.
Step（3）In：The flow process of described direct flotation system is：One roughing once purging selection is combined；
The technique of embodiment 6, a kind of direct-flotation desiliconisation described in embodiment 3 and acidleach demagging Combined Treatment rock phosphate in powder, step（1）
In：Described direct flotation regulator selected from waterglass, prodan, sodium carbonate, sodium acid carbonate, NaOH, potassium hydroxide, six
The mixture of any three kinds of compositions in sodium metaphosphate, lignin, lignosulfonates, naphthalene sulfonic salt, single regulator
Consumption be 1kg/t.Described direct flotation regulator sizes mixing the time for 5min.
Step（2）In：Described direct flotation collecting agent is fatty acid soaps, sizes mixing the time for 5min；Direct flotation collecting agent fat
The consumption of fat acid soap is 1 kg/t raw ores.
Step（3）In：The flow process of described direct flotation system is one roughing, once purging selection and 1 selected combinations；It is selected
A upper flotation operation is returned successively with the chats for scanning generation.
Embodiment 7, a kind of direct-flotation desiliconisation described in embodiment 3 and the technique of acidleach demagging Combined Treatment rock phosphate in powder, walk
Suddenly（1）In：Described direct flotation regulator is selected from waterglass, prodan, sodium carbonate, sodium acid carbonate, NaOH, hydroxide
One kind in potassium, calgon, lignin, lignosulfonates, naphthalene sulfonic salt.The consumption of single regulator is 5kg/t
Raw ore.Described direct flotation regulator sizes mixing the time for 10min.
Embodiment 8, a kind of direct-flotation desiliconisation described in embodiment 1-7 any one and acidleach demagging Combined Treatment phosphorus ore
In the technique of stone：The acid of acidleach operation is selected from sulfuric acid, magnesium bisulfate, phosphoric acid, hydrochloric acid, nitric acid, fluosilicic acid, organic phospho acid, organic
One kind in sulfonic acid, oxalic acid, acetic acid, formic acid, lactic acid, citric acid；The pH value of acidleach operation is 1.The temperature of acidleach operation is 10
Degree Celsius.The liquid-solid ratio of acidleach operation is 1:1.The extraction time of acidleach operation is 0.25.
Embodiment 9, a kind of direct-flotation desiliconisation described in embodiment 1-7 any one and acidleach demagging Combined Treatment phosphorus ore
In the technique of stone：The acid of acidleach operation is selected from sulfuric acid, magnesium bisulfate, phosphoric acid, hydrochloric acid, nitric acid, fluosilicic acid, organic phospho acid, organic
A kind of spent acid in sulfonic acid, oxalic acid, acetic acid, formic acid, lactic acid, citric acid.The pH value of acidleach operation is 4.The temperature of acidleach operation
For 60 degrees Celsius.The liquid-solid ratio of acidleach operation is 4:1.The extraction time of acidleach operation is 3.0 hours.
Embodiment 10, a kind of direct-flotation desiliconisation described in embodiment 1-7 any one and acidleach demagging Combined Treatment phosphorus ore
In the technique of stone：The acid of acidleach operation is selected from sulfuric acid, magnesium bisulfate, phosphoric acid, hydrochloric acid, nitric acid, fluosilicic acid, organic phospho acid, organic
The mixed acid of two kinds of compositions in sulfonic acid, oxalic acid, acetic acid, formic acid, lactic acid, citric acid；The pH value of acidleach operation is 2.Acidleach is made
The temperature of industry is 15 degrees Celsius.The liquid-solid ratio of acidleach operation is 2:1.The extraction time of acidleach operation is 1 hour.
Embodiment 11, a kind of direct-flotation desiliconisation described in embodiment 1-7 any one and acidleach demagging Combined Treatment phosphorus ore
In the technique of stone：The acid of acidleach operation is selected from sulfuric acid, magnesium bisulfate, phosphoric acid, hydrochloric acid, nitric acid, fluosilicic acid, organic phospho acid, organic
The mixing spent acid of two kinds of compositions in sulfonic acid, oxalic acid, acetic acid, formic acid, lactic acid, citric acid；The pH value of acidleach operation is 3.Acidleach
The temperature of operation is 40 degrees Celsius.The liquid-solid ratio of acidleach operation is 3:1.The extraction time of acidleach operation is 2 hours.
A kind of application test one of the technique of embodiment 12, direct-flotation desiliconisation and acidleach demagging Combined Treatment rock phosphate in powder.
Domestic certain phosphorus ore sample ore one, raw ore P2O5Content is 21.61%, MgO 1.50%, and direct flotation is carried out after ore grinding, is top-uped
Flow process is selected to be one roughing, direct flotation experimental condition is:Sodium carbonate 1.0kg/t, waterglass 5.0kg/t, regulator mixing time
5min, direct flotation collecting agent fatty acid soaps 2.5kg/t, collecting agent mixing time 5min.Top-up concentrate selection P after direct flotation2O5Content
For 27.41%, MgO 1.89%.Ore Leaching is carried out after the dense filtration of the concentrate selection that top-ups, Ore Leaching condition is：Sour species is sulfuric acid,
PH value 3.5,50 degrees Celsius of temperature, liquid-solid ratio 2:1, extraction time 1 hour.Concentrate P after leaching2O5Content is 30.23%, MgO
0.42%, P2O5Overall recovery 85.87%.
A kind of application test two of the technique of embodiment 13, direct-flotation desiliconisation and acidleach demagging Combined Treatment rock phosphate in powder.
Domestic certain phosphorus ore sample ore two, raw ore P2O5Content is 22.78%, MgO 2.57%, and direct flotation is carried out after ore grinding, is top-uped
Flow process is selected to be one roughing once purging selection, direct flotation experimental condition is:Waterglass 9.0kg/t, regulator mixing time 2min, just
Flotation collector fatty acid soaps 2.0kg/t, collecting agent mixing time 2min.Top-up concentrate selection P after direct flotation2O5Content is
26.36%, MgO 3.14%.Ore Leaching is carried out after the dense filtration of the concentrate selection that top-ups, Ore Leaching condition is：Sour species is sulfuric acid and phosphorus
Acid, pH value 3.0,55 degrees Celsius of temperature, liquid-solid ratio 2:1, extraction time 1.5 hours.Concentrate P after leaching2O5Content is 30.42%,
MgO 0.57%, P2O5Overall recovery 86.96%.
Claims (15)
1. the technique of a kind of direct-flotation desiliconisation and acidleach demagging Combined Treatment rock phosphate in powder, it is characterised in that：In the process of rock phosphate in powder
In, phosphorus concentrate is obtained with the united method of sour Chemical Leaching using direct flotation.
2. the technique of a kind of direct-flotation desiliconisation according to claim 1 and acidleach demagging Combined Treatment rock phosphate in powder, its feature
It is：Described sour Chemical Leaching adopts spent acid.
3. the technique of a kind of direct-flotation desiliconisation according to claim 1 and 2 and acidleach demagging Combined Treatment rock phosphate in powder, it is special
Levy and be, its step is as follows：
（1）Phosphorus ore ore pulp after ore grinding adds regulator to be sized mixing；
（2）Phosphorus ore ore pulp Jing after sizing mixing adds direct flotation collecting agent to be sized mixing；
（3）After direct flotation collecting agent is sized mixing, phosphorus ore ore pulp enters direct flotation system carries out flotation, sorts through direct flotation system
After obtain the concentrate selection that top-ups, the concentrate be froth pulp, the carbonate mineral containing Phosphate minerals and containing magnesium；
（4）Concentrate selection top-up through dense, the laggard acidleach agitating device of filtration, adds acid solution leaching, the concentrate after acidleach to pass through
Filter obtains final phosphorus concentrate.
4. the technique of a kind of direct-flotation desiliconisation according to claim 3 and acidleach demagging Combined Treatment rock phosphate in powder, its feature
It is：Step（1）Described direct flotation regulator is selected from waterglass, prodan, sodium carbonate, sodium acid carbonate, NaOH, hydrogen
Potassium oxide, calgon, lignin, lignosulfonates, one or more mixtures of naphthalene sulfonic salt.
5. the technique of a kind of direct-flotation desiliconisation according to claim 4 and acidleach demagging Combined Treatment rock phosphate in powder, its feature
It is：The consumption of single regulator be 0.10kg/t-10kg/t raw ores, preferred 1kg/t-5kg/t raw ores.
6. the technique of a kind of direct-flotation desiliconisation according to claim 3 and acidleach demagging Combined Treatment rock phosphate in powder, its feature
It is：Step（1）Described direct flotation regulator sizes mixing the time for 1min-15min, preferably sizes mixing the time for 5min-
10min。
7. the technique of a kind of direct-flotation desiliconisation according to claim 3 and acidleach demagging Combined Treatment rock phosphate in powder, its feature
It is：Step（2）Described direct flotation collecting agent is fatty acid soaps, and the time of sizing mixing, the preferably time of sizing mixing was for 1min-15min
5min-10min.
8. the technique of a kind of direct-flotation desiliconisation according to claim 7 and acidleach demagging Combined Treatment rock phosphate in powder, its feature
It is：The consumption of the direct flotation collecting agent fatty acid soaps be 0.5 kg/t-6kg/t raw ores, preferably 1 kg/t-3kg/t
Raw ore.
9. the technique of a kind of direct-flotation desiliconisation according to claim 3 and acidleach demagging Combined Treatment rock phosphate in powder, its feature
It is：Step（3）The flow process of described direct flotation system is selected from：One roughing, or the combination of one roughing once purging selection, or
One roughing and 1-4 selected combinations, or one roughing, once purging selection and 1-4 selected combinations；It is selected and sweep when existing
When selecting, chats that is selected and scanning generation returns successively a flotation operation.
10. a kind of direct-flotation desiliconisation according to claim 1-9 any one and acidleach demagging Combined Treatment rock phosphate in powder
Technique, it is characterised in that：The acid of acidleach operation selected from sulfuric acid, magnesium bisulfate, phosphoric acid, hydrochloric acid, nitric acid, fluosilicic acid, organic phospho acid,
One or more mixed acid in organic sulfonic acid, oxalic acid, acetic acid, formic acid, lactic acid, citric acid；It is preferred that aforementioned various acid
The spent acid of recycling.
A kind of 11. direct-flotation desiliconisations according to claim 1-9 any one and acidleach demagging Combined Treatment rock phosphate in powder
Technique, it is characterised in that：The pH value of acidleach operation is 1-4, and preferred pH value is 2-3.
A kind of 12. direct-flotation desiliconisations according to claim 1-9 any one and acidleach demagging Combined Treatment rock phosphate in powder
Technique, it is characterised in that：The temperature of acidleach operation is 10-60 degree Celsius, and preferable temperature is 15-40 degree Celsius.
A kind of 13. direct-flotation desiliconisations according to claim 1-9 any one and acidleach demagging Combined Treatment rock phosphate in powder
Technique, it is characterised in that：The liquid-solid ratio of acidleach operation is 1:1—4:1, preferred liquid-solid ratio is 2:1-3:1.
A kind of 14. direct-flotation desiliconisations according to claim 1-9 any one and acidleach demagging Combined Treatment rock phosphate in powder
Technique, it is characterised in that：The extraction time of acidleach operation is 0.25-3.0 hours, and preferred extraction time is 1-2 hours.
A kind of 15. direct-flotation desiliconisations according to claim 1-9 any one and acidleach demagging Combined Treatment rock phosphate in powder
Technique, it is characterised in that：P in described rock phosphate in powder2O5Content is 12-25%, and content of MgO is 0.5-3.5%.
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| CN108568348A (en) * | 2018-04-11 | 2018-09-25 | 武汉工程大学 | A kind of vegetable fatty acid acyl breast ester soap collecting agent and preparation method thereof |
| CN108751150A (en) * | 2018-08-22 | 2018-11-06 | 贵州大学 | A method of being enriched with low-grade phosphate ore stone using low molecular weight organic acid |
| CN109701749A (en) * | 2019-01-22 | 2019-05-03 | 云南磷化集团有限公司 | A kind of method of nitric acid pretreatment direct flotation phosphorus concentrate |
| CN111422878A (en) * | 2020-04-20 | 2020-07-17 | 武汉工程大学 | Method for treating silico-calcium collophanite |
| CN111438002A (en) * | 2020-04-20 | 2020-07-24 | 武汉工程大学 | Method for treating silicon-calcium collophanite by 'floating-chemical' coupling |
| CN112007760A (en) * | 2019-07-23 | 2020-12-01 | 中蓝连海设计研究院有限公司 | Beneficiation method for treating high sesquioxide collophanite |
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| CN111422878A (en) * | 2020-04-20 | 2020-07-17 | 武汉工程大学 | Method for treating silico-calcium collophanite |
| CN111438002A (en) * | 2020-04-20 | 2020-07-24 | 武汉工程大学 | Method for treating silicon-calcium collophanite by 'floating-chemical' coupling |
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