CN111302401A - Method for reducing calcium content in manganese sulfate solution - Google Patents
Method for reducing calcium content in manganese sulfate solution Download PDFInfo
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- CN111302401A CN111302401A CN202010125210.9A CN202010125210A CN111302401A CN 111302401 A CN111302401 A CN 111302401A CN 202010125210 A CN202010125210 A CN 202010125210A CN 111302401 A CN111302401 A CN 111302401A
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- 239000011702 manganese sulphate Substances 0.000 title claims abstract description 211
- 235000007079 manganese sulphate Nutrition 0.000 title claims abstract description 211
- SQQMAOCOWKFBNP-UHFFFAOYSA-L manganese(II) sulfate Chemical compound [Mn+2].[O-]S([O-])(=O)=O SQQMAOCOWKFBNP-UHFFFAOYSA-L 0.000 title claims abstract description 211
- 229940099596 manganese sulfate Drugs 0.000 title claims abstract description 202
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 title claims abstract description 125
- 239000011575 calcium Substances 0.000 title claims abstract description 125
- 229910052791 calcium Inorganic materials 0.000 title claims abstract description 124
- 238000000034 method Methods 0.000 title claims abstract description 75
- 239000012074 organic phase Substances 0.000 claims abstract description 222
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 claims abstract description 88
- 229910052748 manganese Inorganic materials 0.000 claims abstract description 87
- 239000011572 manganese Substances 0.000 claims abstract description 87
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 54
- 229910001424 calcium ion Inorganic materials 0.000 claims abstract description 54
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims abstract description 53
- 230000008569 process Effects 0.000 claims abstract description 33
- 238000007127 saponification reaction Methods 0.000 claims abstract description 28
- 238000002425 crystallisation Methods 0.000 claims abstract description 25
- 230000008025 crystallization Effects 0.000 claims abstract description 25
- 239000007787 solid Substances 0.000 claims abstract description 23
- 239000003350 kerosene Substances 0.000 claims abstract description 19
- 239000012535 impurity Substances 0.000 claims abstract description 17
- 238000002156 mixing Methods 0.000 claims abstract description 17
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 13
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 7
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 7
- 238000000605 extraction Methods 0.000 claims description 133
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 71
- 238000001914 filtration Methods 0.000 claims description 32
- 238000001704 evaporation Methods 0.000 claims description 27
- 239000000344 soap Substances 0.000 claims description 17
- 230000008020 evaporation Effects 0.000 claims description 13
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 230000008929 regeneration Effects 0.000 claims description 6
- 238000011069 regeneration method Methods 0.000 claims description 6
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 239000000243 solution Substances 0.000 description 185
- 229910001437 manganese ion Inorganic materials 0.000 description 31
- 238000010521 absorption reaction Methods 0.000 description 22
- WAEMQWOKJMHJLA-UHFFFAOYSA-N Manganese(2+) Chemical compound [Mn+2] WAEMQWOKJMHJLA-UHFFFAOYSA-N 0.000 description 17
- 239000007864 aqueous solution Substances 0.000 description 14
- 150000002500 ions Chemical class 0.000 description 13
- 230000000717 retained effect Effects 0.000 description 10
- 230000000694 effects Effects 0.000 description 9
- 239000001117 sulphuric acid Substances 0.000 description 9
- 235000011149 sulphuric acid Nutrition 0.000 description 9
- 239000011550 stock solution Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- NUJOXMJBOLGQSY-UHFFFAOYSA-N manganese dioxide Chemical compound O=[Mn]=O NUJOXMJBOLGQSY-UHFFFAOYSA-N 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 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 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- -1 calcium ions Chemical class 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 description 2
- 238000011031 large-scale manufacturing process Methods 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 239000011777 magnesium Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- FBUKVWPVBMHYJY-UHFFFAOYSA-N nonanoic acid Chemical compound CCCCCCCCC(O)=O FBUKVWPVBMHYJY-UHFFFAOYSA-N 0.000 description 2
- 239000003002 pH adjusting agent Substances 0.000 description 2
- 239000007774 positive electrode material Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- QGBLCIBATKETJC-UHFFFAOYSA-N 3,7-dioxido-2,4,6,8,9-pentaoxa-1,3,5,7-tetraborabicyclo[3.3.1]nonane;manganese(2+) Chemical compound [Mn+2].O1B([O-])OB2OB([O-])OB1O2 QGBLCIBATKETJC-UHFFFAOYSA-N 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- 229910000881 Cu alloy Inorganic materials 0.000 description 1
- 229910000616 Ferromanganese Inorganic materials 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 1
- 229910000572 Lithium Nickel Cobalt Manganese Oxide (NCM) Inorganic materials 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- 229910021380 Manganese Chloride Inorganic materials 0.000 description 1
- GLFNIEUTAYBVOC-UHFFFAOYSA-L Manganese chloride Chemical compound Cl[Mn]Cl GLFNIEUTAYBVOC-UHFFFAOYSA-L 0.000 description 1
- 238000003723 Smelting Methods 0.000 description 1
- FBDMTTNVIIVBKI-UHFFFAOYSA-N [O-2].[Mn+2].[Co+2].[Ni+2].[Li+] Chemical compound [O-2].[Mn+2].[Co+2].[Ni+2].[Li+] FBDMTTNVIIVBKI-UHFFFAOYSA-N 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- QUXFOKCUIZCKGS-UHFFFAOYSA-N bis(2,4,4-trimethylpentyl)phosphinic acid Chemical compound CC(C)(C)CC(C)CP(O)(=O)CC(C)CC(C)(C)C QUXFOKCUIZCKGS-UHFFFAOYSA-N 0.000 description 1
- 238000009388 chemical precipitation Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- HPDFFVBPXCTEDN-UHFFFAOYSA-N copper manganese Chemical compound [Mn].[Cu] HPDFFVBPXCTEDN-UHFFFAOYSA-N 0.000 description 1
- QHGJSLXSVXVKHZ-UHFFFAOYSA-N dilithium;dioxido(dioxo)manganese Chemical compound [Li+].[Li+].[O-][Mn]([O-])(=O)=O QHGJSLXSVXVKHZ-UHFFFAOYSA-N 0.000 description 1
- 230000000668 effect on calcium Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- DALUDRGQOYMVLD-UHFFFAOYSA-N iron manganese Chemical compound [Mn].[Fe] DALUDRGQOYMVLD-UHFFFAOYSA-N 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 150000002696 manganese Chemical class 0.000 description 1
- 239000011656 manganese carbonate Substances 0.000 description 1
- 235000006748 manganese carbonate Nutrition 0.000 description 1
- 229940093474 manganese carbonate Drugs 0.000 description 1
- 239000011565 manganese chloride Substances 0.000 description 1
- 235000002867 manganese chloride Nutrition 0.000 description 1
- 229940099607 manganese chloride Drugs 0.000 description 1
- MIVBAHRSNUNMPP-UHFFFAOYSA-N manganese(2+);dinitrate Chemical compound [Mn+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O MIVBAHRSNUNMPP-UHFFFAOYSA-N 0.000 description 1
- 229910000016 manganese(II) carbonate Inorganic materials 0.000 description 1
- XMWCXZJXESXBBY-UHFFFAOYSA-L manganese(ii) carbonate Chemical compound [Mn+2].[O-]C([O-])=O XMWCXZJXESXBBY-UHFFFAOYSA-L 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 229910000859 α-Fe Inorganic materials 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G45/00—Compounds of manganese
- C01G45/10—Sulfates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G45/00—Compounds of manganese
- C01G45/003—Preparation involving a liquid-liquid extraction, an adsorption or an ion-exchange
-
- 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)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
The invention provides a method for reducing the calcium content in a manganese sulfate solution. The manganese sulfate solution contains impurity calcium ions, and the method comprises the following steps: s1, adjusting the pH value of the manganese sulfate solution to 0.5-3; s2, mixing an extracting agent P204 and sulfonated kerosene to obtain an extracted organic phase, wherein the volume concentration of the extracting agent P204 is 5-30%; s3, saponifying the extracted organic phase by ammonia water or sodium hydroxide solution to obtain a saponified organic phase, wherein the saponification rate of the saponified organic phase is 5-20%; s4, extracting the manganese sulfate solution by taking the saponified organic phase as an extractant to obtain a manganese-rich raffinate and a calcium-rich organic phase; and S5, carrying out evaporative crystallization on the manganese-rich raffinate to obtain calcium-removed manganese sulfate solid. The process provided by the invention is used for removing calcium from the manganese sulfate solution, and has the advantages of environmental friendliness, low cost, high calcium ion removal rate and the like, and has wide application prospect.
Description
Technical Field
The invention relates to the technical field of metal salt impurity removal, in particular to a method for reducing the content of calcium in a manganese sulfate solution.
Background
In recent years, the demand of manganese and its compound products in the market has increased dramatically. The high-purity manganese sulfate is mainly used for smelting high-grade ferromanganese alloy and electrolytic manganese metal of manganese-copper alloy; the manganese borate, the manganese nitrate, the manganese chloride and the like are produced by taking high-purity manganese sulfate as a basic raw material; the manganese dioxide is used for providing raw materials for electrolytic or chemical manganese dioxide for high-grade batteries, high-purity manganese carbonate and trimanganese tetroxide for soft magnetic ferrite materials. Among a plurality of functions, the high-purity manganese sulfate is applied to the synthesis of a lithium nickel cobalt manganese oxide ternary positive electrode material and a lithium manganate positive electrode material, and is a research hotspot of the domestic manganese industry in recent years.
Impurities such as calcium contained in manganese series products can seriously affect the quality of the products. However, manganese ore resources in China are mainly poor ores, the impurity content is high, manganese ore leachate (manganese sulfate aqueous solution) often contains a large amount of calcium impurities, and electronic-grade manganese sulfate has strict requirements on the concentration of impurity ions, particularly calcium ions, so that the research and preparation of electronic-grade manganese sulfate mainly aims at removing the impurity calcium ions. However, the removal of calcium in manganese sulfate solution is a great problem in the world, and the extraction method is generally adopted in the current main calcium removal method, but the extraction rate of calcium ions is low in the current process, so that the calcium removal effect is not ideal.
Chinese patent 201710552066.5 discloses a method for preparing battery-grade manganese sulfate, which comprises removing calcium, magnesium and ions by chemical precipitation of manganese sulfate solution with fluoride, and then extracting with alkaline extractant. However, the method uses a large amount of chemical precipitator, adds excessive fluoride ions, corrodes equipment and pollutes the environment. Chinese patent 201611040051.2 discloses a method for preparing battery-grade manganese sulfate, which is high-purity manganese sulfate obtained by extraction and back extraction of saponified caprylic-capric acid, wherein the material used in the method is higher-priced caprylic-capric acid, which is not economical. Chinese patent 201810313444.9 discloses a method for reducing calcium and magnesium ions in qualified electrolytic manganese liquor, which is to extract manganese sulfate containing impurities with manganese soap organic matter to obtain calcium and magnesium loaded organic phase and qualified electrolytic manganese liquor, however, the extractant used in the method is a combined extractant of P507 and Cyanex272, which is a mixed extractant, and has high price, high cost and poor reproducibility.
Therefore, there is a need to provide a process for removing calcium from manganese sulfate solution, which is environment-friendly, low in cost and good in calcium ion removal effect.
Disclosure of Invention
The invention mainly aims to provide a method for reducing the calcium content in a manganese sulfate solution, so as to solve the problem that the prior art cannot consider environment-friendly property, low cost and calcium ion removal rate when the calcium of the manganese sulfate solution is removed.
In order to achieve the above object, according to one aspect of the present invention, there is provided a method for reducing the calcium content in a manganese sulfate solution containing calcium ions as impurities, wherein the method comprises the steps of: s1, adjusting the pH value of the manganese sulfate solution to 0.5-3; s2, mixing an extracting agent P204 and sulfonated kerosene to obtain an extracted organic phase, wherein the volume concentration of the extracting agent P204 is 5-30%; s3, saponifying the extracted organic phase by ammonia water or sodium hydroxide solution to obtain a saponified organic phase, wherein the saponification rate of the saponified organic phase is 5-20%; s4, extracting the manganese sulfate solution by taking the saponified organic phase as an extractant to obtain a manganese-rich raffinate and a calcium-rich organic phase; and S5, carrying out evaporative crystallization on the manganese-rich raffinate to obtain calcium-removed manganese sulfate solid.
Further, in the step S3, after the extraction organic phase is obtained, the method further comprises the step of carrying out soap conversion on the extraction organic phase by adopting a high-purity manganese sulfate solution with the concentration of 80-100 g/L to obtain a soap-converted organic phase; and in step S4, the manganese sulfate solution is extracted using the soap-converted organic phase as an extractant.
Further, in the step S4, in the process of extracting the manganese sulfate solution, the O/A ratio of the extracting agent to the manganese sulfate solution is (1-3): 1.
Further, in the step S4, a 10-30 stage counter-current extraction method is adopted in the process of extracting the manganese sulfate solution.
Further, in the step S4, in the process of extracting the manganese sulfate solution, the extraction temperature is 25-45 ℃.
Further, in step S1, sulfuric acid is used as a pH adjuster for adjusting the pH of the manganese sulfate solution.
Further, in step S5, the process of subjecting the manganese-rich raffinate to evaporative crystallization includes: carrying out first evaporation concentration on the manganese-rich raffinate at the temperature of 70-90 ℃, concentrating until the volume of the manganese-rich raffinate is 1/2-1/3, and filtering to obtain a first concentrated solution; and carrying out second evaporation concentration on the primary concentrated solution at the temperature of 60-70 ℃, concentrating to 3/4-1/2 of the volume of the primary concentrated solution, filtering, and crystallizing to obtain calcium-removed manganese sulfate solid.
Further, in step S5, the process of subjecting the manganese-rich raffinate to evaporative crystallization includes: and (3) evaporating and concentrating the manganese-rich raffinate at the temperature of 70-90 ℃, concentrating to 1/2-1/3 of the volume of the manganese-rich raffinate, filtering, and crystallizing to obtain calcium-removed manganese sulfate solid.
Further, after the calcium-rich organic phase is obtained, the method also comprises a step of back extraction regeneration of the calcium-rich organic phase, wherein the step of back extraction regeneration comprises the following steps: and performing multistage back extraction on the calcium-rich organic phase by adopting sulfuric acid with the concentration of 1-2 mol/L to obtain a calcium-rich back extraction solution and a regenerated organic phase.
Further, after obtaining the regenerated organic phase, the method further comprises the step of returning the regenerated organic phase to step S4 as part or all of the extractant; preferably, after the calcium-rich strip liquor is obtained, the method further comprises the step of concentrating the calcium-rich strip liquor, and returning the concentrated calcium-rich strip liquor to the step S1 as part of the manganese sulfate solution.
The method for reducing the calcium content in the manganese sulfate solution comprises the steps of adjusting the pH value of the manganese sulfate solution to 0.5-3, carrying out ammonia water or sodium hydroxide saponification on an extraction organic phase obtained by mixing an extracting agent P204 with a specific volume concentration and sulfonated kerosene to form a saponification organic phase with a specific saponification rate, and extracting the manganese sulfate solution by using the saponification organic phase, so that calcium ions in the manganese sulfate solution can be well separated. And secondly, evaporating and crystallizing the manganese-rich raffinate obtained by extraction, and further removing impurity calcium ions in the raffinate to obtain calcium-removed manganese sulfate solid. Because the invention adopts the extraction organic phase formed by the extractant P204 and the sulfonated kerosene, the P204 extractant is cheap and can be recycled, the production process is green and environment-friendly, has no pollution, low production and operation cost, and is easy to realize large-scale production. The extraction separation effect of calcium ions is effectively improved by adjusting the process conditions of the proportion of the extractant P204, the saponification rate of the extraction organic phase and the pH value of the manganese sulfate solution, and the removal rate of the calcium ions in the manganese sulfate solution is higher by combining with the evaporative crystallization of raffinate.
In a word, the process provided by the invention is used for removing calcium from the manganese sulfate solution, and has the advantages of environmental friendliness, low cost and high calcium ion removal rate, and has wide application prospect.
Detailed Description
It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. The present invention will be described in detail with reference to examples.
Unless otherwise specified, the solutions in the present invention are all aqueous solutions.
As described in the background art, the prior art cannot consider the aspects of environmental friendliness, low cost, calcium ion removal rate and the like when removing calcium from a manganese sulfate solution.
In order to solve the problems, the invention provides a method for reducing the content of calcium in a manganese sulfate solution, wherein the manganese sulfate solution contains impurity calcium ions, and the method comprises the following steps: s1, adjusting the pH value of the manganese sulfate solution to 0.5-3; s2, mixing an extracting agent P204 and sulfonated kerosene to obtain an extracted organic phase, wherein the volume concentration of the extracting agent P204 is 5-30%; s3, saponifying the extracted organic phase by ammonia water or sodium hydroxide solution to obtain a saponified organic phase, wherein the saponification rate of the saponified organic phase is 5-20%; s4, extracting the manganese sulfate solution by taking the saponified organic phase as an extractant to obtain a manganese-rich raffinate and a calcium-rich organic phase; and S5, carrying out evaporative crystallization on the manganese-rich raffinate to obtain calcium-removed manganese sulfate solid.
The method for reducing the calcium content in the manganese sulfate solution comprises the steps of adjusting the pH value of the manganese sulfate solution to 0.5-3, carrying out ammonia water or sodium hydroxide saponification on an extraction organic phase obtained by mixing an extracting agent P204 with a specific volume concentration and sulfonated kerosene to form a saponification organic phase with a specific saponification rate, and extracting the manganese sulfate solution by using the saponification organic phase, so that calcium ions in the manganese sulfate solution can be well separated. And secondly, evaporating and crystallizing the manganese-rich raffinate obtained by extraction, and further removing impurity calcium ions in the raffinate to obtain calcium-removed manganese sulfate solid. Because the invention adopts the extraction organic phase formed by the extractant P204 and the sulfonated kerosene, the P204 extractant is cheap and can be recycled, the production process is green and environment-friendly, has no pollution, low production and operation cost, and is easy to realize large-scale production. The extraction separation effect of calcium ions is effectively improved by adjusting the process conditions of the proportion of the extractant P204, the saponification rate of the extraction organic phase and the pH value of the manganese sulfate solution, and the removal rate of the calcium ions in the manganese sulfate solution is higher by combining with the evaporative crystallization of raffinate.
In a word, the process provided by the invention is used for removing calcium from the manganese sulfate solution, and has the advantages of environmental friendliness, low cost and high calcium ion removal rate, and has wide application prospect.
In the actual operation process, the concentration of the used ammonia water is preferably 4-8 mol/L, and the concentration of the sodium hydroxide aqueous solution is preferably 200-300 g/L. Therefore, the condition that a water-in-oil structure appears in an extracted organic phase due to the introduction of excessive water in the saponification process is avoided, and the subsequent extraction effect is facilitated.
In order to further improve the extraction separation effect on calcium ions and obtain high-purity manganese sulfate, in a preferred embodiment, in step S3, after obtaining an extracted organic phase, the method further includes a step of performing soap conversion on the extracted organic phase by using a high-purity manganese sulfate solution with a concentration of 80-100 g/L to obtain a soap-converted organic phase; and in step S4, the manganese sulfate solution is extracted using the soap-converted organic phase as an extractant. Compared with the method using the sodium soap organic phase, the soap-converted organic phase is the manganese soap organic phase, and has better extraction and separation effects on impurity calcium ions in the manganese sulfate solution. Meanwhile, the saponification rate of the saponified organic phase used in the invention is 5-20%, which is relatively low, and the amount of manganese sulfate required in the soap conversion process is small.
In a preferred embodiment, in the step S4, during the extraction of the manganese sulfate solution, the O/a ratio of the extracting agent to the manganese sulfate solution is (1-3): 1. The O/A ratio is better than that of the extraction under the condition. More preferably, in the step S4, a 10-30 stage counter-current extraction method is adopted in the process of extracting the manganese sulfate solution. Further preferably, in the step S4, the extraction temperature is 25 to 45 ℃ in the process of extracting the manganese sulfate solution.
In order to avoid the introduction of other impurities, in a preferred embodiment, sulfuric acid is used as a pH adjusting agent in the step S1 for adjusting the pH of the manganese sulfate solution. In the specific operation, sulfuric acid with a concentration of 93% is preferably used as the pH regulator.
As described above, the impurity calcium ions in the manganese sulfate solution can be effectively extracted and separated through extraction, and after the extraction step, calcium ions can be further removed by performing evaporative crystallization on the raffinate, so that the purity of manganese sulfate is improved. And since the extraction effect of the sodium soap or ammonium soap organic phase is different from that of the manganese soap organic phase, in order to make the evaporative crystallization process more compatible, in a preferred embodiment, when the saponified organic phase is used as the extractant to extract the manganese sulfate solution, the step S5 of subjecting the manganese-rich raffinate to evaporative crystallization comprises: carrying out first evaporation concentration on the manganese-rich raffinate at the temperature of 70-90 ℃, concentrating until the volume of the manganese-rich raffinate is 1/2-1/3, and filtering to obtain a first concentrated solution; and carrying out second evaporation concentration on the primary concentrated solution at the temperature of 60-70 ℃, concentrating to 3/4-1/2 of the volume of the primary concentrated solution, filtering, and crystallizing to obtain calcium-removed manganese sulfate solid. When the soap-converted organic phase is used as an extractant to extract the manganese sulfate solution, the process of evaporating and crystallizing the manganese-rich raffinate in the step S5 comprises the following steps: and (3) evaporating and concentrating the manganese-rich raffinate at the temperature of 70-90 ℃, concentrating to 1/2-1/3 of the volume of the manganese-rich raffinate, filtering, and crystallizing to obtain calcium-removed manganese sulfate solid. In the two processes, because the organic phases adopted in the extraction process are different, the content of calcium ions in the raffinate after the soap-converted organic phase extraction is lower than that of the raffinate after the saponification organic phase extraction, so that the corresponding processes are respectively adopted during evaporation crystallization, and the effect of separating crystallized manganese sulfate is better.
In a preferred embodiment, after obtaining the calcium-rich organic phase, the method further comprises a step of back-extraction regeneration of the calcium-rich organic phase, wherein the step of back-extraction regeneration comprises: and performing multistage back extraction on the calcium-rich organic phase by adopting sulfuric acid with the concentration of 1-2 mol/L to obtain a calcium-rich back extraction solution and a regenerated organic phase. Thus, the calcium-rich organic phase can be regenerated by stripping, and more preferably, after the regenerated organic phase is obtained, the method further comprises the step of returning the regenerated organic phase to the step S4 as part or all of the extractant. This can further reduce the production cost. In addition, more preferably, the calcium-rich strip liquor is concentrated and filtered, then is merged into a manganese sulfate solution, and enters the next extraction after the pH value is adjusted, so that manganese sulfate can be completely recovered as far as possible, and the loss of manganese sulfate is avoided. It should be noted that, the strip liquor contains part of manganese ions, if the manganese ions are not returned, the loss of manganese exists, the solubility of calcium sulfate is 0.45g/L at most, after the strip liquor is concentrated, the concentration of calcium is increased and then the calcium is precipitated, so that no more calcium impurities are introduced.
In order to further improve the extraction effect, in a preferred embodiment, before the pH value of the manganese sulfate solution is adjusted, the method further comprises the step of adjusting the content of manganese ions in the manganese sulfate solution to 80-150 g/L.
The present application is described in further detail below with reference to specific examples, which should not be construed as limiting the scope of the invention as claimed.
Example 1
(1) The actual content of each ion in the manganese sulfate solution is determined through atomic absorption, the content of the manganese ion in the manganese sulfate solution is Mn100g/L, and the content of the calcium ion in the manganese sulfate solution is 0.4 g/L. The pH of the manganese sulphate solution was adjusted to 1.8 using 93% sulphuric acid.
(2) Preparing an extraction organic phase, wherein the extraction organic phase consists of an extractant P204 and sulfonated kerosene, and the volume fraction of P204 is 10%. The extracted organic phase was saponified with an aqueous solution of sodium hydroxide having a concentration of 320g/L to obtain a saponified organic phase having a saponification rate of 15%.
(3) And (3) mixing the manganese sulfate solution with the pH value adjusted in the step (1) with the saponified organic phase in the step (2) for multi-stage extraction, wherein the O/A ratio of the saponified organic phase to the manganese sulfate solution is 1.5:1, performing 30-stage countercurrent extraction at the extraction temperature of 25 ℃, and allowing calcium ions in the manganese sulfate solution to enter the saponified organic phase to form a calcium-rich organic phase, wherein the manganese ions are retained in raffinate to obtain manganese-rich raffinate.
(4) And (3) carrying out back extraction on the calcium-rich organic phase in the step (3) by adopting sulfuric acid with the concentration of 2mol/L, wherein the O/A ratio of the calcium-rich organic phase to the sulfuric acid is 2:1, the number of the back extraction stages is 1 stage, so as to obtain a back extraction solution and a regenerated organic phase, and the regenerated organic phase can be recycled to the step (2) for continuous use.
(5) And (4) carrying out evaporative crystallization on the manganese-rich raffinate in the step (3), wherein the specific process is as follows: carrying out first evaporation concentration on the manganese-rich raffinate at the temperature of 90 ℃, concentrating until the manganese-rich raffinate is 1/2 of the volume, and filtering to obtain a first concentrated solution; and then carrying out second evaporation concentration on the primary concentrated solution at the temperature of 60 ℃, concentrating to 3/4 of the volume of the primary concentrated solution, filtering, and crystallizing to obtain a manganese sulfate solid with the concentration of more than 99%.
(6) And (4) concentrating the strip liquor in the step (4) until the manganese concentration is more than 100g/L, filtering, and merging the filtered strip liquor into the manganese sulfate solution to be extracted.
(7) The content of calcium in the manganese sulfate solution treated by the steps is measured by adopting atomic absorption, and the removal rate of calcium ions is more than 98 percent.
Example 2
(1) The actual content of each ion in the manganese sulfate solution is determined through atomic absorption, the content of the manganese ion in the manganese sulfate solution is Mn120g/L, and the content of the calcium ion in the manganese sulfate solution is 0.45 g/L. The pH of the manganese sulphate solution was adjusted to 2 with 93% sulphuric acid.
(2) Preparing an extraction organic phase, wherein the extraction organic phase consists of an extractant P204 and sulfonated kerosene, and the volume fraction of P204 is 10%. The extracted organic phase was saponified with an aqueous solution of sodium hydroxide having a concentration of 320% to obtain a saponified organic phase having a saponification rate of 15%. Secondly, carrying out soap conversion on the saponified organic phase by adopting a high-purity manganese sulfate solution with the concentration of 100g/L to obtain a soap-converted organic phase.
(3) Mixing the manganese sulfate solution with the pH value adjusted in the step (1) with the soap-converted organic phase in the step (2) for multi-stage extraction, wherein the O/A ratio of the soap-converted organic phase to the manganese sulfate solution is 1.5:1, performing 30-stage countercurrent extraction at 25 ℃, and allowing calcium in the manganese sulfate solution to enter the soap-converted organic phase to form a calcium-rich organic phase, wherein manganese ions are retained in raffinate to obtain manganese-rich raffinate.
(4) And (3) carrying out back extraction on the calcium-rich organic phase in the step (3) by adopting sulfuric acid with the concentration of 1mol/L, wherein the O/A ratio of the calcium-rich organic phase to the sulfuric acid is 1:1, the number of the back extraction stages is 1 stage, so as to obtain a calcium-rich back extraction solution and a regenerated organic phase, and the regenerated organic phase can be recycled to the step (2) for continuous use.
(5) And (4) carrying out evaporative crystallization on the manganese-rich raffinate in the step (3), wherein the specific process is as follows: evaporating and concentrating the manganese-rich raffinate at the temperature of 90 ℃, concentrating to 1/2 of the volume of the manganese-rich raffinate, and crystallizing after filtering to obtain manganese sulfate solid with the concentration of 99.5%.
(6) And (4) concentrating the calcium-rich strip liquor obtained in the step (4), filtering the calcium-rich strip liquor until the manganese ion concentration value in the stock solution is reached, and merging the calcium-rich strip liquor into the manganese sulfate solution to be extracted.
(7) The content of calcium in the manganese sulfate solution treated by the steps is measured by adopting atomic absorption, and the removal rate of calcium ions is over 99 percent.
Example 3
(1) The actual content of each ion in the manganese sulfate solution is determined through atomic absorption, the content of the manganese ion in the manganese sulfate solution is Mn100g/L, and the content of the calcium ion in the manganese sulfate solution is 0.4 g/L. The pH of the manganese sulphate solution was adjusted to 3 with 93% sulphuric acid.
(2) Preparing an extraction organic phase, wherein the extraction organic phase consists of an extractant P204 and sulfonated kerosene, and the volume fraction of P204 is 30%. The extracted organic phase was saponified with an aqueous solution of sodium hydroxide having a concentration of 320g/L to obtain a saponified organic phase having a saponification rate of 5%.
(3) Mixing the manganese sulfate solution with the pH value adjusted in the step (1) with the saponified organic phase in the step (2) for multi-stage extraction, wherein the O/A ratio of the saponified organic phase to the manganese sulfate solution is 2:1, performing 30-stage countercurrent extraction at the extraction temperature of 25 ℃, and allowing calcium ions in the manganese sulfate solution to enter the saponified organic phase to form a calcium-rich organic phase, wherein the manganese ions are retained in the raffinate to obtain a manganese-rich raffinate.
(4) And (3) carrying out back extraction on the calcium-rich organic phase in the step (3) by adopting sulfuric acid with the concentration of 2mol/L, wherein the O/A ratio of the calcium-rich organic phase to the sulfuric acid is 2:1, the number of the back extraction stages is 1 stage, so as to obtain a back extraction solution and a regenerated organic phase, and the regenerated organic phase can be recycled to the step (2) for continuous use.
(5) And (4) carrying out evaporative crystallization on the manganese-rich raffinate in the step (3), wherein the specific process is as follows: carrying out first evaporation concentration on the manganese-rich raffinate at the temperature of 90 ℃, concentrating until the manganese-rich raffinate is 1/2 of the volume, and filtering to obtain a first concentrated solution; and performing second evaporation concentration on the primary concentrated solution at the temperature of 60 ℃, concentrating until the volume of the primary concentrated solution is 3/4, filtering, and crystallizing to obtain a manganese sulfate solid with the concentration of more than 99%.
(6) And (4) concentrating the strip liquor in the step (4) until the manganese concentration is more than 100g/L, filtering, and merging the filtered strip liquor into the manganese sulfate solution to be extracted.
(7) The content of calcium in the manganese sulfate solution treated by the steps is measured by adopting atomic absorption, and the removal rate of calcium ions is more than 97.5 percent.
Example 4
(1) The actual content of each ion in the manganese sulfate solution is determined through atomic absorption, the content of the manganese ion in the manganese sulfate solution is Mn100g/L, and the content of the calcium ion in the manganese sulfate solution is 0.4 g/L. The pH of the manganese sulphate solution was adjusted to 0.5 with 93% sulphuric acid.
(2) Preparing an extraction organic phase, wherein the extraction organic phase consists of an extractant P204 and sulfonated kerosene, and the volume fraction of P204 is 5%. The extracted organic phase was saponified with an aqueous solution of sodium hydroxide having a concentration of 320g/L to obtain a saponified organic phase having a saponification rate of 20%.
(3) And (3) mixing the manganese sulfate solution with the pH value adjusted in the step (1) with the saponified organic phase in the step (2) for multi-stage extraction, wherein the O/A ratio of the saponified organic phase to the manganese sulfate solution is 1.5:1, performing 30-stage countercurrent extraction at the extraction temperature of 25 ℃, and allowing calcium ions in the manganese sulfate solution to enter the saponified organic phase to form a calcium-rich organic phase, wherein the manganese ions are retained in raffinate to obtain manganese-rich raffinate.
(4) And (3) carrying out back extraction on the calcium-rich organic phase in the step (3) by adopting sulfuric acid with the concentration of 2mol/L, wherein the O/A ratio of the calcium-rich organic phase to the sulfuric acid is 2:1, the number of the back extraction stages is 1 stage, so as to obtain a back extraction solution and a regenerated organic phase, and the regenerated organic phase can be recycled to the step (2) for continuous use.
(5) And (4) carrying out evaporative crystallization on the manganese-rich raffinate in the step (3), wherein the specific process is as follows: carrying out first evaporation concentration on the manganese-rich raffinate at the temperature of 70 ℃, concentrating the manganese-rich raffinate to 1/2 of the volume of the manganese-rich raffinate, and filtering to obtain a first concentrated solution; and performing second evaporation concentration on the primary concentrated solution at the temperature of 60 ℃, concentrating until the volume of the primary concentrated solution is 3/4, filtering, and crystallizing to obtain a manganese sulfate solid with the concentration of more than 99%.
(6) And (4) concentrating the strip liquor in the step (4) until the manganese concentration is more than 100g/L, filtering, and merging the filtered strip liquor into the manganese sulfate solution to be extracted.
(7) The content of calcium in the manganese sulfate solution treated by the steps is measured by adopting atomic absorption, and the removal rate of calcium ions is more than 98 percent.
Example 5
(1) The actual content of each ion in the manganese sulfate solution is determined through atomic absorption, the content of the manganese ion in the manganese sulfate solution is Mn120g/L, and the content of the calcium ion in the manganese sulfate solution is 0.45 g/L. The pH value of the manganese sulfate solution is adjusted to 1 by using 93 percent sulfuric acid.
(2) Preparing an extraction organic phase, wherein the extraction organic phase consists of an extractant P204 and sulfonated kerosene, and the volume fraction of P204 is 5%. The extracted organic phase was saponified with an aqueous solution of sodium hydroxide having a concentration of 320% to obtain a saponified organic phase having a saponification rate of 20%. Secondly, carrying out soap conversion on the saponified organic phase by adopting a high-purity manganese sulfate solution with the concentration of 120g/L to obtain a soap-converted organic phase.
(3) Mixing the manganese sulfate solution with the pH value adjusted in the step (1) with the soap-converted organic phase in the step (2) for multi-stage extraction, wherein the O/A ratio of the soap-converted organic phase to the manganese sulfate solution is 1.5:1, performing 30-stage countercurrent extraction at 25 ℃, and allowing calcium in the manganese sulfate solution to enter the soap-converted organic phase to form a calcium-rich organic phase, wherein manganese ions are retained in raffinate to obtain manganese-rich raffinate.
(4) And (3) carrying out back extraction on the calcium-rich organic phase in the step (3) by adopting sulfuric acid with the concentration of 1mol/L, wherein the O/A ratio of the calcium-rich organic phase to the sulfuric acid is 1:1, the number of the back extraction stages is 1 stage, so as to obtain a calcium-rich back extraction solution and a regenerated organic phase, and the regenerated organic phase can be recycled to the step (2) for continuous use.
(5) And (4) carrying out evaporative crystallization on the manganese-rich raffinate in the step (3), wherein the specific process is as follows: and (3) evaporating and concentrating the manganese-rich raffinate at the temperature of 80 ℃, concentrating to 1/2 of the volume of the manganese-rich raffinate, filtering, and crystallizing to obtain a manganese sulfate solid with the concentration of 99.5%.
(6) And (4) concentrating the calcium-rich strip liquor obtained in the step (4), filtering the calcium-rich strip liquor until the manganese ion concentration value in the stock solution is reached, and merging the calcium-rich strip liquor into the manganese sulfate solution to be extracted.
(7) The content of calcium in the manganese sulfate solution treated by the steps is measured by adopting atomic absorption, and the removal rate of calcium ions is more than 98.5 percent.
Example 6
(1) The actual content of each ion in the manganese sulfate solution is determined through atomic absorption, the content of the manganese ion in the manganese sulfate solution is Mn120g/L, and the content of the calcium ion in the manganese sulfate solution is 0.45 g/L. The pH of the manganese sulphate solution was adjusted to 3 with 93% sulphuric acid.
(2) Preparing an extraction organic phase, wherein the extraction organic phase consists of an extractant P204 and sulfonated kerosene, and the volume fraction of P204 is 30%. The extracted organic phase was saponified with an aqueous solution of sodium hydroxide having a concentration of 320% to obtain a saponified organic phase having a saponification rate of 5%. Secondly, carrying out soap conversion on the saponified organic phase by adopting a high-purity manganese sulfate solution with the concentration of 100g/L to obtain a soap-converted organic phase.
(3) Mixing the manganese sulfate solution with the pH value adjusted in the step (1) with the soap-converted organic phase in the step (2) for multi-stage extraction, wherein the O/A ratio of the soap-converted organic phase to the manganese sulfate solution is 1.5:1, performing 30-stage countercurrent extraction at 25 ℃, and allowing calcium in the manganese sulfate solution to enter the soap-converted organic phase to form a calcium-rich organic phase, wherein manganese ions are retained in raffinate to obtain manganese-rich raffinate.
(4) And (3) carrying out back extraction on the calcium-rich organic phase in the step (3) by adopting sulfuric acid with the concentration of 1mol/L, wherein the O/A ratio of the calcium-rich organic phase to the sulfuric acid is 1:1, the number of the back extraction stages is 1 stage, so as to obtain a calcium-rich back extraction solution and a regenerated organic phase, and the regenerated organic phase can be recycled to the step (2) for continuous use.
(5) And (4) carrying out evaporative crystallization on the manganese-rich raffinate in the step (3), wherein the specific process is as follows: and (3) evaporating and concentrating the manganese-rich raffinate at the temperature of 80 ℃, concentrating to 1/2 of the volume of the manganese-rich raffinate, filtering, and crystallizing to obtain a manganese sulfate solid with the concentration of 99%.
(6) And (4) concentrating the calcium-rich strip liquor obtained in the step (4), filtering the calcium-rich strip liquor until the manganese ion concentration value in the stock solution is reached, and merging the calcium-rich strip liquor into the manganese sulfate solution to be extracted.
(7) The content of calcium in the manganese sulfate solution treated by the steps is measured by adopting atomic absorption, and the removal rate of calcium ions is more than 98.7 percent.
Example 7
(1) The actual content of each ion in the manganese sulfate solution is determined through atomic absorption, the content of the manganese ion in the manganese sulfate solution is Mn120g/L, and the content of the calcium ion in the manganese sulfate solution is 0.45 g/L. The pH of the manganese sulphate solution was adjusted to 2 with 93% sulphuric acid.
(2) Preparing an extraction organic phase, wherein the extraction organic phase consists of an extractant P204 and sulfonated kerosene, and the volume fraction of P204 is 10%. The extracted organic phase was saponified with an aqueous solution of sodium hydroxide having a concentration of 320% to obtain a saponified organic phase having a saponification rate of 15%. Secondly, carrying out soap conversion on the saponified organic phase by adopting a high-purity manganese sulfate solution with the concentration of 100g/L to obtain a soap-converted organic phase.
(3) Mixing the manganese sulfate solution with the pH value adjusted in the step (1) with the soap-converted organic phase in the step (2) for multi-stage extraction, wherein the O/A ratio of the soap-converted organic phase to the manganese sulfate solution is 1:1, performing 10-stage countercurrent extraction at the extraction temperature of 45 ℃, and allowing calcium in the manganese sulfate solution to enter the soap-converted organic phase to form a calcium-rich organic phase, while manganese ions are retained in raffinate to obtain manganese-rich raffinate.
(4) And (3) carrying out back extraction on the calcium-rich organic phase in the step (3) by adopting sulfuric acid with the concentration of 1mol/L, wherein the O/A ratio of the calcium-rich organic phase to the sulfuric acid is 1:1, the number of the back extraction stages is 1 stage, so as to obtain a calcium-rich back extraction solution and a regenerated organic phase, and the regenerated organic phase can be recycled to the step (2) for continuous use.
(5) And (4) carrying out evaporative crystallization on the manganese-rich raffinate in the step (3), wherein the specific process is as follows: and (3) evaporating and concentrating the manganese-rich raffinate at the temperature of 90 ℃, concentrating to 1/2 of the volume of the manganese-rich raffinate, filtering, and crystallizing to obtain a manganese sulfate solid with the concentration of 99%.
(6) And (4) concentrating the calcium-rich strip liquor obtained in the step (4), filtering the calcium-rich strip liquor until the manganese ion concentration value in the stock solution is reached, and merging the calcium-rich strip liquor into the manganese sulfate solution to be extracted.
(7) The content of calcium in the manganese sulfate solution treated by the steps is measured by adopting atomic absorption, and the removal rate of calcium ions is more than 98.5 percent.
Example 8
(1) The actual content of each ion in the manganese sulfate solution is determined through atomic absorption, the content of the manganese ion in the manganese sulfate solution is Mn120g/L, and the content of the calcium ion in the manganese sulfate solution is 0.45 g/L. The pH of the manganese sulphate solution was adjusted to 1.5 with 93% sulphuric acid.
(2) Preparing an extraction organic phase, wherein the extraction organic phase consists of an extractant P204 and sulfonated kerosene, and the volume fraction of P204 is 10%. The extracted organic phase was saponified with an aqueous solution of sodium hydroxide having a concentration of 320% to obtain a saponified organic phase having a saponification rate of 15%. Secondly, carrying out soap conversion on the saponified organic phase by adopting a high-purity manganese sulfate solution with the concentration of 100g/L to obtain a soap-converted organic phase.
(3) Mixing the manganese sulfate solution with the pH value adjusted in the step (1) with the soap-converted organic phase in the step (2) for multi-stage extraction, wherein the O/A ratio of the soap-converted organic phase to the manganese sulfate solution is 3:1, performing 30-stage countercurrent extraction at 25 ℃, and allowing calcium in the manganese sulfate solution to enter the soap-converted organic phase to form a calcium-rich organic phase while manganese ions are retained in raffinate to obtain manganese-rich raffinate.
(4) And (3) carrying out back extraction on the calcium-rich organic phase in the step (3) by adopting sulfuric acid with the concentration of 1mol/L, wherein the O/A ratio of the calcium-rich organic phase to the sulfuric acid is 1:1, the number of the back extraction stages is 1 stage, so as to obtain a calcium-rich back extraction solution and a regenerated organic phase, and the regenerated organic phase can be recycled to the step (2) for continuous use.
(5) And (4) carrying out evaporative crystallization on the manganese-rich raffinate in the step (3), wherein the specific process is as follows: and (3) evaporating and concentrating the manganese-rich raffinate at the temperature of 90 ℃, concentrating to 1/2 of the volume of the manganese-rich raffinate, filtering, and crystallizing to obtain a manganese sulfate solid with the concentration of 99%.
(6) And (4) concentrating the calcium-rich strip liquor obtained in the step (4), filtering the calcium-rich strip liquor until the manganese ion concentration value in the stock solution is reached, and merging the calcium-rich strip liquor into the manganese sulfate solution to be extracted.
(7) The content of calcium in the manganese sulfate solution treated by the steps is measured by adopting atomic absorption, and the removal rate of calcium ions is more than 98.8 percent.
Example 9
(1) The actual content of each ion in the manganese sulfate solution is determined through atomic absorption, the content of the manganese ion in the manganese sulfate solution is Mn120g/L, and the content of the calcium ion in the manganese sulfate solution is 0.45 g/L. The pH of the manganese sulphate solution was adjusted to 3 with 93% sulphuric acid.
(2) Preparing an extraction organic phase, wherein the extraction organic phase consists of an extractant P204 and sulfonated kerosene, and the volume fraction of P204 is 30%. The extracted organic phase was saponified with an aqueous solution of sodium hydroxide having a concentration of 320% to obtain a saponified organic phase having a saponification rate of 15%. Secondly, carrying out soap conversion on the saponified organic phase by adopting a high-purity manganese sulfate solution with the concentration of 100g/L to obtain a soap-converted organic phase.
(3) Mixing the manganese sulfate solution with the pH value adjusted in the step (1) with the soap-converted organic phase in the step (2) for multi-stage extraction, wherein the O/A ratio of the soap-converted organic phase to the manganese sulfate solution is 0.5:1, performing 8-stage countercurrent extraction at the extraction temperature of 20 ℃, and allowing calcium in the manganese sulfate solution to enter the soap-converted organic phase to form a calcium-rich organic phase, while retaining manganese ions in raffinate to obtain manganese-rich raffinate.
(4) And (3) carrying out back extraction on the calcium-rich organic phase in the step (3) by adopting sulfuric acid with the concentration of 1mol/L, wherein the O/A ratio of the calcium-rich organic phase to the sulfuric acid is 1:1, the number of the back extraction stages is 1 stage, so as to obtain a calcium-rich back extraction solution and a regenerated organic phase, and the regenerated organic phase can be recycled to the step (2) for continuous use.
(5) And (4) carrying out evaporative crystallization on the manganese-rich raffinate in the step (3), wherein the specific process is as follows: and (3) evaporating and concentrating the manganese-rich raffinate at the temperature of 60 ℃, concentrating to 2/3 of the volume of the manganese-rich raffinate, filtering, and crystallizing to obtain a manganese sulfate solid with the concentration of 80%.
(6) And (4) concentrating the calcium-rich strip liquor obtained in the step (4), filtering the calcium-rich strip liquor until the manganese ion concentration value in the stock solution is reached, and merging the calcium-rich strip liquor into the manganese sulfate solution to be extracted.
(7) The content of calcium in the manganese sulfate solution treated by the steps is measured by adopting atomic absorption, and the removal rate of calcium ions is 89.6 percent.
Comparative example 1
(1) The actual content of each ion in the manganese sulfate solution is determined through atomic absorption, the content of the manganese ion in the manganese sulfate solution is Mn100g/L, and the content of the calcium ion in the manganese sulfate solution is 0.45 g/L. The pH of the manganese sulphate solution was adjusted to 3.5 with 50% strength sulphuric acid.
(2) Preparing an extraction organic phase, wherein the extraction organic phase consists of an extractant P204 and sulfonated kerosene, and the volume fraction of P204 is 40%. The extracted organic phase was saponified with an aqueous solution of sodium hydroxide having a concentration of 320g/L to obtain a saponified organic phase having a saponification rate of 50%.
(3) And (3) mixing the manganese sulfate solution with the pH value adjusted in the step (1) with the saponified organic phase in the step (2) for multi-stage extraction, wherein the O/A ratio of the saponified organic phase to the manganese sulfate solution is 1.5:1, performing 30-stage countercurrent extraction at the extraction temperature of 25 ℃, and allowing calcium ions in the manganese sulfate solution to enter the saponified organic phase to form a calcium-rich organic phase, wherein the manganese ions are retained in raffinate to obtain manganese-rich raffinate.
(4) And (3) carrying out back extraction on the calcium-rich organic phase in the step (3) by adopting sulfuric acid with the concentration of 2mol/L, wherein the O/A ratio of the calcium-rich organic phase to the sulfuric acid is 2:1, the number of the back extraction stages is 1 stage, so as to obtain a back extraction solution and a regenerated organic phase, and the regenerated organic phase can be recycled to the step (2) for continuous use.
(5) And (4) carrying out evaporative crystallization on the manganese-rich raffinate in the step (3), wherein the specific process is as follows: and (3) evaporating and concentrating the manganese-rich raffinate at the temperature of 90 ℃, concentrating to 1/2 of the volume of the manganese-rich raffinate, and crystallizing after filtering to obtain a manganese sulfate solid with the concentration of 60%.
(6) The content of calcium in the manganese sulfate solution treated by the steps is measured by adopting atomic absorption, and the removal rate of calcium ions is up to 58%.
Comparative example 2
(1) The actual content of each ion in the manganese sulfate solution is determined through atomic absorption, the content of the manganese ion in the manganese sulfate solution is Mn80g/L, and the content of the calcium ion in the manganese sulfate solution is 0.45 g/L. The pH value of the manganese sulfate solution is adjusted to 3 by using 50 percent sulfuric acid.
(2) Preparing an extraction organic phase, wherein the extraction organic phase consists of an extractant P204 and sulfonated kerosene, and the volume fraction of P204 is 20%. The extracted organic phase was saponified with an aqueous solution of sodium hydroxide having a concentration of 320g/L to obtain a saponified organic phase having a saponification rate of 70%.
(3) Mixing the manganese sulfate solution with the pH value adjusted in the step (1) with the saponified organic phase in the step (2) for multi-stage extraction, wherein the O/A ratio of the saponified organic phase to the manganese sulfate solution is 3.5:1, adopting 8-stage countercurrent extraction, the extraction temperature is 20 ℃, and calcium ions in the manganese sulfate solution enter the saponified organic phase to form a calcium-rich organic phase, and the manganese ions are retained in raffinate to obtain manganese-rich raffinate.
(4) And (3) carrying out back extraction on the calcium-rich organic phase in the step (3) by adopting sulfuric acid with the concentration of 2mol/L, wherein the O/A ratio of the calcium-rich organic phase to the sulfuric acid is 2:1, the number of the back extraction stages is 1 stage, so as to obtain a back extraction solution and a regenerated organic phase, and the regenerated organic phase can be recycled to the step (2) for continuous use.
(5) And (4) carrying out evaporative crystallization on the manganese-rich raffinate in the step (3), wherein the specific process is as follows: and evaporating and concentrating the manganese-rich raffinate at the temperature of 40-60 ℃, concentrating to 1/3 of the volume of the manganese-rich raffinate, filtering, and crystallizing to obtain 50% manganese sulfate solid.
(6) The content of calcium in the manganese sulfate solution treated by the steps is measured by adopting atomic absorption, and the removal rate of calcium ions is up to 55 percent.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A method for reducing the content of calcium in a manganese sulfate solution, wherein the manganese sulfate solution contains impurity calcium ions, and the method is characterized by comprising the following steps:
s1, adjusting the pH value of the manganese sulfate solution to 0.5-3;
s2, mixing an extracting agent P204 and sulfonated kerosene to obtain an extracted organic phase, wherein the volume concentration of the extracting agent P204 is 5-30%;
s3, saponifying the extracted organic phase by ammonia water or sodium hydroxide solution to obtain a saponified organic phase, wherein the saponification rate of the saponified organic phase is 5-20%;
s4, extracting the manganese sulfate solution by taking the saponified organic phase as an extractant to obtain a manganese-rich raffinate and a calcium-rich organic phase;
and S5, carrying out evaporative crystallization on the manganese-rich raffinate to obtain calcium-removed manganese sulfate solid.
2. The method as claimed in claim 1, wherein in the step S3, after obtaining the extracted organic phase, the method further comprises the step of performing soap conversion on the extracted organic phase by using a high-purity manganese sulfate solution with a concentration of 80-100 g/L to obtain a soap converted organic phase; and in step S4, extracting the manganese sulfate solution with the soap-converted organic phase as the extractant.
3. The method as claimed in claim 1 or 2, wherein in the step S4, the O/A ratio of the extracting agent to the manganese sulfate solution is (1-3): 1 during the extraction of the manganese sulfate solution.
4. The method as claimed in claim 3, wherein in the step S4, 10-30 stages of counter-current extraction are adopted in the process of extracting the manganese sulfate solution.
5. The method according to claim 3, wherein in the step S4, the extraction temperature is 25-45 ℃ during the extraction of the manganese sulfate solution.
6. The method according to any one of claims 1 to 5, wherein in step S1, sulfuric acid is used as a pH regulator in the adjustment of the pH value of the manganese sulfate solution.
7. The method according to claim 1, wherein the step S5 of subjecting the manganese-rich raffinate to evaporative crystallization comprises:
carrying out first evaporation concentration on the manganese-rich raffinate at the temperature of 70-90 ℃, concentrating until the manganese-rich raffinate is 1/2-1/3 of the volume, and filtering to obtain a first concentrated solution;
and carrying out second evaporation concentration on the primary concentrated solution at the temperature of 60-70 ℃, concentrating until the volume of the primary concentrated solution is 3/4-1/2, filtering, and crystallizing to obtain the calcium-removed manganese sulfate solid.
8. The method according to claim 2, wherein the step S5 of subjecting the manganese-rich raffinate to evaporative crystallization comprises: and evaporating and concentrating the manganese-rich raffinate at the temperature of 70-90 ℃, concentrating the manganese-rich raffinate to 1/2-1/3 of the volume of the manganese-rich raffinate, filtering and crystallizing to obtain the calcium-removed manganese sulfate solid.
9. The method according to any one of claims 1 to 5, wherein after obtaining the calcium-rich organic phase, the method further comprises a step of back-extraction regeneration of the calcium-rich organic phase, wherein the step of back-extraction regeneration comprises:
and carrying out multistage back extraction on the calcium-rich organic phase by adopting sulfuric acid with the concentration of 1-2 mol/L to obtain a calcium-rich back extraction solution and a regenerated organic phase.
10. The method of claim 9, further comprising, after obtaining said regenerated organic phase, the step of returning said regenerated organic phase to said step S4 as part or all of said extractant; preferably, after the calcium-rich strip liquor is obtained, the method further comprises the step of concentrating the calcium-rich strip liquor at first and then returning the concentrated calcium-rich strip liquor to the step S1 as part of the manganese sulfate solution.
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Application publication date: 20200619 |