CN112575193A - Method for separating copper and manganese and application thereof - Google Patents
Method for separating copper and manganese and application thereof Download PDFInfo
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- CN112575193A CN112575193A CN202011330337.0A CN202011330337A CN112575193A CN 112575193 A CN112575193 A CN 112575193A CN 202011330337 A CN202011330337 A CN 202011330337A CN 112575193 A CN112575193 A CN 112575193A
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
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Abstract
The invention relates to a method for separating copper and manganese and application thereof, wherein the method comprises the following steps: (1) carrying out first extraction on the copper-manganese feed liquid to obtain a first organic phase and a first water phase; wherein the extractant A used in the first extraction comprises 1 or a combination of at least 2 of carboxylic acid extractants; (2) washing and back-extracting the first organic phase obtained in the step (1) in turn to obtain a copper-containing solution; (3) performing second extraction on the first aqueous phase obtained in the step (1) to obtain a second organic phase and a second aqueous phase; and washing and back-extracting the second organic phase in sequence to obtain the manganese-rich solution. By the method, two valuable metals of copper and manganese are effectively separated and extracted, the operation is simple, and meanwhile, the extraction rates of the carboxylic acid extracting agent on Cu and Mn are both more than 99.5%, and the sulfuric acid back extraction rate is more than 99.5%.
Description
Technical Field
The invention relates to the field of wet metallurgy, in particular to a method for separating copper and manganese and application thereof.
Background
At present, in the hydrometallurgical production of cobalt, impurity ions in a cobalt raw material are removed in the impurity removal process of P204 to form chloride solutions containing a large amount of impurity metals such as copper, manganese and calcium, and the solutions are usually precipitated by sodium carbonate to form copper, manganese and calcium carbonate, wherein the content of copper and manganese is the largest, and the value is high. This carbonate slag is produced annually by a large cobalt smelter in the order of tens of millions of tons, with values of valuable metals in the tens of millions.
The solvent extraction technology is an effective technology for separating and extracting various metals from a solution, and has the advantages of high separation efficiency, simple process and equipment, continuous operation, easy realization of automatic control and the like. Has been continuously noticed and developed by many researchers.
At present, there are many related processes for copper-manganese separation, but there are problems of complex separation method, poor copper-manganese separation effect, high cost, and the like. For example, chinese patent (publication No. CN105274352A) adds sulfuric acid to copper carbonate manganese slag to form a sulfate solution, removes calcium sulfate precipitate, then uses copper extraction reagents such as ketoxime or aldoxime to separate copper in the form of copper sulfate, adjusts the pH of the solution after copper removal, adds active metal powder to reduce cobalt into cobalt powder, and separates cobalt powder to obtain manganese-containing filtrate, and adds sodium carbonate to the filtrate to precipitate manganese to obtain manganese carbonate; chinese patent (CN102888513A) precipitates calcium through sulfate, and precipitates copper-cobalt-zinc mixture through carbonate and sulfide to obtain manganese chloride crystal concentrate, then adopts inorganic acid to dissolve copper-cobalt-zinc mixture, and adds reducing agent to reduce copper, adjusts pH value of solution to make solid zinc sulfide, cobalt sulfide and Cu in solution+And (3) carrying out conversion reaction, adding excessive sulfide to ensure that all copper which does not participate in the reaction is generated and precipitated to be removed, finally adjusting the pH value of the cobalt-zinc solution, adding sodium chloride or introducing chlorine to oxidize the cobalt into cobalt hydroxide, and separating out the cobalt hydroxide.
Disclosure of Invention
In view of the problems in the prior art, the invention aims to provide a method for separating copper and manganese and an application thereof, which can effectively separate copper and manganese in feed liquid, is simple to operate, and adopts a carboxylic acid extractant which has low water solubility, high stability and reduced process cost.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a method for separating copper and manganese and application thereof, wherein the method comprises the following steps:
(1) carrying out first extraction on the copper-manganese feed liquid to obtain a first organic phase and a first water phase; wherein the extractant A used in the first extraction comprises 1 or a combination of at least 2 of carboxylic acid extractants; the carboxylic acid extractant has the following structural general formula:
wherein R is1And R2Independently is C3～C9A linear or branched alkyl group; the volume ratio of the extracting agent A to the copper-manganese feed liquid in the first extraction is (0.1-10) to 1; saponifying the extractant A used in the first extraction before use; the pH of the first aqueous phase is 3-4.5;
(2) washing and back-extracting the first organic phase obtained in the step (1) in turn to obtain a copper-containing solution;
(3) performing second extraction on the first aqueous phase obtained in the step (1) to obtain a second organic phase and a second aqueous phase; and washing and back-extracting the second organic phase in sequence to obtain the manganese-rich solution.
By the method, the copper and manganese valuable metals are separated and extracted, the operation is simple, and meanwhile, the extraction rate of the carboxylic acid extracting agent to Cu and Mn is more than 99.5%, and the sulfuric acid back extraction rate is more than 99.5%.
In the present invention, the volume ratio of the extractant a to the copper-manganese feed liquid in the first extraction is (0.1 to 10):1, and may be, for example, 0.1:1, 0.5:1, 1:1, 2:1, 3:1, 4:1, 5:1, 6:1, 7:1, 8:1, 9:1 or 10:1, but is not limited to the values listed, and other values not listed in this range are also applicable.
In the present invention, the pH of the first aqueous phase is 3 to 4.5, and may be, for example, 3, 3.3, 3.5, 3.8, 4, 4.1, 4.2, 4.3, 4.4 or 4.5, but is not limited to the values listed, and other values not listed in the range are also applicable.
As a preferable technical scheme of the invention, the metal elements in the copper-manganese feed liquid in the step (1) comprise: cu, Mn, Ca, Fe, Al, Co and Zn.
Preferably, the concentration of Al in the Cu-Mn feed liquid is less than or equal to 1g/L, such as 1g/L, 0.8g/L, 0.6g/L, 0.4g/L, or 0.2g/L, but not limited to the values listed, and other values not listed in the range are also applicable.
In a preferred embodiment of the present invention, the volume fraction of the extractant a in the first extraction in step (1) is 5 to 30%, for example, 5%, 10%, 15%, 20%, 25%, or 30%, but is not limited to the values listed above, and other values not listed above are also applicable within this range.
Preferably, the first extraction in step (1) is multi-stage countercurrent extraction.
Preferably, the multistage countercurrent extraction has a number of stages of 2 to 30, such as 2, 5, 10, 15, 20, 25 or 30, but not limited to the values recited, and other values not recited in this range are equally applicable.
Preferably, the stirring speed in the first extraction in step (1) is 100-250r/min, such as 100r/min, 150r/min, 200r/min or 250r/min, but not limited to the enumerated values, and other unrecited values in the range are also applicable.
Preferably, the time of the first extraction in step (1) is 5-30min, such as 5min, 10min, 15min, 20min, 25min or 30min, but not limited to the recited values, and other values not recited in the range are also applicable.
As a preferred embodiment of the present invention, the saponification in step (1) is carried out with 6 to 14mol/L of a basic solution, for example, 6mol/L, 7mol/L, 8mol/L, 9mol/L, 10mol/L, 11mol/L, 12mol/L, 13mol/L or 14mol/L, but not limited to the above-mentioned values, and other values not listed in the above range are also applicable.
As a preferred technical scheme of the invention, the washing in the step (2) is multi-stage countercurrent washing.
Preferably, the number of washing stages in step (2) is 2 to 10, and may be, for example, 2, 3, 4, 5, 6, 7, 8, 9 or 10, etc., but is not limited to the recited values, and other values not recited in the range are also applicable.
Preferably, the washing in step (2) is washing with an acid solution.
Preferably, the back extraction in the step (2) is performed by using acid liquor.
In the present invention, the volume ratio of the organic phase to the aqueous phase in the washing and stripping of the first organic phase is (0.1 to 10):1, and may be, for example, 0.1:1, 0.5:1, 1:1, 2:1, 3:1, 4:1, 5:1, 6:1, 7:1, 8:1, 9:1 or 10:1, but is not limited to the values listed, and other values not listed in the range are also applicable.
In a preferred embodiment of the present invention, the extractant B used in the second extraction in step (3) includes a phosphorus-type extractant and/or a carboxylic acid-type extractant.
In the present invention, the phosphorus-based extractant includes C272 and the like.
Preferably, the carboxylic acid extractant has the following structural formula:
wherein R is1And R2Independently is C3～C9Straight or branched chain alkyl.
Preferably, the carboxylic acid type extractant in the extractant B comprises 1 carboxylic acid or a mixture of at least 2 carboxylic acids.
Preferably, the volume fraction of the extractant B is 5 to 30%, for example 5%, 10%, 15%, 20%, 25% or 30%, etc., but is not limited to the recited values, and other values not recited in this range are also applicable.
In a preferred embodiment of the present invention, the volume ratio of the extractant B to the first aqueous phase in the second extraction in step (3) is (0.1 to 10):1, and may be, for example, 0.1:1, 0.5:1, 1:1, 2:1, 3:1, 4:1, 5:1, 6:1, 7:1, 8:1, 9:1 or 10:1, but is not limited to the values listed, and other values not listed in this range are also applicable.
Preferably, the second extraction in step (3) is a multi-stage countercurrent extraction.
Preferably, the multistage countercurrent extraction has a number of stages of 2 to 30, for example 5, 10, 15, 20, 25 or 30, etc., but is not limited to the values listed, and other values not listed in this range are equally applicable.
Preferably, the stirring speed in the second extraction in the step (3) is 100-250r/min, such as 100r/min, 150r/min, 200r/min or 250r/min, but not limited to the enumerated values, and other unrecited values in the range are also applicable.
Preferably, the time of the second extraction in step (3) is 5-30min, such as 5min, 10min, 15min, 20min, 25min or 30min, but not limited to the recited values, and other values not recited in the range are also applicable.
In the present invention, the pH value of the second aqueous phase may have different pH operation intervals due to different extraction agents, and is not specifically limited in the present invention, for example, when C272 is adopted, the pH value of the second aqueous phase is 3 to 4, and when the carboxylic acid extraction agent is adopted, the pH value of the second aqueous phase is 4.5 to 6.5, preferably 5 to 6.5.
In a preferred embodiment of the present invention, the extractant B used in the second extraction in step (3) is saponified before use.
Preferably, the saponification is carried out using 6 to 14mol/L lye, which may be, for example, 6mol/L, 7mol/L, 8mol/L, 9mol/L, 10mol/L, 11mol/L, 12mol/L, 13mol/L or 14mol/L, but is not limited to the recited values, and other values not recited in this range are also applicable.
As a preferred technical scheme of the invention, the washing in the step (3) is multi-stage countercurrent washing.
Preferably, the number of washing stages in step (3) is 2 to 10, and may be, for example, 2, 3, 4, 5, 6, 7, 8, 9 or 10, etc., but is not limited to the recited values, and other values not recited in the range are also applicable.
Preferably, the washing in step (3) is washing with an acid solution.
Preferably, the volume ratio of the organic phase to the aqueous phase in the washing in step (3) is (0.1-10):1, and may be, for example, 0.1:1, 0.5:1, 1:1, 2:1, 3:1, 4:1, 5:1, 6:1, 7:1, 8:1, 9:1 or 10:1, but is not limited to the values recited, and other values not recited in this range are also applicable.
Preferably, the back extraction in the step (3) is performed by using acid liquor.
Preferably, the volume ratio of the organic phase to the aqueous phase in the stripping in step (3) is (0.1-10):1, and may be, for example, 0.1:1, 0.5:1, 1:1, 2:1, 3:1, 4:1, 5:1, 6:1, 7:1, 8:1, 9:1 or 10:1, but is not limited to the recited values, and other values not recited in this range are also applicable.
Preferably, the second aqueous phase is sequentially subjected to oil removal and crystallization to obtain sodium sulfate crystals.
Preferably, the crystallization is by MVR evaporation.
As a preferred technical scheme of the invention, the method comprises the following steps:
(1) carrying out first extraction on the copper-manganese feed liquid to obtain a first organic phase and a first water phase; wherein the extractant A used in the first extraction comprises 1 or a combination of at least 2 of carboxylic acid extractants; the carboxylic acid extractant has the following structural general formula:
wherein R is1And R2Independently is C3～C9A linear or branched alkyl group; the volume ratio of the extractant A to the copper-manganese feed liquid in the first extraction is (0.1-10) to 1, and the volume fraction of the extractant A in the first extraction is 5-30%; the first extraction time is 5-30 min; saponifying the extractant A used in the first extraction before use; the pH of the first aqueous phase is 3-4.5;
(2) washing and back-extracting the first organic phase obtained in the step (1) in turn to obtain a copper-containing solution;
(3) performing second extraction on the first aqueous phase obtained in the step (1) to obtain a second organic phase and a second aqueous phase; washing and back-extracting the second organic phase in sequence to obtain a manganese-rich solution; wherein, the extractant B used in the second extraction comprises a phosphorus type extractant and/or a carboxylic acid extractant; the carboxylic acid extractant has the following structural general formula:
wherein R is1And R2Independently is C3～C9A linear or branched alkyl group; the volume fraction of the extractant B is 5-30%; the volume ratio of the extractant B to the first aqueous phase in the second extraction is (0.1-10) to 1; the time of the second extraction is 5-30 min.
In the invention, the second organic phase obtained by the second extraction can be returned to the first extraction for copper extraction.
In the present invention, when the mixed solution contains zinc, the solution after back extraction contains zinc, and can be removed by conventional methods before the first or second extraction, for example, by using phosphorus type and/or carboxylic acid extractant in step (1), and when the carboxylic acid extractant is used for extraction, zinc ions can be removed by controlling the water phase equilibrium pH to 4.5-5; meanwhile, if the solution contains iron and aluminum, the iron and aluminum can be removed by conventional methods in the prior art, such as chemical precipitation, extraction (e.g., carboxylic acid extractant in the present invention), and then the first extraction is performed.
In the present invention, the diluent of the extractant includes 1 or a combination of at least 2 of mineral spirit, kerosene, Escaid110, hexane, heptane, dodecane.
The combination may be a combination of mineral spirits and kerosene, a combination of Escaid110 and hexane or a combination of heptane and dodecane, etc., but is not limited to the combinations enumerated, and other combinations not enumerated within this range are equally applicable.
In the present invention, the solvent may be mineral spirit No. 200 and/or mineral spirit No. 260.
In the present invention, the dodecane may be n-dodecane or the like.
In the present invention, the alkali solution comprises 1 or a combination of at least 2 of sodium hydroxide solution, potassium hydroxide solution or ammonia water.
The combination may be a combination of a sodium hydroxide solution and a potassium hydroxide solution, a combination of a potassium hydroxide solution and aqueous ammonia, or the like, but is not limited to the listed combinations, and other combinations not listed in this range are also applicable.
In the present invention, the acid solution used in the washing and stripping is sulfuric acid and/or hydrochloric acid, etc., the pH of the acid solution used in the washing is 1 to 2, for example, 1, 1.2, 1.4, 1.5, 1.8 or 2, etc., but not limited to the values listed, and other values not listed in this range are also applicable, the hydrochloric acid used in the stripping is 1 to 6mol/L, for example, 1mol/L, 1.5mol/L, 2mol/L, 3mol/L, 4mol/L, 5mol/L or 6mol/L, etc., but not limited to the values listed, and the sulfuric acid used in the stripping is 0.5 to 3.5mol/L, for example, 0.5mol/L, 1mol/L, 2mol/L, 3mol/L or 3.5mol/L, etc., but not limited to the values listed, other values not listed within this range are equally applicable.
In the invention, the extractant obtained by back extraction of the first organic phase can be returned to the extraction operation after saponification.
In the present invention, the carboxylic acid extractant is a mixture of one or more carboxylic acids, such as extractant BC196 (R in the formula)1Is n-butyl, R2Compound corresponding to isononyl group), extracting agent BC192 (R in the general formula)1Is n-hexyl, R2Compound corresponding to n-nonyl group), a mixture of extracting agents BC196 and BC 192.
In the present invention, the countercurrent extraction is one of the extraction and separation methods, and the water phase and the organic phase containing the extract flow into the extractor from both ends thereof, flow in opposite directions, and are continuously stirred in multiple stages to contact and separate layers, thereby achieving the purpose of separation.
In the present invention, the reaction equation of the relevant process is as follows:
saponification of carboxylic acid extractant: HA(org)+NaOH→NaA(org)+H2O
Extracting with carboxylic acid extractant: 2NaA(org)+MSO4→MA2(org)+Na2SO4
Sulfuric acid back extraction: MA (MA)2(org)+H2SO4→2HA(org)+MSO4
Wherein: m is Cu2+、Mn2+And the like.
Compared with the prior art, the invention at least has the following beneficial effects:
(1) the method provided by the invention has good effect of separating metal ions, can effectively separate and extract copper and manganese in the copper-manganese feed liquid, is simple to operate, has stable process and low operation cost, and in addition, the acid extractant has low water solubility, and the organic phase can be recycled.
(2) In the recovery method provided by the invention, the extraction rate of copper and manganese is more than or equal to 99.5%, and the back extraction rate of sulfuric acid is more than or equal to 99.5%.
Drawings
FIG. 1 is a schematic diagram of a method for separating Cu and Mn from Cu-Mn feed liquid in example 1 of the present invention.
Detailed Description
The present invention is described in further detail below. The following examples are merely illustrative of the present invention and do not represent or limit the scope of the claims, which are defined by the claims.
To better illustrate the invention and to facilitate the understanding of the technical solutions thereof, typical but non-limiting examples of the invention are as follows:
example 1
This example provides a method for separating copper and manganese and its application, as shown in FIG. 1.
The copper-manganese feed liquid in the embodiment is derived from a P204 extraction impurity-removing liquid: 58g/L of manganese, 15g/L of copper, 0.5g/L of calcium, 3.2g/L of zinc and 0.01g/L of iron.
In this example, in order to obtain a single copper solution and a single manganese solution, iron and zinc were removed by using C272 at the beginning of extraction, and a copper-manganese feed solution with iron, aluminum and zinc removed was obtained.
Carrying out 10-stage countercurrent extraction on the copper-manganese material liquid without the iron, aluminum and zinc by using saponified BC196 (the volume fraction of which is 25 percent, the diluent is Escaid110 and the saponification is carried out by using 6mol/L ammonia water solution), wherein the volume ratio of the extracting agent to the copper-manganese material liquid without the iron, aluminum and zinc is 2:1, the extraction time is 8min, the stirring speed is 150r/min, the experimental temperature is 25 ℃, phase separation is carried out, a first organic phase and a first water phase with the pH value of 3.5 are respectively obtained, carrying out 2-stage countercurrent washing on the first organic phase by using sulfuric acid with the pH value of 1.5, carrying out back extraction for 3 times by using 2mol/L sulfuric acid, the volume of the first organic phase and the washing liquid or the back extraction liquid is 8:1, carrying out oil removal on the obtained copper sulfate solution, concentrating and crystallizing, and returning the back extracted organic phase to the saponification process for recycling.
Performing multistage countercurrent extraction on the first aqueous phase by using saponified BC196 (the volume fraction is 25%, the diluent is Escaid110, and saponification is performed by using 6mol/L ammonia water solution), wherein the extraction stage number is 8, the volume ratio of the extractant to the first aqueous phase is 4:1, the extraction time is 8min, the stirring speed is 150r/min, standing is performed for 15min, the experimental temperature is 25 ℃, a second organic phase and a second aqueous phase with the pH value of 5.7 are respectively obtained, performing 5-stage countercurrent washing on the second organic phase by using sulfuric acid with the pH value of 1.5, performing back extraction for 5 times by using 2mol/L sulfuric acid, and the volume ratio of the second organic phase to the washing solution or the back extraction solution is 2:1, thereby obtaining the manganese-rich solution after back extraction.
In this example, the extraction rates of Cu and Mn were 99.7% and 99.8%, respectively, and the back-extraction rates were 99.7% and 99.6%, respectively.
Example 2
The embodiment provides a separation method of copper and manganese and application thereof, wherein in the copper-manganese feed liquid in the embodiment: 10g/L of manganese, 0.01g/L of copper, 0.34g/L of calcium and 1.0g/L of zinc.
Carrying out 7-stage countercurrent extraction on a copper-manganese feed liquid by using saponified BC192 (the volume fraction is 20%, the diluent is 260 # solvent oil, and saponification is carried out by using 10mol/L NaOH solution), wherein the volume ratio of an extracting agent to the copper-manganese feed liquid is 0.2:1, the extraction time is 5min, the stirring speed is 200r/min, standing is carried out for 20min, the experimental temperature is 25 ℃, phase separation is carried out, a first organic phase and a first water phase with the pH value of 4 are respectively obtained, carrying out 4-stage countercurrent washing on the first organic phase by using sulfuric acid with the pH value of 1.2, carrying out back extraction for 1 time by using 2mol/L sulfuric acid, the volume of the first organic phase and a washing liquid or a back extraction liquid is 10:1, carrying out concentration and crystallization on a copper sulfate solution obtained by back extraction after oil removal, and returning the organic phase obtained by back extraction to a saponification process for recycling.
Performing multistage countercurrent extraction on the first water phase by using saponified C272 (the volume fraction is 20%, the diluent is 260 # solvent oil, and the saponifying agent is 10mol/L NaOH solution), wherein the extraction stage number is 5, the volume ratio of the extracting agent to the first water phase is 0.2:1, the extraction time is 5min, the stirring speed is 200r/min, standing is performed for 20min, the experimental temperature is 25 ℃ in the conventional way, the pH value of the water phase is controlled to be 2.5, phase separation is performed to obtain a zinc-loaded organic phase and a first water phase after zinc removal, performing 3-stage countercurrent washing on the zinc-loaded organic phase by using sulfuric acid with the pH value of 1.2, performing back extraction for 2 times by using 2mol/L sulfuric acid, and the volume of the organic phase in washing or back extraction and a washing liquid or a back extraction liquid is 10:1 to obtain a zinc-rich solution, and performing oil removal, concentration and crystallization.
And (3) performing 5-stage extraction on the first water phase subjected to zinc removal by using saponified C272, wherein the volume ratio of an extracting agent to the first water phase is 1:1, the other extraction conditions are the same as above, performing phase separation to respectively obtain a second organic phase and a second water phase with the pH value of 4, performing 3-stage countercurrent washing on the second organic phase by using sulfuric acid with the pH value of 1.2, performing back extraction for 4 times by using 2.5mol/L sulfuric acid, and obtaining a manganese-rich solution by using the volume of the organic phase in the washing or back extraction and a washing solution or a back extraction solution as 10: 1.
In this example, the extraction rates of Cu and Mn were 99.6% and 99.7%, respectively, and the back-extraction rates were 99.7% and 99.8%, respectively.
Example 3
The embodiment provides a separation method of copper and manganese and application thereof, wherein in the copper-manganese feed liquid in the embodiment: 15g/L of manganese, 0.05g/L of copper, 0.4g/L of calcium and 1.2g/L of zinc.
Carrying out 4-stage countercurrent extraction on the copper-manganese-calcium-zinc-containing solution by adopting a manganese-loaded BC196 (from a washed second organic phase), wherein the volume ratio of an extracting agent to a copper-manganese feed liquid is 0.2:1, the extraction time is 10min, the stirring speed is 150r/min, the standing time is 10min, the experimental temperature is 25 ℃, phase splitting is carried out, a first organic phase and a first water phase with the pH value of 4.5 are respectively obtained, carrying out 5-stage countercurrent washing on the first organic phase by adopting sulfuric acid with the pH value of 1, carrying out back extraction for 1 time by adopting 2.5mol/L sulfuric acid, wherein the volume of the first organic phase and a washing liquid or a back extraction liquid is 10:1, carrying out oil removal on copper sulfate solution obtained by back extraction, concentrating and crystallizing, and returning the organic phase obtained by back extraction to a saponification process for recycling.
The method comprises the steps of extracting and removing zinc in a first water phase by using saponified BC196 (the volume fraction of which is 25 percent, the diluent is Escaid110 and saponification is carried out by using 8mol/L NaOH solution), wherein the extraction stage number is 9 stages, the pH of the water phase is controlled to be 4.8, a zinc-loaded organic phase and a first water phase after zinc removal are obtained after phase separation, carrying out 5-stage countercurrent washing on the zinc-loaded organic phase by using dilute sulfuric acid with the pH of 1, carrying out back extraction for 2 times by using 2.5mol/L sulfuric acid, wherein the volume of the first organic phase and a washing solution or a back extraction solution is 10:1, and carrying out oil removal, concentration and crystallization on zinc sulfate solution obtained by back extraction.
Performing multistage countercurrent extraction on the first water phase subjected to zinc removal by using saponified BC196, wherein the extraction stage is 7, the volume ratio of an extracting agent to the first water phase is 2:1, the extraction time is 10min, the stirring speed is 150r/min, the standing is 10min, the experimental temperature is 25 ℃, a second organic phase and a second water phase with the pH value of 6.5 are respectively obtained, performing 7-stage countercurrent washing on the second organic phase by using sulfuric acid with the pH value of 1, performing back extraction for 4 times by using 2.5mol/L sulfuric acid, and obtaining a manganese-rich solution after the back extraction, wherein the volume ratio of the second organic phase to a washing solution or a back extraction solution is 10: 1.
In this example, the extraction rates of Cu and Mn were 99.6% and 99.5%, respectively, and the back-extraction rates were 99.7% and 99.7%, respectively.
Comparative example 1
The only difference from example 1 is that the extractant in the first extraction was replaced with carboxylic acid extractant CA-12, and the extraction rates of Cu and Mn were found to be 98.6% and 99.0%, respectively, and the back-extraction rates were found to be 99.5% and 99.4%, respectively.
The applicant declares that the present invention illustrates the detailed structural features of the present invention through the above embodiments, but the present invention is not limited to the above detailed structural features, that is, it does not mean that the present invention must be implemented depending on the above detailed structural features. It should be understood by those skilled in the art that any modifications of the present invention, equivalent substitutions of selected components of the present invention, additions of auxiliary components, selection of specific modes, etc., are within the scope and disclosure of the present invention.
The preferred embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and the invention is not described in any way for the possible combinations in order to avoid unnecessary repetition.
In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.
Claims (12)
1. A method for separating copper and manganese and application thereof are characterized in that the method comprises the following steps:
(1) carrying out first extraction on the copper-manganese feed liquid to obtain a first organic phase and a first water phase; wherein the extractant A used in the first extraction comprises 1 or a combination of at least 2 of carboxylic acid extractants; the carboxylic acid extractant has the following structural general formula:
wherein R is1And R2Independently is C3～C9A linear or branched alkyl group; the volume ratio of the extracting agent A to the copper-manganese feed liquid in the first extraction is (0.1-10) to 1; saponifying the extractant A used in the first extraction before use; the pH of the first aqueous phase is 3-4.5;
(2) washing and back-extracting the first organic phase obtained in the step (1) in turn to obtain a copper-containing solution;
(3) performing second extraction on the first aqueous phase obtained in the step (1) to obtain a second organic phase and a second aqueous phase; and washing and back-extracting the second organic phase in sequence to obtain the manganese-rich solution.
2. The method of claim 1, wherein the metal elements in the copper-manganese feed solution in step (1) comprise: cu, Mn, Ca, Fe, Al, Co and Zn;
preferably, the concentration of Al in the copper-manganese feed liquid is less than or equal to 1 g/L.
3. The process of claim 1 or 2, wherein the volume fraction of extractant a in the first extraction of step (1) is from 5 to 30%;
preferably, the first extraction in step (1) is a multi-stage countercurrent extraction;
preferably, the extraction stages of the multistage countercurrent extraction are 2-20 stages;
preferably, the stirring speed in the first extraction in the step (1) is 100-;
preferably, the time of the first extraction in the step (1) is 5-30 min.
4. The process according to any one of claims 1 to 3, wherein the saponification in step (1) is carried out with 6 to 14mol/L lye.
5. The method according to any one of claims 1 to 4, wherein the washing in step (2) is a multi-stage counter-current washing;
preferably, the washing in the step (2) is performed in 2-10 stages;
preferably, the washing in the step (2) is washing with acid liquor;
preferably, the back extraction in the step (2) is performed by using acid liquor.
6. The process of any one of claims 1 to 5, wherein the extractant B used in the second extraction of step (3) comprises a phosphorus-type extractant and/or a carboxylic acid-type extractant;
preferably, the carboxylic acid extractant has the following structural formula:
wherein R is1And R2Independently is C3～C9A linear or branched alkyl group;
preferably, the carboxylic acid type extractant in the extractant B comprises 1 carboxylic acid or a mixture of at least 2 carboxylic acids;
preferably, the volume fraction of the extractant B is 5 to 30%.
7. The process of any one of claims 1 to 6, wherein the volume ratio of extractant B to first aqueous phase in the second extraction of step (3) is (0.1-10): 1;
preferably, the second extraction in step (3) is a multi-stage countercurrent extraction;
preferably, the number of stages of the multistage countercurrent extraction is 2-20 stages;
preferably, the stirring speed in the second extraction in the step (3) is 100-250 r/min;
preferably, the time of the second extraction in the step (3) is 5-30 min.
8. The process according to any one of claims 1 to 7, wherein the extractant B used in the second extraction of step (3) is saponified before use;
preferably, the saponification is carried out with 6 to 14mol/L lye.
9. The method according to any one of claims 1 to 8, wherein the washing in step (3) is a multi-stage counter-current washing;
preferably, the washing in the step (3) is performed in 2-10 stages;
preferably, the washing in the step (3) is washing with acid liquor;
preferably, the volume ratio of the organic phase to the aqueous phase in the washing in the step (3) is (0.1-10): 1;
preferably, the back extraction in the step (3) is performed by using acid liquor;
preferably, the volume ratio of the organic phase to the aqueous phase in the back extraction in the step (3) is (0.1-10): 1;
preferably, the second aqueous phase is sequentially subjected to oil removal and crystallization to obtain sodium sulfate crystals;
preferably, the crystallization is by MVR evaporation.
10. A method according to any one of claims 1-9, characterized in that the method comprises the steps of:
(1) carrying out first extraction on the copper-manganese feed liquid to obtain a first organic phase and a first water phase; wherein the extractant A used in the first extraction comprises 1 or a combination of at least 2 of carboxylic acid extractants; the carboxylic acid extractant has the following structural general formula:
wherein R is1And R2Independently is C3～C9A linear or branched alkyl group; the volume ratio of the extracting agent A to the copper-manganese feed liquid in the first extraction is (0.1-10) to 1; the volume fraction of the extractant A in the first extraction is 5-30%; the first extraction time is 5-30 min; saponifying the extractant A used in the first extraction before use; the pH of the first aqueous phase is 3-4.5;
(2) washing and back-extracting the first organic phase obtained in the step (1) in turn to obtain a copper-containing solution;
(3) performing second extraction on the first aqueous phase obtained in the step (1) to obtain a second organic phase and a second aqueous phase; washing and back-extracting the second organic phase in sequence to obtain a manganese-rich solution; wherein, the extractant B used in the second extraction comprises a phosphorus type extractant and/or a carboxylic acid extractant; the carboxylic acid extractant has the following structural general formula:
wherein R is1And R2Independently is C3～C9A linear or branched alkyl group; the volume fraction of the extractant B is 5-30%; the volume ratio of the extractant B to the first aqueous phase in the second extraction is (0.1-10) to 1; the time of the second extraction is 5-30 min.
11. Use of a separation process according to any one of claims 1 to 10 for separating a copper-manganese-containing feed solution from P204 extractions.
12. The application of an extraction reagent containing carboxylic acid compounds with the structure shown as the formula I in the separation of copper and manganese.
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| WO2022048308A1 (en) * | 2020-09-04 | 2022-03-10 | 苏州博萃循环科技有限公司 | Method for separating copper and manganese from mixed solution containing copper, manganese, calcium and zinc |
| WO2022110821A1 (en) * | 2020-11-24 | 2022-06-02 | 苏州博萃循环科技有限公司 | Carboxylic acid compound, preparation method therefor and use thereof |
| WO2022110822A1 (en) * | 2020-11-24 | 2022-06-02 | 苏州博萃循环科技有限公司 | Method for separating copper and manganese, and application thereof |
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| CN114836631B (en) * | 2022-06-15 | 2023-12-01 | 蜂巢能源科技股份有限公司 | Recycling method of copper-manganese liquid generated by extraction and recovery of battery materials |
| CN115159578A (en) * | 2022-06-16 | 2022-10-11 | 荆门市格林美新材料有限公司 | Method for producing battery-grade manganese sulfate by recycling manganese through ternary synergistic extraction system |
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