CN103482641B - A kind of method of separating boron from boracic brine - Google Patents
A kind of method of separating boron from boracic brine Download PDFInfo
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Abstract
A method for separating boron from boracic brine, comprises the steps: that the pH value regulating boracic brine regulates between 1 ~ 4; Extraction agent and mixing diluents are extracted organic phase; By the boracic brine of extracted organic phase extraction after pH value regulates, obtain boracic organic phase; By reverse-extraction agent back extraction boracic organic phase, obtain organic phase and aqueous phase; Aqueous phase is obtained boric acid or borate after evaporation, concentrated, crystallization.The present invention with monohydroxy-alcohol, dibasic alcohol or the alcohol mixture that is made up of monohydroxy-alcohol and dibasic alcohol for extraction agent, with water-fast ethers, for thinner, extraction agent and mixing diluents are extracted organic phase, and by the boracic brine of extracted organic phase multi-stage solvent extraction after pH value regulates, thus obtain boracic organic phase, use reverse-extraction agent back extraction boracic organic phase again, the aqueous phase obtained is obtained boric acid or borate after evaporation, concentrated, crystallization, achieve the separation of boron in boracic brine, separating boron efficiency is high.
Description
[technical field]
The present invention relates to a kind of method being separated boron in boracic brine, particularly relate to a kind of method of separating boron from boracic brine.
[background technology]
Boric acid is a kind of important basic chemical industry raw material, and in the development of the national economy, purposes is very extensive.At present, domestic boric acid year consumption about 320,000 tons, but output only can maintain about 90,000 tons, boron resource scarcity has threatened relevant industries to develop.And in salt lake, contain a large amount of boron, the form mainly with liquid ore deposit exists, and from boracic brine, how to isolate highly purified boron is current problem demanding prompt solution.
At present, in boracic brine, the method for separating boron mainly contains: acidifying removal method, the precipitator method, absorption method,
The methods such as solvent extration.Because solvent extration has, selectivity is good, magazins' layout thorough, boron rate of recovery advantages of higher, and salt lake brine is afterwards carried in boron and will be had broad application prospects.
Disclose in patent CN101676206A and CN102295296A a kind of carry lithium with salt lake after bittern for raw material, with 2-ethyl-1, the alcohol mixture that 3-hexylene glycol combines with isooctyl alcohol, primary isoamyl alcohol respectively extracts the method for boron from bittern, the method from extraction agent volume fraction, acidity, compare, extraction time, extraction temperature, saturated loading capacity, concentration of anti-stripping agent, the aspect such as Stripping times tested, obtain the optimum process condition of alcohol mixture boron extraction from bittern, but organic the mixing of the method is damaged seriously.
Process method for extracting low-concentration boracic acid in magnesium-containing brine is disclosed in patent CN101544378A.At room temperature, the organic phase mixed with monohydroxy-alcohol and non-polar organic solvent is as the bittern after complexing extractant extraction acidifying, be extracted phase, with water, back extraction is carried out to extraction phase again, boric acid is stripped in aqueous phase, organic phase regeneration, can drop to 20-26mg/L by Boron contents in bittern, but cannot reach the requirement (Boron contents is not higher than 1mg/L) to Boron contents in electrolytic preparation MAGNESIUM METAL process.
Patent CN102757062A discloses a kind of method containing boron extraction in the old halogen in magnesium salts lake, and it uses B in raw material
2o
3for 1000mg/L ~ 20000mg/L, magnesium ion content is 20000mg/L ~ 400000mg/L, focus on the selection of extraction agent, after multi-stage counter current extraction, in old halogen, Boron contents drops to 30mg/L, the boric acid rate of recovery reaches 95%, but still the requirement that cannot reach to Boron contents in electrolytic preparation MAGNESIUM METAL process, and extraction agent fatty alcohol has necessarily water-soluble in old halogen, affects bittern subsequent disposal.
[summary of the invention]
Low, organic the mixing of separation efficiency that the technical problem to be solved in the present invention is to overcome boron in prior art separation boracic brine damages defect that is high, complex process, high, organic the mixing of a kind of separating boron efficiency is provided to damage low, the technique simply method of separating boron from boracic brine, the method, by under Boron contents is reduced to 1mg/L in the aqueous solution, meets the requirement to Boron contents in electrolytic preparation MAGNESIUM METAL process.
For solving the problems of the technologies described above, the present invention adopts following technical proposals:
From boracic brine, a method for separating boron, comprises the steps:
Step S1: regulate the pH value of described boracic brine to regulate between 1 ~ 4;
Step S2: extraction agent and mixing diluents are extracted organic phase, wherein, described extraction agent is monohydroxy-alcohol, dibasic alcohol or the alcohol mixture that is made up of monohydroxy-alcohol and dibasic alcohol, and described thinner is water-fast ethers;
Step S3: by the boracic brine of described extracted organic phase extraction after pH value regulates, obtain boracic organic phase;
Step S4: by boracic organic phase described in reverse-extraction agent back extraction, obtain organic phase and aqueous phase, wherein, described reverse-extraction agent is deionized water or alkaline aqueous solution; And
Step S5: described aqueous phase is obtained boric acid or borate after evaporation, concentrated, crystallization.
In the present embodiment, in step S1, described boracic brine is mother liquid of boric acid, carry potassium after at least one in old halogen, the former bittern in salt lake, magnesium sulfate mother liquor or magnesium nitrate mother liquor.
In the present embodiment, in step S1, in step S1, regulate the adjustment of the pH value of described boracic brine to be specially between 1 ~ 4 and regulate the pH value of described boracic brine to be stabilized between 1 ~ 4 with hydrochloric acid.
In the present embodiment, in step S1, in step S2, described extraction agent and thinner by volume per-cent between 1:4 ~ 4:1.
In the present embodiment, in step S2, in step S2, described monohydroxy-alcohol is at least one in 2-second hexanol, 3-methyl butanol, described dibasic alcohol is 2-ethyl-1, 3-hexylene glycol, 2-butyl-2-ethyl-1, 3-hexylene glycol, 3-methyl-2, 4-heptanediol, 2, 2, 4-trimethylammonium-1, 3-pentanediol, 2-butyl-2-ethyl-1, ammediol, 2-methyl-2-nonyl-1, ammediol, 2, 2-diaryl-1, ammediol, 2-ethyl-2-butyl-1, ammediol, 2, 2, 4-trimethylammonium-1, 3-pentanediol, 2-methyl-3-benzyl-1, 3-butyleneglycol, 2.2-dimethyl-1-benzyl-1, ammediol, 2, 2, 5-trimethylammonium-1, 3-hexylene glycol, 2, 3, 5-trimethylammonium-1, 3-hexylene glycol, 2, 3, 6-trimethylammonium-1, 3-heptanediol, 2, 2, 6-trimethylammonium-1, at least one in 3-heptanediol.
In the present embodiment, in step S2, described ethers is methyl-phenoxide, sherwood oil, benzene diethyl ether, dimethylbenzene, ether.
In the present embodiment, in step S3, described extraction is Centrifugical extraction, and centrifuge speed is 1500 ~ 12000r/min, and the condition of described extraction is: complexation time is 1 ~ 20min, and extraction temperature is 10 ~ 60 DEG C; During extraction, described boracic organic phase and aqueous phase volume ratio are 0.2 ~ 5, and described boracic brine flow rates is 20 ~ 2000L/h.
In the present embodiment, in step S4, the condition of described back extraction is: Stripping times is 1 ~ 20min, and back extraction temperature is 10 ~ 30 DEG C, centrifuge speed scope 1500 ~ 12000r/min; During back extraction, described organic phase and aqueous phase volume ratio are 0.3 ~ 3, and described reverse-extraction agent flow rates is 80 ~ 1000L/h.
In the present embodiment, in step S4, described alkaline aqueous solution to be pH be 8 ~ 14 sodium hydroxide or potassium hydroxide aqueous solution.
Adopt technique scheme, beneficial effect of the present invention is:
The method of separating boron from boracic brine that the above embodiment of the present invention provides, with monohydroxy-alcohol, dibasic alcohol or the alcohol mixture that is made up of monohydroxy-alcohol and dibasic alcohol are as extraction agent, with water-fast ethers for thinner, extraction agent and thinner are mixed to get extracted organic phase by certain concentration of volume percent, and by the boracic brine of extracted organic phase multi-stage solvent extraction after pH value regulates, thus obtain boracic organic phase, use reverse-extraction agent back extraction boracic organic phase again, by the aqueous phase obtained through evaporating, concentrated, boric acid or borate is obtained after crystallization, achieve the separation of boron in boracic brine, separating boron efficiency is high.
In addition, the above embodiment of the present invention additionally provides using monohydroxy-alcohol, dibasic alcohol or the alcohol mixture that is made up of monohydroxy-alcohol and dibasic alcohol as extraction agent, adopt multi-stage solvent extraction system, boron impurities in boracic brine can be reduced to below 1mg/L, the requirement to Boron contents in electrolytic preparation MAGNESIUM METAL process can be met.
In addition, the method for separating boron from boracic brine that the above embodiment of the present invention provides, adopts Centrifugical extraction, and the extracting power change of extraction system is little, and extraction agent holds loss rate lower than 0.2%, and extraction agent reusable edible, cost is low, is applicable to suitability for industrialized production.
[accompanying drawing explanation]
The flow chart of steps of the method for separating boron from boracic brine that Fig. 1 provides for the embodiment of the present invention.
[embodiment]
In order to make object of the present invention, technical scheme and advantage clearly understand, below in conjunction with drawings and the specific embodiments, the present invention is further elaborated.Should be appreciated that specific embodiment described herein only in order to explain the present invention, be not intended to limit the present invention.
Refer to Fig. 1, steps flow chart Figure 100 of the method for separating boron from boracic brine that Fig. 1 provides for the embodiment of the present invention, as can be seen from Fig. 1, from boracic brine, the method for separating boron comprises the steps:
Step S1: regulate the pH value of described boracic brine to regulate between 1 ~ 4;
In the present embodiment, boracic brine be mother liquid of boric acid, carry potassium after at least one in old halogen, the former bittern in salt lake, magnesium sulfate mother liquor or magnesium nitrate mother liquor.In above-mentioned boracic brine, boron ionic concn is between 100mg/L-600mg/L, and magnesium ion concentration is higher, and concentration range is between 30000-234000mg/L.
Particularly, the pH value of boracic brine is regulated to be stabilized between 1 ~ 4 with hydrochloric acid.Hydrochloric acid is preferably 30% concentrated hydrochloric acid or dilute hydrochloric acid.
Step S2: extraction agent and mixing diluents are extracted organic phase, wherein, extraction agent is monohydroxy-alcohol, dibasic alcohol or the alcohol mixture that is made up of monohydroxy-alcohol and dibasic alcohol, and thinner is water-fast ethers;
In the present embodiment, extraction agent and thinner by volume per-cent between 1:4 ~ 4:1.
In the present embodiment, monohydroxy-alcohol is at least one in 2-second hexanol, 3-methyl butanol, dibasic alcohol is 2-ethyl-1, 3-hexylene glycol, 2-butyl-2-ethyl-1, 3-hexylene glycol, 3-methyl-2, 4-heptanediol, 2, 2, 4-trimethylammonium-1, 3-pentanediol, 2-butyl-2-ethyl-1, ammediol, 2-methyl-2-nonyl-1, ammediol, 2, 2-diaryl-1, ammediol, 2-ethyl-2-butyl-1, ammediol, 2, 2, 4-trimethylammonium-1, 3-pentanediol, 2-methyl-3-benzyl-1, 3-butyleneglycol, 2.2-dimethyl-1-benzyl-1, ammediol, 2, 2, 5-trimethylammonium-1, 3-hexylene glycol, 2, 3, 5-trimethylammonium-1, 3-hexylene glycol, 2, 3, 6-trimethylammonium-1, 3-heptanediol, 2, 2, 6-trimethylammonium-1, at least one in 3-heptanediol.
In the present embodiment, ethers is preferably methyl-phenoxide, sherwood oil, benzene diethyl ether, dimethylbenzene, ether.
Be appreciated that, choose the particularly important of suitable extraction agent and thinner, technical scheme provided by the invention is using monohydroxy-alcohol, dibasic alcohol or the alcohol mixture that is made up of monohydroxy-alcohol and dibasic alcohol as extraction agent, with water-fast ethers for thinner, the two is carried out according to a certain percentage be mixed to get extracted organic phase, use reverse-extraction agent back extraction boracic organic phase again, the aqueous phase obtained is obtained boric acid or borate after evaporation, concentrated, crystallization, achieve the separation of boron in boracic brine, separating boron efficiency is high.
Step S3: by the boracic brine of extracted organic phase extraction after pH value regulates, obtain boracic organic phase;
In the present embodiment, extraction is preferably Centrifugical extraction, and centrifuge speed is 1500 ~ 12000r/min.
Be appreciated that employing Centrifugical extraction, the extracting power change of extraction system is very little, and percentage extraction still can keep more than 99% of original extraction efficiency, and extraction agent holds loss rate lower than 0.2%, and extraction agent reusable edible, cost is low, is applicable to suitability for industrialized production.
In the present embodiment, the condition of extraction is: complexation time is 1 ~ 20min, and extraction temperature is 10 ~ 60 DEG C; During extraction, boracic organic phase and aqueous phase volume ratio are 0.2 ~ 5, and boracic brine flow rates is 20 ~ 2000L/h.
In the present embodiment, extract as multi-stage solvent extraction.Particularly, during using single alcohol as extraction agent, adopt three grades or level Four extraction system; During using alcohol mixture as extraction agent, adopt 1 ~ 2 grade of extraction system; Or during using single alcohol and alcohol mixture as extraction agent, adopt the mode that 1-2 level single alcohol extraction system combines with 1 grade of alcohol mixture extraction system, boron impurities in low for high magnesium boron bittern can both be reduced to below 1mg/L, to meet the requirement to Boron contents in electrolytic preparation MAGNESIUM METAL process.
Be appreciated that in extraction process, because aqueous phase and organic phase are not dissolved each other, carry out centrifugal mixer, cause very large phase interface, two-phase is fully contacted, boron spreads through phase interface by aqueous phase in extraction agent, reaches balance each other through 1-20min; According to two-phase density difference, can layering be produced by centrifugation, reach the object of separation with this.
Step S4: by reverse-extraction agent back extraction boracic organic phase, obtain organic phase and aqueous phase, wherein, reverse-extraction agent is deionized water or alkaline aqueous solution;
In the present embodiment, the condition of back extraction is: Stripping times is 1 ~ 20min, and back extraction temperature is 10 ~ 30 DEG C, centrifuge speed scope 1500 ~ 12000r/min; During back extraction, organic phase and aqueous phase volume ratio are 0.3 ~ 3, and reverse-extraction agent flow rates is 80 ~ 1000L/h.
In the present embodiment, alkaline aqueous solution to be pH be 8 ~ 14 sodium hydroxide or potassium hydroxide aqueous solution.
Be appreciated that and achieve being separated of boron and organic phase by reverse-extraction agent back extraction boracic organic phase, obtaining organic phase again for extracting the boron in boracic brine, can achieve recycling of extracted organic phase, reducing cost.
Step S5: aqueous phase is obtained boric acid or borate after evaporation, concentrated, crystallization.
Be appreciated that, the aqueous phase of boracic obtains high-purity boric acid or borate after evaporation, concentrated, crystallization, and realize the degree of depth except boron, Boron contents has between original 100mg/L ~ 600mg/L, within dropping to 1mg/L, the requirement that magnesium solution concentration and evaporation produces a set of magnesium products can be met; The degree of depth is except the aqueous salt brine after boron is through concentrated, crystallization, and drying obtains high purity magnesium product (as magnesium chloride or magnesium sulfate), and can as electrolytic metal magnesium raw material.
The method of separating boron from boracic brine that the above embodiment of the present invention provides, with monohydroxy-alcohol, dibasic alcohol or the alcohol mixture that is made up of monohydroxy-alcohol and dibasic alcohol are as extraction agent, with water-fast ethers for thinner, extraction agent and thinner are mixed to get extracted organic phase by certain concentration of volume percent, and by the boracic brine of extracted organic phase multi-stage solvent extraction after pH value regulates, thus obtain boracic organic phase, use reverse-extraction agent back extraction boracic organic phase again, by the aqueous phase obtained through evaporating, concentrated, boric acid or borate is obtained after crystallization, achieve the separation of boron in boracic brine, separating boron efficiency is high.
In addition, the above embodiment of the present invention additionally provides using monohydroxy-alcohol, dibasic alcohol or the alcohol mixture that is made up of monohydroxy-alcohol and dibasic alcohol as extraction agent, adopt multi-stage solvent extraction system, boron impurities in boracic brine can be reduced to below 1mg/L, the requirement to Boron contents in electrolytic preparation MAGNESIUM METAL process can be met.
In addition, the method for separating boron from boracic brine that the above embodiment of the present invention provides, adopts Centrifugical extraction, and the extracting power change of extraction system is little, and extraction agent holds loss rate lower than 0.2%, and extraction agent reusable edible, cost is low, is applicable to suitability for industrialized production.
Set forth the present invention further by the following examples, these embodiments are only presented for purposes of illustration, do not limit the scope of the invention.Except the actual conditions indicated, the test method in embodiment all conveniently condition is carried out.
embodiment 1
Adopt method provided by the present invention separating boron from boracic brine, wherein, boracic brine is the former bittern in salt lake, and its ionic group becomes:
| Element | Mg 2+ | Cl - | Na + | K + | B | SO 4 2- |
| Content (mg/L) | 119000 | 345000 | 1500 | 4750 | 275 | 1450 |
Experimentation:
Concentrated hydrochloric acid with 30% regulates salt lake former bittern pH to 2.0; Adopt 2.2-dimethyl-1-benzyl-1,3-PD, 2,2,5-trimethylammonium-1,3-hexylene glycols according to 1:1 ratio mixing composition extraction agent, adopt methyl-phenoxide as thinner, by above-mentioned extraction agent and thinner by volume 1:1 be mixed to get extracted organic phase; Extracted organic phase is adopted the boracic brine of three stage countercurrent extractions after pH value regulates, obtain boracic organic phase, wherein, extraction is Centrifugical extraction, centrifuge speed is 1500r/min, and complexation time is 1min, and extraction temperature is 25 DEG C, boracic organic phase and aqueous phase volume ratio are 1, and boracic brine flow rates is 20L/h; Using the aqueous sodium hydroxide solution of pH=10 as reverse-extraction agent four-stage counter-current back extraction boracic organic phase, obtain organic phase and aqueous phase, wherein, Stripping times is 1min, back extraction temperature is 30 DEG C, and centrifuge speed scope 1500r/min, during back extraction, organic phase and aqueous phase volume ratio are 0.5, and reverse-extraction agent flow rates is 80L/h; Aqueous phase is obtained boric acid or borate after evaporation, concentrated, crystallization.After above-mentioned process, bittern mutually middle Boron contents is 0.95mg/L, boron removal efficiency 99.6%.
By organic phase recycle after back extraction, after continuous circulation uses 10 times, extraction efficiency 98.7%, still maintains 99.1% of initial extraction efficiency, and this extraction system cycling extraction-reextraction effect stability, is suitable for suitability for industrialized production.
embodiment 2
Adopt method provided by the present invention separating boron from boracic brine, wherein, boracic brine is magnesium sulfate mother liquor, and its ionic group becomes:
| Element | Mg2+ | Na+ | K+ | B | Cl- | SO42- |
| Content (mg/L) | 56700 | 400 | 200 | 236 | 620 | 253200 |
Experimentation:
Concentrated hydrochloric acid with 30% regulates salt lake former bittern pH to 1.0; Adopt 2-butyl-2-ethyl-1,3-hexylene glycol, 2.2-dimethyl-1-benzyl-1,3-PD according to 1:1 ratio mixing composition extraction agent, adopt sherwood oil as thinner, by above-mentioned extraction agent and thinner by volume 1:1 be mixed to get extracted organic phase; Extracted organic phase is adopted the boracic brine of secondary counter-current extraction after pH value regulates, obtain boracic organic phase, wherein, extraction is Centrifugical extraction, centrifuge speed is 10000r/min, and complexation time is 10min, and extraction temperature is 35 DEG C, boracic organic phase and aqueous phase volume ratio are 0.2, and boracic brine flow rates is 1000L/h; Using the aqueous sodium hydroxide solution of pH=12 as reverse-extraction agent three stage countercurrent back extraction boracic organic phase, obtain organic phase and aqueous phase, wherein, Stripping times is 10min, back extraction temperature is 20 DEG C, and centrifuge speed scope 6000r/min, during back extraction, organic phase and aqueous phase volume ratio are 2, and reverse-extraction agent flow rates is 200L/h; Aqueous phase is obtained boric acid or borate after evaporation, concentrated, crystallization.After above-mentioned process, in magnesium sulfate mother liquor aqueous phase, Boron contents is 0.39mg/L, boron removal efficiency 99.8%.
By organic phase recycle after back extraction, after continuous circulation uses 10 times, extraction efficiency 97.3%, still maintains 97.5% of initial extraction efficiency, and this extraction system cycling extraction-reextraction effect stability, is suitable for suitability for industrialized production.
embodiment 3
Adopt method provided by the present invention separating boron from boracic brine, wherein, boracic brine is magnesium nitrate mother liquor, and its ionic group becomes:
| Element | Cl - | SO 4 2- | Ca 2+ | Mg 2+ | K + | Na + | B |
| Content (mg/L) | 7210 | 460 | 33680 | 48970 | 1270 | 5260 | 178 |
Experimentation:
Concentrated hydrochloric acid with 30% regulates salt lake former bittern pH to 1.0; Adopt 2-second hexanol, 2-ethyl-2-butyl-1,3-PD, 2,2,4-trimethylammonium-1,3-pentanediol, according to 1:1:1 ratio mixing composition extraction agent, adopts benzene diethyl ether as thinner, by above-mentioned extraction agent and thinner by volume 1:1 be mixed to get extracted organic phase; Extracted organic phase is adopted the boracic brine of three stage countercurrent extractions after pH value regulates, obtain boracic organic phase, wherein, extraction is Centrifugical extraction, centrifuge speed is 8000r/min, and complexation time is 15min, and extraction temperature is 45 DEG C, boracic organic phase and aqueous phase volume ratio are 2, and boracic brine flow rates is 1000L/h; Using the aqueous sodium hydroxide solution of pH=12 as reverse-extraction agent four-stage counter-current back extraction boracic organic phase, obtain organic phase and aqueous phase, wherein, Stripping times is 15min, back extraction temperature is 20 DEG C, and centrifuge speed scope 8000r/min, during back extraction, organic phase and aqueous phase volume ratio are 0.3, and reverse-extraction agent flow rates is 600L/h; Aqueous phase is obtained boric acid or borate after evaporation, concentrated, crystallization.After above-mentioned process, in magnesium nitrate mother liquor aqueous phase, Boron contents is 0.65mg/L, boron removal efficiency 99.7%.
By organic phase recycle after back extraction, after continuous circulation uses 10 times, extraction efficiency 98.9%, still maintains 99.2% of initial extraction efficiency, and this extraction system cycling extraction-reextraction effect stability, is suitable for suitability for industrialized production.
embodiment 4
Adopt method provided by the present invention separating boron from boracic brine, wherein, boracic brine is old halogen after carrying potassium, and its ionic group becomes:
| Element (mg/l) | Cl - | HCO 3- | SO 4 2- | Ca 2+ | Mg 2+ | K + | B | Li + |
| Numerical value | 339807 | 1992 | 9911 | 146 | 118506 | 816 | 176 | 326 |
Experimentation:
Concentrated hydrochloric acid with 30% regulates salt lake former bittern pH to 1.0; Adopt 2-second hexanol, 2-methyl-3-benzyl-1,3-butyleneglycol, 2.2-dimethyl-1-benzyl-1, ammediol, 2,2,5-trimethylammonium-1,3-hexylene glycol, according to 1:1:1:1 ratio mixing composition extraction agent, adopts dimethylbenzene as thinner, by above-mentioned extraction agent and thinner by volume 1:1 be mixed to get extracted organic phase; Extracted organic phase is adopted the boracic brine of three stage countercurrent extractions after pH value regulates, obtain boracic organic phase, wherein, extraction is Centrifugical extraction, centrifuge speed is 10000r/min, and complexation time is 20min, and extraction temperature is 25 DEG C, boracic organic phase and aqueous phase volume ratio are 4, and boracic brine flow rates is 1500L/h; Using the aqueous sodium hydroxide solution of pH=11 as reverse-extraction agent four-stage counter-current back extraction boracic organic phase, obtain organic phase and aqueous phase, wherein, Stripping times is 15min, back extraction temperature is 30 DEG C, and centrifuge speed scope 10000r/min, during back extraction, organic phase and aqueous phase volume ratio are 1, and reverse-extraction agent flow rates is 800L/h; Aqueous phase is obtained boric acid or borate after evaporation, concentrated, crystallization.After above-mentioned process, after carrying potassium old bittern mutually in Boron contents be 0.91mg/L, boron removal efficiency 99.7%.
By organic phase recycle after back extraction, after continuous circulation uses 10 times, extraction efficiency 98.5%, still maintains 98.8% of initial extraction efficiency, and this extraction system cycling extraction-reextraction effect stability, is suitable for suitability for industrialized production.
embodiment 5
Adopt method provided by the present invention separating boron from boracic brine, wherein, boracic brine is mother liquid of boric acid, and its ionic group becomes:
| Element (mg/l) | Cl - | HCO 3- | SO 4 2- | Ca 2+ | Mg 2+ | K + | B | Li + |
| Numerical value | 339807 | 1992 | 9911 | 146 | 118506 | 816 | 176 | 326 |
Experimentation:
Salt lake former bittern pH to 3.0 is regulated with dilute hydrochloric acid; Adopt 2-second hexanol, 3-methyl butanol, 2-ethyl-1,3-hexylene glycol, 2-butyl-2-ethyl-1,3-hexylene glycol, according to 1:1:1:1 ratio mixing composition extraction agent, adopts ether as thinner, by above-mentioned extraction agent and thinner by volume 1:1 be mixed to get extracted organic phase; Extracted organic phase is adopted the boracic brine of secondary counter-current extraction after pH value regulates, obtain boracic organic phase, wherein, extraction is Centrifugical extraction, centrifuge speed is 12000r/min, and complexation time is 20min, and extraction temperature is 25 DEG C, boracic organic phase and aqueous phase volume ratio are 5, and boracic brine flow rates is 2000L/h; Using the potassium hydroxide aqueous solution of pH=13 as reverse-extraction agent three stage countercurrent back extraction boracic organic phase, obtain organic phase and aqueous phase, wherein, Stripping times is 20min, back extraction temperature is 30 DEG C, and centrifuge speed scope 10000r/min, during back extraction, organic phase and aqueous phase volume ratio are 3, and reverse-extraction agent flow rates is 1000L/h; Aqueous phase is obtained boric acid or borate after evaporation, concentrated, crystallization.After above-mentioned process, in mother liquid of boric acid aqueous phase, Boron contents is 0.85mg/L, boron removal efficiency 99.6%.
By organic phase recycle after back extraction, after continuous circulation uses 10 times, extraction efficiency 99.0%, still maintains 99.4% of initial extraction efficiency, and this extraction system cycling extraction-reextraction effect stability, is suitable for suitability for industrialized production.
embodiment 6
Adopt method provided by the present invention separating boron from boracic brine, wherein, boracic brine is magnesium sulfate mother liquor, and its ionic group becomes:
| Element | Mg 2+ | Cl - | Na + | K + | B | SO 4 2- |
| Content (mg/L) | 122000 | 325000 | 1620 | 865 | 358 | 34000 |
Experimentation:
Salt lake former bittern pH to 4.0 is regulated with dilute hydrochloric acid; Adopt primary isoamyl alcohol, 2-butyl-2-ethyl-1,3-hexylene glycol, 2-ethyl-2-butyl-1, ammediol, according to 1:1:1 ratio mixing composition extraction agent, adopts methyl-phenoxide as thinner, by above-mentioned extraction agent and thinner by volume 1:1 be mixed to get extracted organic phase; Extracted organic phase is adopted the boracic brine of secondary counter-current extraction after pH value regulates, obtain boracic organic phase, wherein, extraction is Centrifugical extraction, centrifuge speed is 12000r/min, and complexation time is 20min, and extraction temperature is 25 DEG C, boracic organic phase and aqueous phase volume ratio are 0.5, and boracic brine flow rates is 2000L/h; Using the potassium hydroxide aqueous solution of pH=11 as reverse-extraction agent three stage countercurrent back extraction boracic organic phase, obtain organic phase and aqueous phase, wherein, Stripping times is 20min, back extraction temperature is 30 DEG C, and centrifuge speed scope 10000r/min, during back extraction, organic phase and aqueous phase volume ratio are 1, and reverse-extraction agent flow rates is 1000L/h; Aqueous phase is obtained boric acid or borate after evaporation, concentrated, crystallization.After above-mentioned process, in magnesium sulfate mother liquor aqueous phase, Boron contents is 0.98mg/L, boron removal efficiency 99.7%.
By organic phase recycle after back extraction, after continuous circulation uses 10 times, extraction efficiency 98.9%, still maintains 99.1% of initial extraction efficiency, and this extraction system cycling extraction-reextraction effect stability, is suitable for suitability for industrialized production.
The above, it is only preferred embodiment of the present invention, not any pro forma restriction is done to the present invention, although the present invention discloses as above with preferred embodiment, but and be not used to limit the present invention, any those skilled in the art, do not departing within the scope of technical solution of the present invention, make a little change when the technology contents of above-mentioned announcement can be utilized or be modified to the Equivalent embodiments of equivalent variations, in every case be do not depart from technical solution of the present invention content, according to any simple modification that technical spirit of the present invention is done above embodiment, equivalent variations and modification, all still belong in the scope of technical solution of the present invention.
Claims (4)
1. the method for separating boron from boracic brine, is characterized in that, comprise the steps:
Step S1: regulate the pH value of described boracic brine to regulate between 1 ~ 4;
Step S2: extraction agent and mixing diluents are extracted organic phase, wherein, the alcohol mixture that described extraction agent is made up of monohydroxy-alcohol and dibasic alcohol, described alcohol mixture comprises the alcohol of more than three kinds, and described thinner is water-fast ethers; In step S2, described monohydroxy-alcohol is at least one in 2-second hexanol, 3-methyl butanol; Described dibasic alcohol is 2,2,4-trimethylammonium-1,3-pentanediol, 2-butyl-2-ethyl-1,3-PD, 2-methyl-2-nonyl-1,3-PD, 2,2-diaryl-1,3-PD, 2-ethyl-2-butyl-1,3-PD, 2,2,4-trimethylammonium-1,3-pentanediol, 2-methyl-3-benzyl-1,3-butyleneglycol, 2.2-dimethyl-1-benzyl-1,3-PD, 2,2,5-trimethylammonium-1,3-hexylene glycol, 2,3,5-trimethylammonium-1,3-hexylene glycol, 2,3,6-trimethylammoniums-1,3-heptanediol, 2, at least one in 2,6-trimethylammonium-1,3-heptanediol; In step S2, described ethers is methyl-phenoxide, benzene diethyl ether, ether;
Step S3: by the boracic brine of described extracted organic phase extraction after pH value regulates, obtain boracic organic phase; In step S3, described extraction is Centrifugical extraction, and centrifuge speed is 1500 ~ 12000r/min; The condition of described extraction is: complexation time is 1 ~ 20min, and extraction temperature is 10 ~ 60 DEG C; During extraction, described boracic organic phase and aqueous phase volume ratio are 0.2 ~ 5, and described boracic brine flow rates is 20 ~ 2000L/h;
Step S4: by boracic organic phase described in reverse-extraction agent back extraction, obtain organic phase and aqueous phase, wherein, described reverse-extraction agent is deionized water; In step S4, the condition of described back extraction is: Stripping times is 1 ~ 20min, and back extraction temperature is 10 ~ 30 DEG C, centrifuge speed scope 1500 ~ 12000r/min; During back extraction, described organic phase and aqueous phase volume ratio are 0.3 ~ 3, and described reverse-extraction agent flow rates is 80 ~ 1000L/h; And
Step S5: described aqueous phase is obtained boric acid after evaporation, concentrated, crystallization.
2. the method for separating boron from boracic brine according to claim 1, is characterized in that, in step S1, described boracic brine is mother liquid of boric acid, carry potassium after at least one in old halogen, the former bittern in salt lake, magnesium sulfate mother liquor or magnesium nitrate mother liquor.
3. the method for separating boron from boracic brine according to claim 1, is characterized in that, in step S1, regulates the adjustment of the pH value of described boracic brine to be specially between 1 ~ 4 and regulates the pH value of described boracic brine to be stabilized between 1 ~ 4 with hydrochloric acid.
4. the method for separating boron from boracic brine according to claim 1, is characterized in that, in step S2, described extraction agent and thinner by volume per-cent between 1:4 ~ 4:1.
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