CN111151141A - Separation method of double-liquid membrane coupling - Google Patents
Separation method of double-liquid membrane coupling Download PDFInfo
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- CN111151141A CN111151141A CN202010015219.4A CN202010015219A CN111151141A CN 111151141 A CN111151141 A CN 111151141A CN 202010015219 A CN202010015219 A CN 202010015219A CN 111151141 A CN111151141 A CN 111151141A
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- 239000007788 liquid Substances 0.000 title claims abstract description 141
- 239000012528 membrane Substances 0.000 title claims abstract description 82
- 238000000926 separation method Methods 0.000 title claims abstract description 57
- 238000010168 coupling process Methods 0.000 title claims abstract description 19
- 230000008878 coupling Effects 0.000 title claims abstract description 17
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 17
- 239000002994 raw material Substances 0.000 claims abstract description 34
- 238000000605 extraction Methods 0.000 claims abstract description 23
- 239000000203 mixture Substances 0.000 claims abstract description 8
- 239000012535 impurity Substances 0.000 claims abstract description 6
- 239000000243 solution Substances 0.000 claims description 62
- IMNFDUFMRHMDMM-UHFFFAOYSA-N N-Heptane Chemical compound CCCCCCC IMNFDUFMRHMDMM-UHFFFAOYSA-N 0.000 claims description 14
- PTFCDOFLOPIGGS-UHFFFAOYSA-N Zinc dication Chemical compound [Zn+2] PTFCDOFLOPIGGS-UHFFFAOYSA-N 0.000 claims description 13
- 239000003795 chemical substances by application Substances 0.000 claims description 11
- 238000000034 method Methods 0.000 claims description 11
- 239000007864 aqueous solution Substances 0.000 claims description 9
- WLZRMCYVCSSEQC-UHFFFAOYSA-N cadmium(2+) Chemical compound [Cd+2] WLZRMCYVCSSEQC-UHFFFAOYSA-N 0.000 claims description 8
- XTAZYLNFDRKIHJ-UHFFFAOYSA-N n,n-dioctyloctan-1-amine Chemical compound CCCCCCCCN(CCCCCCCC)CCCCCCCC XTAZYLNFDRKIHJ-UHFFFAOYSA-N 0.000 claims description 7
- 239000000284 extract Substances 0.000 claims description 5
- USFZMSVCRYTOJT-UHFFFAOYSA-N Ammonium acetate Chemical compound N.CC(O)=O USFZMSVCRYTOJT-UHFFFAOYSA-N 0.000 claims description 4
- 239000005695 Ammonium acetate Substances 0.000 claims description 4
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 4
- 229940043376 ammonium acetate Drugs 0.000 claims description 4
- 235000019257 ammonium acetate Nutrition 0.000 claims description 4
- 229910017604 nitric acid Inorganic materials 0.000 claims description 4
- 239000000839 emulsion Substances 0.000 claims description 3
- 239000011701 zinc Substances 0.000 claims description 3
- SEGLCEQVOFDUPX-UHFFFAOYSA-N di-(2-ethylhexyl)phosphoric acid Chemical compound CCCCC(CC)COP(O)(=O)OCC(CC)CCCC SEGLCEQVOFDUPX-UHFFFAOYSA-N 0.000 claims description 2
- 229910021645 metal ion Inorganic materials 0.000 abstract description 12
- 230000000694 effects Effects 0.000 abstract description 9
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 230000000717 retained effect Effects 0.000 abstract description 2
- 238000003912 environmental pollution Methods 0.000 abstract 1
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- 230000005012 migration Effects 0.000 description 3
- 238000011160 research Methods 0.000 description 3
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- HBAQYPYDRFILMT-UHFFFAOYSA-N 8-[3-(1-cyclopropylpyrazol-4-yl)-1H-pyrazolo[4,3-d]pyrimidin-5-yl]-3-methyl-3,8-diazabicyclo[3.2.1]octan-2-one Chemical class C1(CC1)N1N=CC(=C1)C1=NNC2=C1N=C(N=C2)N1C2C(N(CC1CC2)C)=O HBAQYPYDRFILMT-UHFFFAOYSA-N 0.000 description 1
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
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- 229920009405 Polyvinylidenefluoride (PVDF) Film Polymers 0.000 description 1
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 1
- QCUOBSQYDGUHHT-UHFFFAOYSA-L cadmium sulfate Chemical compound [Cd+2].[O-]S([O-])(=O)=O QCUOBSQYDGUHHT-UHFFFAOYSA-L 0.000 description 1
- 229910000369 cadmium(II) sulfate Inorganic materials 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
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- 238000007796 conventional method Methods 0.000 description 1
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- 239000000945 filler Substances 0.000 description 1
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- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- XMBWDFGMSWQBCA-UHFFFAOYSA-M iodide Chemical compound [I-] XMBWDFGMSWQBCA-UHFFFAOYSA-M 0.000 description 1
- 229940006461 iodide ion Drugs 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 239000001632 sodium acetate Substances 0.000 description 1
- 235000017281 sodium acetate Nutrition 0.000 description 1
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 229910000368 zinc sulfate Inorganic materials 0.000 description 1
- 239000011686 zinc sulphate Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/38—Liquid-membrane separation
- B01D61/40—Liquid-membrane separation using emulsion-type membranes
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- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Extraction Or Liquid Replacement (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a separation method of double-liquid membrane coupling. The double liquid film system consists of back extraction liquid 1 (W)1) Liquid film phase 1 (O)1) Raw material liquid (W)3) Liquid film phase 2 (O)2) And stripping solution 2 (W)2) Five successive contacts (W)1/O1/W3/O2/W2) And (4) forming. Wherein the raw material liquid at least contains two solutes A and B or other impurity solutes. Liquid film phase 1 (O)1) And stripping solution 1 (W)1) Selectively extracting solute A, liquid membrane phase 2 (O)2) And stripping solution 2 (W)2) Solute B can be selectively extracted. The double-liquid membrane can realize the simultaneous selective separation of two solutes A and B, thereby improving the selective separation effect of the traditional liquid membrane. If the impurity solute is retained in the raw material solution, the separation of the solute A, the solute B and the impurity solute can be realized. The invention has certain guiding significance for solving the problem of separating two or more metal ions, chiral enantiomer mixture or other mixed solutes in a high-selectivity separation solution, and is beneficial to solving the problems of separation and purification of the mixture, environmental pollution or resourceRecovery and the like.
Description
Technical Field
The invention belongs to the technical field of chemical separation, and particularly relates to a separation method of double-liquid membrane coupling.
Background
Liquid membranes are an efficient three-phase separation technique (patent application No. US 3410794). The liquid membrane technology integrates extraction and back extraction, has the dynamic effect of membrane separation, and has the advantages of high mass transfer rate, low extractant consumption, strong enrichment capacity and the like. Therefore, the method is expected to replace the traditional extraction technology. The liquid membrane system consists of three phases of liquid membrane phase, raw material liquid and back extraction liquid. Wherein the liquid membrane phase separates the raw material liquid and the back extraction liquid and is a mass transfer medium between the raw material liquid and the back extraction liquid. The liquid membrane belongs to a dynamic separation process. When a mixed solute is separated by a liquid membrane, due to the selective extraction capability of an extractant in the liquid membrane phase, transmembrane permeation rates of different solute components are different, so that the separation of the different solute components is realized. For example, the raw material solution contains solute A and solute B, the transmembrane permeation rate of the solute A is high, and the solute A is transferred to the strip liquor through a liquid membrane in a short time; the transmembrane permeation rate of the solute B is low, the solute B mainly stays in the raw material liquid in a short time, and the migration amount is small; thereby achieving separation of the two. However, further extension of the liquid membrane separation time, solute B, which has a slow transmembrane permeation rate, also migrates through the liquid membrane into the strip liquor. It is easy to understand that the longer the time thereafter, the poorer the separation effect. Moreover, when the properties of the components are similar, the transmembrane permeation rate difference between the components is small, and the separation effect is poor. In addition, when the solute components are of a large variety, it is difficult for the conventional liquid membrane to simultaneously achieve efficient separation between the solute components.
In the actual separation process, the wastewater or mineral leaching liquid often contains two or more metal ions, and the physicochemical property difference among a plurality of metal ions is small. Thus, it is often necessary to achieve complete separation between two or more metal ions using conventional techniques such as multi-stage extraction. However, the multistage extraction process has the disadvantages of high extractant dosage, high extraction equipment investment and many complex process control factors. Although the liquid membrane technology has the problems of poor stability and the like, the separation process has the advantages of higher efficiency, more economy and the like compared with the traditional extraction process. The liquid membrane technology can be used for the separation process of metal ions, and can improve the separation rate, reduce the consumption of an extracting agent, reduce the equipment investment and improve the enrichment capacity. However, the existing liquid membrane still has difficulty in realizing the high-efficiency separation of various metal ions simultaneously, and the development difficulty of the high-selectivity extracting agent is great. Therefore, it is highly desirable toTo develop from the basic principle, a novel improved liquid membrane method is researched to improve the selective separation capability of the liquid membrane. Research reports that the separation effect between mixed gas components can be improved by a double-membrane coupling process (valley peace, Zhuangwan, Shi Jun. continuous double-membrane separation tower research [ J)]Journal of chemical engineering, 1991(02): 140-]University of major graduate, 2012; chenbo, double membrane component reinforced CO2Study on separation of gas mixture [ D]University of major graduate, 2016; research and application progress of Xiaowu, Gaimi, Jiangxiaabin, Ruixihua, Wu Chimei, Lixiangcun, Hegahong, double-membrane component and coupling process [ J]Chemical evolution, 2019, 38(01): 136-. The double-membrane coupling gas separation process mainly depends on the preferential permeation of the membrane A to the solute A, and simultaneously utilizes the preferential permeation of the membrane B to the solute B. Thus, the defect that the solute B which permeates slowly can permeate the membrane A after a long time of single membrane permeation is avoided. Therefore, the separation effect of the solute A and the solute B after double-membrane coupling is greatly improved. Furthermore, similar to mixtures of metal ions, separation of the levorotatory and dextrorotatory enantiomers during chiral separation is also a typical separation problem. The double-membrane coupling technology also has the potential of improving the chiral separation effect.
Disclosure of Invention
Aiming at the defects and shortcomings in the prior liquid film technology, the gas double-film coupling concept is inspired by the gas double-film coupling idea. The invention provides a separation method of double-liquid membrane coupling (see figure 1). The double liquid membrane technology can simultaneously realize the solute A to pass through the liquid membrane phase 1 (O)1) To stripping solution 1 (W)1) Migration of solute B through liquid film phase 2 (O)2) To stripping solution 2 (W)2) High selectivity separation of migration. Therefore, the selective separation capacity of the traditional liquid membrane is improved, and the efficient separation of solute components is realized; and solves the problem of simultaneous separation between multi-component solutes. Is expected to be applied to the separation fields of metal ion separation, chiral resolution and the like. The specific technical scheme is as follows.
The invention provides a separation method of double-liquid membrane coupling, which is characterized by comprising the following steps: the double liquid film system is prepared from stripping liquid 1 (W)1) Liquid film phase 1 (O)1) Raw material liquid (W)3) Liquid film phase 2 (O)2) And stripping solution 2 (W)2) Five successive contacts (W)1/O1/W3/O2/W2) Composition (see fig. 1); raw material liquid (W)3) The medium solute A is more coated with the liquid film phase 1 (O) than the solute B1) Extracted and stripped with stripping solution 1 (W)1) Back extraction; raw material liquid (W)3) The medium solute B is more absorbed by the liquid film phase 2 (O) than the solute A2) Extracted and stripped with stripping solution 2 (W)2) And (4) back-extracting to realize the separation of solute A and solute B.
The liquid film phase 1 (O)1) Respectively reacting with the stripping solution 1 (W)1) And the raw material liquid (W)3) Immiscible, the liquid film phase 2 (O)2) Respectively with the stripping solution 2 (W)2) And the raw material liquid (W)3) Are immiscible.
The liquid film phase 1 (O)1) Or the liquid film phase 2 (O)2) The operation is carried out in the form of an emulsion liquid film, a supported liquid film or a bulk liquid film.
The raw material liquid (W)3) Is a solution containing the solute A and the solute B, or is a solution containing the solute A, the solute B and coexisting impurity metal ions.
The liquid film phase 1 (O)1) An extractant 1 containing a preferential extraction of said solute a; the liquid film phase 2 (O)2) An extractant 2 which preferentially extracts the solute B.
The raw material liquid (W)3) Is a cadmium ion (Cd) containing solute A2+) And solute B Zinc ion (Zn)2+) An aqueous solution of (a); the liquid film phase 1 (O)1) Is n-heptane solution containing extractant 1 Trioctylamine (TOA); the stripping solution 1 (W)1) Is an aqueous solution containing a stripping agent ammonium acetate; the liquid film phase 2 (O)2) Is a normal heptane solution containing extractant 2 di (2-ethylhexyl) phosphate (P204); the stripping solution 2 (W)2) Is an aqueous solution containing the stripping agent nitric acid.
The raw material liquid (W)3) A solution containing the levorotatory enantiomer of solute A and the dextrorotatory enantiomer of solute B, or a solution containing a racemic mixture; the liquid film phase 1 (O)1) Is an extractant 1 solution which preferentially extracts the levorotatory enantiomer; the stripping solution 1 (W)1) Is composed ofA solution of extractant 1; the liquid film phase 2 (O)2) Is a solution containing an extractant 2 for preferentially extracting the dextrorotatory enantiomer; the stripping solution 2 (W)2) Is a solution containing a stripping agent 2.
The invention has the positive beneficial effects that: the double-liquid-membrane system provided by the invention can simultaneously and selectively extract solute A and solute B, and the separation effect is improved. And, if other foreign solutes are not dissolved in the liquid film phase 1 (O)1) And liquid film phase 2 (O)2) The phase extraction is carried out, and the solute A, the solute B and other impurity solutes can be efficiently separated at the same time when the phase extraction is retained in the raw material liquid. Is expected to be applied to the separation fields of metal ion separation, chiral resolution and the like.
Drawings
FIG. 1 shows a two-liquid membrane system (W) according to the invention1/O1/W3/O2/W2) Schematic representation of (a). Wherein the liquid membrane can be formed into emulsion liquid membrane, supported liquid membrane or bulk liquid membrane; the supported liquid membrane may be formed by impregnating the filler film solution into the micropores of the membrane, using a hollow fiber porous membrane, a flat plate porous membrane, or the like as a supporting base membrane.
FIG. 2 is a schematic view of a two-liquid membrane-coupled membrane module using a hollow fiber porous membrane as a support membrane in example 1 of the present invention.
FIG. 3 is a schematic diagram of the back-extraction phase-dispersed double-liquid-membrane coupling separation principle using a flat porous membrane as a support membrane in example 2 of the present invention.
FIG. 4 shows a raw material liquid (W) in example 2 of the present invention3) Cd (2)2+And Zn2+The yield varied with time.
FIG. 5 shows a stripping solution 1 (W) in example 2 of the present invention1) Cd (2)2+And Zn2+The yield varied with time.
FIG. 6 shows a stripping solution 2 (W) in example 2 of the present invention2) Cd (2)2+And Zn2+The yield varied with time.
Detailed Description
The invention is further illustrated by the following figures and examples, but is not limited to the description. Certain features of the drawings may be omitted, enlarged or reduced as would be understood by those skilled in the art. Any variation in shape or structure, whether identical or similar, is within the scope of the invention, whether or not the same or similar embodiments are contemplated by the present application.
Example 1: a double-liquid membrane coupling membrane component with a hollow fiber porous membrane as a support membrane and a using method thereof.
Example 1 is a membrane module and method of use for achieving a two-fluid membrane coupling operation. The membrane module is composed of stripping liquid 1 (W)1) Inlet and outlet of (2), stripping solution (W)2) Inlet and outlet, raw material liquid (W)3) Inlet and outlet, supporting liquid film phase 1 (O)1) Hollow fiber porous membrane, supporting liquid membrane phase 2 (O)2) The hollow fiber porous membrane and the housing. The detailed structure is schematically shown in figure 2. The stripping solution 1 (W) is used1) And stripping solution 2 (W)2) It can be carried out in countercurrent or cocurrent. The membrane module can conveniently increase the contact area of the liquid membrane by increasing the number or length of the hollow fiber porous membranes.
Example 2: back extraction phase dispersion double-liquid-film coupling separation method with flat porous membrane as support membrane and application of back extraction phase dispersion double-liquid-film coupling separation method to Cd2+And Zn2+Separation of (4).
Example 2 consists of the following steps: (1) solution preparation: preparing the raw Material liquid (W)3): mixing CdSO4、ZnSO4Acetic acid, sodium acetate, potassium iodide and the like are dissolved in water to prepare Cd2+And Zn2+An aqueous solution with ion concentration of 25 mg/L, acetate concentration of 0.1mol/L and potassium iodide concentration of 0.05 mol/L, pH = 2; preparing a liquid film phase 1 (O)1): n-heptane solution with trioctylamine TOA content of 5% by volume fraction; preparing stripping solution 1 (W)1): an aqueous solution with the concentration of ammonium acetate of 1 mol/L; preparing a liquid film phase 2 (O)2): a n-heptane solution with a P204 content of 5% by volume; preparing stripping solution 2 (W)2): an aqueous solution of nitric acid with a concentration of 1 mol/L. (2) The liquid membrane device is built and separated: as shown in figure 3, the device is in the form of a back-extraction phase dispersed supported liquid film and comprises three chambers, a middle chamberThe chamber contains a raw material liquid (W)3) The left chamber contains liquid film phase 1 (O)1) And stripping solution 1 (W)1) (stripping solution 1 (W)1) Dispersed in the form of droplets in the liquid film phase 1 (O)1) Middle and right chambers containing liquid film phase 2 (O)2) And stripping solution 2 (W)2) (stripping solution 2 (W)2) Dispersed in the form of droplets in the liquid film phase 2 (O)2) In (1). Liquid film phase 1 (O)1) And a raw material liquid (W)3) Liquid film phase 2 (O)2) And a raw material liquid (W)3) The interval between the two is polyvinylidene fluoride (PVDF) films (the contact part is circular and has the diameter of 35 mm). Wherein the micropores of the two PVDF membranes are preliminarily treated with a liquid membrane phase 1 (O)1) And liquid film phase 2 (O)2) Respectively, to form two supported liquid films. In the separation process, the raw material liquid (W)3) Cd in (2)2+Complexing with iodide ion, preferentially coating with liquid film phase 1 (O)1) Is extracted by the extractant TOA in (1) and is stripped by a stripping solution (W)1) Stripping the stripping agent ammonium acetate; raw material liquid (W)3) Zn in (1)2+Preferentially by liquid film phase 2 (O)2) Is extracted by the extractant P204 in (1) and is stripped by a stripping solution 2 (W)2) The stripping agent in (1) is back extracted by nitric acid. The yields calculated by taking samples at different separation time points and measuring the concentrations are shown in FIGS. 4-6. The yield is defined as: the concentration of metal ions in a certain phase multiplied by the volume of that phase is divided by the initial concentration of the metal ions in the feed solution and then by the volume of the feed solution. The results are as follows: FIG. 4 shows Cd in the raw material liquid2+And Zn2+The yield of (2) varies, both of which gradually decrease with time. FIG. 5 shows stripping solution 1 (W)1) Middle Cd2+And Zn2+Yield change of Cd2+The yield increases at a faster rate over time, while Zn2+The rate of yield increase over time is slow. FIG. 6 shows stripping solution 2 (W)2) Middle Cd2+And Zn2+Yield change of (1), Zn2+The yield increases faster with time, while Cd2+The rate of yield increase over time is slow. Thus, one single run of Cd at an extraction time of 8h (time can be shortened by increasing the contact area of the membrane)2+And Zn2+In stripping solution 1 (W)1) And stripping solution 2 (W)2) The division ratio of (1) is 13 and 10, and the division by multiplying the twoThe separation factor is 130. The above results are influenced by the contact area of the membrane being too small, and the rate and separation effect of the two-liquid membrane separation can be further improved by increasing the contact area of the membrane.
Claims (7)
1. A separation method of double liquid membrane coupling is characterized in that: the double liquid film system is prepared from stripping liquid 1 (W)1) Liquid film phase 1 (O)1) Raw material liquid (W)3) Liquid film phase 2 (O)2) And stripping solution 2 (W)2) Five successive contacts (W)1/O1/W3/O2/W2) Composition is carried out; raw material liquid (W)3) The medium solute A is more coated with the liquid film phase 1 (O) than the solute B1) Extracted and stripped with stripping solution 1 (W)1) Back extraction; raw material liquid (W)3) The medium solute B is more absorbed by the liquid film phase 2 (O) than the solute A2) Extracted and stripped with stripping solution 2 (W)2) And (4) back-extracting to realize the separation of solute A and solute B.
2. The method of claim 1, wherein: the liquid film phase 1 (O)1) Respectively reacting with the stripping solution 1 (W)1) And the raw material liquid (W)3) Immiscible, the liquid film phase 2 (O)2) Respectively with the stripping solution 2 (W)2) And the raw material liquid (W)3) Are immiscible.
3. The method of claim 1, wherein: the liquid film phase 1 (O)1) Or the liquid film phase 2 (O)2) The operation is carried out in the form of an emulsion liquid film, a supported liquid film or a bulk liquid film.
4. The method of claim 1, wherein: the raw material liquid (W)3) Is a solution containing the solute A and the solute B, or is a solution containing the solute A, the solute B and coexisting impurities.
5. The method of claim 1, wherein: the liquid film phase 1 (O)1) An extractant 1 containing a preferential extraction of said solute a; the liquid film phase 2 (O)2) An extractant 2 which preferentially extracts the solute B.
6. The method of claim 1, wherein: the raw material liquid (W)3) Is a cadmium ion (Cd) containing solute A2+) And solute B Zinc ion (Zn)2+) An aqueous solution of (a); the liquid film phase 1 (O)1) Is n-heptane solution containing extractant 1 Trioctylamine (TOA); the stripping solution 1 (W)1) Is an aqueous solution containing a stripping agent ammonium acetate; the liquid film phase 2 (O)2) Is a normal heptane solution containing extractant 2 di (2-ethylhexyl) phosphate (P204); the stripping solution 2 (W)2) Is an aqueous solution containing the stripping agent nitric acid.
7. The method of claim 1, wherein: the raw material liquid (W)3) A solution containing the levorotatory enantiomer of solute A and the dextrorotatory enantiomer of solute B, or a solution containing a racemic mixture; the liquid film phase 1 (O)1) Is an extractant 1 solution which preferentially extracts the levorotatory enantiomer; the stripping solution 1 (W)1) Is solution containing stripping agent 1; the liquid film phase 2 (O)2) Is a solution containing an extractant 2 for preferentially extracting the dextrorotatory enantiomer; the stripping solution 2 (W)2) Is a solution containing a stripping agent 2.
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2020
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| 罗小健: "反萃分散组合液膜迁移和分离金属离子的研究", 《中国优秀博硕士学位论文全文数据库 (硕士)工程科技Ⅰ辑》, no. 6, pages 222 - 225 * |
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