HDEHP和HEH/EHP混合萃取剂在硫酸介质中协同萃取RE(Ⅲ)的机制研究

对HDEHP(H2B2)和HEH/EHP(H2L2)混合萃取剂在硫酸介质中萃取稀土元素(La,Nd,Sm,Gd)的机制进行了研究。研究表明,在水相平衡pH=2.0时,混合萃取剂萃取这几种元素的协萃系数分别为:1.96(La),3.52(Nd),5.96(Sm),5.71(Gd),并且协萃系数随水相平衡pH的升高而增加。利用斜率法分别确定了单一萃取剂HDEHP和HEH/EHP以及混合萃取剂HDEHP HEH/EHP在硫酸体系中萃取稀土元素的配合物结构式分别为RE(SO4)xH2x(HB2)3,RE(SO4)xH2x(HL2)3以及RE(HB2)2(HL2)。计算了反应的平衡常数及形成常数并确定了反应机制为阳离子交换反应。     

P507与N235混合溶剂的稳定性及对NdCl3的协萃效应

稀土萃取分离过程皂化产生的含盐废水严重污染环境。利用P507萃取稀土离子、N235萃取酸的特性,设计了P507-N235双溶剂无皂化稀土萃取体系,研究了双溶剂有机相的稳定性及对Nd3+的协萃效应。P507与N235混合时发生放热现象,红外光谱分析显示其特征峰发生了变化,但32次萃取-再生后的混合萃取剂的化学结构稳定;P507与N235对Nd3+具有显著的协萃效果,形成的萃合物为REA3.(R3N.HA).3R3NHCl。研究结果为无皂化稀土萃取分离新工艺开发提供了依据。     

数学模拟法研究氨化 P507分离 Nd-Sm 工艺

用数学模拟法研究了 NdCl_3-SmCl_3-HCl-H_2O-1.5M 氨化 P507-煤油体系的萃取平衡。提出了采用不氨化和氨化萃取剂的萃取平衡模型。利用这些模型初步进行了分馏萃取模拟,并研究了各种平衡数据之间的相互关系,利用其内在联系提出了较简单的模拟方法,以方便模拟工艺要求的任何氨化率的萃取体系。模拟结果与 Nd-Sm 分离试验结果符合得很好,Nd 和 Sm 产品纯度误差分别为0.13%和1.3%。文中还提出了保证不乳化、进料级位置合理、符合萃取要求的不同 Nd、Sm 组分的优化分离工艺。只用6～7级就可使 Nd、Sm 两种产品纯度达到99%以上。     

P-507回流萃取法富集镥的研究——Ⅰ.P-507萃取分离镱镥混合稀土的性能

本文研究了2-乙基己基膦酸单2-乙基己基酯(P-507)在盐酸和硝酸体系中萃取镱镥混合稀土的性能。说明P-507在硝酸体系中的萃取分离系数较其在盐酸体系中高,而在盐酸体系中有更高的反萃效率。与二(2-乙基己基)磷酸(P-204)相比,P-507具有萃取酸度低、易反萃和不易乳化的优点。我们还确定了回流萃取法分离镥镱的基本参数,表明P-507是一种新型的分离重稀土的良好萃取剂。     

P507萃取色谱法分离镓、铟及其测定

2-乙基已基磷酸-2-乙基己基酯(P507)已广泛用于萃取分离稀土元素,用于萃取镓、铟、铊,在盐酸或硫酸介质中均具有较好萃取性质,易于反萃取。鉴于分析分离中萃取色谱法较萃取分离更为实用,我们进一步研究了萃取色谱分离镓、铟及其伴生元素的方     

双功能离子液体[A336][P507]在盐酸和硝酸介质中对Sc(Ⅲ)的萃取

利用双功能离子液体萃取剂三辛基甲基氯化铵2-乙基己基磷酸2-乙基己基酯盐([A336][P507])在HCl和HNO₃介质中对Sc(Ⅲ)的萃取和分离。 研究表明,萃取剂在低酸度条件下,对Sc(Ⅲ)有较好的萃取能力;但是当水相酸度从0.5 mol/L增加到4 mol/L,Sc(Ⅲ)的萃取率有较大程度的下降。 并且讨论了在HCl介质和HNO₃介质中,[A336][P507]萃取Sc(Ⅲ)的机理,由于Sc(Ⅲ)的半径最小,而且在萃取过程中存在P=O与P-O的竞争作用,使得其萃合物结构与轻稀土不同。 水相中加入盐析剂NaCl或NaNO₃对Sc(Ⅲ)的萃取有一定的促进作用;萃取过程的热力学参数的结果表明,萃取反应是放热反应。 还研究了混合稀土中Sc(Ⅲ)和其它稀土离子的分离,在较低酸度的条件下萃取剂[A336][P507]对其它稀土离子的萃取可以忽略不计,因此该萃取体系对Sc(Ⅲ)和其它稀土离子有较好的分离效果,显示了本研究潜在的应用价值。     

磷酸体系中微量稀土元素萃取回收技术研究

研究了从磷矿硫酸湿法制备磷酸过程中回收伴生稀土元素的萃取分离技术,首先进行了不同萃取剂的筛选,同时考察了萃取剂浓度、磷酸浓度、相比、反应温度、杂质元素等对稀土萃取率的影响.结果表明:在该体系下,P204(二(2-乙基己基)磷酸)单独萃取稀土的能力最强,而且较高的萃取剂浓度、较大相比及低的磷酸浓度有利于稀土的萃取,不同杂质对稀土萃取存在不同程度的影响;并对萃取反应机制进行了考察,得到P204在磷酸介质中萃取微量稀土的反应式,该萃取反应的焙变△H<0,为放热反应.     

Cyanex 923从硫酸体系中萃取钪及其与P507和环烷酸的比较

稀土元素钪(Sc)在相关原料中含量低,伴生杂质元素多,回收困难。针对这一问题,本文系统对比了直链三烷基氧化膦(Cyanex 923)、2-乙基己基磷酸单-2-乙基己基酯(P507)、环烷酸在硫酸体系中对Sc的萃取、分离和反萃。Cyanex 923在高酸度下能完全萃取Sc,而环烷酸和P507则在低酸度下有较高萃取率。Cyanex 923分离Sc与锆(Zr)、钛(Ti)的最佳水相酸度为1 mol/L,分离系数分别为5. 6和10. 6。P507在水相H~+浓度为2 mol/L时对Sc/Zr、Sc/Ti有最大分离系数,分别是21和59. 7。虽然P507有更好的分离效果,但难以反萃。3种萃取剂中仅有Cyanex 923能被有效反萃,在反酸H+浓度为0. 4 mol/L时有最大反萃率。因此,Cyanex 923更适合从含Sc二次资源浸出液中分离回收Sc。     

磷酸体系中微量稀土元素萃取动力学研究

采用新型恒界面池法进行了磷酸体系中用P204萃取La(Ⅲ),Sm(Ⅲ)和Y(Ⅲ)的动力学研究,考察了搅拌速度、温度、比界面积、磷酸浓度及萃取剂浓度等因素对萃取速率的影响.结果表明:磷酸体系中用P204萃取La(Ⅲ),Sm(Ⅲ)和Y(Ⅲ)的表观活化能E_a分别为27.0,22.2和21.1 kJ·mol~(-1),在体相P204浓度大于在液一液界面饱和吸附时的最低浓度C_(min)时,其在界面已达到吸附饱和,反应的主通道由界面变为体相,在该体系下P204萃取La(Ⅲ),Sm(Ⅲ)和Y(Ⅲ)反应为体相化学反应和扩散反应混合控制.     

2-乙基己基膦酸单2-乙基己基酯和二(2-乙基己基)磷酸从硫酸介质中协同萃取Ce(Ⅳ)的研究

研究了用2-乙基己基膦酸单-2-乙基己基酯(HEH/EHP,P507)和二(2-乙基己基)磷酸(HDEHP,P204)从硫酸介质中协同萃取Ce(Ⅳ)的机制.结果表明:在HEH/EHP的摩尔分散在0.6时,体系的协萃系数最大.Ce(Ⅳ)以Ce(SO4)0.5HL2A2的形式被萃人有机相,协萃反应为阳离子交换机制.同时还得到了HEH/EHP和HDEHP从硫酸介质中协同萃取Ce(Ⅳ)时,体系的平衡常数及热力学函数如△G,△H和△S等.     

Adsorption of lanthanides(III) from aqueous solutions by fullerene black modified with di(2-ethylhexyl)phosphoric acid

Fullerene black (FB) - a product of electric arc graphite vaporization after extraction of fullerenes - was modified with the di(2-ethylhexyl)phosphoric acid (D2EHPA). The distribution of D2EHPA between FB and aqueous HNO₃ solutions has been studied. The effect of HNO₃ concentration in the aqueous phase and that of D2EHPA concentration in the sorbent phase on the adsorption of microquantities of La, Ce, Pr, Nd, Sm, Eu, Gd, Tb, Dy, Ho, Er, Tm, Yb, Lu, and Y nitrates from HNO₃ solutions by D2EHPA-modified FB are considered. The stoichiometry of the sorbed complexes has been determined by the slope analysis method. The efficiency of lanthanides’ adsorption increases with an increase in the element atomic number. A considerable synergistic effect has been observed upon the addition of the neutral bidentate tetraphenylmethylenediphosphine dioxide ligand to D2EHPA in the sorbent phase.      

二-(2-乙基己基)磷酸与仲壬基苯氧基取代乙酸混合体系对稀土元素的萃取

考察了二-(2-乙基己基)磷酸(D2EHPA,H2A2)和仲壬基苯氧基取代乙酸(CA100,H2B2)混合体系在HCl介质中对15种镧系元素(除钷)及钇的萃取性能,计算了稀土元素间的分离系数,并比较了混合萃取体系与D2EHPA单独萃取体系对稀土元素的分离能力.研究了D2EHPA-CA100混合体系对镧的协同萃取机理,用斜率法和恒摩尔法探讨了萃取反应方程式,考察了酸度、萃取剂浓度及温度对萃取性能的影响.结果表明:D2EHPA-CA100混合体系对镧系元素的协同效应随原子序数的增加而减弱.在适当的萃取剂配比下,此混合体系对某些稀土元素的分离能力优于D2EHPA,可用于这些稀土元素的分离.D2EHPA-CA100混合体系协同萃取镧的萃合物组成为LaH5A6B2,反应为吸热反应.     

Solvent extraction of zinc from sulphate leaching solution of a sulphide-oxide sample using D2EHPA and Cyanex 272

Solvent extraction of zinc from sulphate leach solution obtained from the treatment of a sulphide-oxide sample, was investigated using D2EHPA and Cyanex 272 diluted in kerosene in a batch reactor. According to the results, D2EHPA exhibited the higher extraction efficiencies than Cyanex 272 at the organic/aqueous ratio of 1:1. The optimum concentration and pH for D2EHPA and Cyanex 272 were distinguished to be 0.5?mol/L and 2.5, and 0.035?mol/L and 3.5, respectively. Under these conditions, extraction efficiency was found to be ～75% for D2EHPA against 41% for Cyanex 272. The plot of log D versus log [D2EHPA] confirmed the presence of 1 mole D2EHPA in dimeric form for 1 mole Zn in the extraction system. Thermodynamic data showed that the zinc extraction process is endothermic. For D2EHPA, two-stage simulated counter-current extraction experiments were performed on the basis of the McCabe-Thiele diagram and the extraction percentage of zinc was found to be about 88%. The synergistic effect of Cyanex 272 and TBP with D2EHPA was particularly investigated. It was found that the mixture of 80% D2EHPA and 20% Cyanex 272 exhibited the best synergistic effect for Zn-extraction with a synergistic coefficient of 1.04.     

Extraction of micro- and macroconcentrations of rare earth ions with the mixture of D2EHPA and TBP in n-hexane and cyclohexane

The synergistic solvent extraction of Eu(III) and some other rare earth elements from nitrate solutions (HNO₃+LiNO₃) by a mixture of (TBP+D2EHPA) in n-hexane and cyclohexane has been investigated at 22 °C. Antagonism found in europium extraction from 0.1M HNO₃ transforms into a synergistic effect. The synergistic effects existing for all investigated metals in extraction from 0.1M HNO₃+3M LiNO₃ were caused by formation of mixed complexes of the type Ln(D2EHPA)_2nH_2n–3+1(NO₃)₁TBP_m, where 1=1 or 2. The selectivity of the extraction in a synergistic system is lower for the La–Yb pair than in the case of D2EHPA extraction under the same conditions. On the other hand, the application of the synergistic mixture is more suitable for Eu–Ho separation. Thus the synergistic effect can be used for the separation or refining of some lanthanides.     

Synergistic extraction of uranium from acidic sulfate leach liquor using D2EHPA mixed with TOPO

Uranium extraction from sulfate leach liquor acid by D₂EHPA and TOPO mixture in kerosene was investigated. The effect of different factors affecting the extraction mechanism such as sulfate leach liquor acid, D₂EHPA and TOPO concentrations and temperature have been studied. The mathematical treatment for the obtained date suggested that the composition of synergistic extraction species is (UO₂(D)₂T). The logarithm of the apparent equilibrium constant, log Kex, of synergistic extraction reaction has been evaluated, to be 3.35 ± 0.1. The effect of temperature on extraction process was investigated and the apparent values of the thermodynamics parameters (?H, ?G and ?S) were 38.2 kJ/mol, ?19.1 kJ/mol and 192.5 J/mol respectively.     

Emulsion liquid membrane extraction of Ni(II) and Co(II) from acidic chloride solutions using bis-(2-ethylhexyl) phosphoric acid as extractant

An emulsion liquid membrane process using bis-(2-ethylhexyl) phosphoric acid (D2EHPA) to extract and separate Ni(II) and Co(II) from acidic chloride solutions is described. Liquid membrane consists of a diluent, a surfactant (Span 80), and an extractant (D2EHPA). Hydrochloric acid was used as the stripping solution. The important parameters governing the permeation of nickel and their effect on the separation process have been studied. These parameters are stirring speed, feed phase pH, surfactant concentration, extractant concentration, stripping phase concentration, phase ratio, initial concentration of metal, and treatment ratio. The optimum conditions have been determined. The separation factors of Ni(II) with respect to Co(II), based on initial feed concentration, have been experimentally determined. Furthermore, the extraction selectivity for Co(II) over Ni(II) has been improved by using D2EHPA during the initial minutes.     

The uranium(VI) extraction mechanism of D2EHPA-TOPO from a wet process phosphoric acid

This paper reports the results of an investigation into the solvent extraction of uranium from technical grade phosphoric acid using industrially available extractants as D2EHPA and TOPO diluted in technical grade kerosene. Preliminary tests showed that, the effect of different parameters such as uranium oxidation stage, temperature and the molar ratio of D2EHPA/TOPO on the uranium recovery was in good agreement with those of previous investigations. However, a detailed investigation into the effect of phosphoric acid concentration, organic concentration and acid/organic phase ratios suggested that the mechanism of D2EHPA/TOPO synergism was rather complex and it presented a different character depending on the acid concentration.     

Extraction of Lanthanide Nitrates in Multicomponent Aqueous-Organic Two-Phase Systems with D2EHPA

Lanthanum nitrate distribution in three-component aqueous-organic systems with D2EHPA from acetate or acetic acid–acetate solutions has been studied, it has been shown that variation in sodium acetate concentration or composition of CH₃COONa–CH₃COOH mixture can affect metal distribution ratios. It has been found that extraction in three-component mixture of 1: 1: 1 composition (aqueous solution Ln(NO₃)₃ + CH₃COONa + CH₃COOH–D2EHPA in hexane–isopropyl alcohol) can provide lanthanide separation, which is dependent on the ratio of sodium acetate and acetic acid in aqueous phase and on D2EHPA concentration in organic phase. Lanthanide–lanthanum separation factors have been calculated for the extraction of lanthanide nitrates from acetic acid–acetate solutions.     

Liquid–liquid extraction of uranium from Egyptian phosphoric acid using a synergistic D2EHPA–DBBP mixture

Extraction of uranium from Egyptian phosphoric acid with synergistic mixture of di-2-ethylhexylphosphoric acid (D2EHPA) and di-butyl butyl phosphonate (DBBP) is reported in this paper. The influence of various factors such as D2EHPA concentration, DBBP concentration, phosphoric acid concentration, contact time, aqueous: organic phase’s ratio (aq:org) and temperature on the degree of extraction has been established. The data on the effect of temperature on the extraction showed that the enthalpy change is −23.12 kJ/mol. Uranium extracted by D2EHPA–DBBP is further subjected to a second cycle of extraction and scrubbing impurities. The uranium is finally converted to a high purity UO₃ product using precipitation with hydrogen peroxide and heat treatment at 375 °C.     

Preparation of titanium dioxide nanostructure from ilmenite through sulfate-leaching process and solvent extraction by D<Subscript>2</Subscript>EHPA

In this study, TiO₂ nanoparticles have been obtained from low-grade ilmenite ore via two consecutive acid digestion and solvent extraction processes. The as-extracted TiO₂ (Anatase phase) product was characterized using techniques such as XRD, XRF, FESEM, FTIR and BET surface area. Diluted sulfuric acid and D₂EHPA (bis-(2-ethyl-hexyl) phosphoric acid) were used as digester agent and an extraction solvent, respectively. The effects of main parameters such as recycling capacities and D₂EHPA concentration, as well as the extraction time and temperature on TiO₂ extraction were investigated. The results demonstrated that the best performance and efficiency for titanium and total iron uptake were 99 and 3.8%, respectively, at the lowest concentration of D₂EHPA.