Reversed micellar solubilization extraction and separation of thorium(IV) from rare earth(III) by primary amine N1923 in ionic liquid

The extraction behavior of thorium(IV) sulfate by primary amine N1923 in imidazolium-based ionic liquid (IL) namely 1-octyl-3-methylimidazolium hexafluorophosphate ([C(8)mim]PF6) was systematically studied in this paper. Results showed that the extraction behavior was quite different from that using conventional solvent as diluent. A reversed micellar solubilization extraction mechanism was proposed for the extraction of thorium(IV) by N1923/[C(8)mim]PF6 via slope analysis method and polarized optical microscopy (POM)/transmission electron microscopy (TEM) observation. The salt-out agent, Na2SO4, was demonstrated to prompt this extraction mechanism.

Extraction kinetics of thorium(IV) with primary amine N1923 in sulfate media using a constant interfacial cell with laminar flow

Extraction kinetics of thorium(IV) with primary amine N1923 in sulfate media has been investigated by a constant interfacial cell with laminar flow. Studies of interfacial tension and effects of the stirring rate, temperature, and specific interfacial area on mass transfer rate show that the most probable reaction zone takes place at the liquid-liquid interface. According to the experimental data correlated as a function of the concentration of the relevant species involved in the extraction reaction, the rate equation of extracting thorium has been obtained as follows: -d[Th(IV)]((o))/dt = 10(-3.10)center dot[Th(IV)](0.89)center dot[(RNH3)(2)SO4](0.74).

Synergistic extraction of rare earths using acid-base coupling extractants of calix[4]arene carboxyl derivative and primary amine N1923

Synergistic effect in the extraction of rare earth (RE) metals by the acid-base coupling (ABC) extractants of calix[4]arene carboxyl derivative Bu-t[4]CH2COOH (H(4)A) and primary amine N1923 (RNH2) has been investigated. The extraction of RE was enhanced by the addition of sodium cations into the aqueous phase not only in the extraction system of Bu-t[4]CH2COOH alone but also in the mixture of Bu-t[4]CH2COOH and N1923. The separation factors (SFs) indicating the extraction selectivity of adjacent RE elements became higher in the mixture system.

Extraction kinetics of cerium(IV) from sulfuric acid medium by the primary amine N1923 using a constant interfacial area cell with laminar flow

BACKGROUND: Thermodynamic studies on Ce(IV) extraction with primary amine N1923 demonstrate that primary amine N1923 is an excellent extractant for separation of Ce(IV) from Re(III). In order to clarify the mechanism of extraction and to optimize the parameters in practical extraction systems used in the rare earth industry, the extraction kinetics was investigated using a constant interfacial area cell with laminar flow in the present work.RESULTS: The data indicate that the rate constant (k(ao).) becomes constant when stirring speed exceeds 250 rpm. The apparent forward extraction rate is calculated to be 10(-1.70). The activation energy (E.) was calculated to be 20.5 kJ/mol from the slope of log kao against 1000/T. The minimum bulk concentration of the extractant necessary to saturate the interface (C-min) is lower than 10(-5) mol L-1.CONCLUSION: Studies of interfacial tension and the effects of stirring rate and specific interfacial area on the extraction rate show that the extraction rate is kinetically controlled, and a mass transfer model has been proposed. The rate equation has been obtained as: -d[Ce(IV)]/dt = 10(-1.70)[Ce(IV)] [(RNH3)(2)SO4](1.376). The rate-controlling step has been evaluated from analysis of the experimental results.

Interfacial behavior of primary amine N1923 and the kinetics of thorium(IV) extraction in sulfate media

The influences of additive, diluents, temperature, acidity of the aqueous phase on the interfacial behavior of primary amine N1923 in sulfate media have been investigated using the Du Nouy ring method. In addition, the effect of concentration of thorium(IV) loaded in the organic phase on the interfacial tension has also been studied. The interfacial tension isotherms are processed by matching different adsorption equations such as the Gibbs and the Szyszkowski. The surface excess at the saturated interface (Gamma (max)) and the minimum bulk concentration of the extractant necessary to saturate the interface (C-min) under different conditions are calculated according to two adsorption equations to be presented in comprehensive tables and figures. It appears that primary amine N1923 has strong interfacial activity and behaves very differently in various diluents systems. The surface excess at saturated interface increase with the type of diluerits in the following order: chloroform < aromatic hydrocarbons < aliphatic hydrocarbons. The relationship between the interfacial activity and kinetics of thorium extraction by primary amine N1923 has been discussed by considering different factors. However, the interfacial activity of primary amine N1923 is only a qualitative parameter suggesting the interfacial mechanism for thorium extraction, it cannot give strong evidence quantitatively supporting this mechanism.

Synergistic extraction of zinc(II) and cadmium(II) with mixtures of primary amine N1923 and neutral organophosphorous derivatives

Synergistic extraction of zinc(IT) and cadmium(11) from hydrochloric acid solution with primary amine N1923 and neutral organophosphorus derivatives Cyanex 923 and Cyanex 925 is the focus of this paper. Extraction mechanisms are discussed as well as how the acidity of the aqueous phase, the composition of the organic phase, and the experimental temperature affect the rates of extraction of metal ions. Differences between synergistic efficiency of Zn(II) and Cd(II) with mixtures of primary amines N1923 and either Cyanex 923 or Cyanex 925 are observed. The equilibrium constants, the composition, and the formation constants of the extracted complexes as well as the values of the thermodynamic functions are calculated. According to the synergy coefficient formula, the synergy effect on the extraction of Zn(II) is in the following order:N1923 + Cyanex 925 > N1923 + Cyanex 923 This order is reversed in the case of cadmium(II). For the same synergistic system, the extraction rate follows the order: Zn(II) > Cd(II). Furthermore, the stereochemical structures of the various extractants and their effect on metal ion extraction rate are also investigated.

Extraction of zinc(II) and cadmium(II) by using mixtures of primary amine N1923 and organophosphorus acids

The extraction of zinc(II) and cadmium(II) from a chloride medium by mixtures of primary amine N1923 and organophosphorus acids [di-(2-ethylhexyl)-phosphoric acid, 2-ethylhexylphosphonic acid mono-2-ethylhexyl ester (HEH/EHP), isopropyl phosphonic acid 1-hexyl-4-ethyloctyl ester, bis(2,4,4-trimethylpentyl) phosphinic acid, bis(2,4,4-trimethylpentyl) monothiophosphinic acid, and bis(2,4,4-trimethylpentyl) dithiophosphinic acid] has been studied in the present paper. Results show that only the mixtures of N1923 + HEH/EHP and N1923 + Cyanex272 have synergistic effects on zinc(II), but the other mixtures have no evident synergistic effects. All six mixtures have no evident synergistic effects on cadmium(H). A possible explanation of the different extraction abilities is given based on the structure of the extractants. Furthermore, the possibilities of separating zinc(II) and cadmium(II) with these mixtures are investigated according to the extractabilities. It is possible to separate Zn2+ from bulk cadmium with N1923 and HEH/EHP mixtures and separate Cd2+ from bulk zinc with N1923 and Cyanex301 mixtures.

Synergistic extraction of zinc(II) by mixtures of primary amine N1923 and Cyanex272

The extraction of zinc(II) and cadmium(II) from chloride solution by mixtures of primary amine N1923 and Cyanex272 (HA) was studied. The synergistic effect was observed for the extraction of zinc(II) while no synergistic effect for cadmium(II), which makes it possible to separate zine(II) and cadmium(II) with the mixtures. The results showed that zinc(II) was extracted as (RNH3Cl)(3) . ZnCIA instead of ZnA(2) . 2HA which was extracted by Cyanex272 alone. The extraction mechanism was discussed and the formation constants and thermodynamic functions were determined. The separation factors between zinc(II) and cadmium(II) were calculated.

Studies on synergistic extraction of rare earths(III) with HBTMPTP and primary amine N1923

The synergistic extraction of rare earths(III) with binary systems containing HBTMPTP and primary amine N1923 from sulfuric acid medium was observed, The syner gistic extraction factor(R) decreased with increasing atomic number of lanthanides. Through the methods of slope analysis, constant mole and saturation titration, the synergistic extraction stoichiometry was obtained, The thermodynamic function was calculated, The IR spectra of the saturated synergistic extraction completely confirmed the mechanism.

HBTMPTP与伯胺N1923对稀土元素(Ⅲ)的协同萃取

研究了二（2，4，4-三甲基戊基）单硫代膦酸（HBTMPTP，HL）和伯胺N1923的正己烷溶液从硫酸介质中对稀土元素（Ⅲ）的协同萃取．并以La（Ⅲ）为例，用斜率法、恒摩尔法和饱和法确定了协萃配合物的组成为（RNH3）3L2La（SO4）2，计算了协萃配合物的生成常数及热力学函数，观测了协萃配合物的IR谱.

甲基膦酸二甲庚酯与伯胺N1923对Cd(Ⅱ)的协同萃取

本文研究了甲基膦酸二甲庚酯(P_(350),以 B 表示)与伯胺 N_(1923)(以RNH_2表示)的正庚烷溶液,在(Na,H)C1介质中对 Cd(Ⅱ)的协同萃取。用等摩尔系列法和斜率法确定二元协萃配合物组成为(RNH_3C1)_2·CdC1_2·B;求得协萃反应平衡常数1gK_(Bc)=2.08,协萃配合物的生成常数1gβ=0.70;计算了协萃反应的热力学函数△H=-14.56kJ/mol,△G=-12.07kJ/mol 和△S=-8.22J/mol·K;还讨论了协萃配合物的 IR 和NMR 谱。

杯芳烃羧酸萃取稀土、钍与含杯配合物结构研究

本文以大环化合物杯芳烃羧酸为萃取体系，系统考察稀土元素在该体系中的萃取分离性能，比较了钍与稀土元素的萃取性质差异，从而为杯芳烃羧酸在该分离领域中的应用提供一定的实验数据，此外，采用无机水热合成制备了含杯[8]芳烃的三元超分子配位聚合物并表征其结构，具体研究内容如下： 1、 合成杯芳烃并进行化学修饰得萃取剂杯芳烃羧酸，采用熔点测定、元素分析、TG-DTA、FT-IR和1H-NMR等分析方法表征，并利用两相滴定法测定了杯芳烃羧酸的基本常数。 2、 研究杯芳烃羧酸-CHCl3/RE-HCl萃取体系碱金属离子、离子强度、酸度、温度和萃取剂浓度对Eu(III)的萃取分配比影响，并分析其萃取机理。在此基础上，探索杯芳烃羧酸的协同萃取性能，发现杯[4]芳烃羧酸与伯胺N1923的ABC酸碱耦合协萃体系对轻、中、重稀土有不同的协萃能力，协萃系数与原子序数呈“双峰效应”。 3、 在萃取热力学基础上，利用层流恒界面池研究杯[4]芳烃羧酸萃取Nd(III)的动力学性质，确定了萃取反应控制模式随条件不同有所变化，化学反应在相界面上进行，并获得了萃取反应速率方程。 4、 以杯芳烃羧酸-CHCl3/Th-HCl体系研究钍的萃取性能，考察了碱金属离子、离子强度、酸度、温度和萃取剂浓度对Th(IV)的萃取影响，比较其与稀土萃取性能的差异，并在此基础上进一步研究与伯胺N1923协同萃取钍的性能，分析了协同萃取反应机制。 5、 水热合成并表征了含磺化杯[8]芳烃，2，2’-联吡啶与镍的三元超分子配合物。磺化杯[8]在该配合物中呈“双-反向锥式”构型，分子间由氢键和C-H…π相互作用将四核Ni簇连接成三维超分子结构。

离子液体在铈（IV）钍及稀土（III）萃取分离中的应用研究

本文对1-辛基-3-甲基咪唑六氟磷酸盐离子液体（[C8mim]PF6）在包头稀土矿分离钍以及攀西矿分离铈工艺中的应用作了初步探索。论文首先研究了伯胺N1923溶于离子液体对硫酸体系钍的萃取分离行为，考察了酸度、盐析剂浓度、萃取剂浓度等对N1923/IL萃取钍的影响，并与庚烷体系的萃取规律作了对比。在此基础上对萃取机理进行了探讨，提出了不同于分子溶剂体系的萃取机理，认为N1923/IL在水相有硫酸钠作为盐析剂时对钍的萃取为“胶束增溶”萃取机理。此外，钍对稀土的分离考察结果认为，虽然N1923/IL对钍的萃取效率降低，但在一定条件下钍对稀土仍能保持较高的分离系数。由此本文对N1923/IL应用于钍的分离实践作了初步评估。 论文的另外一部分工作研究了纯[C8mim]PF6及其与2-乙基己基膦酸二（2-乙基己基）酯（DEHEHP）的混合体系对硝酸铈（IV）的萃取性能。研究发现纯[C8mim]PF6本身对硝酸铈（IV）有良好的萃取选择性，机理考察结果认为铈（IV）的萃取是由于Ce4+离子在富硝酸根溶液中形成络阴离子Ce(NO3)62-并与离子液体的阴离子PF6—发生交换的结果。一种新型含铈离子液体[C8mim]2Ce(NO3)6的合成进一步证实了这一机理。反萃考察发现被萃入离子液相的铈（IV）用水可完全反萃，且萃取和反萃过程中因离子交换机理导致的离子液体流失可以通过添加适量离子液体组分的方法予以抑制。此外，本文考察了DEHEHP溶于[C8mim]PF6对于含氟硝酸体系铈（IV）的萃取行为，发现在一定条件下DEHEHP对铈（IV）的萃取能获得与分子溶剂中等同的萃取机理。在此基础上，采用DEHEHP/IL从氟碳铈矿分解液中进行分离铈和氟的研究，获得纯度为99.9%以上的纳米CeF3产品。由此我们提出一个将离子液体应用于攀西氟碳铈矿铈钍稀土分离流程的模型，为离子液体在稀土清洁分离流程中实现溶剂绿色化的目标提供了一个范例。

稀土分离过程的平衡反应和动力学研究

本论文共分六章，论文首先综述了近年稀土溶剂萃取最新出现的一些萃取体系及萃取方法，然后用溶剂萃取法系统研究了新萃取剂 PT-2 萃取稀土(III)、Cyanex 923 和 Cyanex 925 萃取铈(IV)、钍和稀土(III)的性质，推导层流型恒界面池的理论基础并用恒界面池法研究 Cyanex 272、PT-2 萃取稀土动力学，用高效离心分配色层仪(HPCPC) PT-2、Cyanex 302 和 Cyanex 272-P507 混合体系分离稀土(III)的规律，本论文还在大量实验数据的基础上，提出从氟碳铈矿中提取稀土的具有创新性的绿色工艺流程。论文第一章综述了近年衡土溶剂萃取的研究成果，为探求优于应用于工业生产的萃取稀土(III)的 P507 体系以及萃取钇的环烷酸体系，人们合成大量的有机磷类、羧酸类、苯胲类萃取剂并研究了它们萃取稀土的性能，将现有的萃取剂进行优化组合得到许多稀土的协同萃取体系，还将结晶反萃、还原反萃等方法应用于稀土分离过程。第二章用两相滴定法在测定 PT-2 的 K_d、K_2 等基本常数基础上，研究了 PT-2 的正庚烷溶液在盐酸、硝酸介质中萃取 15 个稀土离子（除了 Pm 外）的分配规律及萃取机理，同硫酸体系、高氯酸体系萃取平衡进行了对比，得到一些在理论上和实际上很有价值的结果。首次发现高位阻的酸性膦酸类萃取剂 PT-2 萃取轻、重稀土(III)时存在不同的机理，在盐酸、硝酸和硫酸体系中， PT-2 萃取轻稀土(III)为阳离子交换机理， PT-2 萃取重稀土时，阳离子交换机理和溶剂缔合机理共存；高氯酸介质中，由于高氯酸根离子难以同稀土(III)形成络合物， PT-2 萃取稀土(III)的机理符合一般的酸性膦酸酯的萃取规律，为阳离子交换机理。第三章探求了多种纯化 Cyanex 923 和 Cyanex 925 的途径，得出了较为行之有效的纯化方法，系统地研究了 Cyanex 923 从硫酸和硝酸介质中萃取 Ce(IV)、Th、La 和 Gd的规律，确定了萃合物的组成，计算了 lgK、ΔG、ΔH、ΔS 等热力学常数。 Cyanex 923 对 Ce(IV)、 Th(IV)的萃取在高酸度时随酸度的增大而降低，而 Ce(IV)、 Th(IV)同时萃取时， Th(IV)的萃取受到 Ce(IV)的抑制。发现 Cyanex 923 是一种良好 Ce(IV)的萃取剂，可用于铈从稀土(III)、钍中的分离、富集，具有很好的应用前景。第四章在层流型恒界面池的传质过程理论研究基础上，研究了二 (2,4,4-三甲基戊基)膦酸(HBTMPP)、PT-2 萃取 Er(III)的动力学，测定了流体线性流速、有机相浓度、水相浓度和酸度、温度及界面面积等因素对萃取速率的影响，对萃取的控制模式作出判断，为 Cyanex 272、 PT-2 在稀土湿法冶金中的应用提供基础参数。推导出层流型恒界面池中扩散控制模式下的萃取过程善于传质量和扩散层厚度两个基本公式。PT-2 萃取 Er(III)的过程属于扩散控制模式，在不同参数（温度、线性流速、界面面积、两相组成等）条件下，以 ln[(1/β + 1)C_b~a/C_(b,0)~a - 1/β] 对时间 t 作图得到都为直线，这些参数的变化对萃取的控制模式没有影响。萃取速率随温度、线性流速、界面面积等的变化规律也表明，该萃取过程为一扩散控制模式。根据萃取速率随线性流速、界面面积和温度的影响推断 HBTMPP 萃取 Er(III)为扩散控制和化学反应共同作用的混合控制模式。利用稳态法推导出该萃取过程的初始速率方程，该速率方程能和实验结果较好吻合。第五章用 HPCPC 研究 PT-2、Cyanex 302 及 Cyanex 272-P507 体系分离重稀土元素，评估 HPCPC 的性能及萃取剂的萃取性能，考察了流动相的流速、 pH 及 HPCPC 的转速等对分离效率的影响，并对这些体系萃取重稀土(III)的机理进行了探讨。发现流速对 HPCPC 的分离效率有显著的影响，随流速的增大，理论板数降低，分离度减小；理论塔板数和分离度随转速的变化无明显的变化；在 D 值相同时， Vs/Vm 越小，理论塔板数 N 越大；pH 越高，D 越大，理论塔板数则越低；萃取剂的浓度越高，理论塔板数越低。用 HPCPC 梯度洗脱法在 Cyanex 302 体系中只经过一次运行可将轻、重稀土混合物 La(III)、Sm(III)、Dy(III)和 Tm(III)分离。第六章针对攀西稀土矿 冶炼工艺中存在由于稀土收率低、放射性钍未得到分离和利用、存在二个放射性废渣和放射性废水等问题，采用溶剂萃取法，从攀西矿氧化焙烧－硫酸浸出液中萃取分离钍和铈(IV)。研究了 N1923 从氟碳铈矿硫酸浸出液中萃取分离钍和铈(IV)的工艺，并在此基础上提出从攀西矿中萃取分离铈(IV)、钍和提取氯化稀土的流程 I。用 N1923 萃取铈(IV)、钍，稀硫酸为洗液，形成含四价铈及钍的有机相和含三价稀土元素的萃余液，实现铈、钍与三价稀土的萃取分离。由于用含过氧化氢的硫酸溶液反萃铈(IV)困难，用含过氧化氢的硝酸溶液反萃铈(IV)、钍，再以 Cyanex 923 萃取钍，实现钍和铈(III)的分离。还研究了用 S501 萃取萃取铈(IV)工艺，以稀硫酸为洗液，用含过氧化氢的硫酸溶液为反萃取液反萃铈(IV)。解决了萃取过程铈(IV)的还原性问题；探明了氟离子对萃取过程的影响以及在料液、洗液、反萃取液中加入硼酸的作用，在大量数据的基础上提出了工艺的各成分的组成。

中空纤维膜基萃取稀土的研究：中空纤维膜基萃取Ce~(4+), Th~(4+)和RE~(3+)及其传质动力学

本文用中空纤维膜基萃取法研究了铈（IV）、钍和 RE（III）的膜基萃取；铈（IV）与 RE（III）、钍和 RE（III）的膜基萃取分离；铈（IV）与 RE（III）的界面化学反应动力学；膜基萃取中的流体动力学；萃取操作中乳化发生的机理；测定了中空纤维膜的孔率和孔径。在铈（IV）、钍和 RE（III）的膜基萃取过程中，研究了水相流量、油相流量、原料液中硫酸浓度、萃取剂 N1923浓度和水相溶质浓度对基于水相总传质系数的影响。钍的总传质系数受水相流量影响较大，不受油相流量影响，从而提出水相扩散层控制的膜基萃取传质机理；铈（IV）的传质系数受水相流量影响，油相流量影响较小，主要为水相扩散层控制的传质机理；RE（III）的传质系数受水相和油相的影响都比较小，为膜内传质过程的传质机理。酸浓度对钍和铈（IV）传质系数影响较小，是由于酸浓度影响分配系数，而对于水相扩散控制的传质过程，水相分传质系数与分配系数无关；酸浓度对 RE（III）的影响，是由于膜内传质阻力与分配系数在关；N1923 对 RE（III）萃取传质系数的影响进一步证明膜内过程控制的传质机理，同时对数曲线的斜率大于1 也说明界面反应为一复杂过程；水相溶质浓度不影响基于水相的总传质系数，进一步证实了传质速度与初始浓度无关，也从一个侧面反应了膜基萃取实验有较好的重复性。实验研究的结果，对铈（IV）的膜基萃取选择油相组成为 10%N1923+4%异辛醇+正庚烷（或煤油），水相酸浓度为 1～2mol/L，水相和油相流量可以在较大的范围内选择；钍的膜基萃取条件相似，只是油组成中萃取剂浓度为 1%N1923。在流体动力学部分，通过作用力分析，利用能量守恒原理，推导出了膜基萃取操作中的雷诺数，建立了层流流动模型；腔内外流体流速的径向分布模型和平均流速的计算式；腔内外压力沿管长度分布的数学模型，并得到了两相流体的压力差计算式。流体的动力学分析对于研究乳化发生的机理、传质的数学模型和扩散层厚度等皆有理论价值。通过流体动力学理论，结合膜破裂压和界面张力的实验方法研究了乳化发生的机理。水相进入有机相的乳化，对于非同级萃取，外压作用是乳化的主要原因，提出了类似于重力液滴形成的乳化模型；对于有机相进入水相的乳化，亲油膜的表面易形成油膜及界面张力形成的附加压力是乳化的基本原因，而随着有机相内溶质浓度增加界面张力降低使乳化在萃取操作的后期较易发生。膜破裂压和界面张力的研究方法使乳化的研究变得可以进行实验测定，这对于膜材的选择是很有价值的。界面反应动力学采用了上升单滴法，这种方法一般具有实验重复性较差的缺点。通过实验发现，影响重复性的因素主要是单滴形成速率的稳定性、聚结界面处油水界面位置的恒定和扩散传质的消除等。我们采用盘管式油加液管的设计，比较简单地解决了单滴形成速率稳定的问题，油水界面恒定是一个技术性问题，在实验中得到了较好的解决，通过传质时间与控制聚结界面的面积解决了消除扩散传质的难题。本论文的创新之处有如下几个方面：1．根据氟碳铈矿中钍、铈（IV）与稀土（III）分离的总目标，首次实现了伯胺 N1923对上述离子的中空纤维膜基萃取，提出了利用动力学差异的新型分离模式；2．对流量改变对传质系数的影响，所有文献报道的流量范围都没有达到流量增加使传质系数减小，而这一较高的流量揭示了油水界面随压力增加向膜内移动的事实，这对防止乳化时的压力控制是非常重要的。流量对扩散层厚度影响是对传质系数影响的主要原因，而混流的影响是次要的因素；3．铈（IV）和 RE（III）、钍和 RE（III）的分离表明，分离系数远远大于由总传质系数预计的结果，从而提出了动力学竞争萃取分离的机理；4．膜破裂压的测定方法是一个创新的设计。这种方法对于膜材选择和萃取时操作压力的控制是非常重要的。在现有文献中，都是直接在膜萃取操作时测定水相中的游离油或油相中游离水的体积的方法进行研究，这即不能研究乳化的机理，也不能测定准确的乳化时间。因此膜破裂压测定为乳化过程提供了一个新的研究方法；5．乳化机理的研究得到了较新的结论，尤其对于油相进入水相的乳化机理，较好地解释了在水相有超压存在下油相漏液的原因；6．界面反应动力学实验装置中盘管式油相加样解决了油滴形成稳定性的问题，提高了实验测定的可靠性的重复性。