磁絮凝法和高梯度磁流体萃取法集成处理含铬废水

将磁分离技术和化学絮凝法、溶剂萃取法相结合,提出磁絮凝法和高梯度磁流体萃取法集成处理高浓度含Cr电镀废水的新工艺。采用磁絮凝法对高浓度含Cr电镀废水进行一次处理,通过正交实验方法获得了最佳磁絮凝条件：pH 8,磁性Fe₃O₄颗粒用量4 g,搅拌速度80 r·min^-1,主絮凝剂PAFC用量6 ml,可使废水中Cr浓度由4325.13 mg·L^-1降为29.8 mg·L^-1;采用高梯度磁流体萃取法对磁絮凝后废水进行二次处理,将该废水流经两个串联的高梯度磁流体萃取装置,持续动态萃取7 h,在最佳萃取条件下,最高萃取率为99.40%,平均萃取率98.97%,总萃余液Cr浓度由29.8 mg·L^-1降为0.31 mg·L^-1,低于国家排放标准;碱性条件下磁流体萃取剂反萃率大于90%,再生磁流体萃取剂可重复使用。     

用磷酸三丁酯萃取分离硫酸铵母液中的HCN

研究了磷酸三丁酯(TBP)-磺化煤油体系从重庆某企业甘氨酸生产副产物硫酸铵母液中萃取分离HCN的工艺,考察了萃取体系、TBP体积分数、母液初始pH值、相比(Vorg∶Vaq)对萃取HCN的影响以及氢氧化钠浓度、相比(Vaq∶Vorg)和平衡pH值对HCN反萃的影响。结果表明:选用TBP作为萃取剂能够对硫酸铵母液中的HCN进行快速有效的萃取;TBP体积分数、母液初始pH值及相比对HCN萃取率影响显著;以含体积分数35%TBP的有机相作萃取剂,在相比(Vorg∶Vaq)为2∶1的条件下,pH值为2.92的含氰1.71 g/L的硫酸铵母液经3级错流萃取,萃余液中含氰低于0.5 mg/L,氰的萃取率接近100%;在相比(Vaq∶Vorg)为1∶1条件下,以0.6 mol/L的氢氧化钠为反萃液,控制反萃液平衡pH值大于13.0,氰的单级反萃率大于96%;含氰0.78 g/L的有机相在相比为1∶1条件下,经过2级错流反萃,氰基本上被反萃完全,贫有机相不经过处理可循环使用。     

微胶囊固定化P507萃取Sm3+的性能研究与优化

为解决传统溶剂萃取回收稀土中两相分离困难、溶剂流失和设备庞大的问题,利用溶剂萃取法结合同轴环管微通道装置制备聚砜微胶囊,研究了微胶囊固定化P507 对Sm³⁺的萃取性能及其优化。系统地考察了微胶囊固定化P507 对Sm³⁺ (300 mg·L^-1) 的萃取动力学、反萃性能和循环萃取反萃稳定性,揭示了微胶囊萃取体系的优点,操作简单、萃取剂流失较小、稳定性高。为强化传质过程,提高萃取、反萃动力学,用煤油稀释负载的P507,考察P507-煤油溶液中P507 体积分数对萃取效果的影响。P507-煤油溶液中的P507 体积分数为40%时,在液液体系中对Sm³⁺的萃取效果最好。将其用于微胶囊体系中,和稀释前相比,萃取平衡时间由120 min 缩短到40 min,萃取容量从由45.09 mg·(g P507)^-1 增大到69 mg·(g P507)^-1,P507 利用率由55%提高到84%,反萃完成时间由600 min 减小到120 min。用煤油稀释负载的P507 能有效提高萃取速率、平衡萃取量和反萃速率。20 次萃取反萃循环表明P507 稀释后微胶囊仍然具有较好的稳定性。     

从铜熔炼烟灰浸出液中萃取分离铜的试验研究

以铜熔炼烟灰浸出液为研究对象，采用N902萃取剂从中分离回收铜，并将铜元素进行富集。研究了萃取剂浓度、相比(O/A)、溶液pH值、振荡时间对铜萃取分离的影响，以及反萃剂浓度、相比、振荡时间对铜反萃率的影响。试验结果表明，在萃取剂质量分数12%、相比(O)/(A)=1∶2、溶液pH值为2.0、振荡时间6 min的萃取条件下，通过两级逆流萃取，铜、锌、铁的萃取率分别为98.26%、1.29%、2.28%;铜与铁、锌的分离系数分别达到4346和2425,实现了铜与铁、锌的有效分离。在选定反萃剂硫酸铜浓度为2.5 mol/L、相比(O)/(A)=2∶1、振荡时间6 min的条件下，通过两级逆流反萃，铜的反萃率为94.68%,反萃后铜质量浓度达到7.04 g/L,相较于浸出液中铜离子质量浓度提高了约3.72倍，实现了铜离子的富集，得到的硫酸铜溶液可用于电积铜生产。     

萃取法分离提取深层富钾卤水中的硼

采用溶剂萃取法分离提取江陵凹陷深层富钾卤水中的硼,研究了萃取剂种类、体积分数、萃取时间、萃取相比、反萃剂体积分数、反萃相比和反萃时间等因素对萃取和反萃取的影响。结果表明:2-乙基-1,3-己二醇是较合适的硼萃取剂;在以体积分数为15%的2-乙基-1,3-己二醇、35%异辛醇的混合醇为萃取剂,50%磺化煤油为稀释剂,萃取相比为1∶1,萃取时间为15min的条件下,硼单级萃取率达95%以上,实现了硼与卤水中钾、钠、钙和镁的有效分离;在反萃剂NaOH浓度为0.625mol/L,反萃相比为2.5∶1,反萃时间为15min的条件下,硼单级反萃率达94%;最优的反萃取条件在确保反萃率较高的同时,提高了反萃液中B2O3质量浓度,由原料的8.33g/L富集到反萃液的19.10g/L,有助于后续硼酸蒸发浓缩阶段能耗的降低。     

3D打印多通道微反应器用于萃取分离In3+和Fe3+

将微流体萃取技术与新兴的3D打印技术相结合，设计并制造了一种结构较为复杂的多通道微流体萃取反应器，通过在微反应器内增加混合反应通道的数目来放大其处理量，以期使3D打印多通道微反应器在能够继承微流体单级萃取效率高优点的同时，也能够极大地扩大其处理量。反应器的结构特征主要包括两相入口、液滴筛板、混合萃取通道、混合液汇集腔及混合液出口等。将此种反应器用于不同初始条件下从硫酸溶液中萃取和分离In³⁺和Fe³⁺的实验，结果表明：随着两相接触时间的增长，萃取剂P204对于金属离子的萃取率呈现出先减小，再增大的趋势；溶液中In³⁺和Fe³⁺的分离系数在pH为0.7、接触时间为90s、萃取剂体积分数为30%时，达到最高值381.9。对初始溶液pH、萃取剂在油相中的体积分数、两相的接触时间等单因素对In³⁺和Fe³⁺的萃取率和分离系数的影响作了详细调查。     

支撑液膜法制备头孢氨苄的研究

建立一个三相体系,实现对头孢氨苄的合成与分离。对支撑液膜及其传质机理进行了简要介绍。实验中,以Isopar L为萃取剂,甲基三辛基氯化铵(Aliquat 336)为载体,1-癸醇为载体助溶剂。萃取部分考察了进料相头孢氨苄的浓度、进料液pH、进料相和有机相体积比对萃取率的影响。反萃部分考察了反萃液pH对反萃率的影响,对比了几种反萃液的反萃效果,最终选择pH=9.0的D-苯甘氨酸甲酯盐酸盐(PGME)溶液作为反萃液。选择进料头孢氨苄浓度为20 mmol/L,进料液pH为9.0,进料相与有机相体积比为1∶1进行实验,得到头孢氨苄的最终收率为58.43%。     

LIX84-I从氨性溶液中提纯铜的研究

研究了LIX84-I对氨性溶液中铜的萃取和反萃取过程,考察了相比、萃取剂体积浓度、振荡时间及萃取次数对萃取过程的影响,并优化萃取试验条件:萃取相比为1:3;萃取剂体积分数为32%;振荡时间为30 s;经过一次萃取,铜萃取率可达98.72%。用硫酸反萃,主要研究了反萃硫酸浓度、振荡时间、相比、反萃次数对反萃的影响,并优化反萃试验条件:反萃取硫酸浓度140g/L;振荡时间为30 s,相比为1:1,经过两次反萃后有机相中铜浓度达到99%以上。     

混合醇萃取剂从浓缩盐湖卤水中萃取提硼的实验研究

以2-乙基-1,3-己二醇和异丁醇按照一定体积比组成混合萃取剂、航空煤油为稀释剂,萃取某硫酸盐型盐湖浓缩卤水中的硼。对萃取剂浓度、浓缩卤水pH、萃取相比、萃取温度、萃取时间、饱和萃取容量和反萃剂浓度、反萃相比等进行了实验研究。结果表明:2-乙基-1,3-己二醇、异丁醇和航空煤油体积比为1∶2∶3,卤水pH为3,萃取相比为1∶1,温度为20℃,萃取时间为5 min;将得到的富硼有机相用0.25 mol/L氢氧化钠溶液进行反萃,反萃相比为1∶2、温度为30℃、反萃取时间为15 min。经三级萃取及反萃,卤水中硼质量浓度降为0.8 mg/L,硼萃取率为99.99%,反萃率为99.78%,硼回收率为99.77%,萃取效果好。     

醛肟萃取剂萃取分离废锂离子电池中的铜

用N902和AD100两种萃取剂分别分离萃取废锂离子电池浸出液中的铜,考察了初始p H值、萃取剂浓度、相比(O/A)和萃取时间对铜回收率的影响.结果表明,室温下,在初始p H 3.0、萃取剂浓度20%(?)及O/A=1:1、萃取时间240 s的条件下,N902对铜的一级萃取率达98.3%;在初始p H 3.0、萃取剂浓度25%(?)及O/A=1:1、萃取时间180 s的条件下,AD100对铜的一级萃取率达97.1%.经硫酸溶液反萃后,2种萃取剂一次反萃率均高于95%,均能高效萃取分离铜,效果接近.     

Solvent Extraction of Au(I) from Auro‐Cyanide Solution with Cetyltrimethylammonium Bromide/Tri‐n‐Butyl Phosphate System using Column‐Shaped Extraction Equipment

Abstract

Solvent extraction of Au(I) from alkaline cyanide solution containing several milligram per liter of gold was investigated with column‐shaped extraction equipment using tri‐n‐butylphosphate (TBP) as extractant with addition of quaternary ammonium salt, cetyltrimethylammonium bromide (CTAB), directly into the aurous aqueous phase in advance. The influences of the volume of TBP and the NaCl concentration in the aurous aqueous phase on Au(I) extraction were investigated. The experimental results for treating 50 L of synthetic auro‐cyanide solution containing 10 mg/L Au(I) and for treating real auro‐cyanide leaching liquor by CTAB/TBP system were reported. The results obtained establish that the column‐shaped extraction equipment was suitable for extracting Au(I) from low content auro‐cyanide solution at high aqueous/organic phase ratio, and that more than 97% of gold(I) could be extracted while the Au(I) concentration in the raffinate was less than 0.3 mg/L. In addition, the stripping of Au(I) from the loaded organic phase and the recycle of the organic phase were also discussed.     

预分散溶剂萃取分离苯酚溶液的研究

Predispersed solvent extraction (PDSE) is a new method for separating solutes from aqueous solution by solvent extraction and one which has shown promise for extraction from extremely dilute solution very efficient and very quick. The use of colloidal liquid aphrons in predispersed solvent extraction may ameliorate the problems such as emulsion formation, reduction of interracial mass transfer and low interfacial mass transfer areas in solvent extraction process. In present paper, colloidal liquid aphrons are successfully generated using kerosene as a solvent,tributyl phosphate(TBP) as an extractant, sodium dodecyl benzene sulphate(SDBS) as surfactant in aqueous phase and Tween-80 in oil phase. Extraction of phenol from dilute solution was studied by using colloidal liquid aphrons and colloidal gas aphrons in a semi-batch extraction column. It has been found that the PDSE process is more suitable for extraction of dilute solutions. It has also been discovered that the PDSE process has a great advantage over traditional single-stage extraction process.     

Studies Related to the Processing of U–Zr and U–Pu–Zr Metallic Fuels Using Tri-iso-amyl Phosphate (TiAP) as Extractant

Metallic fuel is reprocessed by a compact nonaqueous pyrochemical process. The present study explores the possible uses of an aqueous reprocessing-based method as an alternative to the pyro-processing of metallic fuels. Solvent extraction studies in the batch mode were carried out for both U–Zr- and U–Pu–Zr-based metal alloy systems. Earlier studies carried out in our laboratory have established that Tri-iso-amyl Phosphate (TiAP) is a promising extractant for the reprocessing of spent fuels. In the present study, the distribution data has been generated for the extraction of uranium and zirconium as a function of equilibrium aqueous phase metal ion and nitric acid concentration with TiAP and Tri-n-butyl Phosphate (TBP)-based solvents. These studies indicate the formation of a third phase with zirconium in the presence of uranium with TBP under certain experimental conditions whereas it was not encountered with the TiAP system. Flow sheet for the co-extraction and co-stripping of heavy metal ions by 1.1M TiAP and 1.1M TBP in n-dodecane from U–Zr as well as U–Pu–Zr feed solutions in stage-wise mode has been evaluated. Percentage extraction and stripping of metal ions were calculated stage-wise and the results are discussed.     

Nitric Acid Extraction into the TODGA/TBP Solvent

The tridentate diglycolamide ligand N,N,N′,N′-tetraoctyl diglycolamide (TODGA) shows many interesting properties and is a very good extractant for the minor actinides (MAs) and lanthanides but, due to its low loading capacity, requires a phase modifier when used in a solvent extraction process. Consequently, applications of TODGA in conjunction with tri-butyl phosphate (TBP) in novel DIAMEX and SANEX processes for recovering MAs have been reported. However, TODGA and TBP also extract nitric acid and this has a significant influence on process performance. Here new distribution data for the extraction of nitric acid into solvent phases containing TODGA and TBP have been collected and modeled using an equilibrium-based approach accounting for nitric acid activities in the aqueous phase. Models for the extraction of nitric acid using the individual extractants were obtained using a variety of complexes and these were then combined to give the extraction of the mixed TODGA and TBP solvent. Using this approach, the nitric acid extraction of the mixed TODGA/TBP system can be reliably reproduced indicating that no significant synergistic or antagonistic complexes are formed in solution.     

Co-extraction and selective stripping of copper (II) and molybdenum (VI) using LIX 622

LIX 622 diluted with kerosene was used to co-extract copper (II) and molybdenum (VI) from acidic sulphate solutions. The influence of equilibrium pH and extractant concentration on metal co-extraction has been studied. The extraction of both metals is sensitive to equilibrium pH; however, molybdenum is extracted preferably to copper at acidic pH values. For aqueous phases containing both metals, conditions were established for the co-extraction, selective stripping of copper and molybdenum and NH₃ removal from the stripped organic solution.     

Role of Acetohydroxamic Acid in Selective Extraction of Technetium and Uranium Employing N,N-Dihexyloctanamide as Extractant

Straight chain N,N-dihexyloctanamide (DHOA) has been identified as a promising alternate extractant to tributyl phosphate (TBP) for the reprocessing of uranium based spent fuels. The present work compares extraction behavior of technetium using DHOA and TBP solutions in n-dodecane, under varying experimental conditions such as acidity (0.5–6 M HNO₃); extractant concentration (1.1 and 1.5 M), and uranium loading (50 g/L, relevant for Pu rich spent fuel feed solutions). The effect of acetohydroxamic acid concentration on U, Pu, Np, and Tc extraction behavior has also been investigated. Pu(IV)-AHA interaction and its influence on extraction using TBP and DHOA extractants has been studied spectrophotometrically. The experimental data suggest that 1.1 M DHOA is better than 1.1 M TBP with respect to co-extraction of Tc and U, and U decontamination with respect to Np/Pu.     

EXTRACTION OF LITHIUM FROM BRINE CONTAINICG HIGH CONCENTRATION OF MAGNESIUM BY TRI-NBUTYL PHOSPHATE DISSOLVED IN KEROSENE

Tri-n-butyl phosphate (TBP)dissolved in kerosene was chosen as extractant for lithium from a model brine having high magnesium-to-lithium ratio and ferric chloride was added to the system.The influences of contact time,concentration of the extractant,concentrations of some salts (Mg2+,Na+,K+)in the solution,acidity of hydrochloric acid and extraction temperature on the extraction of lithium with TBP-kerosene system were studied.The suitable extraction conditions were found to be :contact time not any less than 20 min;at 20-25℃;[Fe3+]/[Li+]about 1.5-2.0;TBP concentration 50%-70%;[MgCl2]exceeding 3 mol·L-1;pH about 2;while most sodium and potassium salts in the aqueous phase should be removed before the extraction.     

Synergistic extraction and separation of Fe(III) and Zn(II) using TBP and D2EHPA

Waste chloride pickle liquors from hot-dip galvanizing plants, steel plants and flue dust contain reasonable amounts of heavy metals such as Zn, Cr, Ni, etc. Iron is invariably associated with most of these materials and comes into solution during leaching. Thus, the synergistic extraction of zinc(II) and iron(III) from leach solutions in tri-n-butyl phosphate (TBP)–di(2-ethylhexyl) phosphoric acid (D2EHPA) system diluted in kerosene was investigated. The Zn and Fe concentrations in the leach liquor used in the present study were 2 g/L. Experiments were carried out in the pH range of 0.5–4.0, temperature of 25°C, using sole D2EHPA, sole TBP and D2EHPA–TBP mixtures at different ratios. Results showed that the co-extraction of zinc(II) and iron(III) increased with increasing equilibrium pH using D2EHPA. It is demonstrated that the mixtures of TBP and D2EHPA are more efficient and selective than D2EHPA alone. At low pH values, the separation factor is low when pure D2EHPA is used as an extractant; however, using TBP as a synergist, the separation factor increases and results in a better separation of zinc from iron. Increasing TBP to D2EHPA ratios in the organic phase caused a slight shift to the right in the extraction isotherm of iron and a marked shift to the right in the extraction isotherm of zinc, and the maximum separation factor of 13.3 × 10³ was achieved at a TBP to D2EHPA volume ratio of 4:1 (0.58 M TBP: 0.12 M D2EHPA). Furthermore, the effect of equilibrium pH, organic to aqueous phase ratio and Cl^? concentration on the selective extraction was investigated. Using two extraction stages at the O/A ratio of 2:1 and pH_e (equilibrium pH) of 3 and 1 for zinc and iron, respectively, 99% of zinc(II) and 96.25% of iron(III) were extracted.     

Solvent and Emulsion Extractions of Gallic Acid by Tributylphosphate: Mechanisms and Parametric Study

The aim of this paper was to study solvent extraction or liquid-liquid extraction (LLE) and extraction by emulsion (ELM) of gallic acid, a biomolecule present in many plants. A mechanism involving three tributylphosphate molecules for one molecule of undissociated gallic acid with co-extraction of water was found in LLE. ELM process is as fast as LLE and more efficient; in addition, it is more environmentally-friendly because lower extractant concentrations and smaller organic phase volumes were needed.     

TBP, MIBK/FeCl3与Li形成萃合物组成的研究（英文）

To study the characteristic of liquid-liquid extraction equilibrium of lithium from brine sources,the complexes formed from tributyl phosphate(TBP) and methyl isobutyl ketone(MIBK) with lithium were investi-gated using FeCl3 as coextracting agent.Liquid-liquid extraction reaction mechanisms were proposed and the stoichiometry of tetrachloroferrate(III) complex with lithium was obtained by regressing the experimental data.It is found that the stoichiometry of tetrachloroferrate(III) to lithium in the complex is 1︰1 with either TBP or MIBK as extractant in kerosene.The stoichiometry of the complex of TBP with Li was 1︰1 and that of MIBK with Li was 2︰1.The formed complexes of TBP and MIBK with lithium are determined to be LiFeCl4?TBP and LiFeCl4?2MIBK,respectively,according to the rule of neutralization.