乳状液膜法分离水中镉

本文报道了用乳状液膜法分离镉的研究。在此分离体系中,以煤油作为膜溶剂,span80为表面活性剂,磷酸三丁酯(TBP)为载体,液体石蜡为膜增强剂。详细讨论了制乳时间、混合时间、搅拌速度,span80、TBP以及液体石蜡的浓度,乳水比和油内比,内相氨水和外相HCl溶液的浓度对分离的影响,确立了最佳分离条件。     

谷氨酸在Span80-AOT-APS体系中的迁移行为

报道了谷氨酸在乳状液膜体系中的迁移行为,采用失水山梨醇单油酸酯(span80)-乙基己基琥珀酸酯磺酸钠(AOT)为表面活性剂,对氨基苯磺酸(APS)为载体,煤油为膜溶剂,氯化钾为内相试剂.讨论了制乳时间和乳液与外相混合时间、表面活性剂和流动载体浓度、内相试剂浓度、水乳比和油内比对分离效果的影响.确定了最佳分离条件为制乳...     

乳状液膜体系分离锌(Ⅱ)

研究了span80(失水山梨醇单油酸脂)-SDS(十二烷基磺酸钠)与span80-AOT(2-乙基己基琥珀酸酯磺酸钠)两种乳状液膜体系对锌(Ⅱ)分离效果的比较。分别讨论了液膜体系中表面活性剂和内相试剂浓度、乳水比和油内比对锌(Ⅱ)去除率的影响。试验了锌(Ⅱ)与共存组分的分离。     

乳状液膜法分离水中汞的研究

报道了用乳状液膜法分离汞的研究。确定了最佳分离条件；流动载体TBP（磷酸三丁酯）和表面活性剂Span80的浓度均9％，内相溶液NaOH和外相溶液HCl的浓度分别为0.4mol/L和0.02mol/L，制乳时间和混合时间分别为10min和5min，乳水比和油内比分别为0．5和0．8。     

乳状液膜体系分离提取铜离子

以Span80-对氨基苯磺酸(APS)-NH3液膜体系分离提取Cu2+。最佳分离条件为:制乳搅拌速度3500r/min,制乳时间及乳水混合时间分别为10min和20min,乳水比和油内比分别为0.38和0.44,APS、Span80和液体石蜡浓度分别为11%、4.4%和2.2%,内相NH3和外相HCl浓度分别为4.0mol/L和0.5mol/L。用该体系分离提取了模拟样中的Cu2+。     

铜在乳状液膜体系中的迁移行为

近年来膜分离技术在环境治理方面得到广泛应用。本文研究了铜在span80-TBP（磷酸三丁酯）-煤油-NH3液膜分离体系中的迁移行为。用TBP作为载体,在溶液中迁移时,在外相与膜相界面上形成中性络合物后穿过膜相,在膜相与内相界面上络合物再与NH3反应,生成铜氨络离子,释放出来的TBP又返回膜相。     

Span80-TBP-NaOH体系破乳方法及膜内反应研究

采用Span80-TBP-NaOH体系乳状液膜法提取红土矿浸出液中的镍,对提取分离后的乳液进行破乳实验,经过加热-离心联合破乳法,破乳率可达90%.通过比较提取镍前后,乳液的红外光谱图,证明了膜内反应的发生;通过比较原始油相和破乳后油相的红外光谱图,证明了破乳后油相的重复利用性.     

鼠李糖脂应用于微乳毛细管电动色谱快速测定化妆品中激素类物质

采用生物表面活性剂鼠李糖脂建立了无需助表面活性剂的微乳体系,并应用于微乳毛细管电动色谱快速分析化妆品中皮质类激素泼尼松、泼尼松龙和氢化可的松。考察了pH值、鼠李糖脂浓度、离子强度、油相种类和浓度、分离温度、分离电压及进样电压和时间的影响,得出微乳体系最佳组成为0.1%(w/w)鼠李糖脂+0.8%(w/w)正庚烷+99.1%(w/w)硼砂缓冲液(80 mmol/L,pH 9.2)。分离温度20℃,分离电压20kV,电动进样10 kV×3 s,泼尼松、氢化可的松和泼尼松龙在9.4 min内可基线分离。重复进样7次,迁移时间和峰面积的RSD分别小于0.2%和5.0%。3种分析物线性范围均为5～100 mg/L;检出限分别为1.0,1.1和1.3 mg/L(S/N=3)。仅需简单萃取即可用于化妆品样品测定,回收率为81.6%～108%;RSD均小于4.8%。     

螺旋藻生物富集镍的影响因素研究

研究了螺旋藻对金属镍的富集效果,通过实验考察了吸附时间、镍藻比、金属离子浓度、光照时间和温度对螺旋藻富集效率的影响。研究结果表明,吸附时间在80min,镍藻体积比为7%,pH值在10左右,温度35℃,光照为3000lux的条件下,螺旋藻对镍的吸附效果最好。同样条件下,死藻比活藻对镍的生物富集量高。     

油田水中烷基酚的胶束电动色谱分离

采用硼酸盐-十二烷基硫酸钠胶束电动色谱对油田水中存在的烷基酚进行了分离分析。考察了影响分离的各种不同因素：缓冲液浓度、体系的pH值、胶束溶液浓度、分离电流、管住温度及有机添加剂β-环糊精等。在恒流100μA下,38min内可分离20种烷基酚。采用Cl－TBP萃淋树脂对油田水样进行了浓缩富集预处理。     

乳状液膜法分离水中的铬

乳状液膜法由于其独特的物理化学性质,已广泛用于金属离子的萃取分离[1～3]。本文以span80-煤油-NaOH液膜体系分离水中铬。不加流动载体,利用内、外相中被分离物的浓度梯度实现物质迁移。当Cr2O2-7进入内相时,与内相的NaOH发生反应,在内相高浓度的NaOH存在下,可保持Cr2O2-7在液膜两侧有最大的浓度梯度,促使Cr2O2-7的迁移,实现Cr2O2-7与外相溶液的分离。1　实验部分1 1　仪器与试剂D40-1型电动搅拌器(杭州仪表电机厂),78-1型磁力加热搅拌器(江苏金坛新一佳仪器厂),721型分光光度计(上海第三分析仪器厂)。铬标准溶液(100ml/L):准…     

Extraction of cadmium from aqueous solutions by emulsion liquid membrane (ELM) using three different carriers dissolved in a 70:30 ratio of sunflower oil to kerosene

This study explores the use of novel green emulation liquid membranes (GELMs) for the simultaneous extraction and stripping of Cd (II) from aqueous solutions. A solute is transported through the membrane due to the presence of the carrier and then concentrated in the internal phase. Soybean, sunflower, corn, and canola oils were used to form green substitutes to petroleum-based organic diluents for use as GELMs. Bis-(2-ethylhexyl) phosphate (D2EHPA), tri-butyl- phosphate (TBP), and trioctylamine (TOA) were the extractants, span 80 was the emulsifier, and HCl or H₂SO₄ was used as the stripping agent. The best conditions for maximum extraction efficiency (98.68%), stripping efficiency (97.14%), and lowest membrane breakage (0.9%) were achieved using a mixture of sunflower oil and kerosene in the ratio of 70:30. The other optimum values of the variables were: 2% (v/v) Span 80, 10 min emulsification time, 12700 rpm emulsification speed, 400 rpm of agitation speed, 5% (v/v) D2EHPA, an external phase pH was 3.5, an internal phase of 0.25 M HCl, and 5:1 of the treat ratio (external phase to emulsion) at 10 min contact time. The synthesized membrane was reused eight times, with approximately the same efficiency and no significant breakage during the first seven cycles.     

Extraction of Priority Pollutant 4-Nitrophenol from Water by Emulsion Liquid Membrane: Emulsion Stability,Effect of Operational Conditions and Membrane Reuse

This work aims to the extraction of the priority pollutant 4-nitrophenol (4-NP) from water by emulsion liquid membrane (ELM). Liquid membrane consists of a diluent (hexane) and a surfactant (Span 80). Sodium carbonate solution was used as internal aqueous phase. Effects of important experimental conditions governing the stability of the W/O emulsion were investigated. Influence of operating parameters that affects the permeation of 4-NP such as surfactant concentration, emulsification time, sulfuric acid concentration in external phase, acid type in external phase, internal phase concentration, type of internal phase, stirring speed, volume ratio of internal phase to membrane phase, treatment ratio, 4-NP initial concentration, and diluent type was examined. This study also evaluated the effect of Na₂CO₃ concentration in the internal aqueous phase on the stripping of 4-NP. Additionally, the reuse of the recovered membrane was studied. Under most favorable conditions, practically all the 4-NP and aniline (AN) molecules present in the feed phase were extracted. The recovery of the membrane phase was total and the extraction of 4-NP was not decreased. The ELM treatment process represents a very interesting advanced separation process for the removal of 4-NP and AN from aqueous solutions.     

Facilitated Transport of Penicillin G by Bulk Liquid Membrane with TBP as Carrier

The facilitated transport of penicillin G from aqueous solutions to the stripping phase through bulk liquid membrane (BLM) containing TBP in 3% iso-octanol and n-butyl acetate was studied. Na₂CO₃ solution was used as the stripping phase. Experiments were performed as a function of stirring rate, TBP concentration and type of diluent in the liquid membrane phase, pH, and initial penicillin G concentration in the feed phase, Na₂CO₃ concentration in the stripping phase, etc. The results showed that the BLM process could carry out the simultaneous separation and concentration of penicillin G from dilute aqueous solutions, and arise “up-hill” effect due to the characteristic of non-equilibrium mass transfer. The diffusion of penicillin G complex in the liquid membrane phase played an important role in BLM process. The mass transfer mechanism of BLM for this system was also discussed.