Tb(Ⅲ)Transport in Dispersion Supported Liquid Membrane System with D2EHPA as Carrier in Kerosene

The transport of Tb(Ⅲ)in dispersion supported liquid membrane(DSLM)with polyvinylidene fluoride membrane(PVDF)as the support and dispersion solution including HCI solution as the stripping solution and di(2-ethylhexyl)phosphoric acid(D2EHPA)dissolved in kerosene as the membrane solution,has been studied.The effects of pH value,initial concentration of Tb(Ⅲ)and different ionic strength in the feed phase,volume ratio of membrane solution to stripping solution,concentration of HCl solution,concentration of carrier,different stripping agents in the dispersion phase on the transport of Tb(Ⅲ)have also been investigated,respectively.As a result,the optimum transport conditions of Tb(Ⅲ)were obtained,i.e.,the concentration of HCI solution was 4.0 mol/L,the concentration of D2EHPA was 0.16 mol/L,the volume ratio of membrane solution to stripping solution was 30:30 in the dispersion phase and pH value was 4.5 in the feed phase.Ionic strength had no obvious effect on the transport of Tb(Ⅲ).Under the optimum conditions,the transport percentage of Tb(Ⅲ)was up to 96.1% in a transport time of35 min when the initial concentration of Tb(Ⅲ)was 1.0×10-4 mol/L.The diffusion coefficient of Tb(Ⅲ)in the membrane and the thickness of diffusion layer between feed phase and membrane phase were obtained and the values were 1.82×10-8 m2/s and 5.61 μm,respectively.The calculated results were in good agreement with the literature data.     

Study on transport of Dy（III） by dispersion supported liquid membrane

The transport of Dy(III) through a dispersion supported liquid membrane (DSLM) consisting of polyvinylidene fluoride membrane (PVDF) as the liquid membrane support and dispersion solution including HCl solution as the stripping solution and 2-ethyl hexyl phosphonic acid-mono-2-ethyl hexyl ester (PC-88A) dissolved in kerosene as the membrane solution, was studied. The effects of pH value, initial concentration of Dy(III) and different ionic strength in the feed phase, volume ratio of membrane solution and stripping solution, concentration of HCl solution, concentration of carrier, different stripping agents in the dispersion phase on transport of Dy(III) were also investigated, respectively. As a result, when the concentration of HCl solution was 4.0 mol/L, concentration of PC-88A was 0.10 mol/L, and volume ratio of membrane solution and stripping solution was 40:20 in the dispersion phase, and pH value was 5.0 in the feed phase, the transport effect of Dy(III) was the best. Ionic strength had no obvious effect on transport of Dy(III). Under the optimum condition studied, when initial concentration of Dy(III) was 0.8 × 10^?4 mol/L, the transport rate of Dy(III) was up to 96.2% during the transport time of 95 min. The kinetic equation was developed in terms of the law of mass diffusion and the theory of interface chemistry. The diffusion coefficient of Dy(III) in the membrane and the thickness of diffusion layer between feed phase and membrane phase were obtained and the values were 1.99 × 10^?7 m²/s and 15.97 μm, respectively. The results were in good agreement with experimental results.     

Separation of Eu（III） with supported dispersion liquid membrane system containing D2EHPA as carrier and HNO3 solution as stripping solution

The Eu(III) separation in supported dispersion liquid membrane (SDLM),with polyvinylidene fluoride membrane (PVDF) as the support and dispersion solution containing HNO3 solution as the stripping solution and Di(2-ethylhexyl) phosphoric acid (D2EHPA) dis-solved in kerosene as the membrane solution,was studied.The effects of pH value,initial concentration of Eu(III) and different ionic strengths in the feed phase,volume ratio of membrane solution and stripping solution,concentration of HNO3 solution,concentration of carrier,different stripping agents in the dispersion phase on the separation of Eu(III) were also investigated,respectively.As a result,the optimum separation conditions of Eu(III) were obtained as the concentration of HNO3 solution was 4.00 mol/L,concentration of D2EHPA was 0.160 mol/L,and volume ratio of membrane solution to stripping solution was 30:30 in the dispersion phase,and pH value was 5.00 in the feed phase.Ionic strength had no obvious effect on the separation of Eu(III).Under the optimum conditions studied,when initial concentration of Eu(III) was 1.00×10–4 mol/L,the separation rate of Eu(III) was up to 94.2% during the separation period of 35 min.The kinetic equation was developed in terms of the law of mass diffusion and the theory of interface chemistry.The results were in good agreement with the literature data.     

A preliminary study of polymer inclusion membrane for lutetium(III) separation and membrane regeneration

This paper reports on the selective transport of Lu(III) from La(III) and Sm(III) through a polymer inclusion membrane (PIM) composed of 40 wt% di(2-ethylhexyl) phosphinic acid (P227) and 60 wt% poly(vinylidene fluoride) (PVDF). Basically, the changes in surface morphology, thickness and water contact angle of this PVDF-based PIM containing P227 (P227@PVDF PIM) with different polymer concentrations were investigated. By solvent extraction experiments, it is found that Lu(III) can be selectively extracted from La(III) and Sm(III) at pH 1.5 in hydrochloric acid solution. According to this result, P227@PVDF PIM was used to selectively transport Lu(III) from hydrochloric acid feed solution containing similar concentration of La(III) and Sm(III). The recovery factor of Lu(III) is 91% after 36 h, and about 5% of Sm(III) was also transported through the PIM. The concentration of La(III) in the feed solution and the stripping solution does not change. Furthermore, to overcome the ubiquitous decline of transport efficiency caused by the loss of carrier or the damage of membrane structure after long-term use of PIMs, a process for regenerating PIMs was first proposed and implemented. By comparison of the regenerated PIM with the normal PIM, there is almost no difference in the SEM image, ATR-FTIR spectrum and Lu(III) transport efficiency. It is expected that P227@PVDF PIMs have the potential to be applied to the grouped separation of rare earth elements (REEs), and this study also can be as an inspiration for the further study on the PIMs regeneration process.     

Carrier-mediated transport of uranium from phosphoric acid medium across TOPO/n-dodecane-supported liquid membrane

Present studies deals with the application of supported liquid membrane (SLM) technique for the separation of uranium (VI) from phosphoric acid medium. Tri-n-octyl phosphine oxide (TOPO)/n-dodecane is used as a carrier and ammonium carbonate as a receiving phase for the separation of uranium (VI) from the phosphoric acid medium. Throughout the study PTFE membranes are used as a support. The studies involve the investigation of process controlling parameters like feed acidity of phosphoric acid, carrier concentration and stripping agents. The effect of nitric acid and sodium nitrate in feed is also studied. It is found that there is negligible transport of uranium (VI) from pure phosphoric acid medium but it increases to very significant amount if 2 M nitric acid is added to feed phase. More than 90% uranium (VI) is recovered in 360 min using 0.5 M TOPO/n-dodecane as carrier and 1.89 M ammonium carbonate as stripping phase from the mixture of 0.001 M H₃PO₄ and 2 M of HNO₃ as a feed. The flux and permeability coefficient are found to be 9.21 × 10^− 6 mol/m² s and 18.26 × 10^− 5 m/s, respectively. Lower concentration of phosphoric acid with 2 M HNO₃ and higher concentration of carrier is found to be the most suitable condition for maximum transport of uranium (VI) from its low-level sources like commercial phosphoric acid.     

Study on a novel flat renewal supported liquid membrane with D2EHPA and hydrogen nitrate for neodymium extraction

The Nd(III) extraction in flat renewal supported liquid membrane(FRSLM),with polyvinylidene fluoride membrane and renewal solution including HNO3 solution as the stripping solution and di(2-ethylhexyl) phosphoric acid(D2EHPA) dissolved in kerosene as the membrane solution,was investigated.The effects of pH in the feed phase,volume ratio of membrane solution to stripping solution,concentra-tion of HNO3 solution and concentration of carrier in the renewal phase on extraction of Nd(III) were also studied,respectively.As a result,the optimum extraction conditions of Nd(III) were obtained when concentration of HNO3 solution was 4.00 mol/L,concentration of D2EHPA was 0.100 mol/L,and volume ratio of membrane solution to stripping solution was 1.00 in the renewal phase,and pH was 4.60 in the feed phase.When initial concentration of Nd(III) was 2.00×10-4 mol/L,the extraction percentage of Nd(III) was up to 92.9% in 75 min.     

以三正辛胺为载体的微乳液萃取分离钨(Ⅵ)的研究

研究了以三正辛胺(TOA)为载体,由OP-10、异戊醇、环己烷和NaOH溶液组成的微乳液分离钨(的行为及机理。当膜相中三正辛胺浓度为0.020 mol/L、内相NaOH的浓度为0.050 mol/L、外相HCl的浓度为0.010 mol/L时,可使钨(与Fe(,Co(,Ni(,Zn(,Mn(,Cu(,Pb(完全分离,萃取率达98%以上。     

Selective separation of nickel from cobalt in ammoniacal solutions by emulsion type liquid membranes using 8-hydroxyquinoline (8-HQ) as mobile carrier

The selective separation and concentration of nickel from ammoniacal solutions containing nickel and cobalt by an emulsion liquid membrane (ELM) technique using 8-hydroxyquinoline (8-HQ) as carrier has been examined. The emulsion liquid membrane consists of a diluent (kerosene), a surfactant (ECA 4360J), a carrier (8-HQ), and a stripping solution (0.025 M EDTA solution, buffered at pH 4.0). Cobalt (II) in the 6 M ammonia feed solution was oxidised to cobalt (III) by adding H₂O₂ and the pH adjusted to 10 with hydrochloric acid (HCl). The important variables were found to be membrane composition, ammonia concentration, diluent type, surfactant concentration, extractant concentration, EDTA concentration in the stripping solution, pH of the feed and the stripping solutions, phase ratio, and treatment ratio. It was possible to selectively extract 96.5 to 99.0% of nickel from a mixture of nickel and cobalt.     

Ethyl-bis-triazinylpyridine (Et-BTP) for the separation of americium(III) from trivalent lanthanides using solvent extraction and supported liquid membrane methods

The present paper deals with the solvent extraction and supported liquid membrane studies on Ln(III)/An(III) separation using ethyl-bis-triazinylpyridine (Et-BTP) as the extractant. The solvent extraction studies involved evaluation of a) diluents, b) phase modifiers, c) stripping agents and d) role of feed acidity. Though reasonably high separation factor values were obtained when Et-BTP was used along with α-bromo carboxylic acids, the mixtures could not be used for liquid membrane studies due to unsatisfactory stripping. On the other hand, a combination of Et-BTP with chlorinated cobalt dicarbollide (CCD) in nitrobenzene resulted in significant Am(III) mass transfer when used in the solvent extraction as well as SLM studies. Improved transport, membrane stability, and decontamination from lanthanides were observed when the organic phase diluent composition was 60% nitrobenzene + 40% n-dodecane. Using 0.02 M Et-BTP along with 0.005 M CCD in 60% nitrobenzene + 40% n-dodecane, the SLM studies on a mixture of ²⁴¹Am, ¹⁵²Eu and ¹⁴⁷Nd in a feed containing 0.1 M HNO₃, indicated quantitative Am³⁺ transport in 3.5 h with co-transport of about 8% Nd³⁺ and 22% Eu³⁺.     

Simulations of Full-Scale Reverse Osmosis Membrane Process

Performance of a two-stage full-scale reverse osmosis (RO) process for a desalination plant in Florida was simulated with a mathematical model based on the principles of membrane transport and mass conservation. In this model, water flux at any point along the filtration channel is calculated locally according to the basic transport theory of RO membranes. The changes in cross-flow velocity and salt concentration along the filtration channel were determined using mass balance principles of water and salt. Simulations of the plant performance were compared with the in-plant observation data over a period of more than 300 days. The results showed that the model could adequately describe the performance of the full-scale RO process based on a few module and operating parameters. The study also revealed that salt rejection of a RO membrane changed with feed salt concentration. The osmotic pressure coefficient that fits best with performance of this plant was substantially lower than the value determined with the “rule of thumb” (i.e., osmotic pressure in psi ≈ 0.01×total dissolved solids in mg/L) and had to be determined specifically for the particular feed water being processed.     

Extraction and separation of yttrium from other rare earths in chloride medium by phosphorylcarboxylic acids

Two phosphorylcarboxylic acids, 3-((bis(2-ethylhexyloxy))phosphoryl)propanoic acid (PPA) and 3-((bis(2-ethylhexyloxy))phosphoryl)-3-phenylpropanoic acid (PPPA), were synthesized for separating yttrium from other rare earths in the chloride feed of ion-adsorption type rare earth concentrate. The effect of the factors such as pH_1/2, temperature, saponification degree and phase modifiers was investigated. The separation efficiencies of PPA and PPPA are obviously better than the typical extractants such as sec-octylphenoxy acetic acid (CA-12) and naphthenic acid (NA). The extraction process of rare earths by PPA and PPPA is a cation exchanging reaction, which is similar to those of CA-12 and NA. The loaded rare earths in both PPA and PPPA systems can be effectively back-extracted by 0.5 mol/L HCl or higher concentration. A cascade extraction process for separating yttrium from other rare earths was developed using PPPA as the extractant. The yttrium product with the purity of 97.20 wt% was obtained by 35 stages of extraction and 12 stages of scrubbing.     

Separation of nickel from cobalt in sulphate medium by ion exchange

A process is described for the selective removal of nickel from acidic cobalt sulphate solution with Dow ion exchange resin XFS 4195. The results of laboratory fixed-bed (25 mm diameter by 1.5 m deep) studies are presented, showing that raffinate Co/Ni ratios of > 500:1 can be obtained from feeds analyzing 15–30 g/L Co and 0.3–0.7 g/L Ni at pH 2.5, and that the loaded resin can be effectively eluted with 25–50 g/L sulphuric acid. The preferred operating parameters are discussed, and data are presented on the effects of temperature, solution flowrate, and feed nickel concentration during loading, and acid concentration during elution.     

Effect of some operating variables on cobalt(II) transport across a bulk liquid membrane

An experimental study is presented on facilitated transport of cobalt(II) cations through a bulk liquid membrane containing di(2-ethylhexyl)phosphoric acid (D2EHPA). The effects on the kinetics of cobalt(II) transport of stirring rate of the receiving phase and its acidity, mobile carrier (D2EHPA) concentration, emulsifier (Span 80) concentration, initial cobalt concentration, interfacial area, and membrane thickness have been investigated. It has been found that cobalt transport increased with both stirring of the receiving phase and its acidity, while the presence of emulsifier reduced this transport, particularly at the membrane/receiving phase interface. Moreover, the mean cobalt transport rate was practically independent of membrane/feed solution interfacial area (under experimental conditions), while this rate substantially increased with the initial cobalt concentration in aqueous feed solution.     

Modelling of zinc transport through a supported liquid membrane

The transport of zinc (II) from an aqueous solution containing zinc (II), iron (II), calcium (II) and magnesium (II) through supported liquid membrane using di-2-ethylhexyl phosphoric acid dissolved in kerosene as a mobile carrier was studied. The effects of temperature, rate of feed and stripping phase and concentration of stripping phase on the mass transfer coefficients of aqueous boundary layers and membrane were studied. A transport rate model has been derived taking into account diffusion through the feed side aqueous boundary layer, diffusion of carrier–zinc complex through the supported liquid membrane and diffusion through the stripping side aqueous boundary layer as simultaneous controlling factors. The mass transfer coefficient data of the side of the feed phase were correlated in the form of Sh = 0.0047 Re^1.349 Sc^0.3333. This correlation was used to calculate the mass transfer coefficient of the aqueous film at the side of the stripping phase. For some parameters and their levels, the mass transfer coefficients, k_f, k_m and k_s (m s^− 1), were calculated.     

Adsorption behavior of Cd(II) from aqueous solutions onto gel-type weak acid resin

The adsorption and desorption behaviors of Cd(II) on gel-type weak acid resin (GTWAR) have been investigated. The influence of operational conditions such as contact time, initial concentration of Cd(II), initial pH of solution and temperature on the adsorption of Cd(II) has also been examined. The results show that the optimal adsorption condition of GTWAR for Cd(II) is achieved at pH = 5.95 in HAc–NaAc medium. The maximum uptake capacity of Cd(II) is 282 mg/g GTWAR at 298 K. The adsorption of Cd(II) follows the Langmuir isotherm and Freundlich isotherm, and the correlation coefficients have been evaluated. Even kinetics on the adsorption of Cd(II) has been studied. The apparent activation energy E_a and adsorption rate constant k₂₉₈ values are 2.95 kJ/mol and 3.02 × 10^− 5 s^− 1, respectively. The calculation data of thermodynamic parameters which ΔS value of 110 J/(mol K) and ΔH value of 13.1 kJ/mol indicate the endothermic nature of the adsorption process. Whilst, a decrease of Gibb's free energy (ΔG) with increasing temperature indicates the spontaneous nature of the adsorption process. Finally, Cd(II) can be eluted by using 0.5 mol/L HCl solution and the gel-type weak acid resin can be regenerated and reused. The sample was described by IR spectroscopy and scanning electron micrographs (SEM).     

Enrichment process of lanthanum as a nonessential trace element in leaf cells of lettuce (Lactuca sativa L.)

Rare earth elements (REEs) as nonessential trace elements are enriched in living organisms and threaten their health. To early detect and reduce REE enrichment in living organisms, scientists are focused on clarifying the enrichment process of REEs in living organisms and its risks. However, the enrichment process of REEs in edible plant cells has remained unclear. Herein, by using interdisciplinary methods and techniques, the enrichment process of lanthanum (La(III)) in the leaf cells of lettuce (Lactuca sativa L.) was investigated. (1) When La(III) exposure dose is 0.5–5 μmol/L, La(III) is enriched outside the plasma membrane (PM). In this zone, La(III) is bound to vitronectin-like protein (VN) to form La–VN complexes; (2) When La(III) exposure dose is 5–20 μmol/L, besides the zone outside the PM, La(III) is also enriched on the PM and bound to arabinogalactan proteins (AGPs) to form La–AGPs complexes; (3) When La(III) exposure dose is 20–140 μmol/L, besides the zone outside and on the PM, La(III) is enriched inside the PM; (4) When La(III) exposure dose is 60–140 μmol/L, malondialdehyde content (an important indicator of invisible damage) significantly increases. Thus, as La(III) exposure dose increases, La(III) gradually migrates from outside the PM to the PM and inside the PM, enriching in these zones in turn. The enriched La(III) will cause invisible damage to lettuce leaf cells and even enter human bodies along food chains. These results provide references for investigating the enrichment process of REEs in plants and its environmental risks, and finding strategies to early detect and reduce REE enrichment in plants.     

二氧化硫膜电解制备硫磺机理与应用研究

研究了利用316L不锈钢做阴极时,二氧化硫电化学还原制备硫磺过程的机理和影响因素。利用循环伏安法、计时电量法研究了二氧化硫在316L不锈钢电极上的还原机理,提出二氧化硫经历了4个电子4个质子的还原过程。通过离子膜反应器分别考察了电流密度、阴极液酸浓度对二氧化硫电化学还原制备硫磺过程的影响。当二氧化硫浓度5 g/L、硫酸浓度0.5 mol/L、电流密度126.98 A/m^2、电解时间3 h时,二氧化硫转化为硫磺的转化率为73.42%,空时产量0.64 kg/(m^3·h),单位能耗9.64 kWh/kg。     

Mathematical modelling of unsteady-state transport of metal ions through supported liquid membrane

In this study, a mathematical model for unsteady-state transport of metal ions from aqueous solution through supported liquid membrane containing carrier is presented. For a transport process using supported liquid membrane, the three resistances to consider are the membrane resistance and the aqueous boundary layer resistances at the side of feed and stripping phases. The transport of species in the feed, the membrane and the stripping phases is modelled by Fick's second law. Time-dependent boundary conditions for the feed, the membrane and the stripping phases are obtained by means of kinetics of chemical reaction in the feed–membrane and the membrane–stripping interface. Partial differential equations obtained for the feed, the membrane and the stripping phases are analytically solved by using Duhamel's Theorem. Concentration distribution within the aqueous film layers and membrane as a function of position and time was derived from models obtained. The obtained model is checked against experimental data corresponding to the transport of copper ions from aqueous solution through supported liquid membrane by LIX 984.     

盐酸浸出氧化铝赤泥回收镓

研究了拜耳法赤泥盐酸浸出镓的过程。采用正交试验考察浸出温度、时间、液固比和酸度对镓浸出率的影响。结果表明,在最佳浸出条件下:8mol/L盐酸、液固比4.0、109℃浸出5h,镓浸出率达到95.4%。用50%TBP+50%煤油一次萃取,镓萃取率达到98%。用0.5%食盐水反萃,镓反萃率为96.8%。反萃液用0.5mol/L NaOH溶液中和、过滤、烘干后,固体中镓的质量百分数为4.32%,从赤泥中富集了136倍。镓的总回收率达到85%以上。     

特种离子交换树脂从钼酸铵溶液中深度分离钒

研究了采用特种阴离子交换树脂分离钼酸铵溶液中的钒。首先,采用静态吸附考察了料液平衡pH、料液钼浓度、氯离子浓度、吸附时间等因素对分离过程的影响;然后,进行动态交换实验,采用料液pH=8.01,接触时间60 min,处理料液为67倍树脂体积时,除钒率达到99.83%,树脂对V2O5工作交换容量为78.7 g/L,钒钼分离系数达到22522.9;用2 mol/L的NaOH溶液可以对负载树脂实现彻底解析。