Primene JMT Research Articles

Iron Control in Liquid Effluents: Pseudo-Emulsion Based Hollow Fiber Membrane with Strip Dispersion Technology with Pseudo-Protic Ionic Liquid (RNH3+HSO4-) as Mobile Carrier.

The transport of iron(III) from aqueous solutions through pseudo-emulsion-based hollow fiber with strip dispersion (PEHFSD) was investigated using a microporous hydrophobic hollow fiber membrane module. The pseudo-protic ionic liquid RNH3HSO4- dissolved in Solvesso 100 was used as the carrier phase. This pseudo-protic ionic liquid was generated by the reaction of the primary amine Primene JMT (RNH2) with sulphuric acid. The aqueous feed phase (3000 cm3) containing iron(III) was passed through the tube side of the fiber, and the pseudo-emulsion phase of the carrier phase (400 cm3) and sulphuric acid (400 cm3) were circulated through the shell side in counter-current operational mode, using a single hollow fiber module for non-dispersive extraction and stripping. In the operation, the stripping solution (sulphuric acid) was dispersed into the organic membrane phase in a tank with a mixing arrangement (a four-blade impeller stirrer) designed to provide strip dispersion. This dispersed phase was continuously circulated from the tank to the membrane module in order to provide a constant supply of the organic solution to the fiber pores. Different hydrodynamic and chemical parameters, such as feed (75-400 cm3/min) and pseudo-emulsion phases (50-100 cm3/min) flows, sulphuric acid concentration in the feed and stripping phases (0.01-0.5 M and 0.5-3 M, respectively), metal concentration (0.01-1 g/L) in the feed phase, and PPILL concentration (0.027-0.81 M) in the carrier phase, were investigated. From the experimental data, different diffusional parameters were estimated, concluding that the resistance due to the feed phase was not the rate-controlling step of the overall iron(III) transport process. It was possible to concentrate iron(III) in the strip phase using this smart PEHFSD technology.

Coupled cavitation and AOPs treatment of Primene-JMT containing wastewater

The application of various cavitational reactors as the novel approach to remove the emerging contaminant, Primene-JMT (PJMT), in an aqueous solution has been elucidated in this work. Ultrasonic step horn (US step horn), longitudinal horn based ultrasound (LHUS), hydrodynamic cavitation (HC) with single slit venturi (HCSV), and dual slit venturi (HCDV) are the specific reactors studied individually and in combination with Advanced Oxidation Processes (AOPs) involving H2O2, Fenton, O3, and NaClO. Different operating parameters such as oxidant loadings, oxidant ratios, treatment time, and the inlet pressure have been varied to elucidate the optimum conditions. The optimal conditions established in the study are H2O2 dosing of 0.8 g/L, H2O2/Fe2+ ratio of 4/1, O3 flow rate of 3LPH, and NaClO dosing of 0.8 g/L as applicable for the specific process. The US+NaClO and US+Fenton+CaO schemes were shown to be most effective at laboratory scale in achieving a maximum COD reduction of 98 % each at pH of 9 after 120 min and 130 min, respectively. Under the optimum conditions, LHUS+NaClO and HCDV+NaClO schemes were also successfully applied on pilot scale, showing the maximum COD reductions of 90 % and 96 % and cavitational yield of 0.89×10−3mg/J and 26.34×10−3mg/J, respectively. Comparison of different cavitating devices revealed that a dual slit venturi was nearly 30 % more efficient than a single slit venturi under similar conditions. It was clearly demonstrated that a combination strategy under optimum conditions was advantageous for attaining the highest COD reduction and cavitational yield at the lower operational cost.

Development of a recovery process of thorium and possible separation of rare earths from Korean monazite

ABSTRACT Systematic studies were carried out to leach out rare earths and recover thorium from Korean monazite. Monazite was processed with acid baking process (sulfation) where rare earth elements (REEs) and thorium phosphates were transformed to water-soluble sulfates. Various experimental factors such as temperature, H2SO4/monazite concentrate ratio and time were studied to get optimized sulfation system. Near to 88% of leaching of REEs and Th was performed after sulfation followed by water leaching. Moreover, by using 0.1 mol/L of primary amine Primene JM-T (tri-alkyl-methylamine), thorium was separated (more than 95%) from the light rare earth elements present in the leach liquor. Subsequently, rare earth elements were separated by solvent extraction technique using Cyanex 572 as an extractant at different pH conditions. High separation coefficients for different rare earths were obtained with Cyanex 572, while Primene JM-T resulted in the complete separation of the thorium from the leach liquor.

Extraction of phenol from water by primary amine primene JMT

In this work, liquid-liquid extraction of phenol from aqueous solutions using primary amine Primene JMT (Primene® JM-T) was investigated. The extraction capability of Primene® JM-T with different diluents, including 3-heptanone, sulfonated kerosene, methyl isobutyl ketone, n-octanol, toluene and petroleum ether was studied. The experimental results indicated that the distribution coefficient of phenol extracted using Primene® JM-T that was diluted in 3-heptanone could reach 101.74 under the pH of 9.2. Moreover, the extraction reaction was exothermic (enthalpy change for the extraction reaction (ΔrHm) was −21.03 kJ/mol). High temperature showed a negative effect on the extraction of phenol. The results also showed that adding mineral salt was conducive to the extraction process, and the extraction efficiency fell in the descending order of: (NH4)2SO4> NaCl > NH4Cl. Two empirical correlations were put forward to quantitatively describe the salting effect. Furthermore, the equilibrium constants of phenol extraction using Primene® JM-T were calculated to be 78.2 L/mol. The phenol was extracted using Primene® JM-T with the possible stoichiometric formula of: [RNH3+⋅PhOH]org, where R represents the alkyl group of the amine.

Preparation of Pure Uranium, Thorium, and Yttrium Oxides from El-Garra El-Hamra Sulfate Leach Liquor

The study deals with separation of uranium, thorium, and yttrium with highest possible purity from El-Garaa El-Hamara sulfate leach liquor. From the latter, almost complete extraction of uranium (99%) was achieved using Alamine 336 in kerosene at pH 0.8; it was followed by selective precipitation of thorium as thorium peroxide at pH 1.9 using 30% H2O2. Primene JM-T in kerosene separates selectively pure yttrium from the prepared RE cake at pH 1.5. A flowsheet for the preparation of pure oxides of U, Th, and Y was proposed.

Separation, purification and recovery of thorium from monazite leach liquors by counter-current extraction process

Separation and purification of thorium from monazite leach liquors was investigated by counter current extraction process. The Primene JM-T (mixture of highly branched C16 to C22 tertiary alkyl primary amine isomers) was used as an extractant and kerosene as a diluent for the present investigation. Extraction isotherm was plotted at the condition: 0.1 mol/L Primene JM-T, A:O = 3:1, which predicted on requirement of 3 stages for quantitative extraction of thorium. A 99.9% extraction of thorium from the leach liquor was achieved at the optimum conditions leaving 0.1 mg/L of the metal in the raffinate phase. The predicted three counter current stripping stages from the stripping were validated using 0.5 mol/L HCl + 0.5 mol/L NH4Cl as the stripping agent. XRD analysis proved the high purity thorium oxalate precipitated and recovered from monazite.

Solvent extraction, separation and recovery of thorium from Korean monazite leach liquors for nuclear industry applications

The technology for extraction and recovery of the thorium from its source is one of the significant areas of research Present investigation deals on development of a process for extraction of thorium and its separation from the uranium and rare earths contained Korean monazite leach liquor. In the preliminary study, sulfuric acid treatment of monazite concentrate followed by water leaching was carried out. Furthermore double salt precipitation and acid leaching lead to produce thorium rich leach liquor. Various commercial extractants accomplishing D2EHPA, PC88A, Amine and Primene JM-T were tested and optimized for selective separation of thorium. The effective extraction behavior of thorium followed the order as; Primene JM-T>D2EHPA>PC88A and high separation factor was resulted at high acidity (2.5mol/L) of leach liquor, ensuring on high selectivity of Primene JM-T towards loading of Th. The co-extraction of cerium was prevented by changing thorium oxidation state using Fe2+ and H2O2 and reported. The co-extraction of other associated rare earths was scrubbed with sulfuric acid solutions. Subsequently, stripping studies were carryout with two different types of mineral acids and it was quantitative using high acid concentration (5mol/L).

Extraction of indium(III) from sulphuric acid medium by the ionic liquid (PJMTH+HSO4−)

The extraction of indium(III) from acidic sulphuric solution by the ionic liquid (PJMTH+HSO4−) was investigated. This ionic liquid was generated by reaction of the primary amine Primene JMT (PJMT) and sulphuric acid solutions. The metal extraction was investigated under various experimental conditions: equilibration time, temperature, metal and sulphuric acid concentrations in the aqueous feed and extractant concentration in the organic solution. Also, the selectivity of the present system against the presence of other metals in the aqueous feed was examined. Indium stripping is effectively done by the use of sulphuric acid solution. Extraction and stripping isotherms were generated within this work.

Recovery of uranium, thorium and rare earth from industrial residues

This paper addresses the development of a process to recovery uranium, thorium and rare earth elements from an industrial residue, with a subsequent removal of U and Th from the liquor generated. Sulfuric acid digestion followed by water leaching was found to be the best method to solubilise the metals. The acid digestion was carried out with an acid sample ratio of 700 kg t−1 and a reaction time of 2 h, without temperature control. The water leaching step was performed at room temperature (25 ± 2 °C), with 1 h of mechanical stirring and 20% of solids. Under these conditions, a metal dissolution of 94%, 81% and 97% was reached for the REE, Th and U, respectively. After the metal solubilisation, a sulfuric liquor containing 0.08 g L−1 Th, 0.35 g L−1 U, 9.1 g L−1 REE, 16 g L−1 Al, 7.8 g L−1 Fe, 0.47 g L−1 Ca, 0.75 g L−1 Zn and 0.1 g L−1 Si was formed. This liquor was used in the solvent extraction stage in order to separate Th and U from the REE, as well as from other metals. The effect of the type and extractant concentration, acidity of the liquor and type and concentration of the stripping solution were investigated. The results showed that 97% of the uranium and 94% of the thorium were extracted by a mixture of 0.05 mol L−1 of Primene JM-T and 0.1 mol L−1 of Alamine 336, in a single stage. The stripping from the loaded organic phase for the simultaneous removal of U and Th can be effectively done by using 1.7 mol L−1 NaCl solution at pH 1.2.

Solvent extraction of yttrium and rare earth elements from copper pregnant leach solutions using Primene JM-T

The solvent extraction of yttrium and rare earth elements from copper pregnant leach solutions (PLS) using Primene JM-T, a primary aliphatic amine, has been studied. This investigation focused on the effect of extractant concentration to obtain a better understanding of the extraction mechanism. Copper bearing PLS from a leaching operation in Arizona was used as the feed solution in all experiments. Standard experimental conditions were 5 min contact time, 1:1 O:A phase ratio, kerosene as a diluent, and room temperature. The solution chemistry of the PLS was modeled using PHREEQC software. Primene JM-T concentrations in the organic phase ranged from 0.059–0.221 M (2–7.5% v/v). At 0.147 M Primene JM-T, yttrium extraction was 88.4% whereas the LREEs averaged about 95% and the HREEs a little lower at 92%. It was shown that approximately 2.4 mol of Primene JM-T are required per mole of yttrium or rare earth metal at extractant concentrations ranging from 0.07 to 0.10 M. In this Primene JM-T concentration range, it appears that a mixture of metal sulfate complexes is being extracted. At low Primene JM-T concentrations, Me(SO4)33– is the dominant species being extracted. As extractant concentrations increases, the reaction appears to favor of the extraction of Me(SO4)2−.

Recovery of yttrium and neodymium from copper pregnant leach solutions by solvent extraction

The solvent extraction of yttrium and neodymium from copper pregnant leach solutions (PLS) using Primene JM-T, a primary aliphatic amine, has been studied. Effect of contact time, pH, sulfate concentration, and extractant concentration were investigated using synthetic and actual PLS systems. Standard experimental conditions were 5 min contact time, pH ~ 2.5, 10 % v/v Primene JM-T concentration, and 1:1 O:A phase ratio. Distribution isotherms were constructed for the pure systems and for actual copper leach solutions. Synthetic solutions contained 100 ppm Y and ~75 ppm Nd. Copper PLS contained 14.9 ppm Y and 2.1 ppm Y. Results showed that complete extraction of both yttrium and neodymium occurred within 5 min and at pH values greater than 1. It was also found that sulfate concentration does not inhibit extraction at any concentration. Using synthetic solutions of yttrium and neodymium, it was found that the reaction stoichiometry requires 2 moles of Primene JM-T per mole of metal extracted. This suggests that a both bi-sulfate and tri-sulfate complexes are being extraction. For the copper bearing PLS, 3 moles of Primene JM-T were required per mole of metal extracted. This support the tri-sulfate complex as being the predominate species being extracted.

Purification of Coal Fly Ash Leach Liquor for Alumina Recovery Using an Integrated Precipitation and Solvent Extraction Process

The purification of coal fly ash (CFA) leach liquor has been carried out using an integrated solvent extraction and precipitation technique. The integrated technique was employed to primarily remove two dominant impurities, Ti and Fe, from CFA leach liquor. The solvent extraction experiments were carried out at varying factor values of contact time, aqueous-to-organic ratio, and extractant concentration. Preliminary results showed no loading of Fe2+ onto the organic phase, partial loading of Fe3+, and a high loading of Ti4+. Unable to adequately load onto the organic phase due to the high CFA leach liquor acidity at pH 0.1, Fe3+ required reduction to Fe2+ in order to bypass the solvent extraction stage. To achieve this, an integrated solvent extraction and precipitation technique was formulated and adopted. The technique involved iron reduction from Fe3+ to Fe2+ as the first treatment of CFA leach liquor, followed by solvent extraction of Ti4+ and subsequent recovery of titanium as TiO2, crystallization of Al3+ and the precipitation of Fe2+, in the form of Fe(OH)2, as the last treatment. Alumina was recovered as a precipitate product in the form of (NH4) Al(SO4)2·12H2O, and the calcined alumina product contained 99.91% Al2O3. Primene JMT was used in small amounts of ~10% in kerosene for short contact times of ~15 min using an A/O ratio of 1:1 in order to achieve high extraction efficiencies during the solvent extraction step. The results presented in this paper identify the integrated precipitation and solvent extraction route as an effective option for CFA leach liquor purification and alumina recovery.

Transport of indium(III) using pseudo-emulsion based hollow fiber strip dispersion with ionic liquid RNH3+HSO4−

The transport of indium(III) through pseudo-emulsion based hollow fiber strip dispersion technology was investigated. The extractant being an ionic liquid RNH3+HSO4−, previously generated from the reaction of the primary amine Primene JMT, dissolved in Solvesso 100, and sulphuric acid. The feed solution containing In(III) was flowed through the tube side, and pseudo-emulsion of RNH3+HSO4−/Solvesso 100 and sulphuric acid was passed through the shell side in counter-current mode, using a single fiber contactor for extraction and stripping. Several hydrodynamic and chemical parameters, such as variation in flows, feed pH (0.6–2), indium concentration in feed (0.01–0.1gL−1), carrier concentration (0.0025–0.25M), etc., were investigated.

Purification of coal fly ash leach liquor by solvent extraction: Identification of influential factors using Design of Experiments

The solvent extraction of iron and titanium from coal fly ash leach solution was investigated by the use of Design of Experiments. The effect of the factors: hydrogen ion concentration, Primene JMT concentration, aqueous to organic volume phase ratio and temperature on iron and titanium extraction were evaluated. A two level factorial design implemented by statistical software Design Expert® 6, determined the significant factors and any associated interactive effects amongst these factors.Hydrogen ion concentration and the interaction between the aqueous to organic volume phase ratio with Primene JMT concentration had a significant effect on the extraction of iron while temperature did not. Hydrogen ion concentration and temperature did not have a significant effect on the extraction of titanium, while the interaction between Primene JMT concentration and the aqueous to organic volume phase ratio had a significant effect.The maximum iron extraction achieved in the implemented design was 33.8% while 99% of titanium could be extracted from the coal fly ash leach solution. Extraction improvement tests showed that at a hydrogen ion concentration of 0.28M, 88% iron and 99% titanium extraction from coal-fly ash leach solution could be achieved.

Recovery of hydrochloric acid from galvanizing industrial effluents

ABSTRACTThe recovery of hydrochloric acid and its separation from iron, zinc and minor elements, in the galvanizing pickling baths, were studied by solvent extraction (SX) and distillation and by distillation and crystallization. Several extractants were tested, the tri-isooctyl amine, Alamine 308, the primary aliphatic amine Primene JM-T and the mixture of four trialkylphosphine oxides, Cyanex 923. Only Cyanex 923 enabled distillation. The results indicated the feasibility of the processes to treat a real effluent using Cyanex 923 and to obtain high HCl concentrations in the distillate (256–330 g/L).

Preparation of microspheres of carbon black dispersion in uranyl-ascorbate gels as precursors for uranium carbide

A novel technique to fabricate precursors of carbide-ceramic nuclear fuel via synthesis of spherical particles (with a diameter below 150 μm) of carbon black dispersion in uranyl-ascorbate gels by a combination of the Complex Sol–Gel Process and the Double Extraction Process has been elaborated. Applying of ascorbic acid as complexing agent in the Complex Sol–Gel Process allows to obtain stable and uniform dispersion of carbon in an uranyl-ascorbate sol. Traditionally, the dispersability is improved by employment of dispersing agents – surfactants. In the presented Complex Sol–Gel Process, a dispersing agent is needless. The ascorbate sols perfectly wet carbon black and do not form agglomerates. In the Double Extraction Process, dispersion of carbon black in sols is emulsified by drops in the organic phase consisting of 2-ethylhexanol-1 and 1 volume % of Primene JM-T. The microspheres are created by gelation of droplets, through simultaneous extraction of water with 2-ethylhexanol-1 and nitrate ions with Primene JM-T. The elaboration of the optimal gelation conditions requires considering many issues which are described in this paper.

Influence of Selected Surfactants and High-Octane Oxygen Components on Water Content, Electrolytic Conductivity in Gasoline, and Interfacial Tension in the Water/Gasoline System

The influence of selected surfactants and oxygen containing components on solubility of water, electrolytic conductivity in gasoline, and interfacial tension in the water/gasoline system was studied. Anionic sodium bis-(2-ethylhexyl)sulfosuccinate (AOT), the branched alkylamine Primene JM-T, and some hydrophilic additives (alcohols and methyl tert-butyl ether) were examined. Slight amounts of amphiphilic substances can improve the solubility of water, and they may cause the association phenomena with the formation of reverse micelles. Hydrophilic groups of the compounds are located inside the micelles, in which the water pools can be contained. Surfactant aggregates and droplet clusters are contained in the microemulsion solution due to the dipolar interaction between the dispersed droplets. The formation of these structures induces an increase in the solubility of water in gasoline. The improvement of electrolytic conductivity depends on the type and concentration of surfactants and hydrophilic additives. Conductivity is very sensitive to microemulsion structure and it significantly increases because of the presence of reverse micelles, which are able to transport charges. Correlation between conductivity, water content, and interfacial tension has been analyzed. On the basis of the calculated coefficients, the closest correlation between these parameters was osberved in the case of the addition of AOT and hydrophilic components.

α-Dialkylamino N,N-diisobutylacetamides: a new class of anion exchanger with intramolecular buffering properties

A new class of ammonium based anion exchangers embedded with a terminal amide group, viz. α-dialkylamino N,N-diisobutylacetamides has been designed, synthesized and tested for their ability to extract oxometalate anions from nitric acid medium. As a representative example, the molybdate anion has been chosen for the present studies and its extraction behaviour was compared with routinely used anion exchangers like Alamine 336, Aliquat 336 and Primene JMT having no amide functionality. A higher %E value for molybdate was observed with α-dialkylamino N,N-diisobutylacetamides compared to Alamine 336, Aliquat 336 and Primene JMT, from the same HNO3 acidity. The presence of amide group in the ligand is the key to the success of extraction from a relatively higher concentration of nitric acid medium. The amide group in the extractant leads to extra acidity through the intramolecular buffering effect thus enabling the ligand to extract the molybdate anion at higher acidities. Stoichiometry of the ion pair formed during extraction was ascertained by the slope analysis method. The composition of the complex was found to be (LH)2MoO4·HNO3. FTIR and NMR of the loaded extractant indicated that MoO42− is associated with the ammonium site while binding of HNO3 occurred at the amide group.

Measurement and Modeling for the Solubility of Hydrogen Sulfide in Primene JM-T

The primary aliphatic amine Primene JM-T was investigated as a potential absorbent for H2S removal. The solubility of H2S in JM-T was measured at 298, 313, 333, 353, and 368 K with H2S partial pressures from 20 to 760 kPa and H2S loading from 0.02 to 0.8 mol H2S per mol JM-T. Relevant physical properties, such as density, viscosity and dielectric constant, of the material were measured. The thermodynamic model with two-suffix Margules equation was used to correlate the experimental vapor-liquid equilibrium data. Furthermore, the absorption mechanism in non-aqueous system is suggested and the difference between non-aqueous and aqueous absorption system is pointed out.

Transport of Cr(VI) using an advanced membrane technology and (PJMTH+NO3−) ionic liquid derived from amine Primene JMT as green chemicals

The extraction of Cr(VI) from acidic solutions through pseudo-emulsion-based membrane strip dispersion (PEMSD) was conducted in a microporous hydrophobic polyvinylidenedifluoride (PVDF) membrane support and permeation cell. As organic extractant ionic liquids derived from the primary amine Primene JMT in cumene was used. The acidic feed solution containing Cr(VI) was placed in one side of the permeation cell, whereas the pseudo-emulsion of Primene JMT/cumene and acidic solution was placed in the other side of the cell, using a single microporous hydrophobic PVDF membrane support for extraction and stripping. In PEMSD the aqueous acidic (HNO3) solution was dispersed into the organic (Primene JMT/cumene) membrane solution with a mixing arrangement (impeller stirrer) designed to form a strip dispersion. This operation mode provides a constant supply of the ionic liquid extractant/cumene solution to the membrane pores. Various hydrodynamic and chemical parameters, either in the feed or in the pseudo-emulsion phases, were investigated. Results showed that from feed solutions in the pH 3 range, chromium removal efficiencies exceeding 90% are achieving after 3 h, whereas chromium recovery in the strip solution is dependent upon the strippant concentration. Furthermore, the performance of this carrier against other extractants was evaluated.