Journal of Chemistry
Volume 2014 (2014), Article ID 467526, 5 pages
http://dx.doi.org/10.1155/2014/467526

Research Article

Earliest Results in the Use of Activated Composite Membranes for the Transport of Silver Ions from Aqueous Solutions

Yucundo Mendoza-Tolentino,¹ Carlos Andrés Galán-Vidal,¹ Giaan Arturo Álvarez-Romero,¹ M. T. Ramírez-Silva,² and Ma. Elena Páez-Hernández¹

¹Laboratorio 2, Área Académica de Química, Universidad Autónoma del Estado de Hidalgo, 42184 Mineral de la Reforma, HGO, Mexico
²Laboratorio R-105, Área de Química Analítica, Universidad Autónoma Metropolitana-Iztapalapa, 09340 México, DF, Mexico

Received 1 September 2014; Accepted 22 October 2014; Published 17 November 2014

Academic Editor: Eri Yoshida

Copyright © 2014 Yucundo Mendoza-Tolentino et al. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.

Abstract.

This paper presents the results concerning the first use of activated composite membranes (ACMs) for the facilitated transport of silver ions containing di-(2-ethylhexyl)-dithiophosphoric acid (DTPA) as the carrier. DTPA was immobilized by interfacial polymerization in a dense layer that was deposited in a porous layer, which was prepared on a nonwoven fabric support by phase inversion. The influence of fundamental parameters affecting the transport of silver ion as the carrier concentration in the membrane phase and stripping agent variation of the stripping solution have been studied. In the optimal conditions, the amount of silver transported across the ACMs was greater than 50%, whereas if the content of the carrier is modified, more than the 90% of the initial silver is removed from the feed phase.

1. Introduction

Separation processes are essential to the chemical, petroleum refining, and materials processing industries. These are defined as processes using physical, chemical, or electrical forces to isolate selected constituents from a mixture. The functions of separation processes include the removal of impurities from raw materials, products, and by-products as well as the separation of recycle streams and the removal of contaminants from air and water waste streams. The traditional chemical engineering methods of separation and purification include distillation, crystallization, adsorption, extraction, and membrane processes [1].

Liquid membranes (LMs), which are based on solvent extraction technology, have been proposed as a method of separation, representing an attractive alternative for the separation and recovery of chemical compounds. Liquid membranes may contain chemical carriers to facilitate the selective transport of gases or ions. Thus, the carrier reacts with one of the components of the source solution (feed) helping to transport it across the membrane [2]. Liquid membranes have been suggested as a clean technology due to characteristics such as high specificity and productivity as well as low emissions and energy utilization [3]. In recent years, several researchers have worked intensively on the application of liquid membranes for the recovery or separation of metal ions from aqueous solutions [4]. An example of this is the use of LM in extraction of contaminants metal ions such as cadmium, chromium, and lead [5, 6]. In the hollow fiber configuration [7], the LMs have been used to extract copper and cobalt from wastewater, and, recently, ionic liquids have been incorporated as carriers liquid membranes for the selective separation of zinc, cadmium, iron, and copper [8].

However, despite these advantages, it is well known that LMs are not widely used on an industrial scale, mainly due to their poor stability and subsequently short lifetime [9, 10]. Some factors that contribute to these disadvantages are the evaporation of the solvent used to prepare the liquid membrane, the solubility of the liquid membrane components, or its emulsification in the adjacent aqueous phases. In the supported liquid membrane configuration (SLM), membrane pores of the polymeric porous support became more elliptical and dilated which facilitate the loss of carrier from the membrane phase affecting in a significant way the transport process [11, 12]. For these reasons, different approaches to improving LMs stability have been suggested. Thus, an increase of the LM stability with the decrease of the polarity of the solvent used as receiving phase has been demonstrated [13]. Furthermore, stabilization of LM supported in a polymeric support (SLM) has been tried with plasma polymerization surface coating and the formation of barrier layers on membrane surfaces, either by physical deposition or by interfacial polymerization [14–17]. However, the use of a coating to recover the LM may significantly reduce the flux of ions across the membrane [18, 19].

A promising alternative to the transport of ions is the use of the activated composite membranes (ACMs) which immobilize the carrier in one of the polymeric layers that constitute them. Studies completed with these types of membranes have shown ACM to have a higher stability than LM with comparable metal ion permeation, while maintaining all the advantages belonging to LM [21, 22]. Nevertheless, despite having been used for the transport and separation of a variety of metal ions, their effectiveness has not been tested in the extraction and transport of silver ions.

Thus, this paper has proposed the use of activated composite membranes (ACMs) in the transport of silver due to the importance of silver in many industrial applications and because the silver content in samples of environmental interest is increasing due to the use of its components and preparations in industry and medicine. Therefore, their separation and recovery from industrial effluents is of great interest [23–25]. Parameters such as the concentration of carrier agent [di-(2-ethylhexyl)dithiophosphoric acid (DTPA)] in the membrane and the nature of the receptor phase were studied to achieve the maximum silver flow through the ACM.

2. Materials and Methods

2.1. ACM Preparation

The ACMs were prepared as described in the literature [21]. First, to form the porous layer, a polysulfone casting solution was prepared by dissolving the polymer (15%, w/w) in N,N-dimethyl formamide (DMF) by vigorous stirring for 12 h. Then, deposition of a polysulfone solution onto the nonwoven paper support (Hollytex 3329, Talas Co., NY, USA) was performed. The coated support was immersed in a water bath at room temperature to induce phase inversion, whereupon the prepared porous layer was introduced into the oven during 60 min at 55°C to dry. As a second step, a dense layer containing the carrier was formed on the obtained porous layer by interfacial polymerization as follows: the porous layer was impregnated with an aqueous diamine solution (1,3-phenylene diamine in deionized water containing sodium dodecyl sulfate as an aqueous stabilizing agent) and subsequently with an organic solution (1,3,5-benzene-tricarbonyl chloride and the desired concentration of the DTPA in kerosene). The excess of the solution was washed off the membrane surface with distilled water and finally the membrane was dried in an oven during 60 min at 55°C. A blank composite membrane (BCM) was also prepared by following the same procedure without including the carrier (DTPA). Both ACM and BCM were cut into circles to fit an 11.32 cm² area.

2.2. Silver Transport Experiments

The cell used for transport experiments has two compartments [26, 27]: one for the feed solution (source) consisting of silver nitrate  mol L⁻¹ in HNO₃ 0.1 mol L⁻¹, and the other for the receiving solution (stripping) containing a complexing silver agent in sulfuric acid 2 mol L⁻¹. Both compartments have a capacity of 200 mL and are separated by an orifice of 11.32 cm² where the prepared ACM is placed. All transport experiments were carried out in triplicate at room temperature. Both feed and stripping solution are stirred with Teflon stirrers coupled with electric motors connected to a power supply. After the stirrers switch on, samples from feed and stripping solutions are taken at regular time intervals and analyzed in an atomic absorption spectrophotometer (VARIAN SpectrAA-880) in order to find the amount of remaining and transported silver ions. For the flux determination (molAg cm⁻² s⁻¹), the slope of the straight line resulting from the plot of feed or strip phase concentration (molAg L⁻¹) versus time (s) is calculated. Later, the slope was multiplied by the volume phase (L) and divided by the ACM exposed area (cm²) (see (1)) [28, 29]:

3. Results and Discussion

3.1. Study of the Composition of the Receptor Solution for Silver Transport through ACM

In order to promote the transport of silver from the feed to the stripping phase, it was necessary to carry out the process shown in Figure 1.

Figure 1: Silver transport mechanism from a feed to the stripping solution through an activated composite membrane with DTPA as the carrier agent.

According to Figure 1, the transport of silver will take place if the Ag is removed from the ACM by a means of regenerating the carrier agent, which possess acidic properties [30]. This can be achieved using an acid stripping solution that may also contain a complexing reagent; both protons and complexing reagent will have a synergistic effect that can release and remove the silver to the receiving phase.

Thus, the first study consisted of choosing an extracting agent using the information available on agents commonly employed for the reextraction of silver to the stripping solution. Five chemical conditions are shown in Table 1. This table also shows the logarithmic values of the conditional equilibrium constant for global formation at working conditions (when the driving force of the reextraction step is the formation of a complex).

Table 1: Values of global equilibrium constants for silver complexation under different stripping conditions [20].

Stripping solution constituenta
Silver complex

Presence of Ag in the stripping solutionb

NH₃
Ag(NH₃)²⁺
7.22
−

EDTA (Y)
AgY³⁻
5.84
−

HNO₃
—
—
−

NaSCN

10.00
−

tu

13.41
+

Chemical conditions: NH₃ = ammonia buffer (/NH₃ 0.5 mol L⁻¹), pH 9.4; EDTA (Y) = ethylenediaminetetraacetic acid 0.1 mol L⁻¹ in tris (tris(hydroxymethyl)aminomethane), 0.1 mol L⁻¹ pH 9.6; HNO₃ 2 mol L⁻¹; NaSCN 0.5 mol L⁻¹; tu = thiourea 0.3 mol L⁻¹ in sulfuric acid 2 mol L⁻¹.

bIt was considered positive when its concentration in the receiving phase after three hours of experimentation was higher than the detection limit (2.40 × 10⁻⁷ mol L⁻¹).

The results showed that only thiourea is strong enough to break the DTPA-Ag complex and this is facilitated with the carrier regeneration (the replacement of Ag by H) due to sulfuric acid. For this reason, the composition thiourea/sulfuric acid was used for subsequent studies, but optimizing the concentration of thiourea and studying the effect on the reextraction still need to be completed.

Table 2 shows the flows obtained for the extraction of silver from the membrane to the stripping phase containing a solution of 2 mol L⁻¹ sulfuric acid and different concentrations of thiourea. Although the increase of thiourea concentration improves the silver transport, the inconvenience of determining silver in a highly concentrated salt solution forced us to use the nearest previous concentration (0.6 mol L⁻¹) for subsequent experiments.

Table 2: Silver flux from ACM to stripping phase according the thiourea concentration. ACM prepared with DTPA 0.75 mol L⁻¹. Feed phase with Ag 4.64 × 10⁻⁴ mol L⁻¹ in HNO₃ 0.1 mol L⁻¹.

Thiourea in stripping solution (mol L⁻¹ in H₂SO₄ 2 mol L⁻¹)
Ag flux (×10⁻⁶ mol cm⁻² s⁻¹)

0.0
NOa

0.1
NOb

0.3
0.37 (5.71)

0.6
0.58 (11.4)

1.0
1.1 (1.98)

Percentage of standard deviation in parenthesis. NO = not observed. LOD <1.65 × 10⁻⁷ mol L⁻¹; NO = Not observed. LOD <2.40 × 10⁻⁷ mol L⁻¹.

According to these results, it was also possible to confirm that replacing the acidic protons of the carrier is not enough to free silver from the membrane, which indicates the strength of the DTPA-Ag complex [20, 30, 31].

3.2. Variation of the Extraction and Reextraction Flux with regard to the DTPA Contents of the ACM

After selecting the composition of the receiving phase, the study of the variation in the composition of the ACM was performed. Thus, several membranes were prepared from solutions having different DTPA concentrations. The resulting membranes were used to study the transport of silver. Results are shown in Figure 2. According to this, it may be seen that the silver flux is closely related to the DTPA content in the membrane and, depending on the application, a high-DTPA ACM may be chosen if the purpose of the experiment is to recover silver from an aqueous solution. By contrast, if the goal is silver transport or silver preconcentration, the best option is to reduce the DTPA concentration to allow an easy Ag release from the membrane, resulting in the uphill transport phenomenon. This is best illustrated in Figure 3 which shows that increasing the concentration of DTPA in the membrane causes a considerable increase of silver extraction (ca 94%) but only 18% of the initial silver is transported. Conversely, if the content of DTPA in the ACM decreases, the percent of extraction decreased to 75%, but the reextraction is facilitated obtaining 54% of silver transported. It should be noted that in the absence of DTPA, silver did not suffer any variation in feed phase and was undetectable in the stripping phase.

Figure 2: Variation of silver flux in a transport experiment using an ACM with different DTPA content. Feed phase with Ag  mol L⁻¹ in HNO₃ 0.1 mol L⁻¹; stripping phase with thiourea 0.6 mol L⁻¹ in sulfuric acid 2 mol L⁻¹. Bars represent standard deviation.

(a)

(b)

Figure 3: Silver fraction in different phases as function of time during a transport experiment through an ACM prepared with (a) DTPA 0.25 mol L⁻¹ and (b) DTPA 1.00 mol L⁻¹. Feed phase with Ag  mol L⁻¹ in HNO₃ 0.1 mol L⁻¹; stripping phase with thiourea 0.6 mol L⁻¹ in sulfuric acid 2 mol L⁻¹.

4. Conclusions

From this study, a new feasible alternative process for silver recovery is proposed. Under the best extraction conditions, the removed silver is higher than 94%, while using a suitable DTPA content in the ACM, 54% of the initial silver is transported to the stripping phase.

Although it is true that the transport results are not so high compared with some reports from the literature, with this study it is possible to foresee the use of ACM for the extraction of silver from complex solutions due to the great affinity of Ag to DTPA.

Furthermore, considering the results obtained for the transport of silver and similar metal ions such as mercury [21, 30, 31], a possible alternative for separation may arise if a low concentrated thiourea stripping solution allows for the reextraction of Hg but does not favor silver.

Conflict of Interests

The authors declare that there is no conflict of interests regarding the publication of this paper.

Acknowledgments

Ma. Elena Páez-Hernández acknowledges CONACyT (2006-62581 Project) and PROMEP (SEP, Mexico) for the financial support. Yucundo Mendoza-Tolentino is grateful for his postgraduate studies grant. Ma. Elena Páez-Hernández, Carlos Andrés Galán-Vidal, Giaan Arturo Álvarez-Romero, and M. T. Ramírez-Silva gratefully thank the SNI for the distinction of their membership.

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