Abstract
Membrane-based separation of phenol/water mixtures with concentrations of phenol between 3 wt% and 8 wt% in the feed has been performed with nonmodified as well as cross-linked ethylene-methacrylic acid (E-MAA) copolymers with different amounts of methacrylic acid. As cross-linking agents, aluminium acetyl acetonate, which leads to ionically cross-linked membranes, and 2,3,5,6-tetramethyl-1,4-phenylene diamine and glycerine digycidether, leading to covalently cross-linked membranes, have been used. Generally, it was found that with increasing phenol content in the feed, the total flux is increasing whereas the enrichment factor is decreasing. Using nonmodified membranes with higher methacrylic acid monomer content in the polymer, lower fluxes and higher enrichment factors were observed. Investigation of different cross-linked membranes showed that with high phenol concentration in the feed, ionic cross-linking seems to be very promising. Furthermore, variation of feed temperature shows that ionically cross-linked membranes reached higher fluxes as well as higher enrichment factors at elevated temperatures. The temperature-dependent data were fitted based on an Arrhenius-type equation, and activation energies for the permeation of phenol and water through the membrane were calculated.
1. Introduction
In most of the processes which are carried out in the chemical industry, the desired purity of the products is not reached during the reaction process. Therefore, technical separation methods are extremely important in order to reach high-quality products in acceptable yields at low costs. Conventional methods of separating mixtures like distillation, extraction, ad- or absorption as well as crystallization processes and combinations of these methods are well established but in several cases they are cost- and energy-consumptive so that alternative methods like membrane-based separations are investigated. Membrane processes offer the advantages of lower energy consumption compared to distillation as the separation of mixtures can be performed at much lower temperatures than the boiling temperatures of the components.
Development of suitable membrane materials and modules is necessary for successful competition with conventional separation methods. Processes, well established on the continuously growing membrane market, are dehydration of organic solvents by pervaporation, enrichment of oxygen from air by gas permeation, and gasoline vapour recovery by vapour permeation [1]. New fields of membrane applications are the separation of olefin/paraffins [2], the removal of di- and trinuclear aromatic components [3, 4] and sulphur containing aromatic components [5, 6] from gasoline as well as the removal of organic components as p-chloro- and dichlorophenols [7], cresols, alkyl substituted phenols, and aniline derivatives [8–10] from process or waste water streams.
In particular, the removal of phenol is of great interest in waste-water treatment. With a global production of 8 million tons each year in 2001, phenol is one of the most important intermediates in chemical industry. Phenol contaminated effluents arise, for example, during the production processes of bisphenol A, phenol formaldehyde resins, and the Hock process. The average concentration of phenol in these streams has been evaluated to be between 3 wt% and 10 wt% depending on temperature. For the reduction of phenol from waste water, several membrane extraction processes offer very promising separation properties [9, 11, 12]. However, increasing prices for phenol as raw material makes it worthwhile to recycle the valuable product from the stream, which is difficult with membrane extraction processes. In order to realize an economically feasible separation process, it is favorable to combine pervaporation with other separation techniques, as shown in the hybrid process in Figure 1. Such hybrid processes have been already proposed for the separation of other organic compounds from aqueous streams. In this process, a one-step pervaporation process is combined with a liquid-liquid phase separation where the condensed permeate can be treated. The organic phase contains 72.5 wt% of phenol and can be worked up by conventional methods, whereas the aqueous phase, containing 7-8 wt% phenol, can be combined with the feed stream. The retentate of the pervaporation unit contains only a small amount of phenol, and can be reused as process water.
Among all different kinds of membrane polymers investigated for the phenol recovery from process and waste water streams, poly dimethyl siloxanes and modified structures thereof are the most frequently published ones [13–16]. For example, with a concentration of approximately 5 wt% of phenol in feed, a flux of for a PDMS membrane of 50 m thickness was found with a selectivity of 11.6 at 70°C [15]. With Polydimethylsiloxanimide, which is a siloxane imide copolymer at the same feed concentration, much higher fluxes but lower selectivities were found compared to pure PDMS at 60°C. Selectivities between 18–23 and fluxes between 12.4 and have been obtained [17]. For polyimides as membrane material at a feed concentration of 7.8 wt% phenol at 60°C, the selectivity reached is 7.5 and the fluxes are [18, 19]. For polyurethane, at the same phenol concentration in feed at 60°C, a flux of was reported with a selectivity of 74 [20, 21]. The ethylene methacrylic acid copolymer used in this work showed separation data and fluxes comparable to those of the polydimethylsiloxanimide.
Since the permeate is phase separated after condensation, and the aqueous phase can be recombined with the feed stream, for the hybrid process as shown in Figure 1, high flux membranes have much better application potential than high selective membrane materials.
The aim of this work was using a commercially available rubbery polymer (ethylene methacrylic acid copolymer) with functional groups, opening the opportunity of modifying the chemical structure (e.g., performing ionical or covalent cross-linking). This has been shown before for different polymer structures as a very successful method enhancing the separation characteristics as well as the chemical and thermal stability of membrane materials [22–25]. In the case of the ethylene methacrylic acid copolymer used in this project it was even possible to use the basic polymeric material for different separation problems (e.g., aromatics/aliphatics separation as well as removal of phenol from aqueous streams applying suitable modifications) [23, 24, 26].
2. Theoretical Background
2.1. The Pervaporation Process
Pervaporation processes are membrane-based separations of liquid mixtures as principally shown in Figure 2 [24]. Thereby a phase transfer from the liquid phase to the vaporous phase through a polymeric membrane is occuring. In this process, the liquid feed mixture to be separated flows along one side of the membrane while the various feed components are permeating into and through the membrane at different rates. Therefore, the liquid retentate leaving the unit on the same side of the membrane as the feed enters is depleted in the components permeating preferentially. Consequently, the vaporous permeate collected on the back side of the membrane is enriched in the preferentially permeating component. The driving force for the mass transport of each component, through a membrane is the difference of the chemical potential (, , , where ) of the components present in the mixture between feed and permeate side. In pervaporation, the difference in the chemical potential is mainly achieved by keeping the permeate pressure much lower than the feed pressure.
2.2. The Solution Diffusion Model
Often polymeric solution-diffusion membranes are classified as “nonporous” membranes because no pores are existing, only microvoids caused by free volume compartiments of the polymer chains. However, porous membranes, which are separating mixtures based on a sieve mechanism, are moving fast in the direction of nanoporous materials and the difference between porous and nonporous membrane materials is disappearing. Therefore, it is better to classifiy the polymeric membranes used in this work as solution-diffusion-membranes instead of nonporous membranes.
The main features of the so-called solution-diffusion model widely used to describe the mass transport in selective polymeric layers are given in Figure 3. This model not only holds for pervaporation, but also for vapor and gas permeation [27–29]. The basic assumptions of this model are the existence of the thermodynamic phase equilibrium at both boundary surfaces of the selective layer in contact with the upstream feed mixture and the downstream permeate mixture.
The diffusion process inside the selective layer is described by Fick's law, which is assumed to be valid for each component, , (see [30]) where is the mass flux, is the diffusion coefficient, is the coordinate perpendicular to the membrane surface, and is the density of the selective polymer layer. The concentration of each component in this polymer layer is given by its weight fraction , defined as where and are the masses of the various components dissolved and is the mass of the polymer. Under steady-state conditions, integration of (1) gives with being the thickness of the selective layer, while and are the weight fractions of the component in the selective layer in its boundary at the feed side and the permeate side, respectively. These fractions depend on the composition of the corresponding mixture in contact with the boundary. Generally, depends on the weight fraction of each component permeating and consequently, the mass fluxes are mutually dependent.
With (3), of any component permeating can be calculated for a given feed concentration if the solubilities and , the dependency of the diffusion coefficient on composition, the thickness , and the density are known at operating conditions.
The weight fraction of any component in the permeate is given by the ratio of partial molar flux to the total molar flux , In many cases, modeling of the mass transport through membrane materials for better understanding of the factors influencing the transport is difficult although the approaches have been strongly improved in the last ten years [31, 32]. The reason for this is that, for example, experimentally it is not possible to measure concentration-dependent diffusion coefficients in mixtures and furthermore the thickness and density of the membranes are strongly depending on operating conditions, where in many cases swelling of the membrane is occurring. It has been also shown that solubility measurements will not lead to better understanding of the separation performance of different types of polymers since according to Figure 3 only solubliliy experiments representing the steady-state on the feed side and vapour sorption experiments representing the case on the permeate side can be performed. From these experiments no information is obtained about how the concentration gradient is changing in the polymer layer, if capillary condensation, for example, occurs with high boiling components, or how swelling is influencing the membrane microstructure.
In order to obtain realistic results about the membrane performances for different ethylene-methacrylic acid copolymers, in this work concentration- and temperature-dependent pervaporation experiments have been performed and discussed from the point of view of potential industrial application.
2.3. Membrane Separation Characteristics
The separation performance of a membrane material is characterized by two parameters, the permeability which gives an impression on the mass transport through the membrane material and the selectivity which shows the quality of separation The permeability can be measured by the mass flux through the membrane. The flux is normalized by the membrane area, the membrane thickness, and the time, so that its unit is .
In order to compare the quality of separation for the different membranes according to [33] either the enrichment factor which is the ratio of the weight fraction in permeate and feed respectively of the preferred permeating component can be used or the separation factor α, which is used in this work as defined in the following equation:Here are the weight fractions of the components ( is the preferentially permeating component) in the permeate and feed, respectively.
If pervaporation experiments are performed at different feed temperatures using the same feed mixture, generally with increasing temperature increasing fluxes are obtained. In many cases an exponential dependency of total as well as partial fluxes from the temperature are observed. According to (6), activation energies for the permeation of the single components as well as for the mixture through the membrane material can be calculated, thereby is a pre-exponential factor, is the thickness of the dry membrane [m], is the activation energy [], is the common gas constant [], and is the temperature [K].
3. Materials
In order to understand the physical properties of ethylene-methacrylic acid copolymer (Figure 4), the properties of the homopolymers should be discussed shortly.
Whereas the nonpolar hydrophobic polyethylene does not solve in any common solvent and therefore has to be melt-extruded to give foils, tubes, isolations and containers for food packages, the polar, hydrophilic, and in most cases the water soluble polyacrylic acid and polymethacrylic acid are used as super absorbers (if partially cross-linked) in cosmetic, textile, and paper additives as well as for the production of industrial glues. The most important and interesting property of ethylene methacrylic acid copolymer is the functional groups (–COOH) which can be modified by polymer-analogous reactions.
As basic material for the preparation of cross-linked membranes, two different types of ethylene-methacrylic acid copolymer have been investigated, which differ exclusively in the content of methacrylic acid monomer. In Table 1 the basic polymers used are listed.
3.1. Preparation of Cross-Linked Membranes
Cross-linked membranes were obtained by using the two different basic copolymers E-MAA 27 and E-MAA 38 as basic materials. As cross-linking agents, various cross-linkers were applied as listed in Table 2.
3.2. Ionical Cross-Linking
During the cross-linking reaction with aluminium acetyl acetonate, the low volatile acetyl acetone is set free and an ionically cross-linked membrane structure, as shown schematically in Figure 5, is obtained.
It has been found before that ionically cross-linked structures made from rubbery or glassy carboxylic acid containing copolymers can be used very successfully as membranes in different applications [34].
3.3. Covalently Cross-Linked Structures
In this work also covalent cross-linked structures were investigated. As cross-linking agents, an aromatic diamine, 2,3,5,6-tetramethyl-1,4-phenylene diamine, and different di- and triepoxides as shown in Table 2 were used. As an example for the formation of a covalently cross-linked copolymer structure in Figure 6 the reaction of the carboxylic acids on the polymer backbone with diexpoxides to di--hydroxyesters is shown.
For the preparation of ionically and covalently cross-linked membranes, 0.9 g of the E-MAA copolymer was dissolved in 10 mL of tetrahydrofuran (THF). In all cases, an equimolar amount of cross-linker calculated on the desired cross-linking degree was dissolved in 5 mL of THF. After complete dissolution of the polymer, the cross-linking solution was added and the clear solution was stirred for another 30 minutes, filtered and casted on a polyethylene terephthalate (PET) foil into a glass ring having a diameter of 12.4 cm. The membranes were covered with glass funnels to keep away dust particles and dried for 12 hours at room temperature inside the hood. For the cross-linking reaction, the membranes were placed in the vacuum oven rising the temperature from 333 K to 393 K and lowering the vacuum from 500 to 50 mbar within two hours. The membrane samples were kept another 24 hours at the same conditions inside the vacuum oven. After this procedure, clear, noncolored ionically as well as covalently cross-linked membranes were obtained. The membrane thickness of the different samples determined with a micrometer was between 46 m and 69 m.
It was found that cross-linked membranes E-MAA 27 as well as E-MAA 38 cross-linked with aluminium acetyl acetonate, glycerine diglycidylether, and 2,3,5,6-tetramethyl-1,4-phenylene diamine, respectively, were nonsoluble in THF which was used for the membrane preparation. NMR spectroscopic investigations of the cross-linked polymers were not possible as a result of the insolubility of the cross-linked materials. In solid-state NMR, the protons of the cross-links tend to disappear in the baseline. A qualitative or quantitative evaluation of the conducted cross-linking reactions using IR spectroscopy was carried out but thereby only slight tendencies but no quantitative correlation have been found. From other inquiries of esterifications via the acid chloride of E-MAA 27, carboxylic groups with isopropanol we found out that if less than 20% of the carboxyl groups are esterified, it is not possible with an adequate reliability to detect the cross-links. Over 20% nice qualitative correlations have been seen. However, it has been shown that the cross-linking reaction is reproducible and leads to membranes with reproducible separation characteristics. Experiments have been performed with different membrane samples from the same batch, as well as membrane samples prepared independently from each other.
4. Pervaporation Apparatus and Analytical Method
For the pervaporation measurements a slightly modified standard apparatus, described elsewhere in detail, was used [24, 35]. The effective membrane area was 41.9 and the downstream pressure was kept at 15–30 mbar. After steady state has been reached, feed and permeate samples have been collected every 2 hours, the flux has been calculated by weighing the cold traps and the enrichment factor was determined by cooling the feed and permeate compositions by HPLC. For that purpose, the permeate samples, which were phase-separated in most of the cases, had to be homogenized with acetone. Afterwards, 4 L of the samples have been mixed with 1 mL of water and injected into the HPLC column. The solvent of the HPLC was 70/30 acetonitril/water, whereas 0.1 wt% of trifluoro acetic acid was added to the water to prevent the formation of phenolate on the HPLC column. The flux on the column was 0.7 mL/min, and the wave length of the detector was 215 nm. As HPLC column, a nonpolar C18 standard column was used. With this method, the retention time of phenol was 4.14 minutes.
In order to ensure reproducible results, pervaporation data were measured at least with three different membrane samples. For the E-MAA 27 and E-MAA 38, respectively, used in this work as well as for other polymeric materials investigated in our group, it was found that the deviation in flux and selectivtiy is ±10% [36–38] for independently prepared membrane samples. This is in good agreement with deviations of industrial produced membranes.
5. Results and Discussion
First of all, the two basic polymeric materials E-MAA 27 and E-MAA 38 should be tested if they are in principle suitable materials for the removal of phenol from aqueous solutions, and if cross-linking is indeed necessary. Figure 7 shows the separation characteristics of E-MAA 27 with a methacrylic acid monomer content of 27.2 wt% at 313 K. In Figure 7(a), the total flux, and the partial phenol fluxes, and water fluxes are plotted versus the phenol concentration in the feed mixture. With increasing phenol content in the feed, the flux shows a linear increase due to swelling effects in the membrane material. Although the concentration of phenol in the permeate did not change significantly with increasing phenol concentration in the feed, the separation factor shows a significant decrease with increasing phenol concentration, as shown in Figure 7(b). The phenomenon of increasing flux with decreasing selectivity is very common and has been observed before in many studies concering pervaporation but also gas permeation using swelling feed components (e.g., aromatics, sulphur-aromatics, phenol, ethylene oxid, and [39–41]. With increasing concentration of the swelling component), increasing rearrangement of polymer chains is assumed with increasing chain mobility. As a result of this, the flux increases. According to the increased chain mobility reached during swelling, the diffusion coefficients of the different permeating components are changing. In the case of water/phenol, the diffusion rate of the small water molecules accelerates much more compared to the diffusion rate of phenol.
(a)
(b)
In order to show that the swelling of the E-MAA 27 polymer is due to an increase in phenol concentration sorption measurements have been performed exemplarily. Therby binary mixtures of phenol/water have been prepared in different concentrations excluding the miscibility gap. For each sorption experiment, three different membrane samples with an average weight of 150 mg were used. The deviation of the averaged mass uptake of each set of samples was ±10%.
As the data in Table 3 show, the mass uptake is strongly dependent on phenol concentration. If pure water is used, the mass uptake is only 0.3 wt% for the E-MAA 27 whereas the mass uptake in a 3 wt% phenol/water solution was three times higher. If very high phenol concentrations (75 wt%) are applied, the effect continues and the mass uptake is 6.2%.
In order to investigate the phenol and water concentration inside of the membrane, a photometric method was applied based on the oxidative coupling of phenol with 1-methyl-2-benzothiazonlinone hydrazon as already described in [42, 43], which is a commercially applied test for phenol in aqueous solutions according to EPA 420.1, US Standard methods 5530 and ISO 6439. Further details are found in [36].
As also shown in Table 3, the basic membrane material shows strong affinity towards phenol. For example, if the E-MAA 27 membrane is exposed to a 3 wt% a phenol/water solution, a mass uptake of 83 wt% phenol in the membrane has been found. At 7 wt% phenol/water solution an even higher mass uptake of 88 wt% was observed. Based on the results of partial phenol and water mass uptakes, the solubility selectivity is calculated based on (5) as the ratio of weight fractions inside the membrane divided by the ratio of weight fractions in solution. Analogous to (5), the weight fraction of the preferred sorbed substance belongs to the numerator. Thereby values of between 98 and 157 have been determined. The overall selectivity of a membrane-based process is defined as the product of solubility selectivity and diffusivity selectivity according to the solution-diffusion mechanism. However, the kinetic diameter of the phenol is much larger compared to the water molecule and so the diffusivity selectivity has to be smaller than 1. Since experimentally phenol enrichment has been observed it is obvious that the process is solubility controlled. This is in good accordance with many other liquid/liquid membrane-based separation processes as aromatic/aliphatic and water/ethanol separations. Due to the fact that with cross-linking the chain mobility is reduced, the diffusion coefficient of phenol is also lowered. Therefore, an increase of selectivity with cross-linking has to be an effect of increased solubility selectivity.
By increasing the methacrylic acid content in the polymer structure, the copolymer was expected to be more versatile to swelling effects in phenol/water mixtures. As shown in Figure 8(a) with the E-MAA 38, containing a methacrylic acid content of 38.5 wt%, the fluxes do not increase linearly but exponentially with increasing phenol concentration in the feed solution. At phenol feed concentrations of 7 wt%, the total flux of the E-MAA 38 is 3.4 times higher compared to the E-MAA 27 membrane. At the same time, the phenol flux of the E-MAA 38 is merely higher by 1.6 times compared to the E-MAA 27. This is due to the increase in hydrophilicity, which is caused by the higher content of methacrylic acid monomer in the E-MAA 38 compared to the E-MAA 27. Similar effects of increasing water fluxes with increasing hydrophilicity of the polymer backbone have been also observed for different polymer classes [44].
(a)
(b)
5.1. Conditioning Effects on Noncross-Linked Membranes
Conditioning effects have been investigated in earlier work with polyimide membranes [4, 25, 45] and it was shown that durable effects leading to increased fluxes and increased separation factors have been observed. Investigating various conditioning experiments by using different polymers led to the result that the membrane performance did not change even after several measuring cycles if once a maximum feed concentration of the swelling component was applied [38].
The aim of this work was to investigate if similar conditioning effects for the rubbery E-MAA 38 membrane compared to the glassy polyimides can be reached or if undesirable changes of the membrane performance (e.g., loss in selectivity) will occur.
Therefore, pervaporation experiments with the E-MAA 38 membrane were once performed with increasing phenol concentration and after reaching the highest possible phenol concentration in feed, the concentrations were lowered stepwise. The results are shown in Figure 9. After reaching the highest phenol concentration, the total fluxes on the back-measurements were slightly higher compared to the first measurements. It is also obvious from Figure 9, that the separation factors are much higher when the membrane once was exposed to high phenol concentration. So the observed effects described here are conditioning effects which can be used to increase the performance of a membrane material. Such effects have also been observed on other membrane materials (i.e., copolyimides and carboxylic acid containing copolyimides) [3, 4, 25, 38, 45].
(a)
(b)
5.2. Comparison of Different Cross-Linking Agents
Using E-MAA 38 as well as E-MAA 27 as a basic membrane material, different cross-linking agents as well as different concentrations of cross-linking agents have been investigated in order to figure out their influence on the separation characteristics. Thereby all experiments have been performed at a feed concentration of 8 wt%, the membrane temperature was at 313 K, and the permeate pressure was kept at 15–30 mbar.
In Figure 10, the results for E-MAA 38 membranes with a methacrylic acid content of 38.5 wt%, noncross-linked, covalently as well as ionically cross-linked are shown. It can be seen that ionical and covalent cross-linking result in a reduction of fluxes. This is due to the fact that cross-linking leads to a lower mobility of the polymer backbone and so the permeation rate for the single components is lowered. At the same time, the cross-linked membranes showed all higher separation factors compared to the noncross-linked membrane.
From all cross-linkers investigated, the ionic cross-linker aluminium acetyl acetonate seemed to result in the highest separation factor and therefore it was also investigated with the E-MAA 27 membrane having a lower methacrylic acid content of 27.2 wt% compared to 38.5 wt% in the E-MAA 38. For the membranes with the lower content of carboxylic acid groups, the effects on fluxes and separation factor were much higher. In Figure 11, it can be seen that separation factors of up to 6.0 can be reached with the ionically cross-linked membrane.
From the solubility data in Table 3, it is obvious that the diffusivity selectivity has to be much lower than 1. During cross-linking, the chain mobility is reduced and therefore the diffusivity selectivity for phenol in aqueous solution is lowered. The experimental increase in selectivity can only be explained by an increase of solubility selectivity in the cross-linked material.
5.3. Temperature Dependency of the Separation Performance
In the following experiments, it was investigated how changes of temperature affects the separation characteristics. As a membrane material, E-MAA 27 cross-linked ionically (10%) with aluminium acetyl acetonate was chosen. From Figure 12, it is obvious that an exponential increase in fluxes is obtained. It is also interesting that at low feed temperatures, the partial phenol fluxes are significantly lower than the partial water fluxes through the membrane. Whereas at feed temperatures higher than 373 K, the phenol fluxes are slightly higher than the water fluxes, resulting in very high separation factor as also shown in Figure 12.
(a)
(b)
The exponential increase of flux with increasing temperature is assumed to be attributed to (i) increase in solubility with temperature, (ii) increase of diffusivity with temperature, and (iii) increase in diffusivity of the components due to increased swelling of the polymer material. Detailed explanation on the theory and calculations of exponential increase of fluxes with increasing temperatures can be found in [23]. According to the solution-diffusion model as shown in Figure 3, inside of the polymer layer gradients of concentration, swelling effects as well as pressure differences are occuring. It is assumed that only in a minor part of the membrane layer, faced to the permeate side, low pressures as those applied on the permeate side are existing. The major part of the polymer layer is wet and/or swollen. Therefore, the exponential increase in flux is not attributed to increase in vapor saturation, since phenol, for example, has a boiling point of 181.9°C, whereas temperature-dependent pervaporation measurements have been performed between and .
5.4. Activation Energy for Permeation
According to (6) and the Arrhenius plot in Figure 13, the partial fluxes can be plotted versus and the activation energies for the permeation of phenol and water can be calculated.
The activation energy for permeation consists of two terms, the enthalpie of solution (phenol and water, resp., in the membrane) and the activation energy for diffusion. Whereas the activation energy for the diffusion is always positive, the enthalpie of solution can be positve, or negative. For the system water/phenol investigated in this work, for the activation energy of permeation positive values are obtained.
The activation energy for diffusion is considered as the energy that is necessary to form microvoids of adequate size for the permeating molecules. Cohesion forces of the polymer chains are counteracting against microvoid formation. High cohesion forces denote high activation energy for the diffusion. If large molecules (e.g., phenol) are permeating, larger microvoids are necessary, and therefore a higher activation energy for diffusion occurs. It was found that for rubbery polymers the activation energy for diffusion increases linearly with the size of the molecules [46].
For the E-MAA 27, which is also a rubbery polymer, activation energies for the permeation of phenol of kJ/mol, water of 59.7 kJ/mol, and the mixture of 8 wt% of phenol in feed 64.49 kJ/mol were obtained. Thereby phenol has the highest activation energy for permeation, due to the fact that it is the component with the largest kinetic diameter. With the activation energy the experimental data of increasing enrichment factors with increasing feed temperature can be explained.
6. Conclusion
(i)The nonmodified ethylene-methacrylic acid copolymer showed increasing fluxes and decreasing separation factors with increasing phenol content at 310 K.(ii)With increasing methacrylic acid content in the polymers higher fluxes and lower enrichment factors were observed.(iii)It has been shown that conditioning of ionically cross-linked ethylene-methacrylic acid copolymer membranes is possible leading to enhanced separation characteristics for the phenol/water separation.(iv)Cross-linking generally leads to higher separation factors combined with lower fluxes due to the reduced mobility of the polymer backbone. This effect is stronger for the copolymer having the lower methacrylic acid content.(v)For the ionically cross-linked ethylene-methacrylic acid copolymer membrane a strong increase in enrichment factor as well as an exponential increase in flux with increasing temperature is observed.(vi)The activation energy of phenol was found to be higher by 11 kJ/mol compared to water which explains the enhanced separation characteristics at higher temperature.
Acknowledgment
The authors gratefully acknowledge the SFB 663 as well as BASF for providing the basic polymer materials as well as cross-linking components.