Reverse osmosis membrane fouling and its control

Reverse osmosis (RO) membranes can be used to treat ground water, surface water and wastewater, but a major problem in RO membrane applications is fouling. Many studies have investigated the mechanisms of fouling in RO membranes and suggested various methods to control the membrane fouling. This paper reviews several aspects of RO membranes, such as the types of membrane fouling, their effects on RO membrane processes and fouling control technologies, focussed on the appropriate feed pretreatment technologies and cleaning methods, especially on the membrane filtration pretreatment processes, including microfiltration (MF), ultrafiltration (UF) and nanofiltration (NF), which are the new trends in designing a pretreatment system in the application of RO.

Improved extraction of heavy metal ions using membrane technology

Investigates tha application of polymer membranes in industrial wastewater treatment. Several novel membrane systems have been developed. The new systems overcome the problems of low extractant capacity and slow rate of extraction of the traditional membrane system. These new systems offer significant scope for the treatment of industrial wastewater containing heavy metal ions.

Effects of backwashing on PVDF membrane fouling by organic foulants

Membrane is usually subject to fouling by various organic foulants, such as yeast, protein and sodium alginate during filtration. Backwashing is a common practice to reduce membrane fouling. It is essential to evaluate the effects of backwashing on fouling in order to optimize operational parameters. In this experiment, poly(vinylidene fluoride) (PVDF) membranes were used to filter organic foulants from suspensions in a dead-end stirred cell. Three types of organic foulants including yeast, protein and sodium alginate which were stained with fluorescent dyes before filtration were used with different combinations in the experiments. After filtration, the PVDF membrane was backwashed.

Consequently, a stack of images, instrumental data and sample data were captured from the fouling layers on the PVDF membrane surface using confocal laser scanning microscope (CLSM) and its associated image acquisition software LAS AF. Then, the quality of the images was enhanced for better visualization and a set of quantitative fouling data were derived by using the software code developed by the project team at Deakin University.

This collection contains raw image data of poly(vinylidene fluoride) (PVDF) membrane’s fouling layer when three types of organic foulants present, which are captured by confocal laser scanning microscopy (CLSM) and its software, and the instrumental and sample metadata, the processed image data and the geometrical structure properties of the fouling layer. By comparing with the same membrane without backwashing, the efficiency of backwashing was computed.

This data collection would be useful to evaluate the backwashing efficiency of PVDF membrane in order to optimize frequency and operational conditions of backwashing by membrane materials researchers and water researchers.

Biological treatment of oily wastewater from gas stations by membrane bioreactor

In many Asian countries, rapid industrialization and urbanization has led to an increased number of cars, making wastewater from gas stations an important issue of concern in urban environment. This wastewater is characterized by high concentration of oil-water emulsion, which cannot be effectively removed by a conventional gravity separator. An experimental investigation on the treatability of oily wastewater from gas stations using a membrane bioreactor (MBR) system revealed that MBR system could achieve good removal efficiency with stability against shock loading. Optimum operating conditions were found to be at a hydraulic retention time of 4 h and an oil-loading rate of 1.8 kg oil m^sup -3^.d^sup -1^. It was anticipated that adding powdered activated carbon (PAC) in the MBR could help to adsorb the oils. However, operating the MBR with only microbial flocs has an advantage over adding PAC particles into the MBR, since the former condition could provide a prolonged cycle of filtration with a relatively lesser increase in transmembrane pressure.

Application of submerged membrane bioreactor for aquaculture effluent reuse

Discharging the nutrient rich aquaculture effluents into inland water bodies and oceans is becoming a serious concern due to the adverse effect that brings in the form of eutrophication and subsequent damages to those waters. A laboratory scale biological reactor consisting of a denitrifying compartment followed by a submerged membrane bioreactor (SMBR) compartment was used to treat 40 L d−1 of aquaculture effluent with an average concentration of 74 mg L−1 nitrate (NO3 − ). Sugar was added to the aquaculture effluent in order that to enter into the denitrifying compartment at a carbon: nitrogen ratio (C:N) of 2:1 and 4:1. A hollow fibre membrane with a pore size of 0.4 μm and a filtration area of 0.20 m2 was used in the SMBR and was operated at an average flux of 0.20 m3 m−2 d−1. An intermittent suction period of 12 min followed by a relaxation period of 3 min was maintained in the SMBR throughout the experiment. Different aeration rates of 1, 3, 5 and 10 Lpm were applied to the SMBR to determine the rate of membrane fouling and 5 Lpm aeration rate was found to be optimum with respect to the rate of fouling of membrane at a C:N ratio of 4:1. The average rate of fouling at 1, 3, 5 and 10 Lpm were 1.17, 0.70, 0.48 and 0.52 kPa d−1, respectively. The increase in the rate of fouling when the aeration was increased from 5 to 10 Lpm may be due to the breakage of suspended particles into finer particles which could have increased the fouling of membrane. It was also found that increasing the C:N ratio from 2:1 to 4:1 resulted in more cake being formed on the membrane surface as well as an increase in the reduction of NO3 − from 64% to 78%. Preliminary calculations show that 2.4 to 3.2 g of suspended solids could be accumulated per square meter of membrane surface before physical cleaning of membrane is required (at a transmembrane pressure of 20 kPa).

Comparative study on performance of yeast and bacterial membrane bioreactors for high salinity wastewater treatment

Two laboratory-scale membrane bioreactor systems were investigated to treat high saline wastewater containing 1,000 mg/L COD and 32 g/L NaCl, namely: the yeast membrane bioreactor (YMBR) and the bacterial membrane bioreactor (BMBR). COD removal of both processes was above 90% at a hydraulic retention time (HRT) of 5 hours (volumetric loading of 5 kg COD/m³.d), sludge retention time (SRT) of 50 days (the MLSS of above 14 g/L and the F/M of 0.4 d-1). Under these operating conditions, the YMBR could run at a ten-fold lower transmembrane pressure with significantly reduced membrane fouling rate compared to BMBR. This may be because of low production of adhesive extracellular polymers (ECP) and the secondary filtration layer formed from large yeast cells. ECP production of bacterial sludge was increased considerably at high salt concentrations (32 g/L and 45 g/L) and long SRTs. For the bacterial sludge, the increased salinity led to increase in ECP, whereas the ECP content of the yeast sludge was relatively small.

Influence of particle size and size distribution in deep bed filtration and dynamic microfiltration

Particle size and size distribution is an important parameter in solid liquid separation process especially in granular bed filtration and in dynamic microfiltration. This paper discusses their effects on the above processes from extensive experimental data obtained. In granular bed filtration, the experimental results showed that the initial efficiency follows the pattern reported by previous experimental and theoretical studies, i.e., lower efficiency for particles which fall in the range of critical size of 1 m. However, the particle removal during the transient stage increased with an increase in particle size for the range of sizes studied. An attempt was made to quantify these effects in granular bed filtration using semi-empirical approach. In dynamic membrane filtration also, the particle size plays a major role in the retention. However, despite the relative thickness of the membrane (compared to particle size) dynamic microfiltration appears more as a sieving process; the retention is mainly related to the largest pore size.

Enhancement of the antifouling properties and filtration performance of poly(ethersulfone) ultrafiltration membranes by incorporation of nanoporous titania nanoparticles

Nanoporous titania nanoparticles (NTNs) were synthesized and used as an additive at a low concentration of 0.1-1 wt % in the fabrication of poly(ethersulfone) (PES) ultrafiltration membranes via non-solvent-induced phase separation. The structure and properties of nanoparticles were characterized using nitrogen sorption, X-ray diffraction, scanning electron microscopy, and transmission electron microscopy. The NTNs have a size distribution with a particle size of mainly <100 nm and have a Brunauer, Emmett, and Teller surface area of ∼100 m2 g-1. The modified membranes were fabricated and investigated in terms of their pure water flux, solute rejection, and fouling resistance. The water permeability and molecular weight cutoffs (MWCOs) of membranes were determined under constant-pressure filtration in dead-end mode at 100 kPa. The membrane fouling resistance was characterized under constant flux operation using bovine serum albumin as a model foulant. The membranes were characterized in terms of morphology, porosity, pore size distribution, energy-dispersive X-ray spectroscopy, contact angle goniometry, surface free energy, and viscosity of the dope solution. Overall, the modified membrane showed increased wettability and reduced surface free energy and pore size. The modified UF membrane with 0.5 wt % NTN loading exhibited improved fouling resistance (fouling rate of 0.58 kPa/min compared to a rate of 0.70 kPa/min for the control membrane) with ∼80% water flux recovery. The same membrane showed an ∼20% increase in water flux, an improvement in MWCO, and a narrower pore size distribution.

Demulsification of water/sunflower oil emulsions by a tangential filtration process using chemically impregnated ceramic tubes

A tangential filtration process was implemented in this study using porous ceramic tubes made of alpha-alumina produced by the slip-casting technique. These tubes were sintered at 1450 degrees C and characterized by mercury intrusion porosimetry, which revealed a mean pore size of 0.5 mu m. The tubes were chemically impregnated with a zirconium citrate solution, after which they were calcined and heat treated at temperatures of up to 600 and 900 degrees C to eliminate volatile organic compounds and transform the zirconium citrate into zirconium oxide impregnated in the alumina in the form of nanoparticle agglomerates. The microporous pipes were tested on a microfiltration hydraulic system to analyze their performance in the demulsification of sunflower oil and water mixtures. The fluid-dynamic parameters of Reynolds number and transmembrane pressure were varied in the process. The volume of permeate was analyzed by measuring the Total Organic Carbon concentration (TOC), which indicated 99% of oil phase retention. The emulsified mixture was characterized by optical microscopy, while the morphology and composition of the impregnated microporous tubes were analyzed by scanning electron microscopy (SEM). Quantification of the TOC values for the tube impregnated once at 600 degrees C showed the best demulsification performance, with the concentration on permeate smaller than 10 mg/L. The impregnated tube sintered once at 900 degrees C presented low carbon concentration (smaller than 20 mg/L), has the advantage of presenting the greatest trans-membrane flux in relation to the other microporous tube. (c) 2006 Elsevier B.V. All rights reserved.

Influence of membrane-solution interface on the selectivity of SnO2 ultrafiltration membranes

SnO2 supported membranes, presenting 3.0 nm average pore size, have been produced by sol casting on alumina tubular substrate using aqueous colloidal suspensions prepared by sol-gel route. The selectivity and flux throughout SnO2 membrane were analyzed by permeation experiments, using a laboratory tangential filtration pilot equipped with a monotubular membrane. To evaluate the effect of the surface charge at the membrane-solution interface, aqueous salt solutions (NaCl, Na2SO4, CaCl, and CaSO4) of different ionic strength have been filtered and the results correlated with the values of zeta potential measured at several pH. The results show that the retention coefficient is dependent on the electrolyte present in aqueous solution decreasing as: (dication, monoanion) > (monocation, monoanion) approximate to (monocation, dianion) > (dication, dianion). The surface charge and the cation adsorption capacity play a determinant role in these selectivity sequences. (C) 2001 Elsevier B.V. B.V. All rights reserved.

NADPH-CYTOCHROME P-450 REDUCTASE: EVIDENCE FOR TWO SEPARATE STRUCTURAL DOMAINS AND ISOLATION AND CHARACTERIZATION OF THE MEMBRANE ASSOCIATED SEGMENT

Homogenous detergent-solubilized NADPH-Cytochrome P-450 reductase was incorporated into microsomes and liposomes. This binding occurred spontaneously at temperatures between 4(DEGREES) and 37(DEGREES) and appeared to involve hydrophobic forces as the binding was not disrupted by 0.5 M sodium chloride. This exogenously-added reductase was active catalytically towards native cytochrome P-450, suggesting an association with the microsomal membrane similar to endogenous reductase. Homogeneous detergent-solubilized reductase was disaggregated by Renex-690 micelles, confirming the presence of a hydrophobic combining region on the enzyme. In contrast to these results, steapsin protease-solubilized reductase was incapable of microsomal attachment and did not interact with Renex-690 micelles. Detergent-solubilized reductase (76,500 daltons) was converted into a form with the electrophoretic mobility of steapsin protease-solubilized reductase (68,000 daltons) and a 12,500 dalton peptide (as determined by polyacrylamide-SDS gel electrophoresis) when the liposomal-incorporated enzyme was incubated with steapsin protease. The 68,000 dalton fragment thus obtained had properties identical with steapsin protease-solubilized reductase, i.e. it was catalytically active towards cytochrome c but inactive towards cytochrome P-450 and did not bind liposomes. The 12,500 dalton fragment remained associated with the liposomes when the digest was fractionated by gel filtration, suggesting that this is the segment of the enzyme which is embedded in the phospholipid bilayer. Thus, detergent-solubilized reductase appears to contain a soluble catalytic domain and a separate and separable membrane-binding domain. This latter domain is required for attaching the enzyme to the membrane and also to facilitate the catalytic interaction between the reductase and its native electron acceptor, cytochrome P-450. The membrane-binding segment of the reductase was isolated by preparative gel electrophoresis in SDS following its generation by proteolytic treatment of liposome-incorporated reductase. The peptide has a molecular weight of 6,400 as determined by gel filtration in 8 M guanidine hydrochloride and has an amino acid composition which is not especially hydrophobic. Following removal of SDS and dialysis out of 6 M urea, the membrane-binding peptide was unable to inhibit the activity of a reconstituted system containing purified reductase and cytochrome P-450. Moreover, when reductase and cytochrome P-450 were added to liposomes which contained the membrane-binding peptide, it was determined that mixed function oxidase activity was reconstituted as effectively as when vesicles without the membrane-binding peptide were used. Thus, the membrane-binding peptide was ineffective as an inhibitor of mixed function oxidase activity, suggesting perhaps that it facilitates catalysis by anchoring the catalytic domain of the reductase proximal to cytochrome P-450 (i.e. in the same mixed micelle) rather than through a specific interaction with cytochrome P-450. ^

Characterization of Spermidine Binding to Solubilized Plasma Membrane Proteins from Zucchini Hypocotyls1

In this work [14C]spermidine binding to total proteins solubilized from plasma membrane purified from zucchini (Cucurbita pepo L.) hypocotyls was investigated. Proteins were solubilized using octyl glucoside as a detergent. Specific polyamine binding was thermolabile, reversible, pH dependent with an optimum at pH 8.0, and had a Kd value of 5 μm, as determined by glass-fiber-filter assays. Sephadex G-25 M gel-filtration assays confirmed the presence of a spermidine-protein(s) complex with a specific binding activity. By sodium dodecyl sulfate-polyacrylamide gel electrophoresis and native polyacrylamide gel electrophoresis of collected fractions having the highest specific spermidine-binding activity, several protein bands (113, 75, 66, and 44 kD) were identified. The specificity of spermidine binding was examined by gel-filtration competition experiments performed using other polyamines and compounds structurally related to spermidine. Partial purification on Sephadex G-200 led to the identification of 66- and 44-kD protein bands, which may represent the putative spermidine-binding protein(s) on the plasmalemma.

Characterization of soluble and bound EPS obtained from 2 submerged membrane bioreactors by 3D-EEM and HPSEC

This research study deals with the quantification and characterization of the EPS obtained from two 25 L bench scale membrane bioreactors (MBRs) with micro-(MF-MBR) and ultrafiltration (UF-MBR) submerged membranes. Both reactors were fed with synthetic water and operated for 168 days without sludge extraction, increasing their mixed liquor suspended solid (MLSS) concentration during the experimentation time. The characterization of soluble EPS (EPSs) was achieved by the centrifugation of mixed liquor and bound EPS (EPSb) by extraction using a cationic resin exchange (CER). EPS characterization was carried out by applying the 3-dimensional excitation–emission matrix fluorescence spectroscopy (3D-EEM) and high-performance size exclusion chromatography (HPSEC) with the aim of obtaining structural and functional information thereof. With regard to the 3D-EEM analysis, fluorescence spectra of EPSb and EPSs showed 2 peaks in both MBRs at all the MLSS concentrations studied. The peaks obtained for EPSb were associated to soluble microbial by-product-like (predominantly protein-derived compounds) and to aromatic protein. For EPSs, the peaks were associated with humic and fulvic acids. In both MBRs, the fluorescence intensity (FI) of the peaks increased as MLSS and protein concentrations increased. The FI of the EPSs peaks was much lower than for EPSb. It was verified that the evolution of the FI clearly depends on the concentration of protein and humic acids for EPSb and EPSs, respectively. Chromatographic analysis showed that the intensity of the EPSb peak increased while the concentrations of MLSS did. Additionally, the mean MW calculated was always higher the higher the MLSS concentrations in the reactors. MW was higher for the MF-MBR than for the UF-MBR for the same MLSS concentrations demonstrating that the filtration carried out with a UF membrane lead to retentions of lower MW particles.

Environmental assessment of proton exchange membrane fuel cell platinum catalyst recycling

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