Tubular ultrafiltration flux prediction for oil-in-water emulsions: analysis of series resistances

Using the resistance-in-series (RIS) approach to permeate flux modeling, a general relationship between permeate flux, transmembrane pressure, cross-flow velocity, and feed kinematic viscosity was developed for the tubular ultrafiltration (UF) of synthetic oil-in-water emulsions. The fouling layer resistance, R_f, was 63% of the total membrane resistance, R_m′; however, concentration polarization was the predominant factor controlling resistance in the tubular UF system. An explicit form of the resistance index, Φ, was postulated based on the observed interactions between Φ, cross-flow velocity and feed kinematic viscosity and the RIS model was modified to further describe the interactions between permeate flux and operational parameters. The modified model adequately predicted flux–pressure data over the range of experimental variables examined in this study. Additionally, a set point operating pressure was determined as a function of cross-flow velocity and feed viscosity to achieve a balance between polarization and total membrane resistance.     

Modeling of the permeate flux decline during MF and UF cross-flow filtration of soy sauce lees

Cross-flow ultrafiltration and microfiltration have been used to recover refined soy sauce from soy sauce lees for over 25 years. The precise mechanism which dominated the permeate flux during batch cross-flow filtration has not been clarified. In the present study, we proposed a modified analytical method incorporated with the concept of deadend filtration to determine the initial flux of cross-flow filtration and carried out the permeate recycle and batch cross-flow filtration experiments using soy sauce lees. We used UF and MF flat membrane (0.006 m² polysulfone) module under different transmembrane pressures (TMP) and cross-flow velocities. The modified analysis provided an accurate prediction of permeate flux during the filtration of soy sauce lees, because this model can consider the change in J₀ at initial stage of filtration which was caused by the pore constriction and plugging inside membrane, and these changes may not proceed when the cake was formed on the membrane surface. Mean specific resistance of the cake increased with TMP due to the compaction of the cake and decreased with cross-flow velocity due to the change of deposited particle size, but less depended on the membrane in the present study. These results indicate that the value of J₀ determined by modified method was relevant to exclude the effects of the initial membrane fouling by pore constriction due to protein adsorption and plugging with small particles. The modified analytical method for the cake filtration developed in the present study was considered to be capable of selecting an appropriate operating conditions for many cross-flow filtration systems with UF, MF membranes.     

Self-forming dynamic membrane for ultrafiltration of pineapple juice

The formation of self-forming dynamic membrane on a porous ceramic support was studied. Pineapple juice of 12° Brix concentration was used in the experiments which were carried out at 25°C by circulating the pineapple juice at the applied pressure of 100, 200, and 300 kPa and at cross-flow velocities of 1.30–2.95 m s⁻¹ through the ceramic membrane module for 1 h. The experimental data of flux and rejections showed that the dynamic membrane was well-formed after 30 min of circulation under the applied pressure of 300 kPa and at a cross-flow velocity of 2.0 m s⁻¹ in which the steady values of flux and rejections of macromolecules and sugars obtained from the filtration mode were 6.0×10⁻³ m³/m² h, 84–87% and 6%, respectively. The corresponding values for ultrafiltration by alumina membrane of MW cut-off 50,000, using equivalent conditions, were 15.8×10⁻³ m³/m² h, 91% and 10.5%. Ultrafiltration was found to be more promising. The stability of the self-forming dynamic membrane was acceptable when subjected to change of filtration conditions. The permeation flux increased with cross-flow velocity and decreased when the applied pressure was reduced. The resistances for filtration by dynamic membrane and by ultrafiltration were calculated. For a porous support of large pore sizes, an in-pore blockage of solutes which were smaller than the membrane pores reduced the pore volume and induced fouling. Internal fouling resistance (R_f) was, therefore significant and responsible for the values of flux and rejection and was approximately 70% of total resistance. While in ultrafiltration, in which membrane with a smaller pore diameter was used, R_f was only 20% but R_p, the polarized layer resistance, was as high as 60% of total resistance.     

Controlled flux behaviour of membrane processes

Controlling ultrafiltration (UF) and microfiltration (MF) membrane fluxes at or around a region where fouling is minimal can provide an interesting and economic operating regime. Selectivity may be enhanced and cleaning may be easier. For a given flux it is sometimes possible to filter a product suspension at the same trans-membrane pressure (TMP) as for pure water (PWP), but this can require a lot of energy input to maintain cross-flow or high shear in other ways if high fluxes are required. The critical flux is the flux above which one starts to observe fouling. By operating at lower cross-flow velocities and just above the critical flux, and thus, with lower TMPs, periodic cleaning can be effected by temporarily stopping permeation. A change in feed rate demands a change in flux which is obtained by temporarily increasing energy inputs. Controlled flux improves macromolecular fractionation. As flux increases the rejection of high molecular weight materials decreases whilst that of lower molecular weight materials decreases. This paper discusses the causes of fouling and the use controlled flux operation to mitigate its effects.     

Microfiltration through an inorganic tubular membrane with high frequency retrofiltration

High frequency backpulsing is a promising technique of flux enhancement that could contribute to the development of cross-flow micro-/ultrafiltration in water and wastewater treatment. A systematic study of the influence of the operational parameters was carried out with three suspensions, bentonite in tap water, biologically treated wastewater and activated sludge. The alumina membranes were tubular (0.02, 0.05 or 0.2 μm), with internal or external skin, the latter being not suitable. The technique was particularly efficient for bentonite; a minimal cross-flow velocity was required to reach a net flux independent of the cross-flow. The results are less good for the biological suspensions since the same fluxes could be reached by an increase of cross-flow velocity. However, the energy required by high frequency backpulsing is lower. The average reverse fluxes, measured by a tracer method, are surprisingly high and could hamper the development of the technique. At low Reynolds number (Re=3500), the net flux increased with the reverse flux, then reached a plateau corresponding to the total penetration of the laminar layer against the membrane wall by the backwash water.     

Fouling of a ceramic microfiltration membrane by corn starch hydrolysate

The effect of operating parameters on fouling of a ceramic microfiltration membrane by corn starch hydrolysate of 95 dextrose equivalence was studied. Transmembrane pressures above 100 kPa had little or no effect on flux. Cross-flow velocity had a significant beneficial effect. The rate of flux decline was reduced significantly when the feed was adjusted from its natural pH of 4.2 to 10. However, this resulted in a dark brown clarified syrup (permeate). Scanning electron microscopy showed extensive fouling layers on the alumina surface with conventionally processed dextrose solutions and the least fouling layer with corn starch hydrolysate adjusted to pH 10. Maximum steady state flux for unconcentrated hydrolysate at its natural pH was 178 LMH obtained at low transmembrane pressures (103 kPa, 15 psi) and high cross-flow velocities (5 m s⁻¹). Adjustment of the pH to 10 can increase the flux by 40%.     

Yeast cells,beer composition and mean pore diameter impacts on fouling and retention during cross-flow filtration of beer with ceramic membranes

Clarification of rough beer (RB) and pasteurisation of clarified beer (CB) by cross-flow microfiltration (CFMF) stand as potential applications of membranes in the food industry. This study is based on the comparison of the resistances to mass transfer obtained during the filtration of RB and CB. Empirical correlations made it possible to calculate the CB resistances for the same conditions of transmembrane pressure and cross-flow velocity as for the RB filtration runs. The 1.4 μm membrane led to much lower resistances than the other membranes because of the lower retention rates of the beer compounds such as proteins and polyphenols. In this case, the predominant fouling mechanism was due to the yeast cell layer which was very sensitive to cross-flow velocity. On the other hand, with the 0.1, 0.45 and 0.8 μm membranes, the retention or adsorption of the CB compounds, such as proteins and polyphenols was the predominant mechanism. The resistances obtained with the rough and CB were fairly similar. We assume that the presence of yeast cells lead to less compact proteins and polyphenols fouling.     

The role of bentonite addition in UF flux enhancement mechanisms for oil/water emulsion

The main problem in treating oil/water emulsion from car wash waste-water by ultrafiltration (UF) is fouling caused by oil adsorption on the membrane surface and internal pore walls. This study demonstrates that the addition of bentonite clay can reduce the adsorption layer on cellulose acetate UF membrane, resulting in a reduction of total membrane resistance (R_t). Experiments were conducted to identify and describe three possible mechanisms: (i) bulk oil emulsion concentration reduction; (ii) particle aggregation and (iii) detachment of the adsorbed gel layer by shear force. Adsorption of oil emulsion by bentonite can lead to a significant reduction of bulk oil emulsion concentration, one of the major causes of flux enhancement. Results show that contact of oil emulsion with bentonite forms larger particles resulting in flux increment. An optimum particle size of 37 μm, corresponds with a bentonite concentration of 300 mg/l and provided the highest flux. Beyond this limiting concentration, flux improvement gradually declined, possibly due to the formation of packed cake of particles on the membrane surface. The presence of bentonite in the oil emulsion promotes high shear stress which acts against the gel layer. This high shear stress, caused by bentonite particles and cross-flow velocity, reverses the adsorbed gel layer to the bulk of the liquid phase.     

Synergetic cleaning procedure for a ceramic membrane fouled by beer microfiltration

Apart from considerations for hygienic operation, membrane cleaning is essential to maintain consistent permeability and selectivity of membrane systems for clarifying beer and beverages where balanced fractionation of particles/macromolecules is necessary. Experiments involved formulating and optimising chemical cleaning methods for a ceramic microfiltration membrane, which had been severely fouled during clarification of a commercial beer. The cleaning processes employed NaOH, HNO₃, H₂O₂, and Ultrasil 11 as the chemical cleaning agents. The cleaning ability and cleaning kinetics of the processes were evaluated in parallel with the study of the fouling mechanism, formation and strength so as to elucidate the synergetic relationship between fouling and cleaning. A three-step cleaning mechanism was postulated. This led to the development of a fast and effective combined simultaneous caustic cleaning and oxidation method (CSCCO), which was able to restore 87% of the original membrane's water permeability within 8 min. Analysis suggested the concept of a cleaning energy barrier E_c and a cleaning rate constant k_c0. This study confirmed the existence of a synergetic relationship between the prior fouling and optimum formulation of cleaner and optimal cleaning condition. The study varied beer filtration conditions. Transmembrane pressure (TMP) and crossflow velocity during fouling appeared to have a minimal effect on the membrane's subsequent cleanability, especially when the powerful CSCCO process was employed. The number of previous fouling/cleaning cycles was influential. A complete removal of the residual fouling, formed on the virgin membrane's surface proved beyond the means of the harsh chemical cleaning used under any conditions. The degree of residual fouling eventually reached a plateau and a level of 87% of the original water flux could be restored repeatedly.     

Optimum cleaning-in-place conditions for stainless steel microfiltration membrane fouled by terephthalic acid solids

Terephthalic acid (TPA) is a raw material of polyester fiber and polyethylene terephthalate. When TPA is produced by catalytic air oxidation of p-xylene in the presence of acetic acid solvent, most of produced TPA exists in the form of crystalline suspended solids. A microfiltration process may be used to recover TPA, but the microfilters are subjected to fouling and therefore cleaning-in-place (CIP) regimes need to be developed. In this research, the effects of variations to CIP conditions were investigated on the flux recovery accomplished in a TiO₂-sintered stainless steel microfiltration membrane (0.1 μm pore size) fouled with TPA. The extent of flux recovery was estimated as the ratio of the stabilized flux obtained during CIP to the water flux value achieved under corresponding operational conditions. Based upon batch solubility tests, sodium hydroxide (NaOH) was chosen as the major cleaning agent for the present experiment. The extent of flux recovery increased with increasing NaOH concentration over the range of 3–4% (w/v) NaOH, but decreased at NaOH concentrations above 4%. The flux recovery was favored at high cross-flow velocities, high temperatures and low transmembrane pressures. A high temperature run of cleaning did not produce any adverse effects up to 70 °C. The addition of surfactants (SDS and Tween 80) to the caustic cleaning agent led to a significant reduction in cleaning efficiency.     

Membrane fouling in a submerged membrane bioreactor (MBR) under sub-critical flux operation: Membrane foulant and gel layer characterization

Membrane foulants and gel layer formed on membrane surfaces were systematically characterized in a submerged membrane bioreactor (MBR) under sub-critical flux operation. The evaluation of mean oxidation state (MOS) of organic carbons and Fourier transform infrared (FT-IR) spectroscopy demonstrated that membrane foulants in gel layer were comprised of not only extracellular polymeric substances (EPS) (proteins, polysaccharides, etc.) but also other kinds of organic substances. It was also found that fine particles in mixed liquor had a strong deposit tendency on the membrane surfaces, and membrane foulants had much smaller size than mixed liquor in the MBR by particle size distribution (PSD) analysis. Gel filtration chromatography (GFC) analysis showed that membrane foulants and soluble microbial products (SMP) had much broader distributions of molecular weight (MW) and a larger weight-average molecular weight (M_w) compared with the influent wastewater and the membrane effluent. Scanning electron microscopy (SEM) and energy-diffusive X-ray (EDX) analysis indicated that membrane surfaces were covered with compact gel layer which was formed by organic substances and inorganic elements such as Mg, Al, Fe, Ca, Si, etc. The organic foulants coupled the inorganic precipitation enhanced the formation of gel layer and thus caused membrane fouling in the MBR.     

Microfiltration performance of regenerated cellulose membrane prepared at low temperature for wastewater treatment

A series of regenerated cellulose membranes with pore diameters ranging from 21 to 52 nm have been prepared by dissolving cellulose in 5 wt% LiOH/12 wt% urea aqueous solution re-cooled to −12 °C. The influences of cellulose concentration on the structure, pore size, and the mechanical properties of the membrane were studied by using Wide angle X-ray diffraction, scanning electron micrography and tensile testing. Their pore size, water permeability, equilibrium-swelling ratio and fouling behaviors of the cellulose membranes were characterized. The water-soluble synthetic and natural polymers as organic matter were used to evaluate the microfiltration performance of the regenerated cellulose membrane for wastewater treatment in aqueous system. The results revealed that the organic matter with molecular weight more than 20 kDa effected significantly on the membrane pore density, and reducing factor a _2, whereas that having molecular weight less than 20 kDa exhibited a little influence on the membrane pore size reducing factor a ₁. Furthermore, a simple model to illustrate of microfiltration process of the RC membrane for wastewater treatment was proposed.     

A model for determining the steady state flux of inorganic microfiltration membranes

The present paper provides a model based on dimensional analysis that gives the basis for design of the cross-flow microfiltration processes. This gives the permeate flux f in terms of the pressure drop across the filtration membrane ΔP and the velocity V of cross-flow of the feed fluid in the membrane tubes. The model is compared with an extensive series of experimental results with magnesium hydroxide slurries. The model has certain similarities with previous ones and can be used for unit optimization.     

Stereoselective total synthesis of almorexant

A highly stereoselective synthesis of almorexant has been achieved using (R)-tert-butanesulfinamide as a chiral source. The chiral tetrahydroisoquinoline core was constructed through allylation of chiral N-sulfinyl imine followed by ring closure of the secondary amide with a tethered halide. The chiral α-phenyl amide was introduced by means of S_N2 substitution of (S)-methyl 2-phenyl-2-(tosyloxy)acetate with chiral tetrahydroisoquinoline.     

Studies on secondary layer formation and its characterization during cross-flow filtration of microbial cells

The formation of membrane sublayers during cross-flow filtration was studied with a standardized E. coli suspension both in a tubular and a flat channel module with different membrane materials. The height of the layers was calculated for different experimental conditions. Transmembrane pressure, cross-flow velocity, compressibility of the suspended particles, properties of the suspension, particle size and concentration were all found to have a significant effect on the formation of membrane sublayers. A decrease of the layer thickness and corresponding filtration resistance with increasing channel length was observed due to the longitudal transmembrane pressure gradient. The filtration resistance of the layer is found to be the dominant factor determining the flux rate.     

Fouling of nanofiltration membranes used for separation of fermented glycerol solutions

In this study, the glycerol solutions were fermented using Lactobacillus casei bacteria. The broths were pre-treated by microfiltration, followed by a further separation with nanofiltration. The latter process was carried out in two stages, using the NF270 and NF90 membranes, respectively. The concentrates thus obtained were enriched with citric acid (first stage) and then with lactic acid and glycerol (second stage). By means of SEM and AFM microscopy, as well as ATR-FTIR analysis, the intensity of membrane-fouling was studied. The colloidal fouling and bio-fouling caused a more than two-fold decrease in the permeate flux during microfiltration of the broth. This pre-treatment stage was effective, and a permeate turbidity of less than 0.2 NTU was obtained. However, the nanofiltration membranes exhibited a 30 % flux decline over the course of the process, mainly due to the organic fouling.     

Flux decline in crossflow microfiltration and ultrafiltration: experimental verification of fouling dynamics

The theory of fouling dynamics in crossflow membrane filtration is compared with ultrafiltration experiments with suspensions of 0.12 μm silica colloids. It has been experimentally verified that colloidal fouling in crossflow filtration is a dynamics process from non-equilibrium to equilibrium and that the steady state flux is the limiting flux. With the cake concentration c_g identified from an independent experiment and the specific cake resistance calculated by Carman–Kozeny equation, the time-dependent flux and the time to reach steady state in the experiments of this study are correctly predicted with the theory of fouling dynamics.     

Practical and highly stereoselective method for the preparation of several chiral arylsulfinamides and arylsulfinates based on the spontaneous crystallization of diastereomerically pure N-benzyl-N-(1-phenylethyl)-arylsulfinamides

A novel and simple process for the preparation of enantiomerically pure (S_S)-benzenesulfinamide (S_S)-3a, (S_S)-p-toluenesulfinamide (S_S)-3b, (S_S)-p-chloro-benzenesulfinamide (S_S)-3c and (S_S)-p-fluorobenzenesulfinamide (S_S)-3d has been developed. The treatment of arylsulfinyl chlorides with (R)-N-benzyl-1-phenylethanamine in the presence of excess triethylamine gave diastereomeric mixtures of N-benzyl-N-(1-phenylethyl)-arylsulfinamides 1, which underwent spontaneous crystallization to furnish diastereomerically pure (R,S_S)-N-benzyl-N-(1-phenylethyl)-arylsulfinamides (R,S_S)-1a-1d in 28%, 29%, 27% and 31% yields, respectively. The diastereomerically pure compounds (R,S_S)-1 were then converted into four enantiopure (R_S)-methyl arylsulfinates (R_S)-2, and finally into four enantiopure (S_S)-arylsulfinamides (S_S)-3 in good yields.     

Base and catalyst-free synthesis of nitrobenzodiazepines via a cascade N-nitroallylation-intramolecular aza-Michael addition involving o-phenylenediamines and nitroallylic acetates

A [4+3] annulation of o-phenylenediamines with primary nitroallylic acetates affords nitrobenzodiazepines (NBDZs) in good to excellent yield. The reaction which proceeds in MeOH at room temperature in the absence of any base or catalyst involves a cascade S_N2 N-nitroallylation-intramolecular aza-Michael addition sequence. In the case of mono-N-arylated o-phenylenediamines and o-aminobenzamides, the reaction stops at the S_N2 stage affording nitroallylic amines. On the other hand, reaction of o-aminobenzamides with secondary nitroallylic acetates delivers S_N2′ products. Formation of stable S_N2 and S_N2′ products provides insights into the reactivity of primary and secondary nitroallylic acetates and also the mechanism of formation of nitrobenzodiazepines.     

A CNDO/2 approach to electron delocalization in N4S4 and N4S4F4

The electronic structure of N₄S₄ and N₄S₄F₄ molecules is investigated within the framework of the CNDO/2 approximation. A pure alternated system is obtained for the fluorinated compound with respect to the Wiberg bond populations. On the other hand, the N₄S₄ molecule appears to be composed of three highly delocalized “islands”, as defined by Dewar in the case of cyclophosphazenes. The “tub form” of N₄S₄ is due to a strong spatial interaction between non-bonded sulphur atoms and, for this reason, the N₄S₄ molecule may be called the “inorganic cyclooctatetraene”.