Transmembrane Pressure Difference Research Articles

Beer Clarification by Novel Ceramic Hollow-Fiber Membranes: Effect of Pore Size on Product Quality.

In this work, the crossflow microfiltration performance of rough beer samples was assessed using ceramic hollow-fiber (HF) membrane modules with a nominal pore size ranging from 0.2 to 1.4 μm. Under constant operating conditions (that is, transmembrane pressure difference, TMP = 2.35 bar; feed superficial velocity, vS = 2.5 m/s; temperature, T = 10°C), quite small steady-state permeation fluxes (J* ) of 32 or 37 L/m2 /h were achieved using the 0.2- or 0.5-μm symmetric membrane modules. Both permeates exhibited turbidity <1 EBC unit, but a significant reduction in density, viscosity, color, extract, and foam half-life with respect to their corresponding retentates. The 0.8-μm asymmetric membrane module might be selected, its corresponding permeate having quite a good turbidity and medium reduction in the aforementioned beer quality parameters. Moreover, it exhibited J* values of the same order of magnitude of those claimed for the polyethersulfone HF membrane modules currently commercialized. The 1.4-μm asymmetric membrane module yielded quite a high steady-state permeation flux (196 ± 38 L/m2 /h), and a minimum decline in permeate quality parameters, except for the high levels of turbidity at room temperature and chill haze. In the circumstances, such a membrane module might be regarded as a real valid alternative to conventional powder filters on condition that the resulting permeate were submitted to a final finishing step using 0.45- or 0.65-μm microbially rated membrane cartridges prior to aseptic bottling. A novel combined beer clarification process was thus outlined.

Mass transfer and selectivity analysis of a dense membrane contactor for upgrading biogas

The mass transfer of a dense membrane contactor for the removal of CO2 from a biomethane-CO2 mixture was investigated in detail. Pure gas CO2 experiments as well as mixed gas experiments were conducted in order to determine the transmembrane flux and the selectivity of the contactor as a function of the pressure level and the transmembrane pressure difference. Two membranes, a PDMS coated and a Teflon-AF coated composite flat-sheet gas permeation membrane (PolyActive™) were tested in the self-constructed membrane module. The mass transfer was analyzed using a rigorous mass transfer model. With this model, it was possible to determine the mass transfer resistance of the membrane and the liquid boundary layer. It was found that both resistances do significantly contribute to the overall mass transfer resistance that is governing the membrane flux and the selectivity of the dense membrane contactor. Nevertheless, an increased driving force due to an increased pressure difference across the membrane could easily compensate for the additional mass transfer resistance of the membrane. A transmembrane pressure difference of up to two bars and absorbent liquid phase pressures at the permeate side of up to five bars were applied. It could be shown that a higher permeate pressure and a large transmembrane pressure difference is favorable for both, the permeance and the selectivity of the dense membrane contactor.

Elastic free-standing RTIL composite membranes for CO2/N2 separation based on sphere-forming triblock/diblock copolymer blends

Solvent-free, melt-state self-assembly of sphere-forming polystyrene-b-poly(ethylene oxide) diblock copolymer/polystyrene-b-poly(ethylene oxide)-b-polystyrene triblock copolymer (SO/SOS) blends was used to produce free-standing, room-temperature ionic liquid (RTIL) composite membranes with excellent mechanical properties and CO2/N2 separation performance. Membranes were prepared from vitrified SO/SOS diblock/triblock melts by swelling to greater than 94wt% 1-ethyl-3-methylimidazolium bis(trifluoromethylsulfonyl)imide ([EMIM][TFSI]) ionic liquid. These free-standing composite membranes were evaluated for their CO2/N2 separation performance over a range of transmembrane pressures (26-413 kPa), with results traversing the 2008 Robeson upper bound. Even with such high loadings of neat [EMIM][TFSI], these membranes exhibit the mechanical properties of solid elastomers, evident by the ultimate tensile strength of 250kPa and the compressive modulus at 40% strain of 348kPa for the membranes with 46% triblock copolymer content (SOS46). Cyclic loading and unloading in both tension and compression revealed reversible elasticity, with no mechanical property degradation or permanent hysteresis detected. For each composition studied, membrane failure occurred at uniaxial extension ratios of 3.8. The CO2 permeability performance of these membranes was stable for 28 days of testing with no detectable RTIL leakage. Transmembrane pressures exceeding 400kPa could be accommodated, with cyclic application of transmembrane pressure differentials at 230kPa producing neither plastic deformation nor diminished performance in gas separations. Such behavior is intimately tied to the highly distensible and elastic nature of the melt-assembled diblock/triblock network underpinning this RTIL-based composite membrane design.

How can osmosis and solute diffusion be coupled for the simultaneous measurement of the solvent and solute permeabilities of membranes?

A novel experimental method and its associated model are proposed for the simultaneous determination of membrane solute and solvent permeabilities, which are essential transport parameters of reverse osmosis models used for process simulation. The method utilizes a single bench-scale batch apparatus consisting of two stirred half-cells containing solutions of different concentrations separated by a membrane across which coupled non-steady-state solute diffusion and solvent osmosis take place countercurrently in the absence of transmembrane pressure difference. Results are presented from days-long determinations of the water and sodium chloride permeabilities of Filmtec BW30 and NF270 membrane samples for initial transmembrane salt concentration differences ranging from 1gL−1 to 35gL−1. When used as input parameters for the simulation of pilot reverse osmosis desalination tests, the osmotic-diffusive salt permeabilities approximated the experimental rejection rates.

Towards the potential of cyano and amino acid-based ionic liquid mixtures for facilitated CO2 transport membranes

Aiming at developing improved liquid phases for facilitated CO2 separation from post-combustion processes through supported ionic liquid membranes (SILMs), this work explores the use of binary equimolar IL mixtures containing a common imidazolium cation combined with tricyanomethane and five amino acid-based anions, glycinate, l-alaninate, taurinate, l-serinate and l-prolinate. The CO2 and N2 permeation properties of the prepared SILMs were determined at T=318.15K and several trans-membrane pressure differentials. The results indicate that as the trans-membrane pressure differential decrease, the CO2 permeability through the SILMs containing the IL mixtures approaches or even surpasses that of the pure [C2mim][C(CN)3]. Similarly, the CO2/N2 permselectivity significantly increases, meaning that the prepared IL mixtures work as CO2 carriers under low trans-membrane pressure differentials, facilitating the flux of CO2 through SILMs. In particular, large CO2 permeabilities and high CO2/N2 permselectivities were obtained for the IL mixtures containing l-alaninate and taurinate anions, indicating that they can be considered as promising and efficient liquid phases for facilitated CO2 separation.

Multichannel Tubular Ceramic Membrane for Water and Heat Recovery from Waste Gas Streams

For the first time, we report a multichannel ceramic tubular membrane for water and heat recovery from gas streams. Mass and heat transfer performances of the multichannel tubular membrane are systematically investigated and compared with those of a monochannel tubular membrane. Compared with the monochannel tubular membrane, the multichannel membrane has much larger mass and heat transfer resistances, leading to lower mass and heat transfer rates. Operational parameters (e.g., fluid velocities and transmembrane pressure difference) have insignificant effects on mass and heat transfer in the multichannel membrane, suggesting that transfer resistance from the membrane itself rather than the boundary layers dominates mass and heat transfer in membrane condensation. The multichannel membrane shows larger volumetric mass and heat transfer coefficients, comparable water recoveries, but lower heat recoveries compared with the monochannel tubular membrane. Water and heat recoveries exhibit a proportional correla...

An initial investigation of a nano-composite silica ceramic membrane for hydrogen gas separation and purification

The effects of trans-membrane pressure difference on hydrogen recovery are investigated on a preliminary basis. The membrane has been developed for high temperature hydrogen separation from CH4, N2, and Ar gas molecules. Gas permeation and separation performance of the developed membrane was evaluated. The silica fabricated membrane exhibited high H2 gas flux and much lower fluxes for CH4, N2, and Ar and showed a rise in permeance with the inverse of the square root of temperature for H2. Plots obtained with respect to the effects of gauge pressure on H2, N2, CH4 and Ar component gas fluxes through the modified support (silica membrane) at a pressure of 1 bar showed that H2 recorded an almost four-fold high flux value of 0.76 mol/m2.s compared to that of 0.33 mol/m2.s (CH4), 0.25 mol/m2.s (N2) and 0.22 mol/m2.s (Ar). These results were nearly stable for the temperature range investigated (298 K, 373 K and 473 K). In addition, hydrogen maintained a relatively high permeance value of 1.62 × 10−5 mol m−2 s−1 Pa−1 at a low pressure of 0.1 bar under room temperature (298 K) compared to that of N2, CH4 and Ar which were much lower throughout the temperature range studied and in agreement with literature. H2 separation factor (experimental Knudsen) over CH4, N2 and Ar were quite close to the theoretical Knudsen and can therefore be experimentally applied through further optimization in the separation of H2 as a key constituent energy for the future.

Integrated membrane process for purification and concentration of aqueous Syzygium cumini (L.) seed extract

The aim of the present study was to investigate the potentiality of an integrated membrane process for the purification and the concentration of phenolic compounds from aqueous jamun (Syzygium cumini L.) seed extract. The aqueous seed extract obtained at optimal condition (temperature: 49.2°C, time: 89.4min, and liquid to solid ratio: 51.6:1mL/g) was submitted to cross flow ultrafiltration for initial clarification, followed by concentration using nanofiltration under batch concentration mode. A detailed parametric study was carried out to investigate the effect of various process parameters such as transmembrane pressure, cross-flow velocity (or stirrer speed) on the permeate flux and permeate quality. Using classical film theory, a steady state gel polarization model incorporating the effect of transmembrane pressure difference and viscosity variation was proposed for the prediction of permeate flux during cross flow ultrafiltration of aqueous seed extract. The predicted flux values were successfully compared with the experimental results. Experimental results showed that the operating conditions had significant effect on permeate flux, recovery of polyphenols, purity and antioxidant activity of phenolic extract. Ultrafiltration experiments at lower operating pressures (276 and 414kPa) using 100kDa membrane resulted in the recovery of 59–66.7% of total polyphenol content in the clarified extract with the purity of 49–58.3% starting from an extract purity of 39.2%. The clarified extract could be successfully concentrated about three times higher using 250Da nanofiltration membrane at volume concentration ratio of three. The present study revealed that the UF/NF integrated membranes process was successful in clarifying and concentrating phenolic extract obtained from jamun seed with enhanced purity and antioxidant activity.

Pale Lager Clarification Using Novel Ceramic Hollow-Fiber Membranes and CO2 Backflush Program

In this work, the cross-flow microfiltration (CFMF) performance of a rough pale lager, produced in the industrial brewery Birra Peroni Srl (Rome, Italy), was assessed in a bench-top rig, equipped with a 0.8-μm ceramic hollow-fiber membrane module, to overcome the recognized inefficacy of back-flushing cleaning techniques in ceramic multi-channel monolithic modules. In total recycle CFMF trials, as the transmembrane pressure difference (TMP) was increased from 0.59 to 3.56 bar, the quasi-steady-state permeation flux (J*) tended to a limiting value increasing with the cross-flow velocity (v S). To minimize the overall membrane surface to be installed for a prefixed permeate recovery, it was found to be expedient to operate at the aforementioned high cross-flow velocity and TMP of 3.56 bar, thus obtaining quite a high quasi-steady-state permeation flux (mean, μ = 173 L m−2 h−1; standard deviation, sd = 7 L m−2 h−1; number of observations, N = 12). The energy consumption per liter of permeate collected was found to be practically independent of the operating variables v S and TMP selected (μ = 55 W h L−1; sd = 2 W h L−1; N = 21). Yet, a permeate flux greater than 100 L m−2 h−1 was achieved on condition that TMP was greater than 2 bar and v S varied from 4 to 6 m s−1. A few validation batch CFMF tests, carried out using pre-centrifuged, PVPP-stabilized, and cartridge-filtered rough pale lager at TMP = 3.56 bar, v S = 6 m s−1, and 10 °C under a predefined CO2 backwashing program, resulted in an average permeation flux (μ = 239 L m−2 h−1; sd = 24 L m−2 h−1; N = 2) by far greater than that (50–100 L m−2 h−1) claimed at 0–2 °C by the three CFMF processes commercially available. Finally, it was proved the easy transferability of the lager beer clarification and stabilization process, previously developed in a single-tube membrane module, to a ceramic hollow-fiber membrane module industrially upscalable.

Preparation of ZIF-69 membranes for gasoline vapor recovery

The compact ZIF-69 membranes have been prepared by seeded growth method for the recovery of gasoline vapor which is a major challenge in the petrochemical industry. The membrane performances for separating N2/n-alkane mixtures at various operating conditions (e.g. trans-membrane pressure difference, operating temperature, feed concentration, and stage cut) were systematically investigated. The highest separation factor was 2.60 with the corresponding permeance of 5.02 × 10−8 mol/(m2 s Pa) for the N2/n-C6H14 model mixtures. Moreover, the effects of n-alkane components (n-C5H12, n-C6H14, and n-C7H16) on the separation performances were studied, and the separation factors followed α(N2/n-C7H16) > α(N2/n-C6H14) > α(N2/n-C5H12), due to the different adsorption capacities of n-alkanes on ZIF-69 materials. The present work demonstrates that the ZIF-69 membrane is a highly promising candidate for the application in gasoline vapor recovery.

Separation of CO2 from humidified ternary gas mixtures using thermally rearranged polymeric membranes

The recently developed thermally rearranged (TR) polymeric membranes displayed superior gas separation properties over conventional polymeric membranes, owing to the presence of micro-pores appropriately tuned in cavities size and distribution, thus offering great advantages in gas separation applications, especially in CO2 capture from post-combustion flue gas streams.In this work, the transport properties (flux, permeance and selectivity) of TR polymeric hollow fiber membranes were evaluated with both single gases (CO2, N2, O2) and ternary gas mixture (CO2:N2:O2=15:80:5) at different temperatures (25, 50, 75°C) and trans-membrane pressure differences (2–5bar). The results revealed that the CO2 permeance measured under the mixed-gas condition remained the same as the single gas CO2 permeance, while the permeances of other gases decreased, thus leading to a favored increase in selectivity.The effect of water vapor in a ternary gas mixture was studied for the first time, considering that most of the streams of interest contain large amount of water. The presence of water vapor induced a significant permeance decrease for all the three components and a negligible reduction in selectivity. Globally the membranes showed good performance in the whole range of operating conditions investigated.

Development of thin-film composite PRO membranes with high power density

Pressure retarded osmosis (PRO) has recently attracted much attention as a promising alternative energy technology to overcome the problems posed by fossil fuel consumption and greenhouse gas emissions. PRO is a process of generating power using the energy potential that arises from the difference in concentration between two solutions separated by a selective semipermeable membrane. In order to commercialize PRO, new methods for producing high-performance PRO membranes must be developed. The power density of a PRO membrane, calculated as the product of osmotically induced water flux and the transmembrane hydraulic pressure difference, is the key performance measure for these membranes. This study aims to improve membrane components and to develop a polyamide composite PRO membrane with a high power density. To this end, we determined the characteristic factors of a PRO membrane that contribute to increase the osmotically induced water flux and estimated their effect on the power density.

Ultrathin Pd Films on PBI-HFA Membranes for Selective Hydrogen Separation

A polymeric gas separation membrane utilizing polybenzimidazole (PBI) based on 4,4'-(hexafluoroisopropylidene)bis(benzoic acid) (HFA) with an effective permeating area of 8.3 cm2 and a thickness of 30(± 2) mm was prepared and its gas permeation properties were investigated using H2, CO2, CO, and N2 at various temperatures ranging from 24 to 200 oC. The PBI-HFA membrane not only exhibited excellent H2 permeability, but it also displayed superior gas separation performance particularly for H2/N2 and H2/CO2. The permeation parameters for both permeability and selectivity ( PH2 and α(H2/N2); PH2 and α(H2/CO2)) obtained for the new material were found to surpass those reported by Robeson in 2008. The gas permeation properties of the prepared membrane were found to be dependent on trans-membrane pressure difference as well as temperature. A gas-tight palladium (Pd) membrane was fabricated on a PBI-HFA membrane by a vacuum electroless plating technique (VELP). The thickness and effective permeating area of the Pd/PBI-HFA membrane were estimated in the range of 228–261 nm, and 8.3 cm2, respectively. The Pd membrane prepared using the VELP technique had a more uniform microstructure than those manufactured by a conventional electroless plating method (CELP), with no delamination or agglomerated Pd particles observed. The gas permeation properties of the prepared Pd membranes were evaluated using H2, N2, CO2, and CO as functions of:35 to 200 °C temperature, 0.4 to 0.8 MPa pressure difference, and membrane preparation methods including CELP, VELP, and VELP following a H2O2 surface treatment (H-VELP). The Pd film fabricated by the H-VELP method showed superior performance, and proved to be impermeable to nitrogen as well as carbon monoxide. Additionally, the Pd membranes prepared by H-VELP with a 228 nm thickness also demonstrated an excellent gas tightness with an infinite H2/N2 permselectivity, and its separation performance was above the Robeson’s 2008 upper bound.

Transport membrane condenser for water and heat recovery from gaseous streams: Performance evaluation

Using a tubular ceramic membrane as the transport membrane condenser for simultaneous water and heat recovery from gaseous streams is experimentally investigated in the current study. The effects of several important operational parameters (e.g. gas flow rate, coolant flow rate, transmembrane pressure and inlet gas temperature) on the process performance in terms of mass and heat transfer across the membrane are systematically studied. It is found that mass and heat transfer rates can be enhanced by increasing the gas flow rate, coolant water flow rate and the temperature of the inlet gas stream. To improve the water and heat recovery, a low gas flow rate but a high coolant flow rate should be maintained. Increasing the transmembrane pressure difference decreases the mass and heat transfer mainly due to the reduced inlet gas humidity, enthalpy and flow rate. However, water and heat recovery does not change significantly with the change in transmembrane pressure. 20–60% water recovery and 33–85% heat recovery are achievable when using cold water as the coolant. The mass transfer mechanism in membrane condensation is complex and needs further exploration. These findings offer significant implications in using transport membrane condensers for water and heat recovery from gas streams with high moisture.

Partial oxidation of methane using silver/gadolinia-doped ceria composite membranes

Methane was partially oxidised to CO using oxygen permeated through a 1 mm thick silver/Ce0.9Gd0.1O2−x (Ag/CGO) composite membrane operating at 500–700°C with air at 1bar pressure. The membranes were fabricated by sintering ultrafine nanoparticles of gadolinia-doped ceria (<5nm) coated with silver using Tollens׳ reaction. This unique combination led to dense composites with low content of silver (7vol%), no reaction between the components and predominant metallic conductivity. When feeding 4% methane at 700°C to a 1-mm thick Ag/CGO using Ni as reforming catalyst, the conversion reached 21% and the CO selectivity 92% with an estimated oxygen flux of 0.18mLmin−1cm−2 (NTP). The samples were stable in carbon-containing atmospheres and under a large pO2 transmembrane pressure difference at temperatures below 700°C for 48h.

Anaerobic/aerobic treatment of greywater via UASB and MBR for unrestricted reuse.

The aim of the present study was to investigate the efficiency of integrated up-flow anaerobic sludge blanket (UASB) as anaerobic system followed by membrane bioreactor (MBR) as aerobic system for the treatment of greywater for unrestricted reuse. Pilot-scale UASB and MBR units were installed and operated in the NRC, Egypt. Real raw greywater was subjected to UASB and the effluent was further treated with microfiltration MBR. The necessary trans-membrane pressure difference is applied by the water head above the membrane (gravity flow) without any energy input. The average characteristics of the raw greywater were 95, 392, 298, 10.45, 0.4, 118.5 and 28 mg/L for total suspended solids (TSS), chemical oxygen demand (COD), biochemical oxygen demand (BOD), total phosphates, nitrates, oil and grease, and total Kjeldahl nitrogen (TKN), respectively. The pH was 6.71. The UASB treatment efficiency reached 19.3, 57.8, 67.5 and 83.7% for TSS, COD, BOD5 and oil and grease, respectively. When the UASB effluent was further treated with MBR, the overall removal rate achieved 97.7, 97.8, 97.4 and 95.8% for the same parameters successively. The characteristics of the final effluent reached 2.5, 8.5, 6.1, 0.95, 4.6 and 2.3 mg/L for TSS, COD, BOD, phosphates, oil and grease and TKN, respectively. This final treated effluent could cope with the unrestricted water reuse of local Egyptian guidelines.

Stability investigation of micro-configured Pd–Ag membrane modules – Effect of operating temperature and pressure

The long-term stability over a period of up to 50 days has been reported for various designs of microstructured Pd77Ag23 membrane modules for H2 production and purification. Even though microchannels provide sufficient mechanical support for moderate trans-membrane pressure difference and temperatures, i.e., 4–5 bars and 400–450 °C, long-term operation under these operating conditions results in a large deformative settling of the Pd77Ag23 film into the microchannel support. This settling leads to microstructural changes and pore formation on the feed surface of the membrane film that ultimately results in membrane failure. For pressures above approximately 5 bars, the application of microchannel-supported modules is thus not feasible, and for that purpose a continuous porous stainless steel support is introduced that allows for a sufficient stabilisation of the thin Pd77Ag23 films. For such a porous stainless steel supported microchannel module, a hydrogen flux of 195.3 mL cm−2 min−1 is obtained at 450 °C and 5 bars feed pressure, corresponding to a permeability of 3.4·10−8 mol m−1 s−1 Pa−0.5. During the complete operation of 1100 h at 450 °C, the module shows a very good stability up to the highest feed pressure applied of 15 bars. The N2 leakage flux has remained below the detection limit of the equipment, 5 μL cm−2 min−1, resulting in a minimum value for the H2/N2 permselectivity of 39.000 applying the pure H2 flux value obtained at 5 bars.

Recycling of Indium From CIGS Photovoltaic Cells: Potential of Combining Acid-Resistant Nanofiltration with Liquid–Liquid Extraction

Electronic consumer products such as smartphones, TV, computers, light-emitting diodes, and photovoltaic cells crucially depend on metals and metalloids. So-called "urban mining" considers them as secondary resources since they may contain precious elements at concentrations many times higher than their primary ores. Indium is of foremost interest being widely used, expensive, scarce and prone to supply risk. This study first investigated the capability of different nanofiltration membranes of extracting indium from copper-indium-gallium- selenide photovoltaic cell (CIGS) leachates under low pH conditions and low transmembrane pressure differences (<3 bar). Retentates were then subjected to a further selective liquid-liquid extraction (LLE). Even at very acidic pH indium was retained to >98% by nanofiltration, separating it from parts of the Ag, Sb, Se, and Zn present. LLE using di-(2-ethylhexyl)phosphoric acid (D2EHPA) extracted 97% of the indium from the retentates, separating it from all other elements except for Mo, Al, and Sn. Overall, 95% (2.4 g m(-2) CIGS) of the indium could be extracted to the D2EHPA phase. Simultaneously, by nanofiltration the consumption of D2EHPA was reduced by >60% due to the metal concentration in the reduced retentate volume. These results show clearly the potential for efficient scarce metal recovery from secondary resources. Furthermore, since nanofiltration was applicable at very low pH (≥ 0.6), it may be applied in hydrometallurgy typically using acidic conditions.

Facilitated separation of CO2 and SO2 through supported liquid membranes using carboxylate-based ionic liquids

The facilitated separation of CO2 and SO2 in a series of supported ionic liquid membranes (SILMs) impregnated with carboxylate-based ILs (including monocarboxylates and dicarboxylates) was investigated systematically under humidified condition. The effects of transmembrane pressure difference and temperature on the permeability of acidic gases and permselectivity of gas pairs were studied. It is found that dicarboxylate-based ILs are a class of tunable media for the selective separation of acidic gases. When the anions of dicarboxylate-based ILs are fully deprotonated, they could be used as effective carriers for the selective separation of CO2. The permeabilities of CO2 in triethylbutylammonium malonate ([N2224]2[malonate]) and triethylbutylammonium maleate ([N2224]2[maleate]) under the partial pressure of 0.1bar range from 2147 to 2840barrers and the permselectivities of CO2/N2 and CO2/CH4 in them approach to 178–265 and 98–221, respectively. However, when the anions of dicarboxylate-based ILs are half deprotonated, they are efficient solvents for the selective separation of SO2. Triethylbutylammonium dimalonate ([N2224][dimalonate]) could facilitate the permeation of SO2 with a permeability of 7208barrers under the transmembrane pressure difference of 0.05bar, and the permselectivities of SO2/N2, SO2/CH4 and SO2/CO2 are 585, 271 and 18, respectively. The mechanism of facilitated separation is explained successfully from the reversible reactions of CO2 and SO2 with different forms of dicarboxylate-based ILs.

Novel cold sterilization and stabilization process applied to a pale lager

In this work, the crossflow microfiltration (CFMF) performance of different lots of a rough pale lager, produced in the industrial brewery Birra Peroni Srl (Rome, Italy), was assessed in a bench-top plant, equipped with a 0.8-μm ceramic tubular membrane module, under constant crossflow velocity (6ms−1), transmembrane pressure difference (3.74bar), temperature (10°C), and periodic CO2 backflushing. The average permeation flux increased from (86±8) to (252±21) Lm−2h−1, provided that the rough beer was fed as such or pre-centrifuged to minimize the fouling contribution of yeast cells and aggregates, respectively. In both cases, the permeate turbidity at 20°C fulfilled that recommended by the European Brewery Convention standards; but, as expected, the chill haze at 0°C was quite higher than 0.6 EBC unit. A preliminary stabilization of pre-centrifuged beer using 0.5gL−1 of regenerable polyvinylpolypyrrolidone (PVPP) at 0°C for 24h allowed the permeate chill haze to be reduced to (0.63±0.22) EBC unit; but the average permeation flux fell to (161±21)Lm−2h−1. By removing the residual PVPP particles from stabilized beer using a 2.7-μm filter before CFMF, it was possible not only to re-enhance the average permeation flux up to 337Lm−2h−1 (this value being in line with those achievable with conventional DE-filters), but also to obtain a chill haze-free permeate ready for aseptically packaging.By referring to an industrial plant capacity of 2×106hL of lager beer, the estimated overall operating costs and global warming potential for this novel combined pale lager clarification and PVPP stabilization procedure reduced to about the 30% of those associated with the current industrial DE-filtration and regenerable PVPP stabilization procedures.