Gotowe bibliografie tematyczne / Membrane filtration

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Gotowa bibliografia na temat „Membrane filtration”

Autor: Grafiati

Data publikacji: 4 czerwca 2021

Data aktualizacji: 28 lipca 2024

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Artykuły w czasopismach na temat "Membrane filtration"

As'adah, Anis, i Munasir MUNASIR. "REVIEW : PERFORMA MEMBRAN KOMPOSIT MENGGUNAKAN ALIRAN DEAD-END FILTRATION". Inovasi Fisika Indonesia 12, nr 2 (4.07.2023): 92–102. http://dx.doi.org/10.26740/ifi.v12n2.p92-102.

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Teknologi berbasis membran merupakan salah satu teknologi pengolahan air yang paling banyak diminati saat ini karena memiliki beberapa manfaat seperti konsumsi energi yang begitu relatif rendah dan operasi yang sederhana. Membran Graphene Oxide (GO) termasuk membran yang banyak diminati karena memiliki porositas GO yang tinggi serta ukuran pori nano yang baik. Sehingga dilakukan review artikel tentang performa membran komposit menggunakan aliran dead-end filtration. Bahan-bahan lain yang dapat dikompositkan dengan membran GO seperti Ti3C2Tx, Ni, Isophorone Diisocyanate (IPDI), TiO2, Ag, PAM, Attapulgite (ATP) dan SiO2 yang memiliki potensi untuk filtrasi yang berbeda-bedaseperti untuk filtrasi pada pemisahan molekul dan pengolahan air, filtrasi untuk zat pewarna dan lain-lain. Dalam proses filtrasi membran untuk aliran dead-end filtration merupakan aliran yang secara keseluruhannya akan melewati suatu membran serta partikel akan tertahan pada membran tersebut. Pada review artikel ini didapatkan membran komposit GO/SiO2 yang memiliki performa baik dilihat dari nilai fluks tertinggi sebesar 229.15 L/m2.h.bar di antara membran komposit yang lain dan berpotensi untuk filtrasi pencemaran air. Kata Kunci: Membran Komposit, Graphene Oxide, Dead-End Filtration Abstract Membrane-based technology is one of the most popular water treatment technologies today because it has several benefits such as relatively low energy consumption and simple operation. Graphene Oxide (GO) membranes are among the membranes that are in great demand because they have high GO porosity and good nano pore sizes. Therefore, a review of articles on the performance of composite membranes using dead-end filtration was carried out. Other materials that can be composited with GO membranes such as Ti3C2Tx, Ni, Isophorone Diisocyanate (IPDI), TiO2, Ag, PAM, Attapulgite (ATP) and SiO2 which have different potential for filtration such as for filtration in molecular separation and water treatment , filtration for dyes and others. In the membrane filtration process for dead-end filtration flow is a flow that as a whole will pass through a membrane and the particles will be stuck on the membrane. In this review article, it was found that the GO/SiO2 composite membrane had good performance in terms of the highest flux value of 229.15 L/m2.h.bar among other composite membranes and has the potential to filter water pollution. Keywords: Composite Membrane, Graphene Oxide, Dead-End Filtration

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Szwast, Maciej, i Teresa Suchecka. "Membranes: Improving batch membrane filtration". Filtration + Separation 50, nr 2 (marzec 2013): 38–41. http://dx.doi.org/10.1016/s0015-1882(13)70080-6.

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Sutherland, Ken. "Membrane filtration: What's new in membrane filtration?" Filtration & Separation 46, nr 5 (wrzesień 2009): 32–35. http://dx.doi.org/10.1016/s0015-1882(09)70193-4.

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Arahman, Nasrul, Bastian Arifin i Fachrul Razi. "Profil Permeabilitas Berdasarkan Struktur Morfologi Membran Polietersulfon pada Pemekatan Larutan Tokoferol (Permeability Profile based on Morphology Structure of Polyethersulfone Membrane on Concentrating the Tocopherol Solution)". Agritech 36, nr 4 (25.02.2017): 416. http://dx.doi.org/10.22146/agritech.16765.

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Separation technique by membrane technology has been widely applied for separation and purification of minor components from vegetable oil. Membrane was prepared and modified in several way in order to improve the filtration performance in purification process of vegetable oil. In this work, the filtration performance of three types of polyethersulfone hollow fiber membrane was investigated. The main objective of this research was to study the effect of membranes type on the filtration performance of tocopherol solution. Three series of filtration experiment were conducted by using fabricated membrane by dissolving of polyethersulfone (PES) in N-methyl pyrrolydone (NMP) with different polymer composition. The membranes was M1 = PES 20 % + NMP, M2 = PES 18 % + NMP, and M3= PES 20 %+ Polyvinyl pyrrolidone (PVP 5 %) + NMP. The difference structure of membrans was confirmed by scanning electron microscopy measurement. The permeability profile of tocopherol solution of 500 ppm was observed by using a single module of hollow fiber membrane with filtration flow of pressure driven inside (PDI). It is shown that, the permeability of tocopherol solution was maximum and stable using PES membrane was composed by M3 system. Moreover, the improvement of tocopherol concentration in retentate solution was about two times higher than that the original solution that was obtained from filtration system of M1 membrane.ABSTRAKTeknik separasi dengan membran teknologi telah diaplikasikan secara luas untuk pemisahan dan pemurnian komponen minor dari minyak tumbuh-tumbuhan. Membran telah dibuat dan dimodifikasikan dengan berbagai cara untuk meningkatkan kinerja filtrasi pada proses pemurnian minyak tumbuh-tumbuhan. Pada penelitian ini, dipelajari kinerja filtrasi tiga jenis membran hollow fiber yang terbuat dari polimer polietersulfon. Tujuan utama penelitian adalah untuk melihat pengaruh jenis membran terhadap kinerja filtrasi larutan tokoferol. Tiga seri penelitian ultrafiltrasi telah dirancang dengan menggunakan membran yang dibuat dengan melarutkan polietersulfon (PES) dalam N-metil pirolidon (NMP) dengan komposisi polimer yang berbeda. Ketiga jenis membran yang digunakan adalah M1 = PES 20 % + NMP, M2 = PES 18 % + NMP, dan M3 = PES 20 % + Polivinil pirolidon (PVP 5 %) + NMP. Perbedaan struktur morfologi membran telah dikonfirmasikan dengan analisis scanning electron microscopy. Profil permeabilitas larutan tokoferol 500 ppm diobservasi menggunakan modul tunggal membran hollow fiber dengan tipe aliran pressure driven inside (PDI). Hasil penelitian menunjukkan bahwa permeabilitas larutan tokoferol tertinggi dihasilkan dengan menggunakan membran M3. Lebih lanjut, peningkatan konsentrasi larutan tokoferol sekitar dua kali lebih tinggi dari konsentrasi awal dicapai dari proses filtrasi dengan membran M1.

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Liu, Yunxia, Honghai Liu i Zhongrong Shen. "Nanocellulose Based Filtration Membrane in Industrial Waste Water Treatment: A Review". Materials 14, nr 18 (18.09.2021): 5398. http://dx.doi.org/10.3390/ma14185398.

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In the field of industrial wastewater treatment, membrane separation technology, as an emerging separation technology, compared with traditional separation technology such as precipitation, adsorption, and ion exchange, has advantages in separation efficiency, low energy consumption, low cost, simple operation, and no secondary pollution. The application has been expanding in recent years, but membrane fouling and other problems have seriously restricted the development of membrane technology. Natural cellulose is one of the most abundant resources in nature. In addition, nanocellulose has characteristics of high strength and specific surface area, surface activity groups, as well as being pollution-free and renewable, giving it a very wide development prospect in many fields, including membrane separation technology. This paper reviews the current status of nanocellulose filtration membrane, combs the widespread types of nanocellulose and its derivatives, and summarizes the current application of cellulose in membrane separation. In addition, for the purpose of nanocellulose filtration membrane in wastewater treatment, nanocellulose membranes are divided into two categories according to the role in filtration membrane: the application of nanocellulose as membrane matrix material and as a modified additive in composite membrane in wastewater treatment. Finally, the advantages and disadvantages of inorganic ceramic filtrations and nanocellulose filtrations are compared, and the application trend of nanocellulose in the filtration membrane direction is summarized and discussed.

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Dixit, Mandar. "Membranes and filtration: Membrane filtration in the biopharm industry". Filtration & Separation 45, nr 8 (październik 2008): 18–21. http://dx.doi.org/10.1016/s0015-1882(08)70294-5.

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Scott, K., A. J. Mahmood, R. J. Jachuck i B. Hu. "Intensified membrane filtration with corrugated membranes". Journal of Membrane Science 173, nr 1 (lipiec 2000): 1–16. http://dx.doi.org/10.1016/s0376-7388(00)00327-6.

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Klyuchnikov, A. I., D. A. Kazartsev, S. V. Zhukovskaya, M. V. Babayeva i D. V. Klyuchnikova. "ADAPTATION OF THE MICROFILTRATION PROCESS TO THE TECHNOLOGICAL PROCESSES OF BEER FILTERING". Agro-Industrial Technologies of Central Russia 4, nr 30 (grudzień 2023): 20–30. http://dx.doi.org/10.24888/2541-7835-2023-30-20-30.

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This article discusses the prospects for the process of membrane filtration of beer with a dead-end and flow-through organization scheme in order to increase the colloidal and biological stability of the drink. The main advantages and disadvantages of organizing the process of membrane filtration of beer using a dead-end and flow-through scheme are presented, machine and hardware diagrams of filtration processes based on mem-brane cartridges that implement the mechanism of dead-end microfiltration and tubular ceramic membranes that implement a flow-through scheme of product separation are given, and areas of application of membrane filtration in the brewery are indicated. industry, in particular, to isolate marketable beer from lager sludge. Special attention is paid to the results of experimental studies of membrane filtration of beer with a dead-end and flow-through process organization using polymer membranes, the positive effect of using membrane fil-tration in beer filtration technology is shown, physicochemical, microbiological and organoleptic quality in-dicators of beer samples clarified by membrane filtration with Using polymer membranes with different po-rosities, the maximum biological stability of the drink during storage is achieved. The main problems of mass adaptation of the membrane filtration process to technological processes of beer filtration at brewing industry enterprises and ways of their possible resolution are considered.

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Leiviskä, T., i J. Rämö. "Investigation of multimodal zeta potential and size distribution in chemical pulp process water". Water Science and Technology 56, nr 11 (1.12.2007): 123–29. http://dx.doi.org/10.2166/wst.2007.770.

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Multimodal zeta potential distribution in chemical birch pulp process water was studied by filtrating the water into fractions and subsequently measuring zeta potential, charge quantity, turbidity and organic substances. Filtrations were made using 12 μm, 1.6 μm, 1.2 μm, 0.45 μm and 0.1 μm membranes. The number of populations with different zeta potentials diminished with filtration. With the unfiltrated water, 12 μm and 1.6 μm filtrates, three or four different zeta potentials were observed. When the filtration was performed with a 1.2 μm membrane or smaller, only two populations of different zeta potentials were detected. The charge quantity steadily approached zero from unfiltrated water towards a 1.6 μm fraction filtrate. After that, it remained constant. Turbidity constantly decreased when using smaller membranes. The amount of wood extractives decreased to half with 0.1 μm filtration. No significant difference in the amount of carbohydrates and lignin between the filtrated fractions and the unfiltrated water was detected. A comparison dealing with particle size analysis between two different apparatuses was also made.

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Manzoor, Saher, Faheem Qasim, Muhammad Waseem Ashraf, Shahzadi Tayyaba, Nimra Tariq, Agustín L. Herrera-May i Enrique Delgado-Alvarado. "Simulation and Analysis of Anodized Aluminum Oxide Membrane Degradation". Sensors 23, nr 24 (13.12.2023): 9792. http://dx.doi.org/10.3390/s23249792.

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Microelectromechanical systems (MEMS)-based filter with microchannels enables the removal of various microorganisms, including viruses and bacteria, from fluids. Membranes with porous channels can be used as filtration interfaces in MEMS hemofilters or mini-dialyzers. The main problems associated with the filtration process are optimization of membrane geometry and fouling. A nanoporous aluminum oxide membrane was fabricated using an optimized two-step anodization process. Computational strength modeling and analysis of the membrane with specified parameters were performed using the ANSYS structural module. A fuzzy simulation was performed for the numerical analysis of flux through the membrane. The membrane was then incorporated with the prototype for successive filtration. The fluid flux and permeation analysis of the filtration process have been studied. Scanning electron microscope (SEM) micrographs of membranes have been obtained before and after the filtration cycles. The SEM results indicate membrane fouling after multiple cycles, and thus the flux is affected. This type of fabricated membrane and setup are suitable for the separation and purification of various fluids. However, after several filtration cycles, the membrane was degraded. It requires a prolonged chemical cleaning. High-density water has been used for filtration purposes, so this MEMS-based filter can also be used as a mini-dialyzer and hemofilter in various applications for filtration. Such a demonstration also opens up a new strategy for maximizing filtration efficiency and reducing energy costs for the filtration process by using a layered membrane setup.

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Rozprawy doktorskie na temat "Membrane filtration"

Krupp, Armin Ulrich. "Mathematical modelling of membrane filtration". Thesis, University of Oxford, 2017. http://ora.ox.ac.uk/objects/uuid:ae6dd9e4-a862-4476-a8d9-35156848297f.

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In this thesis, we consider four different problems in membrane filtration, using a different mathematical approach in each instance. We account for the fluid-driven deformation of a filtercake using nonlinear poroelasticity in Chapter 2. By considering feeds with very high and very low particle concentrations, we introduce a quasi-static caking model that provides a suitable approximation to the full model for the physically realistic concentration regimes. We illustrate the agreements and differences between our model and the existing conventional cake-filtration law. In Chapter 3, we introduce a stochastic model for membrane filtration based on the quantised nature of the particles and show how it can be applied for feeds with different particle types and membranes with an interconnected pore structure. This allows us to understand the relation between the effects of clogging on the level of an individual pore and on the macroscopic level of the entire membrane. We conclude by explaining the transition between the discrete and continuous model based on the Fokker--Planck equation. In Chapter 4, we consider the inverse problem of determining the underlying filtration law from the spreading speed of a particle-laden gravity current. We first couple the theory of gravity currents with the stochastic model developed in Chapter~3 to determine a filtration law from a given set of experiments. We then generalise this idea for the porous medium equation, where we show that the position of the front follows a power law for the conventional filtration laws, which allows us to infer the clogging law in certain instances. We conclude the thesis by showing in Chapter 5 how we can combine experimental measurements for the clogging of a depth filter and simple fluid dynamics to accurately predict the pressure distribution in a multi-capsule depth filter during a filtration run.

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Mayor, Russell. "Some problems in filtration". Thesis, University of Oxford, 1994. http://ethos.bl.uk/OrderDetails.do?uin=uk.bl.ethos.320650.

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Mignard, Dimitri. "Mass transport studies in membrane filtration". Thesis, University of Edinburgh, 1998. http://hdl.handle.net/1842/12654.

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First, a programme to model concentration polarisation was written using the finite difference approach developed by Ilias and Govind. It was validated with experiments using Centrisystem C-300 and C-400 cartridges and BSA solutions (1-5 g/L), and experimental data from Yeh and Cheng with an H1P30-20 Amicon cartridge and Dextran T-500. The next step was to incorporate fouling into this model. To calculate the configurational Derjaguin-Landau-Vervey-Overbeek (DLVO) forces and the resulting osmotic pressures, large use was made of the work of Bowen et al. Concentration dependent diffusivities were calculated from the generalised Stokes-Einstein equation, and used in the transport equation to describe the concentration polarisation profile. It was shown that, when the transport equation did not have a solution at the membrane (or membrane + cake) surface, and that concentration was greater than the highest-concentration local maximum for the diffusivity, coagulation would occur. In this case, a monolayer of globular protein was assumed to deposit, and concentration polarisation was recalculated with this additional resistance. Experiments with 1g/L BSA solutions and Amicon H1P30-20, for a range of transmembrane pressure, ionic strengths and pH, were compared with the model predictions. Both showed that fouling increased with ionic strength away from the Iso-Electric Point of BSA (IEP), and decreased with zeta potential. Simulation also showed that fouling could decrease with increased ionic strength around the IEP, in accordance with classical results. Total resistance to flux from experiments and simulation were in a similar range, although the lack of data relating zeta potentials and pH prevented further comparison. The model would also determine the critical pressure above which fouling occurred. However, observed values were significantly lower than predicted. Direct adsorption of the BSA onto the polysulfone membrane or the effect of high local pore velocities may both explain these discrepancies.

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Ye, Yun School of Chemical Engineering &amp Industrial Chemistry UNSW. "Macromolecular fouling during membrane filtration of complex fluids". Awarded by:University of New South Wales. School of Chemical Engineering and Industrial Chemistry, 2005. http://handle.unsw.edu.au/1959.4/33245.

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Macromolecular components, including protein and polysaccharides, are viewed as one type of major foulants in the complex feed membrane filtration systems such as membrane bioreactor (MBR). In this thesis, the mechanisms of macromolecular fouling including protein and polysaccharide in the complex feed solution are explored by using Bovine serum albumin (BSA) and alginate as model solution. During the filtration of BSA and washed yeast with 0.22 ????m PVDF membrane, it was found that the critical flux of mixture solution was controlled by washed yeast concentration while the existence of BSA significantly changed the cake reversibility of much larger particles. The fouling mechanisms of alginate, as a model polysaccharide solution, were investigated both in dead end and crossflow membrane filtration. In the dead end experiments, it was found that the cake model appears to fit the entire range of the ultrafiltration data while the consecutive standard pore blocking model and cake model are more applicable to microfiltration membranes. The alginate was featured with high specific cake resistance and low compressibility despite some variations between different membranes. The specific cake resistance ( c ) is similar to c of BSA and actual extracellular polymer substance (EPS) in MBR systems reported in the literature, and higher than that of many colloidal particles. In a system contained alginate-particles mixture, it was found that the existence of alginate dramatically increased the cake specific resistance and decreased the cake compressibility. The fouling mechanism of alginate was also studied using long term cross flow filtration under subcritical flux. A two-stage TMP profile similar to that typically observed in MBR was obtained, confirming the important role of EPS during membrane fouling in MBR. In addition to adsorption, trace deposition of alginate also contributed to the initial slow TMP increase during the subcritical filtration. TMP increase during the long-term filtration was found not only due to the increase of the amount of deposition, but also the increase of specific cake resistance. A combined standard pore blocking and cake filtration model, using a critical pore size for the transition time determination, was developed and fit the experimental results well.

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Dragosavac, Marijana M. "Membrane emulsification and filtration for engineered particles". Thesis, Loughborough University, 2011. https://dspace.lboro.ac.uk/2134/8980.

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In many applications employing particles, the distribution of particle sizes has significant influence on the properties of the resultant material. Membrane emulsification (ME) is a method for manufacturing uniformly sized emulsion droplets where a dispersed phase is forced through a membrane into the continuous phase. It is the shear applied on the membrane surface that detaches the droplets thereby generating an emulsion. Formulation of the dispersed and the continuous phase influences the final droplet size of the emulsion. Therefore one of the aims of this research is to broaden the existing knowledge on particle production by membrane emulsification using nickel microengeneered disk membrane with cylindrical pores and the Dispersion Cell. The Dispersion Cell was successfully used to produce W/O/W emulsions (the oil phase was pumpkin seed oil). Also W/O emulsions (the water phase was acidified sodium silicate) were produced and additionally solidified in order to manufacture solid silica particles with high surface area and internal porosity. The particles were additionally functionalized using 3-aminopropyltrimethoxysilane and turned into ion exchange material capable to sorb copper. Since the silica particles do not swell such ion exchange material might be interesting for applications in nuclear industry. Having in mind an industrial application of membrane emulsification the Dispersion Cell cannot be used due to the problems with the scaling up. Therefore two novel systems: Oscillating and Pulsating were developed and reported for continuous production of the particles. Both systems were commissioned using sunflower oil for production of O/W emulsions. Additionally the Pulsating system was successfully used for production of complex coacervates. In the Oscillating system the nickel membrane was in the shape of a candle and the shear on the membrane surface was induced by vertical oscillations of the membrane. In the Pulsating system a tubular nickel membrane was used and the shear on the membrane surface was applied by oscillations of the continuous phase. The scaling up of both Oscillating and Pulsating system can be achieved by providing a larger membrane area (elongating the membrane) as well as connecting the membranes in parallel. It was successfully shown that a simple force balance can be used to model the size of emulsion droplets as a function of the shear stress. The average shear stress worked better when modelling the droplet sizes in the Dispersion Cell, but the correction for the droplet neck had to be taken into consideration when higher dispersed phase flow rates were used. In the Oscillating and Pulsating systems it was the maximal shear stress that gave the better prediction, but in both systems it was clear that additional forces were present which influenced the final droplet size. An alternative field of application for the Dispersion Cell, relevant to the tests of functionalized silica particles, was investigated. The Dispersion Cell was modified into a continuous flow stirred cell with a slotted nickel membrane on the bottom. The continuous flow stirred cell is shown to be an effective technique for both mass transfer kinetics as well as equilibrium data acquisition combining both into a single step, and simplifying ion exchange analysis. To commission the system the commercial ion exchange resin (Dowex 50W-X8) was used. Once determined, the design parameters can readily be used to model ion exchange contacting in a well mixed system, column operations or any process that requires ion exchange material. Using the continuous flow stirred cell it was shown that the silica particles produced using the Dispersion Cell and functionalized using 3-aminopropyltrimethoxysilane were capable to sorb copper. As a part of the collaboration within the DIAMOND (Decommissioning, Immobilisation And Management Of Nuclear wastes for Disposal) project a novel ion exchange material (copper hydroxide acetate suitable for iodide sorption) produced in the Department of Chemistry (Loughborough University) was successfully tested using the continuous flow stirred cell and equilibrium and mass transfer parameters were determined. The continuous flow stirred cell is particularly relevant to instances when the mass of ion exchange material available for the testing is low (less than 1g) and when dealing with hazardous or expensive materials. It is a technique employing microfiltration and ion exchange (or sorption), of the engineered particles that could be produced by membrane emulsification described in this thesis.

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Ofsthun, Norma Jean. "Cross-flow membrane filtration of cell suspensions". Thesis, Massachusetts Institute of Technology, 1989. http://hdl.handle.net/1721.1/14481.

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Siddiqui, Farrukh Arsalan. "Membrane filtration : fouling and cleaning in forward osmosis, reverse osmosis, and ultrafiltration membranes". Thesis, University of Oxford, 2017. https://ora.ox.ac.uk/objects/uuid:bcaadfaa-62fb-4910-8218-bff387a19a11.

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A comparison of fouling in osmotically driven processes with that in pressure driven processes is the main focus of the thesis. Forward osmosis (FO) and reverse osmosis (RO) have received considerable attention for water treatment and seawater desalination. This research compared the nature of fouling in FO mode with that in RO starting with the same initial flux in connection with cleaning effects and then comparing to those in ultrafiltration membranes. In all cases, with cleaning as an integral part, the extent of fouling reversibility, and the question whether a critical flux could be determined were examined. The work during the first phase (undertaken at Oxford) quantified the removal of reversible fouling through rinsing by cold and hot water for a range of concentrations using the foulants dextran and carboxymethyl cellulose. The flux-TMP relationship was conventionally compared to that of the clean water flux. The later phase (at Singapore) compared the fouling in FO and RO by alginate in terms of multiple parameters using cellulose tri acetate (CTA) and thin film composite (TFC) membranes. Silica and alginate were selected as model foulants. Whilst experimental water flux profiles in the present study did not exhibit significant differences in trend between FO and RO fouling, foulant resistance for FO was found to be increasingly greater than for RO with the progression of the fouling tests. This was further corroborated by membrane autopsies post fouling tests; both foulant mass deposition density and specific foulant resistance for FO were greater than for RO. The analysis clearly revealed that FO is essentially more prone to fouling than RO which was presumably due to less flux decline in FO (or greater average flux) as compared to that in RO in result of ICP-self compensation effect which is opposite to the prevailing claim in the literature. Additionally, the present study did not find evidence that hydraulic pressure in RO has a role in foulant layer compaction. FO membrane fouling by real waters was the focus of the final phase of the research at SMTC. Pilot scale FO experiments were conducted on spiral wound CTA membrane with treated waste water obtained from a NEWater factory (Singapore) as the feed. In the second stage, experiments were repeated at bench scale with membrane coupons taken from the spiral wound membranes used earlier. The key finding was that the mass transfer coefficients in the Spiral-Wound module were around 50% lower than the corresponding values in the flat sheet unit and this severely limited the fluxes. The reason could be attributed to strong internal concentration polarisation in the former, where tightly wound spacers act to increase the structural parameter.

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Kyllönen, Hanna. "Electrically or ultrasonically enhanced membrane filtration of wastewater /". Espoo [Finland] : VTT Technical Research Centre of Finland, 2005. http://www.vtt.fi/inf/pdf/publications/2005/P576.pdf.

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Machenbach, Ingo. "Drinking Water Production by Coagulation and Membrane Filtration". Doctoral thesis, Norwegian University of Science and Technology, Department of Hydraulic and Environmental Engineering, 2007. http://urn.kb.se/resolve?urn=urn:nbn:no:ntnu:diva-2142.

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Drinking water production with low-pressure hollow-fibre membranes is becoming increasingly more widespread as replacement for conventional separation technology. Upstream coagulation can mitigate fouling layer formation on membranes and allows removal of colloidal and soluble compounds smaller than the membrane pores. However, integrating membrane systems with coagulation bears the risk of impaired system performance due to unfavourable aggregate characteristics. This is of particular importance when treating humic substances due to their strong dependence on the solution environment.

The experimental work in this study aimed at finding optimal coagulation, flocculation, and membrane operating conditions for treating a typically Nordic surface water with high humic content. Commercial aluminium-based coagulants and chitosan were applied in the pre-treatment step. Short, controlled flocculation was achieved by using a pipe, jet-mix, or packed-bed flocculator. An outside-in operated ultrafiltration system based on a polymeric hollow-fibre was used as separation unit.

The study showed that optimized coagulation conditions are crucial to successful operation of the membrane unit. For the applied raw water (colour 50 mg Pt/L), a specific aluminium dosage of 3 mg Al/L and a coagulation pH in the range of 6–6.5 were found optimal with respect to permeate quality, membrane operation, and metal residuals. Coagulant dosages exceeding the optimal dosage and a pH drop increased hydraulically not-reversible fouling significantly. Chitosan neither met the expectations for NOM removal for the investigated raw water nor did its use seem favourable in combination with a polymeric membrane. Controlling floc aggregation can reduce pressure increase rates on the hollowfibre membrane provided that flocculators are designed for low velocity gradients (G<30 ^s−1). The packed-bed flocculator outperformed the other flocculators. However, flocculation times longer than 5 minutes should be applied to avoid rapid backwash pressure increases on the membrane.

The membrane system was operated with fluxes in the range of 45–75 LMH during filtration and a 1.5 times higher value during backwashes. Forward filtration without air scouring proved feasible. To improve detachment of fouling layers, vigorous air scouring was used during backwashes. A filtration cycle of 30–60 minutes followed by a backwash interval of about 30 seconds gave good results. Increasing coagulant dosage and flux were the two most significant contributors to hydraulically non-reversible fouling. Water recovery only had a minor effect on the pressure development of the membrane. However, the results suggest that efficient sludge removal from the immersion tank is of importance. Operation at lower NOM concentrations left pressure increase rates unchanged, rendering the application potential of the system highest for NOM-rich surface waters.

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Taha, Taha. "CFD modelling of slug flow enhanced membrane filtration". Thesis, University of Oxford, 2003. http://ethos.bl.uk/OrderDetails.do?uin=uk.bl.ethos.403424.

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Książki na temat "Membrane filtration"

Inc, SBP Technologies, i Center for Environmental Research Information (U.S.), red. Membrane filtration. [Cincinnati, Ohio: U.S. Environmental Protection Agency, Center for Environmental Research Information, 1992.

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Zhang, G. S. Rotary microporous membrane filtration studies. Manchester: UMIST, 1990.

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Jacangelo, Joseph G. Membrane filtration for microbial removal. Denver, CO: AWWA Research Foundation and American Water Works Association, 1997.

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Merlo, Christina A. Membrane filtration handbook/selection guide: A guide on membrane filtration technology for the food processing industry. Dublin, CA: National Food Processors Association, 1993.

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Basile, Angelo, i Catherine Charcosset. Integrated membrane systems and processes. Chichester, West Sussex, United Kingdom: John Wiley & Sons Inc., 2016.

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G, Jacangelo Joseph, i AWWA Research Foundation, red. Low pressure membrane filtration for particle removal. Denver, CO: AWWA Research Foundation and American Water Works Association, 1992.

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Purwanto, W. Rotary membrane filtration in microbial cell recycle. Manchester: UMIST, 1994.

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Bodzek, Michał. Membrany w biotechnologii. Gliwice: Wydawn. Politechniki Śląskiej, 1993.

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Kyllönen, Hanna. Electrically or ultasonically enhanced membrane filtration of wastewater. Espoo [Finland]: VTT Technical Research Centre of Finland, 2005.

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Foundation, AWWA Research, Lyonnaise des eaux-Dumez (Firm) i South Africa. Water Research Commission., red. Water treatment membrane processes. New York: McGraw-Hill, 1996.

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Części książek na temat "Membrane filtration"

Böddeker, Karl W. "Membrane Filtration". W Liquid Separations with Membranes, 57–71. Cham: Springer International Publishing, 2018. http://dx.doi.org/10.1007/978-3-319-97451-4_5.

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Brose, Daniel J., Michael Dosmar i Maik W. Jornitz. "Membrane Filtration". W Pharmaceutical Biotechnology, 213–79. Boston, MA: Springer US, 2002. http://dx.doi.org/10.1007/978-1-4615-0549-5_5.

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Chen, J. Paul, Honghui Mou, Lawrence K. Wang i Takeshi Matsuura. "Membrane Filtration". W Advanced Physicochemical Treatment Processes, 203–59. Totowa, NJ: Humana Press, 2006. http://dx.doi.org/10.1007/978-1-59745-029-4_7.

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Gill, Gary W. "Membrane Filtration". W Cytopreparation, 85–100. New York, NY: Springer New York, 2012. http://dx.doi.org/10.1007/978-1-4614-4933-1_7.

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Hausmann, A., M. C. Duke i T. Demmer. "Principles of Membrane Filtration". W Membrane Processing, 17–51. Oxford, UK: Blackwell Publishing Ltd., 2012. http://dx.doi.org/10.1002/9781118457009.ch2.

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Mattiasson, Bo. "Membrane Affinity Filtration". W Chromatographic and Membrane Processes in Biotechnology, 335–49. Dordrecht: Springer Netherlands, 1991. http://dx.doi.org/10.1007/978-94-011-3470-5_19.

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Fulekar, M. H., i Bhawana Pathak. "Membrane Filtration Technology". W Environmental Nanotechnology, 225–46. Boca Raton : Taylor & Francis, CRC Press, 2018.: CRC Press, 2017. http://dx.doi.org/10.1201/9781315157214-9.

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Kroner, K. H., W. Hummel, J. Völkel i M. R. Kula. "Effects of Antifoams on Cross-flow Filtration of Microbial Suspensions". W Membranes and Membrane Processes, 223–32. Boston, MA: Springer US, 1986. http://dx.doi.org/10.1007/978-1-4899-2019-5_23.

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Liao, Baoqiang. "Membrane Filtration in Biorefinery". W Encyclopedia of Membranes, 1–2. Berlin, Heidelberg: Springer Berlin Heidelberg, 2015. http://dx.doi.org/10.1007/978-3-642-40872-4_2113-1.

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Jonsson, Gunnar. "Selectivity in Membrane Filtration". W Synthetic Membranes: Science, Engineering and Applications, 343–66. Dordrecht: Springer Netherlands, 1986. http://dx.doi.org/10.1007/978-94-009-4712-2_12.

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Streszczenia konferencji na temat "Membrane filtration"

Smith, Karl J. P., Joshua Winans i James McGrath. "Ultrathin Membrane Fouling Mechanism Transitions in Dead-End Filtration of Protein". W ASME 2016 14th International Conference on Nanochannels, Microchannels, and Minichannels collocated with the ASME 2016 Heat Transfer Summer Conference and the ASME 2016 Fluids Engineering Division Summer Meeting. American Society of Mechanical Engineers, 2016. http://dx.doi.org/10.1115/icnmm2016-7989.

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Ultrathin membranes will likely see great utility in future membrane-based separations, but key aspects of the performance of these membranes, especially when they are used to filter protein, remain poorly understood. In this work we perform protein filtrations using new nanoporous silicon nitride (NPN) membranes. Several concentrations of protein are filtered using dead end filtration in a benchtop centrifuge, and we track fouling based on the amount of filtrate passed over time. A modification of the classic fouling model that includes the effects of using a centrifuge and allow for the visualization of a transition between pore constriction and cake filtration demonstrate that for a range of protein concentrations, cake filtration supersedes pore constriction after ∼30 seconds at 690 g.

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Hale, Jack S., Alison Harris, Qilin Li i Brent C. Houchens. "The Fluid Mechanics of Membrane Filtration". W ASME 2007 International Mechanical Engineering Congress and Exposition. ASMEDC, 2007. http://dx.doi.org/10.1115/imece2007-43656.

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Reverse osmosis and nanofiltration membranes remove colloids, macromolecules, salts, bacteria and even some viruses from water. In crossflow filtration, contaminated water is driven parallel to the membrane, and clean permeate passes through. A large pressure gradient exists across the membrane, with permeate flow rates two to three orders of magnitude smaller than that of the crossflow. Membrane filtration is hindered by two mechanisms, concentration polarization and caking. During filtration, the concentration of rejected particles increases near the membrane surface, forming a concentration polarization layer. Both diffusive and convective transport drive particles back into the bulk flow. However, the increase of the apparent viscosity in the concentration polarization layer hinders diffusion of particles back into the bulk and results in a small reduction in permeate flux. Depending on the number and type of particles present in the contaminated water, the concentration polarization will either reach a quasi-steady state or particles will begin to deposit onto the membrane. In the later case, a cake layer eventually forms on the membrane, significantly reducing the permeate flux. Contradictive theories suggest that the cake layer is either a porous solid or a very viscous (yield stress) fluid. New and refined models that shed light on these theories are presented.

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Leo, Pedersen, Scott Smiley, Peter Bechtel i Chris Spengler. "Stickwater Processing by Membrane Filtration". W A Sustainable Future: Fish Processing Byproducts. Alaska Sea Grant College Program, 2010. http://dx.doi.org/10.4027/sffpb.2010.11.

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Grigus, Mike. "Caustic Recovery Using Membrane Filtration". W ASME 2009 Citrus Engineering Conference. American Society of Mechanical Engineers, 2009. http://dx.doi.org/10.1115/cec2009-5507.

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Food and beverage processors that use dilute caustic solutions for cleaning process equipment have shown increased interest in recovering the used caustic. The primary reason is that the price of caustic has increased significantly in the past year or so. Membrane filtration technology can be used to remove suspended solids (clarify with microfiltration) and/or dissolved solids (purify with nanofiltration) from these used caustic solutions. These treated caustic solutions are suitable for reuse within the processing plant as cleaning solutions. While an end-user’s specific process, performance, capital and operating cost parameters require pilot testing and process design evaluations to determine the economic viability of caustic recovery, the existing body of information from commercial and process development work allows for an evaluation of a “typical” caustic recovery application. Paper published with permission.

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Kalboussi, Nesrine, Jerome Riarmand, Fatma Ellouze i Nihel Ben Amar. "Optimization of membrane filtration systems". W 2017 International Conference on Control, Automation and Diagnosis (ICCAD). IEEE, 2017. http://dx.doi.org/10.1109/cadiag.2017.8075667.

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Han Wang, Gaofeng Zheng i DaoHeng Sun. "Electrospun nanofibrous membrane for air filtration". W 2007 7th IEEE Conference on Nanotechnology (IEEE-NANO). IEEE, 2007. http://dx.doi.org/10.1109/nano.2007.4601408.

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Mao, Ning, Jingxian Liu, Deqiang Chang i Xi Sun. "Comparison of filtration performances between membrane and non-membrane filters". W 2015 International Symposium on Computers and Informatics. Paris, France: Atlantis Press, 2015. http://dx.doi.org/10.2991/isci-15.2015.296.

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Jahangiri Mamouri, Sina, Volodymyr V. Tarabara i André Bénard. "Numerical Simulation of Filtration of Charged Oil Particles in Stationary and Rotating Tubular Membranes". W ASME 2015 International Mechanical Engineering Congress and Exposition. American Society of Mechanical Engineers, 2015. http://dx.doi.org/10.1115/imece2015-52038.

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Cross flow filtration (CFF) is a common membrane separation process with applications in food, biochemical and petroleum industries. In particular, membranes can be used for liquid-liquid separation processes such as needed in oil-water separation. A major challenge in cross flow filtration is membrane fouling. It can decrease significantly the permeate flux and a membrane’s efficiency. Membrane fouling can be mitigated by inducing shear on the membrane’s surface and this can be enhanced by inducing a swirl in the flow. In addition, a possible approach to improve membrane efficiency consists of repelling droplets/particles from the porous surface toward the centerline using a repulsive electric force. For this purpose, the surface of the membrane can be exposed to electric potential and droplets/particles are also induced to have the same electric charge. In this work, numerical simulations of charged non-deformable droplets moving within an axially rotating charged tubular membrane are performed. The results show that by increasing the electric potential on the membrane surface, the repelling force increases which obviously improves the grade efficiency of the membrane. However, the electric field gradients found in the flow field require large potentials on the membrane surface to observe a noticeable effect. Hence, a smaller solid cylinder is located in the centerline of the flow channel with zero potential. This solid cylinder enhances the electric field gradient in the domain which results in higher repelling forces and larger grade efficiency of the membrane at small potentials. The addition of a small cylinder in the flow field also improves the grade efficiency increases due to the higher shear stress near the membrane surface.

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G. Giorges, Aklilu T., i John A. Pierson. "The Comparison of Membrane Blocking Process and Yeast Membrane Filtration Data". W ASME 2016 International Mechanical Engineering Congress and Exposition. American Society of Mechanical Engineers, 2016. http://dx.doi.org/10.1115/imece2016-66944.

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Membrane filtration systems are used in a variety of processing industries where their performance meet and exceed the requirements in cost and quality. However, it is a challenge to design a small pore-size membrane system that treats very concentrated, large-volume streams within a reasonable time period. In the processing industries, several membrane technologies are used to separate various fluid streams where the concentrate or filtrate contains high-value products. Nevertheless, pore blocking is one of the major factors determining the applicability, efficiency and performance of the membrane filtration and separation system. Inside and outside membrane pore blockages lead to concentration polarization and cake buildup that reduces the flux rate and increases losses in system efficiency. There are four pore blocking mechanisms identified and modeled (complete, standard, intermediate and cake). Several experimental and theoretical works exist that describe the pore flow and blocking process. Depending on the processing fluid and membrane characteristics, all or some of the blocking mechanisms will be exhibited during the filtration process. Understanding the fluid and membrane size and characteristics in addition to pore blocking mechanisms is very important to designing effective membrane filtration systems that overcome the drawbacks associated with membrane performance. Furthermore, developing a membrane filtration system with a target cleaning process that controls membrane performance declines and maintains a reasonable flux for an extended period of time requires understanding and identifying the cause of membrane blocking. In this study, the membrane blocking during the filtration process was investigated experimentally. The experiment was designed to simulate the characteristics of a fluid stream encountered in food processing. The higher concentration was selected to manage the experiment time as well as to address worst-case scenarios, while the lower concentrations were selected to manage the filter area reduction. Dead-end filtration of two yeast solution concentrations were filtered through two different filter areas. In addition, the dynamic tests were conducted with shear generated using an impeller operated at various rotational speeds. Several tests were performed and the filtrate volume, time, pressure and agitation rate were recorded. The volume was measured with a graduated cylinder and the time measured in seconds. The results show the membrane blocking process is significantly affected by the membrane and fluid characteristics. The plots of pore blocking models and the experimental membrane filtrate data show the dominant pore blocking observed for both filters and flow process is cake filtration. The side-by-side comparison also indicates that the dominant pore blocking mechanisms depend on time. Thus, the initial and final pore blocking may not be attributed to the same pore blocking mechanism. Although it cannot be clearly shown from the current study, some part of the experimental flux profile may also be shaped by the combined pore blocking effects.

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Fernandes, C. S., M. R. Bilad i N. A. H. M. Nordin. "Silica incorporated membrane for wastewater based filtration". W THE 2ND INTERNATIONAL CONFERENCE ON APPLIED SCIENCE AND TECHNOLOGY 2017 (ICAST’17). Author(s), 2017. http://dx.doi.org/10.1063/1.5005374.

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Raporty organizacyjne na temat "Membrane filtration"

William A. Greene, Patricia A. Kirk, Richard Hayes i Joshua Riley. CENTRIFUGAL MEMBRANE FILTRATION. Office of Scientific and Technical Information (OSTI), październik 2005. http://dx.doi.org/10.2172/859218.

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Daniel J. Stepan, Bradley G. Stevens i Melanie D. Hetland. CENTRIFUGAL MEMBRANE FILTRATION. Office of Scientific and Technical Information (OSTI), październik 1999. http://dx.doi.org/10.2172/761675.

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Stevens, B. G., D. J. Stepan i M. D. Hetland. EM Task 9 - Centrifugal Membrane Filtration. Office of Scientific and Technical Information (OSTI), listopad 1998. http://dx.doi.org/10.2172/3835.

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Stepan, D. J., T. A. Moe i M. E. Collings. Task 9 - centrifugal membrane filtration. Semi-annual report April 1--September 30, 1996. Office of Scientific and Technical Information (OSTI), maj 1997. http://dx.doi.org/10.2172/485944.

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Stepan, D. J., i M. E. Grafsgaard. Task 9 -- Centrifugal membrane filtration. Semi-annual report, April 1--September 30, 1997. Office of Scientific and Technical Information (OSTI), grudzień 1997. http://dx.doi.org/10.2172/631131.

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Shamsuddin Ilias. FLUX ENHANCEMENT IN CROSSFLOW MEMBRANE FILTRATION: FOULING AND IT'S MINIMIZATION BY FLOW REVERSAL. Office of Scientific and Technical Information (OSTI), styczeń 2005. http://dx.doi.org/10.2172/836731.

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Shamsuddin Ilias. Flux Enhancement in Crossflow Membrane Filtration: Fouling and It's Minimization by Flow Reversal. Office of Scientific and Technical Information (OSTI), sierpień 2005. http://dx.doi.org/10.2172/859173.

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Stephan, Daniel J., i Michael E. Grafsgaard. Task 9- Centrifugal Membrane Filtration. Semiannual report, November 1, 1996--March 31, 1997. Office of Scientific and Technical Information (OSTI), grudzień 1997. http://dx.doi.org/10.2172/619743.

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