Abstracts - peq / coppe / ufrj

Amirkabir Univ. Tech., IranApplication of the UNIQUAC-HB Model in the Sorption Behavior of Ethanol/WaterMixtures into Polydimethylsiloxane Membrane at Different TemperatureAli Shokouhi, Gholamreza Pazuki, Ahmadreza Raisi, Mohammad IraniAmirkabir Univ. Tech., IranSeparation Performance of Polyethersulfone/NaX Zeolite Mixed Matrix Membranes forCarbon Dioxide RemovalMostafa Talebian, Abdolreza Aroujalian, Ahmadreza Raisi, Mohammad IraniAmirkabir Univ. Tech., IranModification of Polyethersolfone Ultrafiltration Membrane by Corona Treatment andCoating TiO 2 Nanoparticle on the SurfaceVahid Moghimifar, Ahmadreza Raisi, Abdolreza Aroujalian, Mohammad IraniAmirkabir Univ. Tech., IranFabrication of Composite Polyvinyl Alcohol/Polyethersulfone Membrane forDehydration of Alcohols by Pervaporation ProcessYousef Fathi, Ahmadreza Raisi, Abdolreza Aroujalian, Mohammad IraniCameronMaximizing Hydrocarbon Liquids Recovery while Recovering High Purity CO2: NewOperation Strategy for Membrane Based CO2 Removal FacilitiesJason Dietrich, Ankur Jariwala, G. Edward Mahley, Richard PetersEmbrapa- IQ/UFRJ-EQ/UFRJDefinition Of The Limiting Flux Condition In The Nanofiltration Of A Grape Marc ExtractContaining 30% EthanolAna Paula Gil Cruz, Natalia Barbosa Eitel, Luiz Fernando Menezes da Silva, Suely PereiraFreitas, Alexandre Guedes Torres, Lourdes Maria Correa CabralEmbrapa- IQ/UFRJ-EQ/UFRJEvaluation Of Reverse Osmosis And Nanofiltration For The Concentration Of BioactiveCompound Recovered Of Grape MarcAna Paula Gil Cruz, Natalia Barbosa Eitel, Luiz Fernando Menezes da Silva, Suely PereiraFreitas, Alexandre Guedes Torres, Lourdes Maria Correa CabralEmbrapa- IQ/UFRJ-EQ/UFRJEvaluation Of The Application Of Nanofiltration To Concentrate The HydroethanolicExtract Obtained From Grape Juice MarcNatalia Barbosa Eitel, Ana Paula Gil Cruz, Luiz Fernando Menezes da Silva, Suely PereiraFreitas, Lourdes Maria Correa CabralEMBRAPA/UFSCRecovery and Concentration of Isoflavones of Tofu Whey Using the NanofiltrationSilvia Benedetti, Lara Alexandre Fogaça, Guilherme Zin, Elane Schwinden Prudêncio,Rodrigo Santos Leite, José Marcos Gontijo Mandarino, José Carlos Cunha PetrusEQ/UFRJEnvironmental Performance Comparison between Bench Scale and WastewaterTreatment Plant Membrane BioreactorsTiago Chagas de Oliveira Tourinho, Ofélia de Queiroz Fernandes Araújo, Isaac VolschanJuniorEQ/UFRJBiofilm formation on Laboratory Nanofiltration MembraneFrancisca Pessoa de França, Daniel Serwy Braz, Juliana Domingues Sampaio, RenataOliveira da Rocha CalixtoEscola de Eng. de Lorena –EEL/USP Production of Filtrating Membranes from the Components of Sugarcane Bagasse Guilherme Gonçalves de Godoy, Rafael Garcia Candido, Adilson Roberto GonçalvesEurodia/ Ameridia Electrodialysis as desalting or purification step in petrochemical industries Florence Lutin; Daniel BarGE Water /Sanasa / EMALtdaSANASA Capivari II – The First Full Scale Municipal MBR in Latin AmericaRenato Rossetto, Renata Lima Pereira de Gasperi, Juliana Pontes Machado Andrade,Rovério Pagotto Jr., Romeu Cantusio Neto, Joubert Trovati, Marcus Vinicius GueriniVallero, Brian Arntsen, José Everaldo Elorza PradoGung University - TaiwanDesalination of High Salinity Wastewater Using Electrodialysis: Operating VariableEffects and Water Transport PhenomenaShingjiang Jessie Lue and Jie-Ting YuHoseo University Membrane Fouling Control using High Voltage Impulse (HVI) Techniques Ji-Sun Lee and In-Soung ChangICMPE/CNRS, Kuban StateUniv.Evolution of Ion-Exchange Membranes Behavior in Full Scale Electrodialysis for FoodIndustryW Garcia-Vasquez, L Dammak, C Larchet, V Nikonenko, D GrandeIENPreparation and Characterization of Nanofiltration Membranes based onPolisulfonamideCelina C. R. Barbosa, Edna T. R. Bastos, Elizabeth E.M. Oliveira, Eliane P. B. Soares, JaciaraC. Silva, José Luis MantovanoIENDevelopment of Sulfonated Polysulfone Composite Membranes for AmmoniumRejectionEdna T. R. Bastos, Celina C. R. Barbosa ,Jaciara C. Silva, Vanessa B.C. Queiroz and Delmo S.VaitsmanIEN- IQ/UFRJSelectivity of Nanofiltration Membranes for Treatment of Liquid Waste ContainingUraniumElizabeth E. M. Oliveira, Celina C. R. Barbosa and Júlio C. AfonsoINPROMEMClarification of RED Beetroot Juice Using Rotating Ceramic Membrane Discs to Obtain aBetalain Pigment SolutionBeatriz Cancino-Madariaga, Andrés Ramírez Salvo, Paula Pinto Villegas

Inst. Inf. Tech. /Faculty ofBios. Eng.Gas separation properties of Mixed Matrix Membranes comprising of Matrimid andFuntionalized Mesoporous MCM-41Asim Laeeq Khan, Chalida Klaysom, Amit Gahlaut, Ivo VankelecomInst. Inf. Tech. /Faculty ofBios. Eng.Synthesis and Gas permeation properties of Mixed Matrix Membranes comprised ofAcrylate derivitized PSf and Amine functionalized Mesorporous MCM-41 for CO 2separationAsim Laeeq Khan, Chalida Klaysom, Amit Gahlaut, Ivo VankelecomInst. Inf. Tech. /Faculty ofBioscience Eng.Synthesis and characterization of Fluorinated and Sulfonated Aromatic PEEKmembranes; Application in CO 2 separationAsim Laeeq Khan, Chalida Klaysom, Amit Gahlaut, Ivo VankelecomInst. Tecn.de Buenos Aires Simulating Pressure Retarded Osmosis Using UniSim Design Guillermina Gentile, Paula Llano, María Fidalgo de CortalezziINT/UFRJStudy of Parameters on Preparation of Composite Membranes Based on ActivatedCarbonKarla Patricia Macedo Licona, Marcello Pojucan Magaldi Santos, Amal Elzubair Eltom andJosé Carlos da RochaKoch Memb. / Águas doBrasil Drinking water: Single step Ultrafiltration treatment of high turbid River Water Kevin Phillips, Isadora Argentoni Nagaoka, Manny Singh, André Lermontov, Alberto CostaMintekIn-module chemical modification and assessment of polyethersulfone capillaryultrafiltration membranesK. Philemon Matabola, Banele Vatsha and Richard M. MoutloaliMintekCatalytic Microfiltration Membranes containing Fe/Ni Bimetallic Nanoparticles for theReductive Degradation of Azo Dyes and Organochlorines in WaterKeneiloe Sikhwivhilu, Richard M. MoutloaliPAM/COPPE/UFRJAdhesion between Layers of composite Membranes in a Hollow Fiber ShapeSynthesized by Simultaneous Extrusion for Reverse OsmosisFelipe Coelho Cunha, Frederico de Araujo Kronemberger e Cristiano Piacsek BorgesPAM/COPPE/UFRJ Membrane Adsorber Process for Decontamination of Injectable Solutions Almeida, K. M., Ferraz, H. C. e Almeida, M. MPAM/COPPE/UFRJMixed Matrix Membranes for Gas Separation: Morphological Characterization andTransport Properties for O2/N2Sandro Eugenio da Silva, Bruno da Silva Gonçalves Alves, Helen Conceição Ferraz, CristianoPiacsek BorgesPAM/COPPE/UFRJEvaluation of Solubility of Propylene and Propane gas in Facilitated TransportMembranes Containing Silver as Carrier AgentCarolina Guedes Fioravante Rezende, Cristiano Piacsek borgesBorges, Alberto ClaudioHabertPAM/COPPE/UFRJ Development membranes for osmotic power generation Jader Conceição da Silva, Cristiano Piacsek BorgesPAM/COPPE/UFRJDevelopment of Functionalized Poly(etherimide) Membrane for Application inHemodialysisAlana Melo dos Santos, Alberto Claudio Habert e Helen Conceição FerrazPAM/COPPE/UFRJ -Univ.Nova de LisboaSuperficial Characterization and Long-term Test of Reverse Osmosis Membranes Coatedwith PVA and Natural BiocidesJuliana A. Guimarães, Claudia Galinha, Helen C. Ferraz, Cristiano P. Borges, João Paulo S. G.CrespoPAM/COPPE/UFRJ Bio-Lubricant Production by Pervaporation-Assisted Reaction Paola Andrea Borda Díaz, Frederico Kronemberger, Alberto Claudio HabertPAM/COPPE/UFRJSuccinic Acid Liquid-Liquid Extraction with Membrane ContactorsLuciana de Souza Moraes, Frederico de Araujo Kronemberger, Helen Conceição Ferraz andAlberto Claudio HabertPAM/COPPE/UFRJStudy of PVC Membranes Prepared Via Non Solvent Induced Phase Separation ProcessLiana Franco Padilha, Cristiano Piacsek BorgesPAM/COPPE/UFRJDirect Osmosis Process for Power Generation using Salinity Gradient: FO/PRO PrototypeInvestigation using Hollow Fiber ModulesNicolas Roger Jean-Daniel Mermier, Cristiano Piacsek BorgesPAM/COPPE/UFRJSystems for composite hollow fibers synthesis combining simultaneous phase inversionand interfacial polymerizationNicolas Roger Jean-Daniel Mermier, Cristiano P. BorgesPAM/COPPE/UFRJ Feasibility and Metodology for the Reuse of Reverse Osmosis Modules Paula Werneck Teixeira Reuther, Cristiano Piacsek Borges, Frederico KronembergerPAM/COPPE/UFRJPolyurethane Membranes to Remove Sulfur Compounds from Naphtha byPervaporation ProcessRafael Aislan Amaral, Alberto Cláudio Habert, Cristiano Piacsek BorgesPAM/COPPE/UFRJ Antimicrobial polyvinyl alcohol films with in situ synthesized silver nanoparticle Beatriz Thompson Binoto Ferreira, Helen C. Ferraz, Liliane D. Pollo

PAM/COPPE/UFRJSynthesis and Characterization of Polyvinyl Alcohol Containing Carbon Nanoparticles forthe Separation of Olefin/Paraffin MixtureJuliana Jatobá, Luíza Martins de Almeida, Jane Hitomi Fujiyama-Novak, Alberto CláudioHabertPAM/COPPE/UFRJ Study from Hydrodynamics Aiming to Reduce Fouling in MBR Thaissa P. Silva, Cristiano P. Borges, Frederico A. KronenberguerMarina N. Souza, Jéssica Schner, Jane H. Fujiyama-Novak, Maria E. F. Garcia, Maria EugêniaPAM/COPPE/UFRJPreparation of Chlorine-Resistant NF Membrane Fabricated by Interfacial Polymerization Sena, Alberto C. Habert, Cristiano Borges, Mônica O. PennaPAM/COPPE/UFRJ Study of New Permeators for Membrane Bioreactors (MBR) Aiming at Fouling Control Robson Rodrigues Mororó, Cristiano Piacsek Borges, Frederico de Araujo KronembergerPAM/COPPE/UFRJDevelopment of Poly(ethylene oxide) Membranes for Desulfurization of Gasoline byPervaporationMaria Elizabeth Ferreira Garcia, Sandra Renata Rossi, Carlos Alberto de Araujo Monteiro,Cristiano Piacsek BorgesPAM/COPPE/UFRJCoagulation, Flocculation and Microfiltration processes for wastewater reuse inSugarcane IndustryGisele Mattedi, Cristiano P. Borges, Lidia YokoyamaPAM/COPPE/UFRJRecovery and concentration of effluent from the delignification stage in the productionprocess of lignocellulosic ethanolAna C. M. Costa, Gisele Mattedi, Cristiano P. Borges, Lidia Maria Melo Santa AnnaAna C. M. Costa, Gabriela M. dos Ramos, Gisele Mattedi, Cristiano P. Borges, Rodrigo S. deThe use of different types of antiscalants to prevent barium sulphate precipitationPAM/COPPE/UFRJSouza, Vânia M. J. SantiagoPAM/COPPE/UFRJ Membrane Reactors for Transesterification of Triglycerides Dilson da Costa Maia Filho, Vera Maria Martin Salim, Cristiano Piacsek Borges.PAM/COPPE/UFRJ Polycaprolactone membranes by phase inversion process Cristina Cardoso Pereira and Cristiano Piacsek BorgesPAM MembranasPerformance of Cartridge Filters as Pre-Treatment of Pressurized MicrofiltrationJocarla da Silva Rogerio, Walter Bom Braga Junior, Gabriela Marques dos Ramos, RobertoBentes de CarvalhoAna C. M. Costa, Gabriela M. dos Ramos, Gisele Mattedi, Paula W. T. Reuther, Cristiano P.PAM/COPPE/UFRJ-Petrobras Evaluation of Reversal Electrodialysis Process to Treat Refinery WastewaterBorges, Rodrigo S. de Souza, Vânia M. J. SantiagoPAM/COPPE/UFRJ-Petrobras - UFBAOily Wastewater Treatment by Membrane Separation Processes Aiming Reuse:Considerations Based on Experimental DataAlbérico Ricardo Passos da Motta, Cristiano Piacsek Borges, Karla Patricia de OliveiraEsquerre, Asher Kiperstok, Rafaela Oliveira FloresPAM/COPPE/UFRJ-Univ.ColômbiaContinuous Production of Biodiesel using a Liquid-Liquid Film Reactor packed withHollow Fiber MembranesAderson Imbachi, Nevardo Bello Yaya, Luz Dary Carreño Pineda, Juan Guillermo CadavidEstrada, Alberto Claudio Habert , Paulo César Narváez RincónPAM/COPPE/UFRJ-EQ/UFRJ Use of Membrane Contactor to Improve the Ozone Transport in Gas-Liquid SystemFelipe Rodrigues Alves dos Santos, Fabiana Valéria da Fonseca Araújo, Cristiano PiacsekBorgesPolyvinyl Alcohol / Activated Carbon Composite Thin Layer to Improve ChlorinePAM/COPPE/UFRJ-IMA/UFRJ Resistance of Commercial RO Polyamide MembranesLucinda F. Silva , Ricardo C. Michel, Cristiano P. BorgesPAM/COPPE/UFRJ-IQ/UFRJ New Polyamide Membranes from PAMAM and GlutaraldehydeHilenio da Silva Monteiro, Liana Camboin, Mylene Fernandes, Alberto Claudio Habert,Vanessa Rodrigues FurtadoPAM/COPPE/UFRJ -IQ/UFRJSynthesis and Characterization of Mixed Matrix Membranes Containing MOFs for CO 2CaptureJéssica de S. Ribeiro , Talita O C. Leite, Elisângela S. Costa, Alberto Claudio Habert, HelenConceição Ferraz, Bruno da S. Gonçalves Alves, Jussara L. de MirandaPAM/Pam memb. Characterization of National Hollow FiberMembranesfor Use in Hemodialysis Nascimento, C. R. F.,Ferraz, H. C., Almeida, K. M. .e Borges, C. P.PAM/COPPE/UFRJ-PetrobrasFacilitated Transport of Propylene Through a Membrane Containing Silver Salt asCarrierLuíza M. de Almeida, Douglas V. Fernandes, Felipe C. Cunha, Jane H. Fujiyama-Novak,Liliane Pollo, Cristiano Borges, Alberto C. Habert, Carlos R. K. RabelloPAM/COPPE/UFRJ-Petrobras-EQ/UFRJApplication of Ceramic Membranes for Oilfield Produced Water Treatment in OffshorePlatformsSilvio Edegar Weschenfelder, Ana Maria Travalloni Louvisse, Cristiano Piacseck Borges,Juacyara Carboneli CamposPAM-COPPE/UNIFAP/ UFPACopper Waste Recovery from Hydrometallurgical Industry by Membrane ContactorSystemKleber Bittencourt Oliveira; Helen Conceição Ferraz; Emanuel Negrão Macêdo

PAM-COPPE/UNSAEthanol dehydration through crosslinked PVA/PES composite membranes with plasmatreated asymmetric supportBetina Villagra Di Carlo ,Elza Castro Vidaurre, Alberto Claudio HabertPAM-COPPE/PetrobrasNewly Developed Composite Hollow Fiber Membrane by Interfacial Polymerization ofHydrazineAna C. M. Costa, Paula W. Teixeira, Maria E. F. Garcia, Jane H. Fujiyama-Novak, Gabriela M.Ramos, Alberto C. Habert, Cristiano Borges, Mônica O. PennaPAM-COPPE/Univ. Nac.ColombiaModeling and Simulation of Membrane Reactor for Biodiesel ProductionMario Noriega, Anderson Imbachi, Nevardo Bello Yaya, Luz Dary Carreño Pineda, JairoErnesto Perilla Perilla, Juan Guillermo Cadavid Estrada, Alberto Claudio Habert, PauloCésar Narváez RincónPetrobras Assessment of Membranes Potential for Ballast Water Treatment Rafael Ferreira de Jesus, Ana Maria Travalloni Louvisse, Celso Alleluia MauroPetrobrasCO 2 Removal Systems with Membranes at Petrobras Offshore UnitsLeandro Fernandes Nolasco Quintanilha, Paulo Roberto de Jesus, Rafael Henrique PecoraGomesPetrobras Sulphate Removal Units Monitoring Martins Jr, Elpidio CorreaPetrobras/ EQ-UFRJ CO 2 Separation from Natural Gas with Membrane Permeators and Gas-Liquid Contactors José Luiz de Medeiros, Ofélia de Queiroz Fernandes Araújo e Wilson M. GravaPolymem AS - FranceGigamem® : An Innovative Ultrafiltration Membrane Process Application To SeawaterFiltration For Injection On Large 250,000 bpd (10 Mgd) Oil PlatformsOlivier Lorain / Jean Michel EspenanPoroGen Corporation, USAAdvances in polymeric membrane material technology open new options for naturalgas treatingBen Bikson, and Yong DingPorometerCharacterization of the Pore Size of Polymeric Membranes by Capillary Flow Porometryand Comparison with other Characterization TechniquesLuc Stoops, Chris Dotremont, Danny Pattyn and Angels Cano-OdenaSolvaySolvay Materials for UF/MF Membranes and Development TrendsAnna Maria Bertasa, Pasquale Campanelli, Emanuele Dinicolo, Thomas Kohnert, TheodoreMoore, Aldo SanguinetiUBE Industries Polyimide Hollow Fiber Membranes which contribute to Energy Creation Nozomu TANIHARA1, Nobuhiko FUKUDA, Tomohide NAKAMURA, Tetsuo NAKAYASUUBE Industries Characteristic and Applications of Polyimide Hollow Fiber Membrane Tetsuo NAKAYASU, Nozomu TANIHARA and Tomohide NAKAMURAUCSMicrofiltration and Ultrafiltration applied to Concentration of Pectinases Produced bySolid-State FermentationPatrícia Poletto, Eloane Malvessi, Mára Zeni, Mauricio Moura da SilveiraUCS/ UFRGS Characterization of Poly (ether imide) Microfiltration Membrane Carine Pertile, Camila Baldasso, Mara Zeni, Isabel C.TessaroUCS/UFU/UFESCharacterization of Cellulose Acetate Membranes Produced from Recycling Corn Huskfor Application in UltrafiltrationElaine Angélica Mundim Ribeiro, Carla da Silva Meireles, Guimes Rodrigues Filho, JuliaGraciele Vieira, Rosana Maria Nascimento Assunção, Jocelei Duarte, Mara ZeniUCS/UFU/Univ. Genova Characterization of Cellulose Acetate Membranes Produced from Mango SeedCarla S.Meireles, Sabrina D. Ribeiro, Elaine A. Mundim, Guimes Rodrigues Filho, JoyceRover Rosa, Rosana M.N.Assunção, Mara Zeni, Aldo Bottino, Gustavo CappanelliUEMPurification of Protein Coagulant from Moringa oleifera SeedAline Takaoka Alves Baptista; Pedro Henrique Freitas Cardines; Carole Silveira; MarianaOliveira Silva, Marcelo Fernandes Vieira; Rosângela Bergamasco; Angélica MarquetottiSalcedo VieiraUEMRemoval of Trihalometanes Precursors by Combined ProcessCoagulation/Flocculation/Membranes in water treatmentMilene Carvalho Bongiovani, Franciele Pereira Camacho, Letícia Nishi, Karina CardosoValverde, Livia de Oliveira Ruiz Moreti, Driano Rezende, Carlos Henrique Furlan, AngélicaMarquetotti Salcedo Vieira, Rosângela BergamascoUEM - UNINGA -PAM MembranasFuture of Membranes for Greywater ReuseTaísa Machado de Oliveira, Cláudia Telles Benatti, Célia Regina Granhen Tavares, RobertoBentes de Carvalho, Rafael Alberto NishimuraUERJElectroflocculation and Reverse Osmosis in the Treatment of Oily WastewaterLeonardo Firmino da Silva, Patrícia Braz Ximango, Alexandre Andrade Cerqueira, MônicaRegina da Costa Marques, Fábio Merçon

UFSCUFSCUFSCUFSCUFSCUFSCarUFSCarUFSJ-UFUPretreatment Influence on Hexane Permeability in Nanofiltration and Reverse OsmosisCommercial Polymeric MembranesEffect of Dense CO 2 on Polymeric Commercial MembranesMagnetic Field Influence on Cleaning of Ultrafiltration Membranes Applied to Treatmentof Textile WastewaterUse of Precipitation and Ultrafiltration to Purify Inulinase Obtained by Solid StateFermentation of Sugarcane BagasseSeparation of Mixtures of Soybean Oil and Organic Solvents by Ceramic MembranesPEI/PEIS blends reinforced with sepiolite Clay for fuel cell polymeric electrolytes:evaluation of applicabilityPC/PCS blends reinforced with sepiolite clay for polymeric PEMFC electrolyte:Evaluation of applicabilityA Study of the Resistances During Permeate Flux Decline in Crossflow Microfiltration ofPassion Fruit JuiceKatia Rezzadori, Frederico M. Penha, Mariane C. Proner, Lara Fogaça, José C. C. Petrus,Marco Di LuccioKatia Rezzadori, Josamaique G. Veneral, Lucas Pires, J. Vladimir Oliveira, José C. C. Petrus,Marco Di LuccioFranciele Carlesso, Selene M. A. G. U. Souza, Antônio A. U. Souza, J. Vladimir de Oliveira,Marco Di LuccioSimone Maria Golunski, Helen Treichel, Marco Di LuccioJonas R. M. de Melo, Ricardo Verlindo, Ana Paula Picolo, Diane Rigo, Débora Z. Flôres,Marcus V. Tres, Juliana Steffens; J. Vladimir Oliveira, Marco Di LuccioAna C. O. Gomes, Fernando N. S. Monteiro, Caio M. Paranhos, L. A. PessanAna C. O. Gomes, Eduardo Backes, Caio M. Paranhos, L. A. PessanRui Carlos Castro Domingues,Miria Hespanhol Miranda Reis,Vicelma Luiz CardosoUFVTreatment of Kraft Pulp Mill (EPO) Bleaching Plant Filtrates Using Membrane Technology Rafael Quezada Reyes, Claudio Mudado SilvaUFVMonitoring the Shelf Life of Microfiltered WheyMaura Pinheiro Alves, Renam de Oliveira Moreira, Guilherme Mendes da Silva, RafaelOliveira Bento, Cláudia Lúcia de Oliveira Pinto, Antônio Fernandes de CarvalhoUNICAMPParametric Analysis of a Ethylbenzene Dehydrogenation Model carried on a MembraneReactor with heat and mass transferGermano Possani, Roger J. Zemp.UNICAMPClarification of Artichoke By-product Extract by Membrane Process: MembraneSelection Criteria and Fouling Mechanism Modeling During FiltrationMariana Teixeira da Costa Machado, Miriam Dupas HubingerUNIRIO Water treatment to health clinics Anna Lecticia Martinez Toledo, Maria Eugênia SenaUnitek Ultrafiltration as pretreatment in river water desmineralization by reverse osmosis Manuel García de la MataUniv. Cartagena /Univ.MurciaOptimizing Cobalt (II) Removal from Aqueous Solution by Bulk Liquid MembranesContaining D2EHPA. Study of Transport ParametersG. León, A. Hidalgo, M. Gómez, M.D. Murcia, B. Miguel, M.A. GuzmánUniv. Cartagena /Univ.MurciaCharacterization of RO90 membrane using saline solutions. Application of Spiegler-Kedem-Kachalsky modelA. Hidalgo, G. León, M. Gómez, M.D. Murcia, M.A. Guzmán, C. GuardiolaUniv. ChileExtraction of the light lanthanide metal ions by means of emulsified liquid membranesusing several kinds of organophosphorus extractants as carrier C. Basualto F., F. Valenzuela L., L. Molina C., J. Sapag H.Univ. Chile Effect of Particle Diameter on the Permeability of Polypropylene/Silica Nanocomposites Diego Bracho, Moisés Gómez, Humberto Palza, Raul QuijadaUniv. EdinburghMulti-stage Design for Carbon Capture from Coal-fired Power Plants: From ProcessDesign to Economic AnalysisDavide Bocciardo, Maria-Chiara Ferrari, Stefano BrandaniUniv. Edinburgh1D and 2D Approach for Modelling Hollow-fiber and Spiral-wound Permeators For GasSeparationDavide Bocciardo, Maria-Chiara Ferrari, Stefano BrandaniUniv. L’Aquila/ USP Effect of the UF-Membrane Cut-off on the Invertase Activity Francesco Di Addezio, Ester Junko Yoriyaz, Maria Cantarella and Michele VitoloUniv. Nac. Colombia Performance of Batch Pervaporation Membrane Reactor for Isoamyl Acetate SynthesisWilmar Osorio-Viana, Jesús David Quintero-Arias, Javier Fontalvo,Izabela Dobrosz-Gómez,Miguel Ángel Gómez-García

Univ. Nac. Colombia Isoamyl Acetate Production - Membrane Reactor Design GuidelinesWilmar Osorio-Viana, Jesús David Quintero-Arias, Javier Fontalvo,Izabela Dobrosz-Gómez,Miguel Ángel Gómez-GarcíaUniv. Nac. Colombia Measurement of the solubility of water - ethanol mixtures in PDMS membranes Andrea Fuertes, Mario Noriega, Miguel Ángel Gómez García, Javier FontalvoUniv. Nac. Colombia Performance of Liquid Membranes in the Taylor Flow regimeJuan David García-Mahecha, Alan Didier Pérez-Ávila, Miguel Ángel Gómez-García, JavierFontalvo-AlzateUniv. Passo FundoProduction of Whey Protein Concentrated (WPC) by Ultrafiltration followed by dialysisCaroline Dalcin Zanon, Gabriela Viganó, Juliane Mosmann, Vera Maria Rodrigues, VandréBarbosa BriãoUniv. Tolouse/CNRSElectrodialysis for food and environmental applications. Scientific targets and industrialrealizationsHélène Roux-de BalmannUniv. Tolouse/CNRS USP Demineralization of waste waters containing phenol by electrodialysis H. Roux-de Balmann , F.J. Borges, R. GuardaniUniversidade Nova deLisboa, Universidade deLiliana C. Tomé, Luís P.N. Rebelo, Carmen S.R. Freire, David Mecerreyes, Isabel M.Ionic Liquids and Polymeric Ionic Liquids Membranes for COAveiro, University of the2 SeparationMarruchoBasque CountryUniversidade Nova deLisboa, Universidade deAveiro, University of theBasque CountryLight Olefin/Paraffin Separation Using Polymeric Ionic Liquid Membranes Containing Ag + -IL as CarrierLiliana C. Tomé, David Mecerreyes, Carmen S.R. Freire, Luís P.N. Rebelo, Isabel M.MarruchoUNSAComparison of the Performance of Membranes in Treatment from Industry TanneryWastewaters.Estela María Romero-Dondiz, Jorge Emilio Almazán, Verónica Beatriz Rajal and Elza FaniCastro-Vidaurre.UNSAPreparation and evaluation of ciprofloxacin delivery from poly(3-hidroxybutirate)membranesJosé M. Bermudez, Analía I. Romero, Mercedes Villegas, M. Florencia Dib Ashur, Mónica L.Parentis y Elza F. Castro VidaurreUNSA/UFSCarPolycarbonate Modified Membranes With Silanized Clays For Use In Ethanol / WaterPervaporationL. Dada, M. Toro, C. Carrera, E. Erdmann, C. Paranhos, L. Pessan, H. DestéfanisUNSA/Univ California atDavisUltrafiltration Membranes Modified by Plasma and Its Application in The Viral RemovalIn Water TreatmentMercedes L. Méndez, Verónica Rajal, Elza F. CastroUOP Honeywell Industrial Application of Membranes for CO 2 Removal from Natural Gas William I. EchtUSPMembrane Distillation Process Design Applied to Highly Concentrated Brines:Mathematical Model and Operating Conditions AnalysisCarlos Eduardo Pantoja, Marcelo Martins Seckler, Yuri NariyoshiUSPPolymeric nanofiltration Membranes based on PVC and C-butyl Pyrogallol[4]arene or C-butyl Resorcin[4]areneSilvânia Marilene de Lima and Grégoire Jean-François DemetsUSPStudy of integrated use of Coagulation / Flocculation and Membrane SeparationProcesses Microfiltration and Ultrafiltration in WheyPaulo Ricardo Amador Mendes, Júlia de Goes Monteiro Antônio, Luís Fernando FigueiredoFariaUSPDiffusion of Monovalent Cations through Membranes Based on Polymers andcucurbituril IonophoresTiago Mateus B. Teodósio, Gregoire Jean-Françóis DemetsUTFPRRiver Water Treatment by Microfiltration with Sedimentation Pretreatment with anAlternative CoagulantAline Neher, Lucila Adriani Coral, Fatima de Jesus BassettiUTFPR/UFSC Saxitoxins Removal by NF270 e NF90 Nanofiltration Membranes Lucila Adriani Coral, Fatima de Jesus Bassetti, Flávio Rubens LapolliVictoria University / DeakinUniversityEffect of Plasma Activation on Polyamide Reverse Osmosis Membrane for ImprovedChlorine ToleranceRackel REIS, Ludovic Dumée, Mary She, John ORBELL, Mikel DUKE

Maximizing Hydrocarbon Liquids Recovery while Recovering High Purity CO 2 :New Operation Strategy for Membrane Based CO 2 Removal FacilitiesJason Dietrich * , Ankur Jariwala, G. Edward Mahley, Richard PetersCameron International, Jason.Dietrich@c-a-m.comCameron Cynara® CO 2 removal membranes have been successful and very well proven in theonshore as well as offshore markets for over 25 years. In recent years, there is a significant emphasisfrom Oil and Gas producers to maximize hydrocarbon liquids recovery while removing CO 2 fromnatural gas.Cameron operates the Cynara® membrane facility at SACROC in West Texas – owned by Kinder-Morgan – which processes 750 MMSCFD of natural gas by removing CO 2 from 90 mol% in the feedgas to 10 mol% in the product gas. Traditionally this facility was focused on maximizing natural gasrecovery while recovering high purity CO 2 using membranes. With growing demand of natural gasliquids in last couple of years, Kinder-Morgan is maximizing the advantage of Cynara® membranes towithstand and recover hydrocarbon liquids while removing CO 2 from natural gas. This was achievedby implementing several improvements in the existing facility including targeted membranereplacement, feed flow optimization, temperature increase, and improved temperature stability.The recent improvements in temperature control and increased heat capacity, along with membranereplacements, have resulted in large performance gains in certain parts of the facility. Combined withthe consistent monitoring of plant performance data in real-time, these changes have had a directresult in terms of hydrocarbon recovery gain, without negative effects to the CO 2 permeate purity.

Gas separation properties of Mixed Matrix Membranes comprising of Matrimid andFuntionalized Mesoporous MCM-41Asim Laeeq Khan a *, Chalida Klaysom b , Amit Gahlaut b , Ivo Vankelecom ba Department of Chemical Engineering, COMSATS Institute of Information Technology, Lahore,Pakistanb Center of Surface Chemistry and Catalysis, Faculty of Bioscience Engineering, KU Leuven, Belgiumalaeeqkhan@ciitlahore.edu.pkMixed matrix membranes (MMMs) can potentially improve the separation performance oftraditional polymeric membranes while still maintaining their processing advantages and lower costs.In this work, MMMs composed of Matrimid and SO 3 functionalized mesoporous silica spheres wereprepared by the solution casting method. Matrimid was chosen as the polymer matrix due to itsseveral inherent properties such as good processability, easy commercial availability, goodseparation properties, and good mechanical and thermal stability. The filler particles werefunctionalized with sulfonic acid (-SO 3 H) groups to increase the separation performance of themembranes by increasing the CO 2 solubility. The fast diffusion of gases through the mesoporousmaterials, accompanied by this increased CO 2 solubility, resulted in the simultaneous increase of gaspermeability and selectivity. CO2 permeation data and SEM images of the synthesized MMMssuggest that the fillers adhered well to the polymer matrix. DSC analysis of the membranes showsthat incorporation of unmodified MCM-41 particles into the Matrimid matrix has very little effect onthe T g , indicating the absence of interaction between the inorganic and polymeric phases. On theother hand and somehow surprising, the addition of SO 3 H - MCM-41 increased the T g of MMMs. Thispoints toward an increased interaction between the Matrimid and the filler particles, the nature ofwhich is not really clear. The comparison of DSC results suggest that the incorporation of the SO3Hfunctionalizedfillers in MMMs can be used as an effective tool to tailor the structure and propertiesof the membranes. Gas permeation tests indicated that the addition of functionalized MCM-41 topolymer matrix increases both the gas permeability and selectivity.The highest ideal selectivitiesobtained here for CO 2 /N 2 and CO 2 /CH 4 were 32.97 and 31.48 (CO 2 permeability = 9.13 Barrer),respectively. In order to evaluate the practical commercial viability of these membranes, they weretested under different operating pressures and temperatures and the results were plotted on theRobeson trade-off upper-bound.Fig. 1 TEM image of as-synthesized MCM-41Fig.2. SEM images of cross-sections of Matrimid membranescontaining 30% loading of (a-c) MCM-41

Synthesis and Gas permeation properties of Mixed Matrix Membranes comprisedof Acrylate derivitized PSf and Amine functionalized Mesorporous MCM-41 for CO 2separationAsim Laeeq Khan a *, Chalida Klaysom b , Amit Gahlaut b , Ivo Vankelecom ba Department of Chemical Engineering, COMSATS Institute of Information Technology, Lahore,Pakistanb Center of Surface Chemistry and Catalysis, Faculty of Bioscience Engineering, KU Leuven, Belgiumalaeeqkhan@ciitlahore.edu.pkMixed matrix membranes (MMMs) can potentially improve the separation performance oftraditional polymeric membranes while still maintaining their processing advantages and lower costs.In this work, MMMs composed of acrylate derivatized polysulfone and mesoporous MCM-41 wereprepared by solution casting. MCM-41 is a hexagonal member of the family of mesoporous silicamaterials, and possesses well-ordered one-dimensional pores. It is a promising material for MMMsbecause of several inherent advantages, such as high specific surface area, high CO 2 adsorption, highmechanical and thermal stability and easy surface modification. The high porosity of MCM-41facilitates faster gas diffusion through the pores compared to zeolites. The voids at the polymer-fillerinterface were removed by the introduction of covalent linkages between the modified polymer andthe functionalized fillers. Amino functional groups were deposited on the surface of as-preparedMCM-41 via a grafting method. Mesoporous silica MCM-41 with 100–150 nm in diameter wassuccessfully prepared. The as-prepared MCM-41 showed a highly ordered structure as can beconfirmed by the TEM image. Gas permeation results and SEM images of the synthesized MMMsconfirmed a good adhesion and dispersion of the fillers within the polymer matrix. In comparison toMMMs with unmodified MCM-41, covalently linked MCM-41 fillers rendered the MMMs significantlyhigher CO 2 /CH 4 and CO 2 /N 2 selectivities due to the presence of a covalent link between the -NH 2group of the filler and the acrylate of the polymer. The highest ideal selectivities obtained here forCO 2 /N 2 and CO 2 /CH 4 were 32.97 and 31.48 (CO 2 permeability = 9.13 Barrer), respectively. Theperformance of membranes under mixed gas feeds and different operating temperatures was alsostudied. The performance of MMMs was further investigated by varying the feed temperature. Theresults were in agreement with the expected trends for gas transport via solution–diffusionmechanism in glassy polymers. The higher temperature increases the CO 2 permeability due to theincrease in flexibility and free volume within the polymer matrix. However, the flux of the nondesirablegas (CH 4 and N 2 ) increases slightly more with the increase in temperature, resulting in anoverall decrease in selectivity with increasing temperature.abFig. 1. SEM images ofcross-sections of MMMs containing a 30% loading of (a) PSfAc-MCM-41 and(b)PSfAc-NH2-MCM-41.

Fig. 2 Pure gas (CO 2 ) permeabilities and ideal selectivities for PSfAc-MCM41 and covalently linkedMMMs (10 bar and 25 o C).

Synthesis and characterization of Fluorinated and Sulfonated Aromatic PEEKmembranes; Application in CO 2 separationAsim Laeeq Khan a *, Chalida Klaysom b , Amit Gahlaut b , Ivo Vankelecom ba Department of Chemical Engineering, COMSATS Institute of Information Technology, Lahore,Pakistanb Center of Surface Chemistry and Catalysis, Faculty of Bioscience Engineering, KU Leuven, Belgiumalaeeqkhan@ciitlahore.edu.pkThis paper describes the performance of fluorinated and sulfonated aromatic poly(ether etherketone) (FS-PEEK) membranes, directly prepared from the sulfonated monomer, for CO 2 separationfrom gas mixtures containing N 2 or CH 4 . Dense membranes with different degrees of sulfonationwere prepared via solvent evaporation. Increasing degree of sulfonation simultaneously improvesthe permeability and selectivity of both gas pairs. The effect of counterions was investigated byconverting FS-PEEK membranes from the Na + -form in which they are prepared, to the H + andmultivalent cationic forms. Gas permeability and selectivity for polymers with divalent and trivalentcounterions were higher than those for polymers in the monovalent and H + -forms. In order to studythe stability and potential industrial application of these membranes, they were tested at differentconditions of feed pressure, temperature and CO 2 feed concentration.

Evaluation Of The Application Of Nanofiltration To Concentrate TheHydroethanolic Extract Obtained From Grape Juice MarcNatalia Barbosa Eitel* 1 , Ana Paula Gil Cruz 2 , Luiz Fernando Menezes da Silva 3 , Suely PereiraFreitas 1 , Lourdes Maria Correa Cabral 31 Universidade Federal do Rio de Janeiro - Escola de Química/UFRJ, Rio de Janeiro, Brasil.2 Universidade Federal do Rio de Janeiro - Instituto de Química/UFRJ, Rio de Janeiro, Brasil.3 Embrapa Agroindústria de Alimentos, Rio de Janeiro, Brasil.*e-mail: natalia.eitel@poli.ufrj.brSome environmental problems followed the rapid industrialization of the past decades. In the case ofthe food industry, particularly the ones processing vegetables and fruits, the main problem observedis the inadequate disposal of its wastes. When it comes to grape juice industries, the main wastegenerated and also of the highest volume is the marc, basically consisting of skins and seeds. Thisresidue has a large recovery potential and a high cost of treatment due to its high biochemical andchemical oxygen demand (BOD and COD) [1, 2]. Because of its rich phenolic composition and greatantioxidant potential, several works have been conducted to evaluate its use as an alcoholic extract[3-6]. It is known, however, that these bioactive compounds are thermolabile. The aim of this study,therefore, is to evaluate the application of nanofiltration to concentrate the hydroethanolic extractobtained from grape juice marc. The nanofiltration was chosen due to its characteristics: energysavings, selectivity, separation of thermolabile compounds and simplicity of operation [7].The bagasse, previously hydrated during 1 hour at 30°C, suffered a hydroethanol extraction with 30%ethanol, pH 4.0 adjusted with citric acid, in proportion of 9:1 solvent: substrate during 120 min at50°C under a mechanical stirring of 48RPM. The nanofiltration was carried out in spiral woundpolyamide membrane modules system with a filter area of 2,5m 2 . The process was conducted during61min at 40°C with applied pressure of 12 bar in the system, which was previously determined byevaluation of the limiting flux at 20°C, 30°C and 40°C, under a fed batch until a volumetricconcentration factor of at least 10 was reached. The permeate stream was fully collected and its fluxmeasured in kg.h -1 m -2 every 5 minutes. Samples of the streams were collected and submitted foranalyzes of antioxidant activity (AA) [8, 9], total phenolics (TP) [10 modified by 11] and total (TA) andmonomeric (MA) anthocyanins [12]. The results are shown in Table 1 below.Table 1 – Analytical Results Obtained For The Different Process StreamsStream AA 1 TP 2 TA 3 MA 3Feed 4,32 ± 0,13 55,40 ± 2,77 13,71 ± 0,07 10,90 ± 0,06Permeate N/D N/D N/D N/DRetentate 49,02± 6,72 593,17 ± 25,64 155,23 ± 3,48 119,42 ± 4,131-μmol Trolox∙g -1 ; 2-mg Gallic acid∙100g -1 ; 3-mg malvidin-3,5-diglucoside∙100g -1 ); N/D- Not DetectedThe nanofiltration process proved itself as an attractive alternative for the concentration of bioactivecompounds recovered from the grape marc through a hydroethanol extraction. However other testsshould be performed to confirm these results and determine the influence of other processparameters on its concentration and its permeate flux.

[1] M. R. Kosseva (2009), Processing of food wastes, Adv. Food Nutr. Res., 58, 57-136.[2] A. C. Habert et al. (2006), In: Processos de Separação por Membranas, Rio de Janeiro, E-papers.[3] M. A Bustamante et al. (2008), Waste Management, 28, 372–380.[4] D. Amendola et al. (2010), J. of Food Engineering, 97, 384-392.[5] J. M. Luque-Rodríguez et al. (2007), Bioresource Technology, 98, 2705-2713.[6] G. Spigno et al. (2007), J. of Food Engineering, 81, 200-208.[7] Y. Yilmaza et al. (2006), J. of Food Composition and Analysis, 19, 41-48.[8] V. L. Singleton et al. (1965), Am. J. Enol. Vitic., 16, 144-168.[9] R. Re et al. (1999), Free Radic. Biol. Med., 26, 1231-1237.[10] S. Georgé et al. (2005), J. of Agricultural and Food Chemistry, 53, 1370-1373.[11] M. M. Giusti et al. (2001), Characterization and mesasurement of anthocyanins by UV-visible pectroscopy,In: Current Protocols in Food Analytical Chemistry, New York: Wiley.[12] M. S. Rufino et al. (2007), Metodologia Científica: Determinação da atividade antioxidante total em frutaspela captura do radical ABTS + , Comunicado Técnico Embrapa Agroindústria Tropical, 128.

Environmental Performance Comparison between Bench Scale andWastewater Treatment Plant Membrane BioreactorsTiago Chagas de Oliveira Tourinho (1)*Ofélia de Queiroz Fernandes Araújo (1)Isaac Volschan Junior (1)(1) Universidade Federal do Rio de Janeiro – tiago_tourinho2@yahoo.com.brWastewater treatment with membrane bioreactor (MBR) combines biological process with amembrane separation process. It is increasingly adopted to treat municipal wastewaters, producinghigh-quality effluent with a small footprint [1], and is one of the most outstanding and up to datetechnologies applied to wastewater treatment. However, it presents some disadvantages, like highenergy consumption (0.4–1 kWh/m 3 compared to conventional activated sludge process (CASP),values ranging from 0.3 to 0.4 kWh/m 3 ) [2], and the necessity of chemical cleaning to prevent fouling.All these features have to be considered in the decision-making process of MBRs implementation,not only on the economic but also on the environmental point of view, aiming a holistic evaluation.Aiming at a better understanding of the environmental impact differences between CASP and MBRprocesses, this study evaluates the environmental performance of MBRs in two scales: MBR benchexperiments (BE) and MBR wastewater treatment plants (WwTPs). In this direction, the study intendsto 1) investigate energy consumption (assumed hydropower), sodium hypochlorite (NaClO) forchemical cleaning, and permeated pollutants, expected to exhibit biggest potential impact; 2)identify which impact category is the most relevant; 3) compare the impacts of MBR-BE to MBR-WwTPs to identify scale effects; 4) discuss correlations between operational conditions andenvironmental effects [3][4]. SimaPro 7.2, a life cycle analysis software, was used as a tool for theevaluation of the overall environmental impacts. The results indicated, for all investigated cases, thatelectricity was the most impacting aspect. The most relevant impact category, for NaClO andelectricity, was human toxicity, while for the permeated pollutants the category freshwatereutrophication showed highest impact. A reduction of impact with an increase in process scale wasobserved: 98.4% for energy; 30.4% for NaClO, and 98.3% reduction for overall impact. Last, it wasobserved that when the NaClO(g)/kWh ratio is greater than or equal to 2.595, NaClO will be moreenvironmentally impacting than energy consumption.References[1] J.-H. Choi, H. Y. Ng (2008), Chemosphere, 71, 853–859.[2] A. Hospido et al. (2012), Desalination, 285, 263–270.[3] M. Gander et al. (2000), Separation and Purification Technology, 18, 119–130.[4] S. Judd (2011), The MBR Book: principles and applications of membrane bioreactors for water andwastewater treatment. 2nd ed. Oxford: Elsevier.

Electrodialysis as desalting or purification step in petrochemical industriesFlorence Lutin* ; Daniel Bar**(*) Eurodia Industrie S.A. (Fr) florence.lutin@eurodia.com(**) Ameridia (US) dbar@ameridia.comOn offshore platforms for gas production, Natural gas is dehydrated to avoid corrosion or pipelineplugging due to ice or hydrate formation. The traditional way to dehydrate the gas is by absorption inTriethylene Glycol (TEG) or Diethylene Glycol. This glycol solution is recycled but it becomes loadedwith (sea)salt. To avoid pipeline plugging due to the precipitation of salt, the Ethylene Glycolsolutions must be treated. The conventional process to regenerate Glycol solutions are vacuumdistillation and ion exchange resins. Electrodialysis (ED) technology can be applied to remove saltsfrom Glycol solution. Compared to vacuum distillation, the ED process is more economical. The mainbenefit compared to ion exchange resins is to avoid the huge consumption of chemicals forregeneration.Another application of ED is amine purification/regeneration in flue gas scrubbing processes inindustries such as chemical, sulphur smelters, or oil refineries. The goal is to clean the flue gasses andobtain a regenerable Sulfur Dioxide (SO 2 ) stream. This technology uses an aqueous amine solution toachieve a high efficiency selective absorption of Sulfur Dioxide from a large variety of gas streams.The process is similar to conventional amine-based gas treating units in refineries and natural gasprocessing. ED is applied to purify the amine solution from heat-stable salts. Regenerating theabsorbent eliminates the high cost of consumables, while its high capacity and selectivity reducecapital costs. Effluents from the process are minimal compare to ion exchange; as a result, it can beconsidered as an “eco-friendly” process.EURODIA has developed a three-compartment EUR40 ED stack for these customers. The amine isneutralized or substituted by another anion inside the stack. Alternate processes require thedemineralization of the amine solution with conventional two-compartment ED stacks.During the last few years, Eurodia Industrie has developed new types of electrodialysis (ED) stacks toachieve high one-pass desalination rates of up to 80 % and allow for very compact systems. Thesesystems are very well suited to process brackish waters or salted solution with low salt levels(between 1 and 5 g/l). These compact ED systems can also easily be paired with reverse osmosisunits to increase the water recovery rate from ~75% to 95%. In addition, Eurodia is very interested inthe Capacitive Deionization (CDI) Technology, because of the great process simplifications that canbe achieved, still with high recovery rates (90% with desalination rates of up to 90%). To developapplications for CDI, Eurodia is working in partnership with Enpar Technologies (Guelph, Ontario,Canada). Overall, the main objective of Eurodia for water treatment applications is to develop small,compact, and simple units, consuming low energy (potentially powered by solar energy), and thatcan be installed in batteries for larger capacities.In the agro-food industries, EURODIA proposes complete process line for desalination andpurification of products such as whey, speciality sugars (Inuline, FOS, etc.), starches, and wine. Allthese processes combine several membrane technologies: such as ED, NF, and RO to propose themost cost effective processes with an “eco-friendly” strategy while obtaining the highest qualityend-products. In Brazil several plants are in operation for whey demineralization (DM90) and winemuststabilization.

SANASA Capivari II – The First Full Scale Municipal MBR in Latin AmericaRenato Rossetto 1 , Renata Lima Pereira de Gasperi 1 *, Juliana Pontes Machado Andrade 1 ,Rovério Pagotto Jr. 1 , Romeu Cantusio Neto 1 , Joubert Trovati 2 , Marcus Vinicius GueriniVallero 2 , Brian Arntsen 2 , José Everaldo Elorza Prado³1 Sociedade de Abastecimento de Água e Saneamento S/A - SANASA, 2 GE Water and ProcessTechnologies, ³E.M.A. Engenharia de Meio Ambiente Ltda,* tratamento.esgoto@sanasa.com.brThe macro region of Campinas (Brazil) is rapidly evolving with new housing developments andindustries, with the challenge of finding new ways to treat wastewater to a quality that can bereused in order to overcome water scarcity problems. To address this challenge, SANASA (publiclyowned water & wastewater concessionaire from Campinas) has recently constructed the “EPAR(Water Reuse Production Plant) Capivari II with the GE ZeeWeed 500D ® UF membrane system. This isthe first large scale MBR system in Latin America with biological tertiary treatment capability(nitrogen and phosphorus removal), being able to treat an average flow of 182 L/s in its first phase ofconstruction (Figure 1). The filtration system is composed of 3 membrane trains with more than36.000 m 2 of total membrane filtration area.Figure 1: Aerial view of the SANASA Capivari II Wastewater Treatment and Reuse Facility inCampinas, Brazil.The MBR plant was commissioned in April, 2012 and during the first year of operation permeatequality has exceeded expectations. COD removal rates are above 95% on a consistent basis. The

average permeate BOD 5 and NH 3 concentrations were respectively 0,92 mg/L and 0,15 mg/L, with aturbidity lower than 0,3 NTU (Table 1).Table 1 Summary of feed and effluent quality for the SANASA Capivari II MBR plant.ParameterFeed(raw sewage)Permeate(treated effluent)AverageRemovalRange Average Range Average (%)COD (mg/L) 650 – 770 725 17 – 30 23,4 96,9BOD 5 (mg/L) 324 – 390 360 0,5 – 2 0,92 99,8TKN (mg/L) 66 – 96 83 0,01 – 1,80 0,74 98,6NH 3 -N (mg/L) 32 – 69 54 0,01 – 0,29 0,15 99,7TN-N (mg/L) 68 – 97 85 4,5 – 6,9 5,3 93,8TP (mg/L) 8,2 – 10,0 9,1 0,98 – 7,35 3,05 73,0TSS (mg/L) 276 – 332 307 0,6 – 2,0 1,1 99,7Turbidity (NTU) - - 0,18 – 0,28 0,23 -Treated effluent is sent to a water reuse accumulation tank (from where in future reuse water will bepumped to potential customers) and currently it is being discharged to the Capivari River.This paper will present key information related to the MBR system design, start-up and operation,giving special attention to design recommendations for the generation of high quality effluent forpotential reuse. The procedures for the successful start-up of the MBR system will be discussed andthe performance data (biology performance and membrane performance) from the first year ofoperation will be presented.

Desalination of High Salinity Wastewater Using Electrodialysis: OperatingVariable Effects and Water Transport PhenomenaShingjiang Jessie Lue* and Jie-Ting YuDepartment of Chemical and Materials Engineering and Green Technology Research Center, ChangGung University, Kwei-shan 333, Taoyuan, TaiwanEmail: jessie@mail.cgu.edu.twThe objective of this study is to establish desalination efficiency for wastewater using electrodialysis(ED) technology. The effects of applied current density and process time on electrical efficiency,power consumption, salt rejection, and water recovery were investigated for industrial high-salinitywastewater from polycarbonate industry. In the electrodialysis of 6 % NaCl solution, the salt rejectioncould achieve 99.95 % with 60 % water recovery at 4 A (7.81 mA/cm 2 ). The power consumption was46.04 kWh/m 3 and average current efficiency was 47.09 % during the operation for 11 hours. Whenprocessing the industrial wastewater at the same current density, the rejection was 99.98 % with52.63 % water recovery. The power consumption was 131.18 kWh/m 3 and average current efficiencywas 20.08 % during the 13-hour operation. For industrial wastewater, the power consumption andoperating time were higher than that for the model NaCl solution to obtain similar desalination level.The water recovery in the ED process was studied and the water transports across the membranewere determined and ascribed to ion hydration and osmotic pressure effects. Water transport withhydrated ions was mainly affected by the salt reduction level. It was assumed that water loss for theindustrial wastewater due to ion hydration was the same as the model NaCl solution at thecomparable salt removal level. The water loss due to osmotic pressure was higher for the industrialwastewater than that of the model NaCl solution. The water loss could be as high as 2.55 L from 10-Lfeed in the former case. The water quality was evaluated before and after the ED process. Theconcentration of total dissolved solids, total organic compounds, ionic species, and conductivity werereduced by 99.77 %. This study demonstrates that ED is an effective way to recover and reclaimpurified water from high salinity wastewater.Fig. 1. Permeate conductivity decreased withoperating time at different applied voltages(12 and 20 V) on wastewater.Fig. 2. Permeate water loss in electrodializedwastewater due to hydration and osmosis as afunction of salt reduction level using differentdifferent applied voltages (12V and 20V).

Evolution of Ion-Exchange Membranes Behavior in Full Scale Electrodialysisfor Food IndustryW Garcia-Vasquez 1* , L Dammak 1 , C Larchet 1 , V Nikonenko 2 , D Grande 1 ,1 Institut de Chimie et des Matériaux Paris-Est (ICMPE) UMR 7182 CNRS, Thiais, France.2 Kuban State University, Krasnodar, Russia.* garcia-vasquez@icmpe.cnrs.frIn this communication, physico-chemical, structural and mechanical properties of ionexchangemembranes (IEMs) were investigated throughout their lifetime in a full scaleelectrodialysis (ED) stack used for whey demineralization, to get a deeper insight into theunderstanding of IEM degradation. This fundamental investigation reveals significant issuesconcerning IEMs properties and their long-term behavior. The approach is based upon theinterpretation of the membranes characterization in actual ED for whey demineralization bymeans of a systematic analysis of new samples and samples used at different times.Samples of a cation-exchange membrane (CEM) and an anion-exchange membrane (AEM),CMX-SB and AMX-SB respectively, were taken from an industrial ED stack at 45%, 70% and100% of their lifetime in whey demineralization (several thousands of h). To take out everysample it was necessary to stop the production and disassembly the ED stack; a fresh samplewas also studied to compare a new membrane with the used ones and to establish theevolution of membrane characteristics with time. This kind of membranes are made offunctionalized polystyrene crosslinked with DVB (PS-DVB) and finely powdered poly vinylchloride (PVC), all of this coated onto a PVC cloth used as reinforcing material. Membraneswere characterized by its physicochemical properties: conductivity, permeability, exchangecapacity, thickness, water uptake, contact angle; structural and elemental properties: SEM,EDX, FTIR, ICP, nitrogen sorption porosimetry, etc.; mechanical by the tensile strength test.The microheterogeneous model was applied to describe the samples structure/propertiesrelations.After characterization, it was seen that CEM samples were more robust and resistant thanthe AEM counterparts, which were more unstable. Furthermore, CEM samples were stillfunctional while AEM had to be replaced from the ED stack. The same phenomenon wasobserved previously when the same kind of membranes were studied for anotherapplication in ED for the food industry [1-3]. The results of AEM will be explained in furtherdetail to get a deeper insight into the understanding of AEM degradation.With increasing time of operation, the membranes became darker and more fragile. Therewas not a significant loss of the ion-exchange capacity or degradation of the functionalpoly(styrene-co-divinylbenzene). However, fouling (observed by FTIR) causes a decrease inthe counter-ion mobility within the membrane which produces a reduction of the electricalconductivity (Fig 1).

Conductivity (mS/cm)Contact angle (°)Permeability (10 -9 m 2 *s -1 )By means of SEM images and the BET specific surface area (Sp) it was possible toacknowledge that membrane porosity increased gradually with the time of operation. Thisexplains the increase in permeability by the appearance of new pores which form channelsfor non-selective electrolyte transfer.9.28.88.48.07.67.26.86.46.00 20 40 60 80 100Lifetime (%) Water content (%)282624222018• Thickness (mm)0.190.180.170.160.150.140.130.1210090807060503,02,52,01,51,00,50,00 20 40 60 80 100Lifetime (%)Fig. 1. Physico-chemical properties of AEM samples in function of their lifetime. Conductivity,water uptake, thickness and contact angle (right). 0.1M NaCl permeability (left)Via Soxhlet extraction with THF, 44% of the new membrane was recovered as extractable.This decreased gradually up to 11.4 for the membrane at 100% of lifetime. Extractable wasrecognized by FTIR we as PVC. Accordingly, new pores in the membrane were created by theloss of PVC washed out from the membrane during the cleaning-in-place process in ED.These new pores contribute not only to increasing electrolyte permeability, but also togrowing conductivity in the last stage of ED. The latter is due to the fact that there is asubstitution of non-conductive regions occupied by PVC for pores filled with electrolytesolution apparently containing also organic components of whey.The new AEM sample presented a combination of the mechanical properties associated withthe two polymeric components, i.e. the rigidity of PS-DVB and the toughness of PVC.However, the loss of PVC had severe consequences in the mechanical properties of the AEM.As it was seen in the stress-strain curves, the Young Modulus, which indicates the rigidity ofa material, decreased by 20% from A0 to A3. The breaking strength, which represents themembrane plasticity, decreased by 45% and the area under the stress-strain curvedecreased of almost 80%, which strongly indicated a loss of the material toughness.ConclusionWe have found that there are several events accompanying the process of membraneageing. Fouling occurs from the beginning of the operation leading to a decrease in thecounterion mobility. The following phases of membrane deterioration are apparently due tothe loss of PVC which results in formation of non-charged pores within the membranematrix, available for electroneutral electrolyte solution and for large molecules coming fromwhey. In addition, membrane toughness decreases. Gradually the AEM membraneconverted from rigid and tough to rigid and brittle material. This caused formation of cracksand tears leading to membrane final failure in the ED stack.

References[1] R. Ghalloussi, W. Garcia-Vasquez, N. Bellakhal, C. Larchet, L. Dammak, P. Huguet, D.Grande, Ageing of ion-exchange membranes used in electrodialysis: Investigation of staticparameters, electrolyte permeability and tensile strength, Sep. Purif. Technol., 80 (2011)270-275.[2] R. Ghalloussi, W. Garcia-Vasquez, L. Chaabane, L. Dammak, C. Larchet, N. Bellakhal,Decline of ion-exchange membranes after utilization in electrodialysis for food applications,Phys. Chem. News, 65 (2012) 66-72.[3] R. Ghalloussi, W. Garcia-Vasquez, L. Chaabane, L. Dammak, C. Larchet, S. Deabate, E.Nevakshenova, V. Nikonenko, D. Grande, Ageing of ion-exchange membranes inelectrodialysis: A structural and physicochemical investigation, J. Membr. Sci., In press(2013).AcknowledgementsThe study was realized within French-Russian laboratory "Ion-exchange membranes andrelated processes". We are grateful to CNRS, France, and to RFBR (grants 11-08-93107_CNRSL, 12-08-00188_CNRSL, 13-08-96508r_yug) Russia, and to FP7 Marie CurieActions "CoTraPhen" project PIRSES-GA-2010-269135 for financial support.

Preparation and Characterization of Nanofiltration Membranes based onPolisulfonamideCelina C. R. Barbosa 1 , Edna T. R. Bastos 1* , Elizabeth E.M. Oliveira 1 , Eliane P. B. Soares 1 ,Jaciara C. Silva 1 José Luis Mantovano 21Instituto de Engenharia Nuclear (IEN / CNEN)Rua Hélio de Almeida 75 – 21941-906 - Rio de Janeiro – Brasil* ednaruas@ien.gov.brAbstract. The membrane separation processes are becoming an increasingly important alternativepurification of the products and in water treatment in general. One such process is nanofiltration(NF), an intermediate process between reverse osmosis and ultrafiltration membranes. The NFmembranes have the property of separate molecules of low molecular weight and multipurpose ion[1]. NF membranes are obtained mainly by interfacial polymerization between a diamine and an acidchloride. The performance of NF membranes is dependent on several factors such as type and ratioof monomers used, preparation and condition of post-treatment. The piperazine (PIP) is a monomerwidely used for interfacial polymerization, which reacts with trimesoíla chloride (TMC), leading toformation of NF membranes poly (piperazinamida) [2] .This work aims to synthesize, characterize and evaluate NF membranes with selective layerpolisulfonamide obtained through the reaction between diamines: PIP/4,4diaminodiphenylsulfone(DDS) and the acid chloride (TMC) using as support the commercial membrane UF of poly (ethersulfone) (PES). The membranes were characterized as transport properties and content of DDSincorporated in the selective layer for the following analyzes: Infrared (IR) and X-ray diffraction.Experiments to determine the transport properties: permeate flux and rejection of sulphate ionswere performed using a permeation system with displacement tangential flow with operatingpressure of 15 bar. The concentration of sulfate in the solutions permeated and feeding weredetermined in ICS-1000 ion chromatograph and the rejection of the membranes calculated accordingto the equation:R (%) = (1-Cp/Ca) x100Regarding the results it can be concluded that the rejection of sulphate ions decreases withincreasing content of DDS, probably due to the larger size pores of the selective layer. Through X-raydiffraction was confirmed incorporation of the DDS in every synthesized membrane.Keywords: nanolfiltration,polisulfonamide, interfacial polymerizationReferences[1] W. J. Lau, A. F. Ismail, N. Midsdan, M. A. Kassim. A recent progress in thin film composite membrane: areview, Desalination. (2011) 1-10.[2] M. Jahanshahi, A. Rahimpour, M. Peryavi. Developing thin film composite poly (piperazine-amide) and poly(vinyl-alcohol) nanofiltration membranes, Desalination 257 (2010) 129-136.

Development of Sulfonated Polysulfone Composite Membranes forAmmonium RejectionEdna T. R. Bastos *1 , Celina C. R. Barbosa 1 ,Jaciara C. Silva 2 , Vanessa B.C. Queiroz 2 and DelmoS. Vaitsman 31Instituto de Engenharia Nuclear (IEN / CNEN)Rua Hélio de Almeida 75 – 21941-906 - Rio de Janeiro – Brazil2 Bolsista CT/Petro3Departamento de Química Analítica, Instituto de Química, Universidade Federal do Rio deJaneiro,Av. Athos da Silveira Ramos, 149, room A-519 – 21941-909 - Rio de Janeiro – Brazil* ednaruas@ien.gov.brAbstract. In the present investigation, were synthesized compositemembranes prepared by simultaneous casting of two polymersolutions using the technique of phase inversion by immersion /precipitation [1,2]. The support layer was prepared usingpolyethersulfone and polysulfone as base polymer and for the toplayer was used sulfonated polysulfone (SPSU) with 50% sulfonationdegree [3,4] . The morphology of the resulting membranes wascharacterized by scanning electron microscopy (SEM). The finalresults showed that it is possible to prepare composite membranesby simultaneous casting of two polymer solutions with adherencebetween the two layers. Regarding the permeation tests, thedeveloped membranes presented values of hydraulic permeabilitywithin the range of commercial nanofiltration (NF) membranes [5,6](Table 1). Values rejection of 80% ammonium ions can be increasedby using a SPSU with a greater degree of sulfonation [7].

CodeMembraneTable - Transport Properties of the compositemembranes synthesized and commercialPermeateflux(L/m 2 . h)Hydraulicpermeability(L/m 2 h. bar)(NH 4 ) 2 SO 4(%) R NH4+NH 4 ClM-12 18 2.0 71 4M-15 2 1.2 80 4M-22 24 4.1 78 4M-23 29 8.0 15 3M-30 131 22.1 < 1 < 1M-32 123 19.1 < 1 < 1*DK 12 2.4 99 3*DL 11 2.0 92 3*commercialKeywords: polysulfone sulfonated; composite membrane; ammoniumrejection.References[1] Bastos, E.T.R. (2006), “Development and application of polymericmembranes in the removal ammonium in wastewater" Universidade Federaldo Rio de Janeiro, Brazil.[2] Chen, S.H., Liou, R.M., Lin, Y.Y., Lai, C.L., Lai, J.Y. (2009), "Preparation andcharacterizations of asymmetric sulfonated polysulfone membranes by wetphase inversion method", European Polymer. J., 45, 1293-1301.[3] Ding, Y., Bikson, B. (2010), "Preparation and characterization of semicrystallinepoly (ether ketone) hollow fiber membranes", Journal ofMembrane Science, 357, 192–198.[4] Lufrano, F., Baglio, V., Staiti, P., Arico, A. S., Antonucci, V. (2006),"Development and characterization of sulfonated polysulfone membranesfor direct methanol fuel cells" Desalination, 199, 283- 285.[5] Mulder, M. (2000), Basic principles of membrane technology, 2 nd ed.,Kluwer Academic Publishers, Dordrecht.[6] Schafer, A.I., Fane, A.G. and Waite, T.D. (2005), Nanofiltration: principlesand applications, Elsevier, Oxford.[7] Mashallah, R., Saeed, S., Sayed, N.A. (2012), “Simulation of ammoniaremoval from industrial wastewater streams by means of a hollow - fibermembrane contactor" Desalination, 285, 383-392

Selectivity of Nanofiltration Membranes for Treatment of Liquid WasteContaining UraniumElizabeth E. M. Oliveira 1* , Celina C. R. Barbosa 1 and Júlio C. Afonso 21Instituto de Engenharia Nuclear (IEN / CNEN)eemoju.gmail.com2Departamento de Química Analítica, Instituto de Química,Universidade Federal do Rio de JaneiroThe Nuclear Fuel Factory of INB is one of the most modern industry for the production of nuclear fuelfor the light water reactors PWRs (Pressurized Water Reactor), adopted by Brazil for the generationof nuclear-electricity. These reactors use enriched uranium in the isotope 235, which to the undergofission generates thermal energy in the reactor core. The production of uranium dioxide (UO 2 ) fromthe reconversion of uranium hexafluoride gas (UF 6 ) is the most important step in the cycle of nuclearfuel. The UF 6 (g) is heated in an autoclave and vaporized into a tank containing demineralized waterto 100 º C, where it is mixed with other two gases: carbon dioxide (CO 2 ) to prevent clogging of thenozzle of UF 6 and ammonia gas (NH 3 ) [1]. The chemical reaction between these compounds producesuranato tricarbonate (VI) ammonium known as (TCAU), yellow solid water insoluble. Theregenerating streams of waste liquid containing uranium, one of these waste streams is called"carbonated water" due to the presence of high concentration of CO 3 2- in its composition, this wasteis originated from washing of the gases generated in the thermal hydrolysis of the uranato thetricarbonate (VI) and ammonia is generated a volume of approximately 2.5 m 3 per tonne of uraniumoxide. This type of waste can contain up to 0.050 g L -1 of uranium in solution. The goal is recover theuranium, which may return to the productive process of UO2 pellets. The application of PSM in thetreatment of radioactive waste is relatively recent, only in recent years membrane technology hasbeen gradually introduced in the nuclear area for the treatment of radioactive waste of low andmedium activity (

References*1+ “Indústrias Nucleares do Brasil, http://www.inb.gov.br (2009).*2+ Z.T. Grażyna, H. Marian and, G.C. Andrzej (2001), Separation and Purification Technology., 22-23, 617-625.[3] Z.T. Grażyna, Journal of Membrane Science 225, (2003), p 25-39[4], S.J. Macnaughton, J.K. McCulloch, K. Marshall and, R.J. Ring (2002), in Technologies for the treatment ofeffluents from uranium mines, mills and tailings, IAEA, Vienna, pp. 55-65.[5] CONAMA - National Brazilian Environmental Council (2005), Directory 357, March 17, 2005, Official Journal,March 18 (in Portuguese).[6] CNEN - Directory 6.05 (1985), Radioactive wastes management in nuclear installations, CNEN, Brasília (inPortuguese).[7] M. Dulama, N. Deneanu, E. Dumitru, I.V. Popescu and M. Pavelescu (2008), Proceedings of NUCLEAR 2008annual international conference on sustainable development through nuclear research and education,Pitesti, May, pp. 426-433.[8] L. Kwang-Lung, Chu, Min-Lin and Shieh, Mu-Chang (1987), Desalination, 61, 125-136.[9], A.I. Schäfer, A.G. Fane and, T.D. Waite (2005), Nanofiltration: principles and applications, Elsevier, Oxford,2005.

Clarification of RED Beetroot Juice Using Rotating Ceramic Membrane Discs toObtain a Betalain Pigment SolutionBeatriz Cancino-Madariaga*, Andrés Ramírez Salvo, Paula Pinto VillegasINPROMEM E.I.R.L. (Research in membrane Process) Address: Carrera 241, Villa Alemana, CHILE.bcancinomadariaga@gmail.comRed beetroot (Beta vulgaris) is one of the most important sources of betalains used in food coloring.Betalains have healthy properties and can be used as additives in desserts, baked foods, dry mixes,dairy products and meat products. Common betalain extraction from red beetroot is generallyperformed using water mixed with organic solvents such as methanol or ethanol. However,nowadays there is an increased preference for natural extraction methods without the addition ofsolvents. Thus, the use of membranes and warm water extraction is an alternative for juiceclarification. The clarified pigment solution can then be concentrated by other membrane processes,such as Nanofiltration. The aims of this work we present the use of rotating ceramic membrane discs(RCMD), to clarify a red beetroot juice to obtain a betalain pigment solution free of turbidity.Methods. To obtain the betalain solution, fresh beetroot was processed. The steps in the operationwere peeling, milling, warm water extraction and centrifugation. The liquid phase was used as theprocess fluid for microfiltration. An RCMD with an area of 0.1 m2 and a pore size of 0.2 µm was used.Since the turbulence of the membrane leads to fouling, permeability and membrane foulingresistance were studied. The RCMD was tested at 15 °C with water at different rotation frequenciesbetween 0 and 30 Hz and between 0 and 1.4 bar obtaining a model function. The RCMD with theprocess fluid was also studied at the same temperature and rotating frequency, and with twotransmembrane pressure levels (TMP), 0.6 and 0.8 bar. Turbidity, sugar and betalains weredetermined. Turbulence was measured in terms of Reynold and shear stress (SS). The influence ofthe feed flow was also studied using two different pumps.Results. The model function to describe the behavior of the water was obtained. The behavior for theprocess fluid at different frequencies was also developed for TMP levels of 0.6 and 0.8 bar. For bothTMPs the turbidity in the permeate was 0; however, there are differences in the flux. The best fluxfor 0.6 bar, was 1.55 •10 -5 m³/m²s at 20 Hz. The flux was optimal at this frequency. There was noinfluence from the pumps on the behavior of betalain permeation or on permeate flux. The SS of theRCMD depends on the rotation frequency, with less than 1 s -1 not relevant.Conclusions: SS produced by RCMD is not relevant for betalain properties, as structure andcharacteristics are maintained. The betalain transmission is over 80% depending on rotationfrequency and TMP. The clarification of the red beet juice using RCMD is complete, producing apermeate with 0 NTU of turbidity.

Study of Parameters on Preparation of Composite Membranes Based onActivated CarbonKarla Patricia Macedo Licona*, Marcello Pojucan Magaldi Santos*, Amal Elzubair Eltom**and José Carlos da Rocha** National Institute of Technology** Metallurgical and Materials Engineering Program, COPPE/UFRJIn this work, membranes based on activated carbons have been studied, and because of thelarge surface area and, consequently, adsorption capacity of pores, has a wide use forpurification of liquids or gases in its fullness. The basic idea is the sophistication oftechnologic domain to obtain composite membranes based on organic resin – activatedcarbons that have apparent porosity as UF membranes. The membranes were prepared with40% epoxy resin and 60% commercial activated carbon MADECARBO® micro and mesaporous, raw state and dried at 100° C, analyzing three types of solvents (toluene, ethylacetate and ethyl alcohol). The physical properties, as Arquimedes density, showed apparentporosity between 47%-70% to raw carbon and 49%-62% to dried carbon. The microstructureof the specimens was evaluated by scanning electron microscopy, indicating goodhomogeneity of the resin-carbon interaction for both formulations with raw and driedcarbons. The flow tests were performed in a cell test for tubular membranes that simulatesparallel flow type filter. For the flow, the formulation that presented lowest results of thisproperty was the carbon dried in ethyl acetate. As for the raw carbon, the lowest flow resultobtained was the same dried carbon but dried in ethyl alcohol. From the results, it wasconcluded that this filtration systems are strongly influenced by the formulation obtainingprocess and, consequently, the microstructure plays an important role for the type offiltration obtained.

Definition Of The Limiting Flux Condition In The Nanofiltration Of A GrapeMarc Extract Containing 30% EthanolAna Paula Gil Cruz¹*, Natalia Barbosa Eitel², Luiz Fernando Menezes da Silva³, Suely PereiraFreitas², Alexandre Guedes Torres¹, Lourdes Maria Correa Cabral³¹Universidade Federal do Rio de Janeiro/UFRJ, Instituto de Química, Rio de Janeiro, Brasil. -ana_gil@uol.com.br.²Universidade Federal do Rio de Janeiro/UFRJ, Escola de Química, Rio de Janeiro, Brasil.³ Embrapa Agroindústria de Alimentos, Rio de Janeiro, Brasil.Grape marc, being composed of skins and seeds, presents an interesting composition in phenoliccompounds, whose recovery has aroused the interest of research and productive sectors [1]. Extractsrich in natural antioxidant compounds are being tested as ingredients in food formulations to inhibitthe creation of free radicals and / or interrupt the auto oxidation, allowing a reduced use of artificialadditives in ready for consumption food preparation [2].However these compounds are more efficiently extracted using solvents, which often hinder theirconcentration by membrane separation processes [3]. The ethanol content in the feed fraction maybe a limiting factor for membrane processes [4]. On the other hand, the temperature and pressureapplied to the system can also influence the permeate flux. The objective of this study was,therefore, to determine the limiting flux in the nanofiltration of a Pinot noir grape marc extractcontaining 30% ethanol. Thus, the extract was obtained as by [5] and the limiting flux determined atdifferent temperatures. The nanofiltration system used was composed of a polyamide spiral woundmembranes with maximum working temperature of 45°C.As the extraction was carried out at 50°C, this temperature didn’t damage the bioactive compounds.The limiting flux was determined at 20, 30 and 40°C temperatures at a flow rate of 700 L h -1 . Asexpected, increasing temperature had a positive influence in the permeate flux (Fig. 1). However, thiseffect wasn’t linear, i.e. the increase observed from 20 to 30°C wasn’t the same as from 30 to 40°C.Higher temperatures increase the permeate flow. As concluded the rheological study of the extractperformed by [6], this is a non-Newtonian, shear thinning and temperature dependent fluid. Thepressure also had a positively action on the permeate flux. The limiting flux was reached at 20°C and30°C with pressure of 16 bar, while the 40°C limiting flow has been reached at a transmembranepressure of 12 bar. Thus, the best condition for the nanofiltration of grape marc extract containing30% ethanol was 40°C with a 12 bar pressure applied to the system.

Fluxo de Permeado (L.h-¹.m²)15010020°C30°C40°C5000 5 10 15 20 25P (Bar)Figure 1 – Limiting fluxReferences:[1] C. BRAZINHA and J. CRESPO (2010), Filtration + Separation (2010).[2] M. S. BREWER (2011), Comprehensive Reviews in Food Science and Food Safety (2011) 221-242.[3] M. TSUI and M. CHERYAN (2004), Journal of Membrane Science, 237, 61-69.[4] N. LEIDENS (2011), UFRGS, 37p.[5] A. P. G. CRUZ et al. (2012), XXII Congresso Brasileiro de Fruticultura, 5059-5062.[6] C. C. B. HIGTINO (2012), UFRJ, 87p.

Evaluation Of Reverse Osmosis And Nanofiltration For The Concentration OfBioactive Compound Recovered Of Grape MarcAna Paula Gil Cruz¹*, Natalia Barbosa Eitel², Luiz Fernando Menezes da Silva³, Suely PereiraFreitas², Alexandre Guedes Torres¹, Lourdes Maria Correa Cabral³¹Universidade Federal do Rio de Janeiro/UFRJ, Instituto de Química, Rio de Janeiro, Brasil. -ana_gil@uol.com.br.²Universidade Federal do Rio de Janeiro/UFRJ, Escola de Química, Rio de Janeiro, Brasil.³ Embrapa Agroindústria de Alimentos, Rio de Janeiro, Brasil.In the food industry, especially in the ones of fruit and vegetable processing, it’s estimated that 10 to60% of the feedstock turn into waste [1]. In Brazil, about 57% of the grape crop is destined forprocessing. Grape marc is the generated residue in greater volume, 16% of the processed grapes [2].The disposal of this waste presents serious environmental constraints, caused by high chemical andbiochemical oxygen demand, which increases the need for treatments with higher costs associated.However, this co-product stands out for its rich composition in bioactive compounds, which may berecovered. This recovery increases its value and can reduce the costs of its treatment to a properenvironmental disposal.The membrane separation processes, particularly the ultra- and nanofiltration and reverse osmosis,have been studied as a technology with great potential to concentrate and to achieve a betterstability of phenolic compounds [3], which are easily degraded in the presence of inadequate oxygenconcentrations, pH, temperature and other inadequate conditions [4]. However, the extraction ofthese compounds is more efficient with the use of solvents instead of water [5]. On the other hand,the presence of a solvent may impair the concentration in polymeric membranes, since those caninteract with the membrane material, in such a way the membranes could lose their permeabilityand selectivity characteristics or also their integrity [6].Thus the aim of this study was to evaluate the use of a reverse osmosis membrane and nanofiltrationsystems for the concentration of bioactive compounds from a grape marc extract containing 70%ethanol. A reverse osmosis polyamide membrane has been tested on a plate and frame system withtotal filtering area of 0.288 m². The nanofiltration membranes tested were the ceramic, α-alumina, atubular type with 0.023 m² and a polymer polyamide-spiral type with a total area of 2.5 m². Theethanol present in the extract interacted strongly with the reverse osmosis membrane, whoseintegrity was lost after the second process. The ceramic membrane was not efficient for theconcentration of the compounds of interest, which have permeated. The nanofiltration membranewas the most efficient system for concentrating these compounds. The retention coefficient reached98% for phenolic compounds and 100% for anthocyanins.

a b cFigure 1 – Nanofiltration streams of a 70% hidroethanolic extract obtained from a white winegrape marca- Feed Stream; b- Retentate; c- PermeateReferences:[1] W. E. EIPESON and R. S. RAMTEKE (2003), In: H. S. Ramaswamy, et al. Handbook of Postharvest TechnologyCereals, Fruits, Vegetables, Tea, and Spices, cap. 28 , 819-844.[2] M. A. BUSTAMANTE et al. (2008), Waste Management, 28, 372-380.[3] B. DÍAZ-REINOSO et al. (2009), J. of Food Eng., 91, 587-593.[4] M. NAZCK and F. SHAHIDHI (2004), J. Chromatography A, 1054, 95–111.[5] J. CHANDRASEKHAR et al (2012), Food and Bioproducts Processing, 90, 615-623.[6] E. M. TSUI and M. CHERYAN (2004), Journal of Membrane Science, 237, 61-69.

New Polyamide Membranes from PAMAM and Glutaraldehyde1 Hilenio da Silva Monteiro, 1 Liana Camboin, 1 Mylene Fernandes, 2 Alberto Claudio Habert,3 Vanessa Rodrigues Furtado *1 Escola de Química/UFRJ, 2 COPPE/UFRJ, 3 Instituto de Química/UFRJvanessa@iq.ufrj.brNew polyamide membranes have been prepared from PAMAM G4 dendrimer and glutaraldehyde byinterfacial polymerization over a polyethersulphone microporous support [1], followed by crosslinkof the polymer clusters with glutaraldehyde. PAMAM G4 is a globular polymer with a highlyfunctionalized surface (64 primary amines) and inner voids with controlled size. Synthesisparameters explored included glutaraldehyde/PAMAM molar ratios (ranging from 8 to 64), thePAMAM G4 solution concentration, in addition to polymerization and crosslinking reaction times.Membrane characterization was evaluated measuring surface roughness, permeability and molecularweight cut-off for several standards organic and inorganic solutes.The membranes were resistant to acidic and slightly alkaline pH (pH 8) and their performance werestable in extended runs experiments, with excellent reproducibility. The best performances wereachieved with membranes prepared with glutaraldehyde/PAMAM molar ratios between 16 and 32and PAMAM concentrations between 10 and 25 mg/mL. Measured fluxes ranges from 7 to 20 L/h.m²for operating pressures of 12 to 20 bars. Typical rejection values from 90 up to 100% were obtainedfor polyethyleneglicol (MW 1,000 to 20,000), while ionic solutes such as for NaCl and MgSO 4 showedresults from 80 to 95 %. No fouling effects were observed.As the PAMAM dendrimer polyamide membranes allow inner void size control by changing thereaction variables, and a further surface modification, conveniently achieved due to the reactivity ofthe PAMAM surface amines, the results indicate good prospects of this material for nanofiltrationapplications.[1] L.M. Jin, S.L. Yu, W.X. Shi, X.S. Yi, N. Sun, Y.L. Ge, C. Ma (2012), Polymer 53 (2012) 5295e5303

IntroductionSimulating Pressure Retarded Osmosis Using UniSim DesignGuillermina Gentile, Paula Llano, María Fidalgo de Cortalezzi*Dep. of Chemical Engineering, Instituto Tecnológico de Buenos Aires*mfidalgo@itba.edu.arPressure retarded osmosis can be used to produce electricity, based on two different solutions: oneof high osmotic pressure (draw) and the other of low osmotic pressure (feed); which are separatedby a semi permeable membrane [1]. Water will permeate from the feed solution (FS) to the drawsolution (DS) which was previously pressurised. Afterwards, a part of the DS is depressurized througha hydroturbine to obtain electricity [1].The objective of this study is to simulate PRO, to predict net power density and to assess thepossibility of installing a PRO plant taking into account natural water qualities and equipmentneeded.MethodologyThe software employed was UniSim Design R390 and the fluid package was OLI Electrolyte. PROsimulation included a membrane module, DS high pressure, FS low pressure and recycle for part ofthe diluted DS (DDS) pumps, pressure exchanger and hydroturbine (Figure 1).Figure 1: UniSim layout of simulationWe considered a situation for the Río Negro (Province of Río Negro, Argentina). The averageminimum daily flow was 75 m 3 /s during 1997-2010 [2]; 10% of which was taken as FS, due toeconomic and environmental reasons. FS and DS were completely defined. Temperature andconcentrations are possible ones for the Río Negro and Atlantic Ocean. We assumed pressures andcomposition of certain streams, permeate, recycle of DDS, pressure increase at pumps, and efficiencyof pumps, pressure exchanger and hydroturbine

The output variables in this study are power consumed by pumps and power obtained fromhydroturbine. Then, net power production can be known for different operating conditions.ResultsWe examined the feasibility of obtaining power considering different concentrations of FS and DS.The results were considered when net power production was positive. Varying concentration of FS,net power resulted in 1.962 - 125.1 kW. Modifying concentration of DS, net power resulted in 34.41 -125.1 kW. We could derive a necessity of 5.5x105 m 2 of membrane.ConclusionsSimulating PRO with UniSim is useful, when it is not possible to have all the equipments required toperform specific tests.The permeating flux was obtained from: Jw=A(-P). However, other models or laboratory resultscould be used.Two objectives were accomplished: we determined that, with data assumed, the range of possibleconcentrations in both solutions resulted small, and the membrane area required was derived fromthe simulation.References[1] A. Achilli et al (2009) Journal of Membrane Science 343, 45-52[2] Red Hidrológica Nacional - Publicaciones Hidrometeorológicas 2010 / compilado por Fabián López. - 1a ed. -Buenos Aires: Sec. de Obras Públicas. Subsec. de Recursos Hídricos (2011)

Drinking water: Single step Ultrafiltration treatment of high turbid RiverWaterKevin Phillips, Isadora Argentoni Nagaoka, Manny Singh, André Lermontov*, Alberto CostaKoch Membrane Systems, Koch Membrane Systems, Koch Membrane Systems, Águas do Brasil,Águas do Imperador. kphillips@kochmembrane.com, nagaokai@kochmembrane.com,msingh@kochmembrane.com, andre.lermontov@grupoaguasdobrasil.com.br,acosta@aguasdoimperador.com.brObtaining new cost reduction processes for drinking water has become more important over theyears. Hollow fiber Ultrafiltration (UF) is a key process in multiple potable water applications. Theimportance of UF is essentially the complete removal of suspended solids and pathogens. Typically,most hollow fiber membrane systems require clarification pretreatment for feed waters withturbidity values greater than 1000 NTU.This paper will discuss the pilot test results of a UF cartridge that treated river water with turbiditiesup to 8000 NTU at an existing drinking water plant in Brazil. The pilot uses a new pressurized hollowfiber UF module. Along with new operating protocols, the membrane cartridge is designed toproduce high quality permeate at low fouling rates with high feed water solids.The pilot demonstrated that a single unit operation without coagulant dosing can be used to producehigh quality product water regardless of the feed water quality. The pilot data will be used to designa membrane system with the same capacity as the existing plant. This membrane system capitalcosts and operating costs, both power and chemical, will be evaluated. This design will then have aside-by-side comparison to the existing water treatment plant that incorporates conventiontechnologies with coagulant addition. The comparisons will also include disinfection cost, productwater quality, and infrastructure costs.

In-module chemical modification and assessment of polyethersulfonecapillary ultrafiltration membranesK. Philemon Matabola, Banele Vatsha and Richard M. Moutloali*DST/Mintek Nanotechnology Innovation Center, Advanced Materials Division, 200 Malibongwe Drive,RANDBURG, 2125; e-mail: richardm@mintek.co.zaMembrane technologies/systems have revolutionised the water treatment industry in alleviating the plight oflack of access to clean water worldwide [1]. This is as a result of their potential in providing an absolute barrierfor bacteria, viruses and other water-borne diseases which are alleged to be the leading causes of childhoodmorbidity and mortality [2]. The drawback associated with membrane applications in water is the decrease inpermeation with time due to fouling caused by cake formation on the membrane surface. Current researchtowards alleviating membrane fouling is through surface modification with respect to hydrophilicity andsurface charge. This study explores the surface modification of the capillary ultrafiltration (CUF) membranes byintroducing hydrophilic molecules on the surface as a fouling reduction strategy. Poly(sodium-4-styrenesulfonate) (PSS) together with potassium persulfate and potassium bisulfite couple were used as thehydrophilic monomers and initiators respectively for the chemical modification. The modification was carriedout by permeating the mixture of the hydrophilic polymer and the initiators through the sealed CUF membranemodule for 24 h followed by rinsing and backwashing with pure water. The effect of PSS content on theproperties of the modified membranes was investigated. Both the unmodified and the modified membraneswere characterised by the FTIR, contact angle, AFM and HRSEM.FTIR analysis confirmed the successful grafting of the PSS on the CUF surface as evidenced by theappearance of the band at 1040 cm -1 observed in the modified membrane which is attributed tosymmetric stretching of SO 3 - of the PSS unit. Decreasing contact angle measurements indicated thatthe hydrophilicity of the modified CUF membranes increased with increasing PSS loading (Figure 1).The AFM results exhibited significant increase in the density of nodules, coupled with increasedsurface roughness also confirmed the attachment of PSS molecules on the surface. The crosssectionalSEM analysis showed no meaningful morphological changes in the modified membranes orevidence of pore collapse was observed (SEM analysis) indicating that the method can be used for inmodulemembrane modification. Fouling and flux recovery was investigated using BSA a modelcompound. The flux of the modified membranes could be recovered significantly when compared tobase membranes indicating improved fouling resistance due to surface modification.A B CFigure 1: Drop shapes of water droplet on the washed membranes (A), CUF modified with 4000 ppmPSS (B) and CUF modified with 6000 ppm PSS (C)References:

[1] H. Ma, C. N. Bowman, R. H. Davis (2000), Membrane fouling reduction and surface modification. Journal ofMembrane Science, 173, 191-200.[2] R. Bergamsco, F. V. da Silva, F. S. Arakawa, N. U. Yamaguchi, M. H. M. Reis, C. J. Tavares, M. T. P. Sousa deAmorim, C. R. G. Tavares (2011), Drinking water treatment in a gravimetric flow system with Tio2 coatedmembranes. Chemical Engineering Journal, 174, 102-109.

Catalytic Microfiltration Membranes containing Fe/Ni BimetallicNanoparticles for the Reductive Degradation of Azo Dyes andOrganochlorines in WaterKeneiloe Sikhwivhilu*, Richard M. MoutloaliDST/Mintek Nanotechnology Innovation Centre, Advanced Materials Division, Mintek,Private Bag X 3015, Randburg, 2125, South Africa.*e-mail: keneiloes@mintek.co.zaThe decline in water quantity and quality has accelerated the adoption of membrane-based watertreatment technologies (reverse osmosis and nanofiltration) as reliable sources of potable water.Widespread implementation of membrane-based water treatment technologies; however, isconstrained by the energy requirements of conventional membrane processes. Thus, a suite of novelselective and/or reactive membranes is needed to meet water resource needs in an energyconstrained environment. The adaptation of nanotechnology to conventional membrane processes,whereby catalytic nanoparticles (NPs) are supported on porous membranes to degrade organicpollutants in water, offers new opportunities for the intensification of water processes.In this paper we report on the catalytic reductive degradation of azo dyes and organochlorines, usingMethyl Orange dye and Trichloroethylene as model compounds respectively, by Fe/Ni bimetallic NPssupported on polyvinylidene fluoride (PVDF) microfiltration (MF) membrane. The MF membrane wasemployed as a substrate for the NPs in order to reduce particle loss and agglomeration of NPs whichcan lead to a dramatic loss of reactivity. The aim of the study is to assess the catalytic efficiency ofwell-known nanocatalysts supported on microfiltration membranes as a treatment option for organiccompound-polluted water.Anchoring of the Fe/Ni bimetallic NPs on the surface of the PVDF membranes was achieved with theaid of thermally grafted cross-linked polyacrylic acid molecules, which acted as chelating agents tothe metal particles. Batch reactor and convection flow testing of the membrane nanocompositesshowed gradual degradation of the model pollutants by the supported Fe/Ni NPs with time; withhigher degradation activity observed under acidic conditions. A study of the effect of bimetal loadingon the degradation efficiency of the membrane nanocomposite at varied pH of the testing solution,showed the reaction rate constant and hence the kinetics of the reaction are prescribed by the pH ofthe reaction media. Leaching of the metal NPs from the membrane substrate was observed, anddepending on the method of membrane nanocomposite preparation, the leaching minimized whilethe high degradation activity of the membrane nanocomposite was maintained. The results of thestudy demonstrated that the nano-enabled catalytic membranes are effective for the degradation ofdyes in water and that this composite system can potentially be used for the development of energyefficientmembranes for removal of organic pollutants in water.

Performance of Cartridge Filters as Pre-Treatment of PressurizedMicrofiltrationJocarla da Silva Rogerio, Walter Bom Braga Junior, Gabriela Marques dos Ramos, RobertoBentes de Carvalho*PAM-Membranas Seletivas Ltda., Parque Tecnológico do Rio de Janeiro – CidadeUniversitária – Rio de Janeiro - RJ - CEP: 21941-907- País - Tel: +55 (21) 3733-1980 - e-mail:bentes@pam-membranas.com.brThe decay of permeate flow with time is caused mainly by fouling, which is a problem inmembrane microfiltration. Membrane fouling is caused by solid components of effluent, whichaccumulate forming a cake. This increase in resistance leads to a raise in energy demand and incleaning frequency, increasing operational costs.The present work aims at studying the efficiency of polypropylene filters operated withbackwash as pre-treatment of microfiltration process associated to the aerobic biological treatmentof wastewater. The objective is to reduce the concentration of suspended solids in effluent that willbe submitted to microfiltration, and, thus, to retard fouling. This is an innovative conception in thebiological treatment field since it allows employing pressurized microfiltration and hence conduces toa higher flexibility in pressure control.The cartridge, which nominal rating is 5µm, was tested immersed in activated sludge from atreatment plant. The filter was operated at negative pressure inside the cartridge to create a drivingforce to permeation. The automatic operation alternated 10min of filtration and 20s of backwashingwith permeate. It was used an aeration system outside the filter to delay the cartridge clog.Permeated and effluent’s streams were analyzed by chemical oxygen demand (COD), turbidity,settleable solids, and total solids. After permeated flow decrease, the cartridge was treated withbackwashing, sodium hypochlorite, and citric acid, aiming at recovering its permeability.It was observed a decay in permeate flow due to the small the cartridge area (0.09 m²).Maximum COD reduction was 65%, 85% for turbidity and 98% removal from total solids. The resultsof settleable solids analysis (using Imhoff cone) showed that the use of cartridge filters removedcompletely settleable solids from wastewater, as shows Fig. 1.(a) (b) (c) (d)Fig 1: Settleable solids analysis (Imhof cone): (a) wastewater sample before analysis, (b) permeatesample before analysis, (c) wastewater sample after analysis and (d) permeate sample after analysis.

Table 1 shows the results of permeability recovery of cartridge filter after chemical and physicalcleaning for several filtration steps. Data in table 1 indicate that the cartridge permeability remainsessentially constant even after several successive filtration and cleaning steps. These results pointout the cartridge filter as a promising alternative of pre-treatment for pressurized microfiltrationwith the objective of retarding the fouling.Table 1: Hydraulic permeability of cartridge filter after successive filtration and cleaning stepsConditionPermeability(L/hm 2 bar)Before the tests 4,034After 3 days testing 2,851After backwash with air (0,5 bar/ 10 min) 3,219After 24h soaked in hypoclorite (5000ppm) followedby backwash with air (0,5 bar/ 10 min)4,456After 3 days more testing 1,757After backwash with air (0,5 bar/ 10 minutos) 3,116After 24h soaked in hypoclorite (5000ppm) followedby backwash with air (0,5 bar/ 10 min)4,637After 2 days more testing 2,857After backwash with air (0,5 bar/ 10 minutos) 3,096After 24h soaked in hypoclorite (5000ppm) followedby backwash with air (0,5 bar/ 10 min)3,595After 36h soaked in acid citric (pH 3) 3,542

Development of Functionalized Poly(etherimide) Membrane for Application inHemodialysisAlana Melo dos Santos * , Alberto Claudio Habert e Helen Conceição FerrazAlberto Luiz Coimbra Institute – Graduate School and Research in Engineering, Federal University ofRio de Janeiro, Rio de Janeiro, RJ, Brasil, alana@peq.coppe.ufrj.br.According to data from the Brazilian Society of Nephrology, about 10 million people suffer fromkidney disease in Brazil, which can envolve to a chronic stage if not previously detected. In this stage,hemodialysis becomes indispensable until kidney transplantation.Hemodialysis is a treatment that aims the elimination of toxic metabolits and excess of water, actingas an artificial kidney. This is accomplished, generally, by the movement of solutes and solvent(water) across a semipermeable membrane, which allows the passage of metabolic waste productssuch as urea, creatinine, uric acid, and inorganic phosphate to move from bloodstream of patients tothe dialysate , preventing at the same time, the elimination of important blood proteins such asalbumin and immunoglobulin [1]. Despite being the most widely method of treatment used forchronic kidney disease, hemodialysis still requires improvements in its process in order to decreasethe mortality and increase the quality of life of patients.Commercial membranes generally used in hemodialysis consist of polymers such as polysulfone,polyethersulfone, polycarbonate, polyamide or cellulose acetate [2]. These membranes are importedand they represent a high cost to the SUS (Unified Health System), in addition to limiting the numberof patients who can be treated. Thus, the present study aims to synthesize membranes ofpolyetherimide (PEI) for hemodialysis, with chemical immobilization of heparin on its surface in orderto increase their biocompatibility. PEI is a polymer with interesting properties, as considerablemechanical strength, thermal stability, chemical resistance and good processability[3]. Furthermore,it can be covalently functionalized by reaction of macromolecules with the aminated repeating imidegroup [4].The PEI membranes synthesized are characterized by morphological analysis, hydraulic permeabilityand rejection to the following solutes: urea, creatinine, vitamin B12, β2-microglobulin and albumin.Moreover, the efficiency of heparin immobilization on the membrane is evaluated.[1] N. J. Ofsthun; S. Karoor; M. Suzuki (2008), New Jersey: John Wiley & Sons, p. 519-537.[2] J. Barzin et al. (2004), J of Membrane Science, 237, p. 77-85.[3] S. Senthilkumar et al (2012), J Polym Res, 19, p. 1-11.[4] W. Chinpa (2010), J of Membrane Science, 365, p. 89-97.

Newly Developed Composite Hollow Fiber Membrane by InterfacialPolymerization of HydrazineAna C. M. Costa* 1 , Paula W. Teixeira 1 , Maria E. F. Garcia 1 , Jane H. Fujiyama-Novak 1 , GabrielaM. Ramos 2 , Alberto C. Habert 1 , Cristiano Borges 1 , Mônica O. Penna 31 Programa de Eng. Química/COPPE – Universidade Federal do Rio de Janeiro, Brasil2 PAM Membranas Seletivas Ltda3 PETROBRAS/ CENPES/PDEP/TEE*acosta@peq.coppe.ufrj.brThe increasingly strict environmental regulations and the economic advantages of using membranes,such as the reduced waste disposal, led to advances in nanofiltration (NF). However, there are stillmany limitations to overcome with the development of better membranes. The major restrictionsare the increase in productivity of treated water (permeability) while maintaining membranesselectivity, the production of membranes more resistant to fouling and the production ofmembranes that can be operated in a wide range of pH, high temperature and/or in the presence ofoxidative reagents [1,2].In this context, the aim of this work was to develop membranes with enhanced resistance to foulingand high selectivity. We have investigated the synthesis of NF hollow fiber membranes by usingpolyetherimide (PEI) as a porous support. This polymer presents good chemical and thermalstabilities and asymmetric morphology generated by the Loeb-Sourirajan phase inversion technique[3]. The use of the additives to the polymer solution and the influence of the synthesis parameters onthe membrane morphology and performance will be presented in this study.The dense layer was made by interfacial polymerization of hydrazine, piperazine and trimesoylchloride (TMC) on the outer surface of the PEI support. The scanning electron microscopy imagesrevealed the existence of pores (size range 100-400 nm) on the support, while no visible pores couldbe observed on the selective layer. The thickness of the active layer is less than 0.5 mm. The hollowfiber NF membranes showed a salt rejection rate of more than 85% and permeability of 2.0l/h.m 2 .bar for a feed aqueous solution containing 2000 mg/l MgSO 4 operated at 10 bar.[1] T. Matsuura (2001), Desalination, 134, 47-54.[2] S. Atkinson (2002), Membrane Technology, 11-12.[3] D. Wang, K. Li, W. K. Teo (1998), J. Memb. Science, 138, 193-201.

Evaluation of Reversal Electrodialysis Process to Treat RefineryWastewaterAna C. M. Costa* 1 , Gabriela M. dos Ramos 1 , Gisele Mattedi 1 , Paula W. T. Reuther 1 ,Cristiano P. Borges 1 , Rodrigo S. de Souza 2 , Vânia M. J. Santiago 21 Chemical Engineering Program/COPPE/UFRJ2 Water Treatment and Reuse Technologies Management/CENPES/PETROBRASacosta@peq.coppe.ufrj.brThe lack of potable water has become a worldwide problem due to the growth in waterdemand and because of inadequate recharge. The quality of water sources are reducingprincipally because of the indiscriminate discharge of domestic and industrial effluents withoutadequate treatments[1]. This situation requires solutions to satisfy the increasing waterdemand and decreasing supply. In this context, water reuse and desalination came out as goodalternatives, which is evidenced by the rising use of desalination plants around the world [2,3].Electrodialysis has been successfully used to desalt surface and wastewaters because of itstolerance to turbidity values and because of membranes resistance to effective level s ofoxidizing disinfections.In this work, electrodialysis reversal (EDR) process has been evaluated in order to treatPetrobras refinery effluent. The EDR plant is located downstream stabilization lagoon and thefeed solution is pre-treated by coagulation-floculation. Antiscaling was added to preventbarium precipitation. The plant was also monitored by electric current and voltage toinvestigate salt precipitation on membrane surface.The results presented in Figures 1 and 2 show a good stability of EDR plant over 12 months ofoperation. The plant operated with 75% of product recovery and the conductivity of theproduct was maintained below 400 µS/cm.Figure 1. Concentrate and product flows.Figure 2. Feed and product conductivities.The product obtained had good quality and could be reused in refinery process, for example incool towers.References[1]. C.C. Teodosin, M.D.Kennedy, H.A. Van Straten, J.C. Schippers.(1999). Wat. Res. 33, 2172-2180.[2]. P. Gioli, G. E. Silingardi, G. Ghiglio (1987). Des. 67, 271-282.[3]. P. Bernardo, E. Drioli. Comp. Memb.Sci.Eng. (2010), 211-239.

Antimicrobial polyvinyl alcohol films with in situ synthesized silver nanoparticlesFerreira, B. T. B.* (1), Ferraz, H. C.(2), Pollo, L. D. (3)(1) and (2) Universidade Federal do Rio de Janeiro(3) Universidade Federal do Rio Grande do Sul*bferreira@peq.coppe.ufrj.brThe food industry faces the constant challenge of keeping its products free of undesiredmicroorganisms, without compromising the safety, the freshness of the quality. The simplest way toachieve these goals is by packing the product in an antimicrobial food packaging, which is a type ofactive packaging.Active packages contain additives that interact either with the product or with the inside-packageenvironment in order to extend the shelf-life. Metals nanoparticles are one of the most interestingadditives currently, since they have small sizes but a great contact surface, allowing an effectiveinteraction with the microorganism’s cell wall.Silver is a metal that has been used through the centuries to inhibit microbial growth. Researchersare constantly trying to ally the well-known properties of silver to the advantages of nanoparticles.Silver nanoparticles (AgNPs) are produced through the reduction of silver ions. There are severaltechniques that can be used in order to do so. In this work, the AgNPs were synthesized throughtermal annealing, using silver nitrate as the precursor salt.The chosen polymer matrix was polyvinyl alcohol, that is biodegradable, biocompatible, chemicallystable and highly hydrophilic. This last characteristic allows using water as solvent, but isn’t desirablein food packaging. It was needed to crosslink the polymer. The crosslinking agent used was maleicacid, since it agrees with the Brazilian parameters for food-contact materials.The synthesized films were evaluated in their affinity with water, their chemical modification (FourierTransform Infrarred – FTIR) and thermal resistance (Differential Scanning Calorimetry – DSC). In orderto confirm the AgNPs’ presence and their distribution in the polymeric matrix, spectroscopy in theUV-Visible region, Scanning Electron Microscopy (SEM) and Transmission Electron Microscopy (TEM)analysis were carried out. The film’s efficiency against bacteria was evaluated through the halomethod.The results of the tests revealed that films in presence of AgNPs have less affinity with water. Thisresult was coherent with the reduction in the –OH band under the same conditions, evaluatedthrough the FTIR spectra. The novel films have a higher glass transition temperature (Tg) than thepure one, probably due to the nanoparticles’ ability to fill in the spaces between the polymericchains. The UV-Visible spectroscopy indicated the presence of AgNPs, which was confirmed by bothSEM and TEM analysis. The synthesized nanoparticles have an average size of 13nm. Theantimicrobial analysis showed positive results, with a clear inhibition halo around the films.

Evaluation of Solubility of Propylene and Propane gas in Facilitated TransportMembranes Containing Silver as Carrier AgentCarolina Guedes Fioravante Rezende 1 , Cristiano Piacsek borgesBorges 2 , Alberto ClaudioHabert* 21-PhD student of Universidade Federal do Rio de Janeiro; 2- Professor of Universidade Federal do Riode Janeiro. habert@peq.coppe.ufrj.br.Facilitated transport membranes have been used recently as an alternative to separate gases frompetroleum industry with similar physical-chemical properties as propane and propylene gases.Currently these gases are separated by distillation, a process that requires high energy consumptionand capital investment. [1] In facilitated transport membrane with fixed carrier, the carrier agentsare dissolved in the polymer matrix and allow specific and reversible transport across the membraneof propylene [2]. The olefin is carried through an additional mechanism to sorption-diffusion byolefin complexation by carrier agent (usually silver ions), this cause an increase in permeability andselectivity [3,4,5]. This work aims to study the sorption step that occurs during the transport of gases.For this, the solubility of propane and propylene gases in the polyurethane membrane containingsilver particles, was evaluated by pressure decay method [6]. The test was efficient and it waspossible to obtain the sorption isotherms for propane and propylene at temperature of 40 º C.[1] R. B. ELDRIDG (1993), Ind. Eng. Chem. Res.,32, 2208-2212.[2] H. C. FERRAZ; L. T. DUARTE; M.Di LUCCIO; T.L M. ALVES; A. C HABERT;. C. P., BORGES (2007), BrazilianJournal of Chemical Engineering, 24,.101-118..[3] R. D. NOBLE (1990), Journal of Membrane Science, 50, 207.[4] R. D. NOBLE (1991), Journal of Membrane Science, 60, 297.[5] R. D. NOBLE (1992), Journal of Membrane Science, 75, 121.[6] W. J. KOROS; D. R. PAUL(1976), JOURNAL OF POLYMER SCIENCE, 14 , 1903-1907

Polycaprolactone membranes by phase inversion processCristina C. Pereira and Cristiano P. BorgesChemical Engineering Program/COPPE/UFRJcristina@peq.coppe.ufrj.brThe development of biodegradable and biocompatible polymer membranes has been investigatedwith great interest for several biomedical applications, such as hemodialysis, drug delivery devices,and scaffolds for tissue engineering. The membrane plays an important role in tissue engineering,which is an interdisciplinary field involving mainly engineering and medical science, applied forrepairing a damaged tissue or even optimizing a tissue function.The success of the replacement of tissues and organs by direct transplantation is often reduced dueto limitations, such as rejections or lack of available donor organs and tissues, as well as risks ofinfection. The use of membranes as scaffolds for cell culture in vitro has been investigated as analternative to overcome these difficulties before implantation to the host.The use of biodegradable and biocompatible polymer membranes, synthetic or natural, as guidedtissue regeneration avoids further risks of infection or immune response. It is also desired that thepolymer material presents an adequate degradation rate to keep its properties while tissue healingtakes place. The polymer degradation avoids the necessity of further implant removal. Researchworks have been carried out to investigate the use of porous or dense membranes as selectivebarriers to allow the passage of the components necessary to promote tissue regeneration, such ascells nutrients, as well as, the removal of metabolic products. Polylactic acid, polycaprolactone, andpoly(lactic-co-glycolide) are frequently investigated as biodegradable polymers for membranepreparation which focus on this theme.In the present work, phase inversion by immersion-precipitation technique has been used forpreparing polycaprolactone flat sheet and hollow fiber membranes. This technique allows producingmembranes with a large variety of morphologies and to adjust the final membrane transportproperties for a desired application. Different membrane synthesis parameters, such as polymerconcentration, temperature of polymer solutions and precipitation baths have been investigated.The membranes morphologies were characterized by Scanning Electron Microscopy (SEM). Thevelocities of precipitation of the polymer solutions at different casting conditions have beenevaluated by using the light transmission decay during membrane formation.The results showed that the increase of polymer concentration did not affect the morphology of themembranes investigated. It was possible to observe the presence of pores on the membrane surfaceobtained by 13 and 20%wt. polymer concentration solutions at different temperatures. On the otherhand, by using ethanol as precipitation bath, the membrane presented sponge-like structure.References[1] D. F. Stamatialis, B. J. Papenburg, M. Gironés, S. Saiful, S. N.M. Bettahalli, S. Schmitmeier, M.Wessling (2008) J. Membr. Sci. 308, pp. 1–34.[2] X. Wen, P. A. Tresco (2006) Biomaterials, 27, pp. 3800–3809.[3] C. Yen, H. He, L. J. Lee,W.S. Winston Ho (2009) J. Membr. Sci. 343, pp. 180–188.

Membrane reactors for transesterification of triglycerides: mass transferstudy and a simplified analysis of the coupled reactive separation process.Dilson da Costa Maia Filho*, Vera Maria Martin Salim, Cristiano Piacsek Borges.Programa de Engenharia Química/COPPE/UFRJ dilson@peq.coppe.ufrj.brIn the transesterification reaction, through the interchange of the alkoxy moiety, triglyceridesare converted in glycerol and in a mixture of fatty acid alkyl esters (FAAE). These two products can beapplied as raw materials for further synthesis or directly used as high value-added useful chemicals[1]. Actually, the main use of this reaction is to produce biodiesel, employing conventional reactors,such stirred tank reactor, with methanol and refined vegetable oil as reagents and strong solublebasic as homogenous catalyst. This process is used for the biggest companies of the area, howeverthere are a lot of drawbacks in this convention process[1], such as: a)requires the use of highlyrefined oils, b)there are mass transfer and immiscibility limitations, c)Incomplete conversion, and d)purification problem, i.e. the traditional downstream purification such as water washing maygenerate large amounts of toxic waste water (at least 3.0 L per liters of biodiesel produced wasrelated).Hence, some process intensification technologies have been developed in order to overcomethe problems of the transesterification. These technologies either utilize novel reactors(for example,microchanel[4] and oscilatory flow reactors[5]) or coupled reaction/separation processes ( i.e.reactive distillation[6] and membrane reactors[7]). The use of membranes integrated in reactors isone of the most promising approaches, due to the potential to explore advantageous aspects of thelatest technologies proposed. However, the available studies do not discuss a number of functionsthat a membrane could exert in transesterification reactors[8]. In order to develop new conceptionsof membrane reactor, in this work we evaluate the performance of permeation membrane modulesapplied to the byproducts extraction from models transesterification medium. The global andspecifics mass transfer coefficients of glycerol extraction using different membranes were quantifiedand the rate-controlling mechanisms are identified. The coupled process was studied using a simplemodel based on the empirical functions determined. The simulated results point to the possibility ofthe use of these membranes and modules to improve the performance of the transesterificationreaction, simplifying and reducing purification steps of the process and increasing conversion byshifting the reaction equilibrium to the product side.[1] O. P. P., N. L. Harrison Lik, C. Junghui, C. Mei Fong, and C. Yuen May, “A review on conventionaltechnologies and emerging process intensification (PI) methods for biodiesel production 1-s2.” 2012.[2] N. Shibasaki-kitakawa, H. Honda, H. Kuribayashi, and T. Toda, “Biodiesel production using anionic ionexchangeresin as heterogeneous catalyst,” vol. 98, pp. 416–421, 2007.[3] C. S. Cordeiro, F. Rosa, F. Wypych, and P. Ramos, “CATALISADORES HETEROGÊNEOS PARA A PRODUÇÃODE MONOÉSTERES GRAXOS (BIODIESEL),” vol. 34, no. 3, pp. 477–486, 2011.[4] J. Sun, J. Ju, L. Ji, L. Zhang, and N. Xu, “Synthesis of Biodiesel in Capillary Microreactors,” Industrial &Engineering Chemistry Research, vol. 47, no. 5, pp. 1398–1403, Mar. 2008.

[5] A. P. Harvey, M. R. Mackley, and T. Seliger, “Process intensification of biodiesel production using acontinuous oscillatory flow reactor,” Journal of Chemical Technology & Biotechnology, vol. 78, no. 2–3, pp.338–341, Feb. 2003.[6] S. Steinigeweg and J. Gmehling, “Transesterification processes by combination of reactive distillation andpervaporation,” Chemical Engineering and Processing: Process Intensification, vol. 43, no. 3, pp. 447–456, Mar.2004.[7] M. a Dubé, a Y. Tremblay, and J. Liu, “Biodiesel production using a membrane reactor.,” Bioresourcetechnology, vol. 98, no. 3, pp. 639–47, Feb. 2007.[8] K. K. Sirkar, P. V Shanbhag, and A. S. Kovvali, “Membrane in a Reactor : A Functional Perspective,” pp.3715–3737, 1999.

Adhesion between Layers of composite Membranes in a Hollow Fiber ShapeSynthesized by Simultaneous Extrusion for Reverse OsmosisFelipe Coelho Cunha*, Frederico de Araujo Kronemberger e Cristiano Piacsek BorgesPEQ/COPPE/Federal University of Rio de Janeiro. *fcoelho@peq.coppe.ufrj.brNowadays there are around 15.000 desalination facilities worldwide, which are responsiblefor the production of 40 million cubic meters of potable water per day and approximately 50% of thisamount uses Reverse Osmosis membrane technology [1]. The majority of membranes are in a flatsheet shape and the market for membranes in a hollow fiber shape is still underdeveloped; however,there are clearly reasons to believe that the latter membranes can substitute the former ones,because of some intrinsic advantages, such as: (1) larger packing density, (2) self-mechanical supportand (3) easier module fabrication [2]. Besides these hollow fibers’ advantage, this work deals withdual-layer hollow fiber membranes synthesized by simultaneous extrusion process. Hence, a secondstep of depositing a selective layer upon the hollow-fiber membrane support is not necessaryanymore. Furthermore, the selective layer is situated inside the hollow fiber, which decreasessignificantly the possibility of external damage. This work had done strictly thermodynamicexperiments (Turbidity Experiments associated to Hansen Solubility Parameters) and experimentstaking into account both thermodynamic and kinetic phenomena (Initial Precipitation VelocityExperiments) in order to elucidate what happens in the very beginning of the contact between bothpolymeric solutions, right after they exit from the spinneret. This work proposes that the adhesionbetween the layers is intrinsically related to the first moment of fabrication. And the mainconclusion is that the measured Initial Precipitation Velocity can be used as a powerful tool to predicta possible adhesion or delamination between two distinct polymeric solutions in the hollow-fibersynthesis.[1] L. F. Greenlee, D. F. Lawler, B. D. Freeman, B. Marrot e P. Moulin (2009), Water Research, 43, 2317-2348.[2] N. N. Li, A. G. Fane, W. S. W. Ho, T. Matsuura (2008), Advanced Membrane Technology and Applications.

Use of Membrane Contactor to Improve the Ozone Transport in Gas-LiquidSystemFelipe Rodrigues Alves dos Santos* ,1 , Fabiana Valéria da Fonseca Araújo 2 and CristianoPiacsek Borges 1 .1 Chemical Engineering Program, Alberto Luiz Coimbra Institute – graduate school andresearch in engineering – COPPE / Federal University of Rio de Janeiro2 Inorganics Processes Department of Chemical School, Federal University of Rio de Janeiroe-mail: felipe@peq.coppe.ufrj.brOzone is a powerful oxidant compound and provides many chemical reactions with variousmolecules in aqueous phase. By this aspect, the water treatment process by ozonation becomes apromising and important technique mainly due to the ozone attack to a wide range of recalcitrantcompounds and to be considered a “clean” technology. The conventional ozonation is performedwith bubble columns or venture injectors. This technology has use limitations such as high cost withthe ozone generation, generated in situ by electric discharges, and the great loss of O 2 due to the lowconversion in O 3 generation step (conversions between 2 and 7%) and limited surface area ofbubbles for mass transfer.In this study the ozone process was coupled with a membrane separation process to improveefficiency of ozone transference for aqueous phase and consequently reduce water and wastewatertreatment costs. The membrane process used was hollow fiber membrane contactor that shows highpacking density and promotes non-dispersive contact between both phases.The experiments were conducted in a membrane contactor with polypropylene hollow fiber. In a firststep, oxygen was used to evaluate the mass transfer as well as the chemical reaction influence ofconsumption of the transferred oxygen to liquid phase. Furthermore, the mass transfer processinfluence of some variables of this process was verified, such as gas and liquid flow rate and oxygenreceptor concentration. Through these results, a mathematical model was written to show thebehavior of the oxygen in the mass transfer in gas-liquid system and afterward it was converted tothe process with ozone mass transfer.In the following step a bubbling process and polypropylene membrane contactor using ozone wasperformed, both in demineralized water with pH 2 and 7. Both the mass transfer and decay rateswere calculated with data obtained in these experiments. The preliminary tests indicated that themembrane process is capable to reduce the costs of the conventional ozone process by optimizingozone mass transfer, and consequently, reducing the oxygen consumed and energy expenditure forozone generation.

Coagulation, Flocculation and Microfiltration processes for wastewater reusein Sugarcane IndustryGisele Mattedi 1* , Cristiano P. Borges 1 , Lidia Yokoyama 21 Chemical Engineering Program/COPPE/UFRJ 2 Chemical Engineering Department -EQ/UFRJgiselemattedi@peq.coppe.ufrj.brEnergy cogeneration in sugarcane industry occurs through bagasse-cane burning in boilers to steamgeneration [1]. The cogeneration process produces large volumes of wastewater with high sootconcentrations (40 g/L) [2]. In this context, this work proposes a solution to treat this effluent,combining the conventional processes (coagulation and flocculation) with membrane process(microfiltration), to reduce their environmental impact and the possibility of water reuse.In coagulation and flocculation processes, conventional coagulants (ferric chloride and aluminumsulfate) were studied, with or without polymers presence (cationic and anionic). The best resultsshowed coagulation doses between 0.25 and 2.0 mg/L. In microfiltration process, the effluent sootconcentration and air flow rate applied are studied. Finally, the coupled process (coagulation,flocculation and submerged microfiltration) were also studied, as well as its influence on permeateflux performance.The microfiltration results showed that the effluent has a high potential for membrane fouling, and itwas possible to recover with backwash. The permeate flux before backwash is 36 L/(h.m 2 ) and afterbackwash, is 100 L/(h.m 2 ) (Figure 1). Equivalent to 72.3% of total resistance, the most transportresistance is caused by particles deposition on membrane surface, which represents the majorfouling cause by this effluent.The the coupled process showed an increase in microfiltration permeate flow (Figure 2).Figure 1. Backwash effect.Figure 2. Effect of coupling processesThe results showed the feasibility of the effluent treatment by process proposed, producing a hightquality permeate, which allows the water reuse.References[1] LEME, R. M. Estimated emissions of air pollutants and water use in the production of electricity frombiomass cane sugar. Dissertation (MSc in Energy Systems Planning), University of Campinas. Campinas, SP,2005.[2] TORQUATO JR H. et al. Characterization of the wash water of ash and gas boilers in the industry of canesugar, Maceio.

Recovery and concentration of effluent from the delignification stage inthe production process of lignocellulosic ethanol.Ana C. M. Costa 1 , Gisele Mattedi *1 , Cristiano P. Borges 1 , Lidia Maria Melo Santa Anna 21 Chemical Engineering Program/COPPE/UFRJ2 Biotechnology Department/CENPES/PETROBRASgiselemattedi@peq.coppe.ufrj.brIn recent years, bioethanol has received great attention due to energy crisis and globalwarming issue. Bioethanol production lignocellulosic residue is mainly composed of lignin, ashand some carbohydrates. The lignin can be extracted from the residue to improve the processof converting lignocellulosic residue steps regarding saccharification and fermentationalcoholic and the lignin can be used in high-value-added chemicals, which would create higherprofits for the bioethanol industry. However, the above separation methods are not easy toapply into industrial-scale production due to the high cost or complex process. So an adequateseparation method is necessary for bioethanol production residue’s future application. Themost common method to isolate lignin is by using alkali-solution.In this context, the aim of this work is to investigate a membrane separation process torecover sodium hydroxide (NaOH) used in the lignin extraction stage, in addition to increasingthe concentration of polyphenols.The proposed process is a combination of a microfiltration step to remove suspended solids(microorganisms, macromolecules and colloids), and a nanofiltration step (Koch SR50) toseparate polyphenol compounds. Both nanofiltration streams are treated again: theconcentrate one is treated by electrodialysis to recover NaOH, and the permeate streamproceeds to Nanofiltration step (NF DOW-90) for the concentration of polyphenols.The results of microfiltration process showed that the effluent has a high potential formembrane fouling and it was possible to obtain a partial recovery of polyphenols and TOC.The first step of nanofiltration resulted in 80% retention of polyphenols and 70% retention ofTOC. However, this step resulted in low retention of monovalent ions. In the secondnanofiltration stage, the permeate stream presented conductivity and TOC rejections, orconcentration of polyphenols above 96%, showing the technical feasibility of the process.The NF (Koch) concentrate stream was treated by electrodialysis process and the resultsobtained showed that there was practically no permeation of polyphenols during the process.Direct electrodialysis of effluent showed NaOH removal time 100 minutes (Figures 1 and 2).Time (minutes)Figure 1. pH in the effluent electrodialysis.References[1]. Guo, G. et al, 2013, Bioresource Technology, 135, 738-741.Time (minutes)Figure 2. NaOH in the effluent electrodialysis.

The use of different types of antiscalants to prevent barium sulphateprecipitationAna C. M. Costa 1 , Gabriela M. dos Ramos 1 , Gisele Mattedi* 1 , Cristiano P. Borges 1 , Rodrigo S.de Souza 2 , Vânia M. J. Santiago 21 Chemical Engineering Program/COPPE/UFRJ 2 Water Treatment and Reuse TechnologiesManagement/CENPES/PETROBRASgiselemattedi@peq.coppe.ufrj.brIn membrane processes, fouling control is an important issue. Antiscalants may be used in order toreduce the need for frequent cleaning of membrane elements and consequent disruption of theprocess [1]. This study aims to evaluate the use of different antiscalants on fouling control ofElectrodialysis Reversal (EDR) process for treating refinery effluent.Initially, tests were carried out in a reverse osmosis bench scale system. Two different antiscalants (Aand B) were used and the concentration chosen was 40 mg/L . The water feed conductivity wasabout 1700 µS/cm and the tests were performed up to 5000 µS/cm. At the end of the tests, themembranes were analyzed to observe the presence of barium sulphate precipitate. The resultsshowed barium sulphate precipitation in tests carried out with no antiscalant. In tests performedwith antiscalants A and B, the presence of salt precipitation was not observed.To simulate refinery conditions, long term tests were performed in an electrodialysis bench scalesystem, situated in a Petrobras refinery. Three different antiscalants (A,B and C) were used. Thewater feed conductivity was about 1500 µS/cm and the tests were performed controlling theconductivity around 5000 µS/cm. The concentrations chosen were 40mg/L for antiscalant A and 10mg/L for antiscalants B and C. The results are shown in Figure 1.Figure 1: membranes and spacers after long-term test with antiscalantsWe observed the presence of salt precipitation on the surfaces of all electrodialysis membranesused. Analysis by MEV/EDS and DRX showed that the salt present on membrane surfaces was notbarium sulphate, but calcium carbonate. Antiscalants B and C were considered to be more effectivethan antiscalant A to treat the specific refinery effluent, as they were used in a lower concentrationthan antiscalant A.References[1]. J. Qin, M. H. Oo, F. Wong. (2005), Separation and Purification Technology, 46, pp. 46–50.

Synthesis and Characterization of Mixed Matrix Membranes Containing MOFs forCO 2 CaptureJéssica de S. Ribeiro¹ , Talita O C. Leite¹, Elisângela S. Costa 1 , Alberto Claudio Habert 2 , HelenConceição Ferraz 2 , Bruno da S. Gonçalves Alves 2 , Jussara L. de Miranda¹*1- Instituto de Química/UFRJ: jussara@iq.ufrj.br2- Programa de Eng. Química/COPPE/UFRJMOFs are defined as a new class of hybrid metal organic porous materials with great capacity forgases adsorption. These porous materials have a high chemical versatility, since crystallinesupramolecular structures are well-defined. UiO-66 (UiO = University of Oslo) belongs to the class ofhybrid materials, presents zirconium as the metal ion and terephthalic acid as the organic linker. UiO-66 was synthesized using solvothermal method (DMF as solvent).Application of these hybrid structures for gas separation has been investigated. One approach isusing MOFs dispersed in mixed matrix membranes (MMM). MMM take advantage of the selectivityof certain nanoparticles (carbon nanotubes, silica, zeolite, MOFs, etc) and the processability ofpolymeric materials. The combination of materials with different diffusivity and solubility for gasescan give rise to favorable effects.The objective of this work was to develop and characterize mixed matrix membranes for CO 2 /N 2separation. Flat sheets were produced by casting a polymeric solution containing the MOFs followedby solvent evaporation to produce the membranes. The polymer polyurethane (PU) and UiO-66 wereemployed to manufacture the membranes, which were characterized by scanning electronicmicroscopy (SEM) and through their transport properties (permeability and selectivity), obtained in agas permeation system using pure gases.Through SEM photomicrography of the MMM’s surface layer, it was observed a good dispersion ofMOFs on the polymeric matrix. In the cross section, particles were observed through the entiresection. MMM permeability values were 69.1-81.4 Barrer for CO 2 and 2.1-2.3 Barrer for N 2 . Theincrease was of 96% to CO 2 and 156% to N 2 compared to pure membrane. Since both gasespermeability increased, it was observed a decrease of CO 2 /N 2 selectivity, from 44.73 in the PU puremembrane to 34.24 in the MMM in the MMM with 28% (m/m) MOF. Future steps includeinvestigating other polymer matrix for MOFs dispersion as well as other MOFs structures moreselective to CO 2 .

Development membranes for osmotic power generationJader Conceição da Silva*, Cristiano Piacsek BorgesFederal University of Rio de Janeiro/Chemical Engineering Program*jader@peq.coppe.ufrj.brOsmotic power is a renewable source generated through mixing free energy from two solutions withdifferent salinity concentration, based between in free energy involved river (feed solution, lowconcentration) and ocean (draw solution, high concentration) waters mixing [1]. Pressured RetardedOsmosis (PRO) is a membrane process that was proposed to extract osmotic energy from estuaries[2]. Reverse salt flux (from draw to feed solution) and Internal Polarization Concentration (PCI) thatoccurs within porous support is an obstacle which reduces the available osmotic driving force. Themain purpose of this work is to develop membranes for osmotic power generation. In this paper, itwill be present the first part of this work: investigate porous support structure and its effects on masstransport, specially permeate water flux and reverse salt flux in forward osmosis module.Based in previous works, for porous support synthesis was selected Poly(Ether Sulfone) (PES),Poly(Vinyl Pyrrolidone) (PVP) [3]. The solvents chosen were N,N-Dimethylacetamide (DMA),Dimethylformamide (DMF), N-Methyl-2-pyrrolidone (NMP) and NMP/DMF mixtures. Flat sheetporous support was prepared through spreading polymeric solution on glass plate and immersed atwater or water/solvent bath. The solvent composition (NMP/DMF) effect was examined in supportformation in water bath precipitation. Membranes were characterized by Scanning ElectronMicroscopy (SEM) and hydraulic permeability.The picture shows cross-section PES-PVP membranes dissolved in mixtures DMF/NMP.a b c200 μm 200 μm 200 μmFigure 1: SEM micrographs displaying the cross-section of support membranes cast from 14/14 wt%(PES/PVP) dissolved in NMP/DMF mixtures: (a) 20/80, (b) 40/60 and (c) 60/40%.The mixture of solvents modifies the polymer precipitation velocity. Thus, phase separation iscontrolled by NMP/DMF concentrations. For the cast solution with the higher NMP concentration,the support structure was dominated by macrovoids. The presence of NMP in the solvent mixturecauses the shift of the non-solvent diffusion front at a faster rate than vitrification. Then, the systemis put under rapid demixing conditions and sustains the driving force required to create prolongedmacrovoids [4].[1] R. Pattle (1954), Nature, 174, 660–660.[2] S. Loeb (1976), Journal of Science Membrane, 1, 49-63[3] L. M. C. Cabral, (1994), Tese de Doutorado, UFRJ.[4] S. A. McKelvey, W. J. Koros (1996), Journal of Science Membrane, 112, 29-39.

Superficial Characterization and Long-term Test of Reverse Osmosis MembranesCoated with PVA and Natural BiocidesJuliana A. Guimarães a *, Claudia Galinha b , Helen C. Ferraz a , Cristiano P. Borges a , João Paulo S.G. Crespo baPrograma de Engenharia Química, COPPE, Universidade Federal do Rio de Janeiro, Rio de Janeiro,Brazil. *(jguimaraes@peq.coppe.ufrj.br)bREQUIMTE/CQFB, Departamento de Química, Faculdade de Ciências e Tecnologia, UniversidadeNova de Lisboa, Lisboa, Portugal.Reverse osmosis (RO) is a viable separation technique in the process water treatment, especially inthe desalination of water. However, despite the several advantages compared to conventionalprocesses, this process presents operational limitations as biofouling that one of the most seriousproblems associated with the membrane system of RO [1-3].Commercial reverse osmosis membranes (BW30, FilmTec – DOW) were coated with polyvinyl alcohol(PVA) and natural biocides (propolis extract – PE and clove oil – CO) by dip coating technique. Theeffects of surface modification of RO membranes were studied in terms of surface properties andreverse osmosis performances by scanning electron microscopy (SEM, JSM-5300 JEOL), contact angleanalyzer, 2D fluorescence spectroscopy (Cary Eclipse, Varian), and cross-flow membrane module inlong-term test with fouling feed solution.Contact angle (CA) analysis by a sessile drop method showed that modified membranes with PVAshowed CA of approximately 75°. The CA of modified membranes decreases after biocide addiction(CA for PVA/PE-coated is 62° and for PVA/CO-coated is 69°). This indicates that the hydrophilicity ofmodified PVA/biocides membranes is improved. The membrane modified with PVA solution showedthe most homogeneous surface then the uncoated membrane, thus, it appears that the coatingreduced the surface roughness of the membrane. Transport properties characterization presentedthat additional layer on the surface of the membrane keeps the high salt rejection with highinfluence on the permeability. 2D fluorescence spectroscopy revealed that membranes coated withPVA had less irreversible fouling onto membrane surface after long-term test.[1] J. S. Baker, L. Y. Dudley (1998), Desalination, 118, 81-90.[2] B. J. A. Tarboush, D. Rana, T. Matsuura et al. (2008), Journal of Membrane Science, 325, 166–175.[3] M. Al-Ahmad, F. A. Abdul Aleem, A. Mutiri et al. (2000), Desalination, 132, 173-179.

Synthesis and Characterization of Polyvinyl Alcohol Containing CarbonNanoparticles for the Separation of Olefin/Paraffin MixtureJuliana Jatobá* 1 , Luíza Martins de Almeida 1 , Jane Hitomi Fujiyama-Novak 2 ,Alberto Cláudio Habert 21 Escola de Química, Universidade Federal do Rio de Janeiro, Brasil2 Programa de Eng. Química/COPPE – Universidade Federal do Rio de Janeiro, Brasil*julianajatoba@eq.ufrj.brThe separation of olefins and paraffins, which are produced by steam cracking, is currentlyperformed in petrochemical industries by means of an expensive and energy-intensive process.There is, therefore, great interest in the development of new separation technologies. The workpresented here analyzes the incorporation of three different types of carbon nanoparticles (CNp) asnanofillers in the poly(vinyl alcohol (PVA) matrix for propylene-propane gas separation using amembrane-based technology.For the preparation of the novel hybrid membranes, glutaraldehyde was applied as a crosslinkingagent and the β-cyclodextrin (β-CD) as a dispersant of the carbon nanoparticles [1]. Initially it wasused an amorphous spherical CNp to evaluate the influence of nanoparticles on the PVA crossslinkingprocess. The structural and morphological properties of these prepared composite membranes havebeen characterized by Differential scanning calorimetry (DSC), Thermal gravimetric analysis (TGA),Swelling test and Scanning electron microscopy (SEM).The gas permeability measurements were carried out using an automatic permeation apparatus. TGAstudies indicated that both pure PVA and β-CD-CNp/PVA hybrid membranes exhibited similardegradation behavior. It was observed a slight increase in glass transition temperature (Tg) of thehybrid membrane when compared to the pure PVA. The swelling degree of the membrane, andtherefore the crosslinking reaction, was not significantly altered in the presence of the CNp. ScanningElectron Microscopy (SEM) micrographs demonstrated that the aggregation of CNp was improved byincorporation of CD. Although the permeation flux of propylene and total permeation flux werereduced when the CD-CNp content increased from 0 to 1%, nanocomposite membranesdemonstrated better selectivity in separation of propylene from the gaseous mixture containing 50%C 3 H 6 and 50% C 3 H 8 (vol%). Further studies will be conducted to evaluate the effect of the carbonnanotubes and fullerene on the separation of mixtures of lower paraffins/olefins.[1] F. Peng, C. Hub, Z. Jiang, (2007), J. Membr. Sci., 297, 236-242.

Membrane Adsorber Process for Decontamination of Injectable SolutionsAlmeida, K. M.*, Ferraz, H. C. e Almeida, M. MChemical Engineering Program, Alberto Luiz Coimbra Institute for Graduate Studies andResearch in Engineering, Federal University of Rio de Janeirokarix@peq.coppe.ufrj.brOne of the problems in the production of injectable solutions, such as protein solutions, isthe contamination by endotoxins. Endotoxins are substances present in the cell wall of Gramnegativebacteria, responsible by pathogenicity of this type of bacterium. The presence of endotoxinsin injectable solutions can causes serious physiologic variations in the human beings, including fever,vasodilatation, diarrhea, blood coagulation, damage in the liver functions and in the endocrinesystem, chills, headache, malaise, yawns and even the death.Processes using the phenomenon of selective adsorption, as the affinity chromatography andmembrane adsorber processes, propitiate a minor or no loss of the interest product due to specificityof a ligand by this product. These processes can be applied to endotoxins removal and especiallymembrane adsorber process is promising due to several significant advantages when compared toaffinity chromatography process. Membrane adsorbers enable treating higher feed solution flowrates than the affinity chromatography process since mass transfer is not limited by diffusion withinmembrane pores, being governed mainly by convection. Therefore high fluxes can be obtained withmoderate pressures making possible the attainment of a high productivity and a low operation time[1-8].The objective this work is to apply the membrane adsorber technology to removeendotoxins, aiming at a high efficiency in terms of removal and flux as alternative to conventionalprocesses, without denaturation and loss of products. The membranes prepared are basicallyconstituted of nylon covered with polyvinyl alcohol and ligand histidine. Ligand densities determinedwere between 6.3 and 8.4 mg of histidine/g of dry membrane, superior to those reported inliterature [4;9]. The results showed endotoxin removals of aqueous solutions up to 40%, with highvalues of endotoxin concentration in the feed. These adsorbed endotoxin amounts should be close tothe value of adsorption maximum capacity of the membrane adsorber. In adittion, the removalobtained was greater than others previously reported [4] with the same buffer used in this work andsimilar conditions of ionic strength and pH.The nylon membrane did not present nonspecific adsorption of endotoxins which confirmsthat the removal is only because of the membrane specificity. Besides, a novel method of analysis ofendotoxins, the Purpald method, is being evaluated in this work as comparison with the methodsused in the industry such as methods LAL and KDO, which are much more expensive than themethod Purpald [10-12]. The Purpald method seemed to be adequate in the determination ofendotoxin concentrations, however, still needs improvement. The membrane adsorber processpresented potential to remove endotoxins of injectable solutions and tests are still beingaccomplished to evaluate efficiency and equilibrium parameters.References[1] F. Cattoli and G. C. Sarti (2003), ed Elsevier, Italy, 263-281.

[2] Y. Zhang et al. (2007), Reactive and Functional Polymers, 67, 728-736.[3] Z. Wei et al. (2007), Journal of Chromatography B, 852, 288-292.[4] C. Acconci (1998), FEQ/UNICAMP[5] D. Petsch et al. (1998), Journal of Chromatography B, 707, 121-130.[6] W. Zhang, (1993), Reprodienst at the University of Twente, Enschede, Netherlands.[7] F. Santos et al. (2000), Medicine Virtual Magazine, 6, v. 1.[8] R. L. Machado (2003), FEQ/UNICAMP[9] D. Petsch et al. (1998), Journal of Chromatography B, 693, 79-91.[10] C. Lee and C. Tsai (1999), Analytical Biochemistry, 267, 161-168[11] M. S. Quesenberry and Y. C. Lee (1996), Analytical Biochemistry, 234, 50-55.[12] C. Lee and C. E. Frasch (2001), Analytical Biochemistry, 296, 73-82.

Study of PVC Membranes Prepared Via Non Solvent Induced Phase SeparationProcessLiana Franco Padilha*, Cristiano Piacsek Borges.Membrane Separation Processes Laboratory, Chemical Engineering Program, Alberto LuizCoimbra Institute for Graduated Studies and Researcher in Engineering, Federal University ofRio de Janeiroliana@peq.coppe.ufrj.br.The polyvinyl chloride (PVC) is a membrane material well-known for its good stiffness, physical,chemical and mechanical properties as well as acids, alkalis and solvent resistance. Besides, it has agreat chemical compatibility with usual solvents to polymer solution as N,N-dimethylformamide(DMF), N,N-dimethylacetamide (DMAc) and tetrahydrofuran (THF), etc. Preparation, morphology andtransport of PVC membrane were investigated varying the polymer concentration, solvent andadditives.PVC solutions using DMAc and NMP as solvents were prepared with 14, 17 and 20% w/w in polymerconcentrations. The presence of polyvinyl pyrrolidone (PVP) was also tested varying the additiveconcentration between 5 – 10% w/w. Also, the solution time exposure before immersion wasmeasured in order to verify its influence on morphology. The cloud point curve for the systemsPVC/DMAc/water, PVC/NMP/water and PVC-PVP/DMAc/water was determinated at 30°C by titrationmethod. The membrane was prepared by casting solution on a glass plate with a 0.1 µm stainlesssteel blade and immersed into a bath with microfiltrated water at room temperature. Afterimmersion, the membrane was maintained in a water bath for 12 hours to remove the left solventfollowing by at least 24 hours of 40% glycerol in water bath to avoid porous collapse. Scan electronmicroscopy was performed by a FEI Co., Quanta 200 microscopy with sputtering gold samples brokeninto liquid nitrogen. The hydraulic permeability was measured using a flat stainless steel cell intangential flux.PVC precipitates rapidly when in contact with water indicating the occurrence of the instantaneousdemixing mechanism indeed by the phase diagram which is very close with the polymer-solvent axis.This mechanism results in a dense skin with finger-like porous supported by a sponge-like structureas seen in this work. As the concentration increases, the macrovoids formation decreases and asponge layer is raised until its predominance. The time exposure before immersion and the polymerconcentration actuated with a macrovoids suppressor. The NMP solvent promotes the macrovoidspresence at low polymer concentration such as the PVP addition. At higher PVP concentration asponge-like morphology is predominated over macrovoids formation. The hydraulic permeabilityvaried between 0,5 up to 100 L/h*m 2 *bar as the polymer concentration decreases.Therefore, the thermodynamics and kinetics effects should be evaluated simultaneously in eachsystem. The desired morphology can be reached by varying even the thermodynamics parameters, aspolymer and additive concentration, or process parameters like time exposure and demixing rate.

Succinic Acid Liquid-Liquid Extraction with Membrane ContactorsLuciana de Souza Moraes * , Frederico de Araujo Kronemberger, Helen Conceição Ferraz andAlberto Claudio HabertChemical Engineer Program PEQ/COPPE, Federal University of Rio de Janeiro, Brazillmoraes@peq.coppe.ufrj.brOrganic acids are very important raw materials for the chemical industry. In addition, newapplications derived from their biodegradation characteristics have emerged, being the productionof bioplastics the most prominent. For these applications, it is preferred to use raw materialsobtained from renewable sources, increasing the demand for organic acids produced byfermentation. However, the exploitation of the fermentative route replacing the traditional organicacid production by chemical synthesis still relies on the improvement of the product recoveryprocess. Various methods have been proposed, including membrane extraction, which appears to betechnically and economically promising, using an organic compound as extraction agent. Unlikeconventional extraction, when membranes are used, the liquid phases do not disperse in each otherand their contact area is greatly enhanced. Extraction and re-extraction of the organic acid can becoupled in the same experimental system. In case of an industrial application, the acid would beremoved from the fermentation broth and further purified in just one step.This work aims at studying the membrane extraction process of succinic acid, investigating both theextraction to the organic phase and the re-extraction into a new aqueous phase. The objective is toobtain purified acid, improving efficiency using hollow fiber modules as contactors. The extractantsused were a primary alcohol (1-octanol) and a mixture of this one with some amines and phosphates.Equilibrium data were obtained from extraction tests by direct contact (liquid-liquid extraction). Theextraction with membrane was evaluated, using non-porous cellulose acetate hollow fiber modules.In extraction experiments the extent of recovery of acid was similar to values obtained by liquidliquidextraction, achieving good fluxes. In addition the mass transfer coefficients in the membranephase are close to the results found in the literature for organic acid extraction with microporousmembrane contactors. Those promising results indicate a good potential for the proposed process.The overall recovery of the acid, coupling the extraction and the re-extraction steps, will be furtherinvestigated, using succinic acid solutions as well as model solutions to simulate fermentation broths.

Polyvinyl Alcohol / Activated Carbon Composite Thin Layer to ImproveChlorine Resistance of Commercial RO Polyamide MembranesLucinda F. Silva *1,3 Ricardo C. Michel 2 , Cristiano P. Borges 31 Instituto de Engenharia Nuclear - IEN/CNEN/RJ, 2 Instituto de Macromoléculas ProfessoraEloísa Mano - IMA/UFRJ, 3 Programa de Engenharia Química - PEQ/COPPE/UFRJRio de Janeiro, Brasil* lucinda@ien.gov.brOne of the major limitations in the use of commercial aromatic polyamide thin film composite (TFC)reverse osmosis (RO) membranes is to maintain high performance over a long period of operation,due to the sensitivity of polyamide skin layer to oxidizing agents, such as chlorine, even at very lowconcentrations in feed water [1, 2].In this work, commercial thin-film composite reverse osmosis (RO) membranes (BW30 - Dow Filmtec)were modified by covering it with a poly(vinyl alcohol) (PVA) membrane crosslinked withglutaraldehyde (GA) and a composite membrane containing powdered activated carbon (PAC) in amatrix of PVA, in order to improve its resistance to chlorine.This study compares the performance of the original commercial membrane and the modified onesin an oxidizing medium (NaClO 300 mg/L, NaCl 2,000 mg/L, pH 9.5). The exposure time and thechlorine concentration were monitored and taken in terms of ppm.h (ppm chlorine concentrationsolution exposed to membrane for a fixed time in h).PVA membranes were prepared by casting 1%wt. aqueous solution of hydrolyzed PVA 99%. Chemicaland physical stability of PVA membranes were provided by crosslinkingreaction with glutaraldehyde (GA), mainly because this compound reacts at mild temperatures.Powdered activated carbon was used as load in the polymeric composite due to its knowncharacteristics of adsorbent material. Composite PVA/PAC membranes were prepared using similarmethodology described for PVA membranes. ATR-FTIR and TGA analysis confirmed the crosslinkingreaction between GA and PVA besides the influence of PAC in the PVA matrix of the compositemembrane. SEM images of the original and modified membranes were used to evaluate the surfacecoating of the membranes. Adsorption isotherms were obtained for the adsorbent (PAC), PVAmembranes and PVA/PAC composite membranes. The results showed that the adsorbent material(PAC) remains with high adsorption capacity for NaClO even imbibed in PVA matrix.The salt rejection (NaCl) and water permeability were measured during more than 100 h periodunder oxidant conditions. Both surface modifications have effectively demonstrated the increase forthe chlorine resistance of the commercial RO membrane from 1,000 ppm.h to more than 15.000ppm.h [3]. Figure 1 shows the effect of exposure time on the NaCl rejection and Figure 2 on thehydraulic permeability.

Rejection (NaCl - R%)Lp (L/h.m 2 .bar)100,0080,0060,00R(%) BW30R(%) BW30/PVAR(%) BW30/PVA/CAP40,0020,000,000 10000 20000 30000 40000[NaClO] ppm.hFigure 1 - Effect of exposure time (ppm.h) on salt rejection of the tested membranes20Lp BW30Lp BW30/PVALp BW30/PVA/CAP1510500 20 40 60 80 100 120[NaClO] ppm.hFigure 2 - Effect of exposure time (ppm.h) on hydraulic permeability of the tested membranesIt is clear from Figure 1 and Figure 2 that the covered TFC commercial membrane (BW30/PVA/PAC)showed best performance when compared to the original membrane. The results indicate theeffective protection of the commercial RO membrane against chlorine, avoiding its degradation.References:[1] Y-N. Kwon and J.O. Leckie, Hypochlorite degradation of crosslinked polyamide membranes. I. Changes inchemical/morphological properties, J. Memb. Sci., 283 (2006) 21-26.[2] G-D. Kang, C-J. Gao, W-D. Chen, X-M. Jie, Y-M. Cao, Q. Yuan, Study on hypochlorite degradation of aromaticpolyamide reverse osmosis membrane, J. Memb. Sci., 300 (2007) 165-171.[3] L. F. Silva, R. C. Michel, C. P. Borges, Modification of polyamide reverse osmosis membranesseeking for better resistance to oxidizing agents, Memb. Wat. Treat., 3 n.3 (2012) 169-179.

Facilitated Transport of Polypropylene through a Membrane ContainingSilver Salt as a CarrierLuíza M. de Almeida* 1 , Douglas V. Fernandes 1 , Felipe C. Cunha 2 , Jane H. Fujiyama-Novak 2 ,Liliane Pollo 3 , Cristiano Borges 2 , Alberto C. Habert 2 , Carlos R. K. Rabello 41 Escola de Química, Universidade Federal do Rio de Janeiro, Brasil2 Programa de Eng. Química/COPPE – Universidade Federal do Rio de Janeiro, Brasil3 Universidade Federal do Rio Grande do Sul, Brasil4 Petrobrás/CENPES/P&D-AB* luiza.almeida@peq.coppe.ufrj.brOlefins – manufactured by steam cracking with paraffins during oil refining and natural gasprocessing – have a huge utility in the petrochemical industry as precursors of high-value products.The separation of mixtures formed by hydrocarbons with close boiling points, such as propane (-41.9 o C) and propylene (-47.6 o C) is commonly carried out in the petrochemical industry by means ofcryogenic distillation. This technology requires an enormous capital investment and imposes heavyoperation costs associated with high energy consumption. One promising alternative is the use ofacilitated transport membranes, which contains specific carrier agents in the polymer matrix thatinteract reversibly with the double bond in the olefin molecule, promoting the simultaneousincrease of its permeability and selectivity [1,2]. In addition to the aim of developing an efficientmembrane for separation of this gas mixture, this work includes the preparation of membrane andthe execution of permeation tests employing a pilot-scale gas configuration that accommodatesplate and frame membrane module. For the synthesis of composite membranes, silvernanoparticles (AgNp) were incorporated in the active polyurethane (PU) layer which was spread byusing a coating system on a poly(vinylidene fluoride) (PVDF) support. The membranes werestructurally characterized by Scanning Electron Microscopy (SEM) and X-ray diffraction (XRD). Thethickness of PU layer has not been modified (5-8 mm) in the presence of silver salt. Mixture ofpropylene and propane with similar molar concentration (propylene vol.% = propane vol.% = 50%)were used as the feed gas for investigating the real separation potency of membranes. Theeffective permeation area was enhanced from a 5.8 cm 2 (laboratory scale) to 2,450 cm 2 . Initialresults on lab scale devices indicate polyurethane-membrane permeability ranging from 2 to 4.2Barrer (10 -10 cm 2 cm -3 s -1 cmHg -1 ) and propylene selectivity from 1.3 to 1.8. On the other hand, themembranes containing the silver nanoparticles showed the best performance, reaching a selectivityof 5.1 and permeability of 17 Barrer.[1] I. Pinnau, L.G. Toy, J. Membr. Sci. 184 (2001) 39.[2] Y.S. Park, J. Won, Y.S. Kang, J. Membr. Sci. 183 (2001) 163.

Development of Poly(ethylene oxide) Membranes for Desulfurization ofGasoline by PervaporationMaria Elizabeth Ferreira Garcia 1 *, Sandra Renata Rossi 1 , Carlos Alberto de Araujo Monteiro 2 ,Cristiano Piacsek Borges 11 Universidade Federal do Rio de Janeiro/COPPE/Programa de Engenharia Química, Centro deTecnologia-CETER, Rio de Janeiro, RJ, *e-mail: megarcia@peq.coppe.ufrj.br2 CENPES / PDAB / HPE, PETROBRAS – Petróleo Brasileiro S. A.ABSTRACTThe commercial gasoline consists of a complex mixture of alkanes (C 5 -C 14 ) cycloparaffins, olefins andaromatics, products derived from the reactions of isomerization, reforming and catalytic cracking.Moreover, commercial gasoline presents contaminants such as mercaptans, sulfides, disulfides,thiophenes and its derivatives. The sulfur removal from gasoline may be obtained by catalytichydrodesulfurization (HDS). However, this process of conventional hydrotreating results in significantreduction of octane due to olefin saturation [1].One of the processes which utilize membranes, the pervaporation, has been used to remove sulfurfrom gasoline. This new desulfurization technology has attracted increasing attention fromresearchers and refineries because it meets the need for less polluting fuels [2].In this work poly(ethylene oxide) [PEO] membranes were prepared and used for the gasolinedesulfurization by pervaporation. Dense or composite membranes were obtained from PEOmolecular weight of 300,000 Da in chloroform or aqueous solutions. The solutions were cast over theporous support of poly(ether sulfone) [PES] or poly(vinylidene fluoride) [PVDF] and compositemembranes were obtained. After drying and heat treated the membranes were evaluated byscanning electron microscopy - SEM, swelling and pervaporation experiments with naphtha solutionsof known concentration. SEM results showed that composite membranes were more uniform thandense membranes, although small surface defects due to crystallization of PEO. The PEO densemembrane showed swelling of 7.5 w% in naphtha solution and permeation flux (1,5 Kg/m 2 h) wasobtained with composite membrane in pervaporation experiment.[1] H. R. Mortaheb, F. Ghaemmaghami, B. Mokhtarani (2012), Chem. Eng. Res. Des., 90, 409-432.[2] L. Lin, Y. Zhang, Y. Kong (2009), J. Colloid Interf. Sci., 339, 152–159.

Preparation of Chlorine-Resistant NF Membrane Fabricated by InterfacialPolymerizationMarina N. Souza* 1 , Jéssica Schner 2 , Jane H. Fujiyama-Novak 3 , Maria E. F. Garcia 3 , MariaEugênia Sena 2 , Alberto C. Habert 3 , Cristiano Borges 3 , Mônica O. Penna 41 Escola de Química, Universidade Federal do Rio de Janeiro, Brasil2 Universidade Federal do Estado do Rio de Janeiro, Brasil3 Programa de Eng. Química/COPPE – Universidade Federal do Rio de Janeiro, Brasil4 PETROBRAS/CENPES/PDEP/TEE*marinasouza@eq.ufrj.brSulfate removal is crucial for deep water oil operations, where membrane durability andreliability are key to lowering maintenance and operating costs while maximizing oilextraction. Nanofiltration process efficiently removes sulfate ions but disinfection bychlorination is required to control growth of microorganisms (biofouling) on the surface ofthe membrane. Development of a chlorine-resistant PA membrane is the ultimate solution tocontrol biofouling, thereby increasing membrane life.Thin film composite (TFC) membranes prepared via interfacial polymerization (IP) haveoften been used for nanofiltration (NF) due to their superior permeation performance [1]. Inthis work composite nanofiltration membranes have been fabricated using hydrazine (Hz),piperazine (PIP) and chloride trimesoyl (TMC) with a controlled fabrication technique.Interfacial composite membranes are formed over polyethersulfone porous support by in situpolycondensation of amine in an aqueous phase and TMC in an organic phase at the interfaceof these solvents.A surface modification of the polyamide composite membrane was made by covering it witha thin film of poly(vinyl alcohol) PVA to improve its resistance to chlorine. Crosslinkingreaction was carried out at 25 degrees C by using TMC [2] at different reaction time.Scanning electron microscopy images of the composite and modified membranes confirmedthe formation of the PVA layer. Nanofiltration test of the membranes resulted in Na 2 SO 4rejection of 91% when tested for 2600 mg/l feed solutions at 5 bar operating pressure withreasonable permeability (1.5 l/h.m 2 .bar). The chlorine resistance of original and modifiedmembranes was evaluated by exposing it to an oxidant solution (NaOCl 5 mg/l, Na 2 SO 4 2600mg/l). The resistance performance of composite membrane had a significant increase from 1ppm.min to 250 ppm.min after covering with PVA layer.[1] S.P. Nunes, K.V. Peinemann, Membrane Technology in the Chemical Industry, Wiley-VCH, Weinheim, 2001.[2] Q. An, F. Li, Y. Ji, H. Chen, J. Membr. Sci.367 (2011) 158-165.

Characterization of National Hollow Fiber Membranes for Use inHemodialysisNascimento, C. R. F.*(1), Ferraz, H. C.(2), Almeida, K. M. (3) e Borges, C. P. (4)(1) PAM-Membranas Seletivas Ltda, Rio de Janeiro, Brasil.(2), (3) e (4) COPPE, Universidade Federal do Rio de Janeiro.cnascimento@peq.coppe.ufrj.brThe process of hemodialysis is indicated for patients who have kidney functional capacity decreasedto less than 10 %. When it occurs, the patient is submitted to a hemodialysis session and his blood ispumped through a dialyzer containing a semipermeable membrane, allowing clearance of metabolicsubstances and restoring the ions balance [1] .The objective of this study was the establishment of methodologies for the characterization anddetermination of the parameters for effective performance comparison in relation to membranesalready in use in the medical field.For the tests commercial dialyzers were used: cellulose diacetate (Baxter DICEA 170G), polysulfone(Fresenius F7HPS) and polyethersulfone (Baxter Xenium 170), each with an area of 1.7 m².Membranes produced in PAM laboratory with different compositions were also analyzed. For testthe solutes, the following reagents were used: Polyethyleneglycol (PEG) (Fluka Chemie AG), Urea(Sigma-Aldrich), Creatinine (Merck), Vitamin B 12 (Merck), Phosphate (Vetec). For determination ofresidual solvent reagents were used: N-methyl-2-pyrrolidone (Vetec), Polysulfone (Sigma-Aldrich)and Polyvinylpyrrolidone k10 (Sigma-Aldrich). Quantitative analysis included: Urea Enzymatic Method(Laborlab), Creatinine (Bioclin), Phosphate Colorimetric Method Gomori (Doles), N-methyl-2-pyrrolidone (Environ Científica), Vitamin B 12 (Química Nova, vol. 23). The instruments were:Chromatograph Clarus 500 Perkin Elmer, portable Refractometer Instrutherm Ltda. model RT-10ATC,Spectrophotometer 6405 UV-VIS, Jenway.The characterization of national membranes showed properties similar or better than importedcommercial membranes currently used. The parameters evaluated were: hydraulic permeability,solute retention of the different molecular sizes, release of residual solvent. The results of the soluteretention standard PEG indicated that the produced membranes had characteristics andperformance similar to commercial ones. Tests, as clearance of solutes in hemodialysis machine andin vivo tests, are still under review for further comparison.The test for release of residual solvent aimed quantification of components released by nationalmembranes after permeation. The results indicated a higher release of residual solvent in themembranes produced with respect to commercial membranes. Which can be significantly reduced byincreasing the number of washing steps.[1] LI, Norman N, et. al. (2008), Advanced Membrane Technology and Applications, 519-522.

Direct Osmosis Process for Power Generation using Salinity Gradient: FO/PROPrototype Investigation using Hollow Fiber ModulesNicolas Roger Jean-Daniel Mermier*, Cristiano Piacsek BorgesChemical Engineering Program, Federal University of Rio de Janeiro – PEQ/COPPE/UFRJnicolas@peq.coppe.ufj.br, cristiano@peq.coppe.ufrj.brWith the exponentially growing population and the depletion of fossil fuels, water andenergy have become two of the most important global resources. Both water shortages and energycrises have plagued many communities around the world. Less polluting renewable energy sourcesallow to reduce harmful gases emissions into the environment, promoting greater sustainability.Therefore, the development of renewable energy sources like solar energy, biodiesel, ethanoland wind power becomes a global priority. Meanwhile, attractive and innovative membrane-basedtechnologies options such as forward osmosis (FO) and pressure retarded osmosis (PRO) processeshave shown great promise in both water supply and energy production. In these processes, a netwater movement occurs through a semi-permeable membrane under osmotic pressure gradient.This stream can be partially used for electric power generation.Although this concept is quite old, the process is still facing some difficulties to be widelyoperationalized by lack of adequate membranes that shall make the process economicallycompetitive.Currently, one of the few initiatives in the pilot and plant scale development of electricpower generation process by direct osmosis is done by Norwegian company STATKRAFT. In Brazil, thelaboratory of membranes separation processes of COPPE/UFRJ has been involved in membranessynthesis and processes researches for nearly three decades, being a national and internationalreference in the field. The area of phase inversion techniques for the preparation of anisotropicmembranes has been one of the keys to their success.This work consists in the production of self-supported polymeric hollow fibers membranesmade of a porous support body and a top dense thin layer skin which can maximize the water fluxacross the membranes, maintaining a high salt rejection. These fibers must be packed in permeationmodules within the flow of solutions with different salinity on both sides of the membrane generatesan osmotic pressure difference which can be turned into electric power. The design andconfiguration of these modules is also an object of study and innovation, mainly in order to reducehydraulic losses and to control the mass transfer. Therefore the building and testing of a FO/PROprototype is part of this work’s purpose.

Systems for Composite Hollow Fibers Synthesis Combining SimultaneousPhase Inversion and Interfacial PolymerizationNicolas Roger Jean-Daniel Mermier*, Cristiano Piacsek BorgesChemical Engineering Program, Federal University of Rio de Janeiro – PEQ/COPPE/UFRJnicolas@peq.coppe.ufj.br, cristiano@peq.coppe.ufrj.brThe objective of this work was to produce hollow fibers by simultaneous phase inversion andinterfacial polymerization. This innovative method shall reduce the preparation time and the volumeof solvent needed, reducing the ambiental impact in the industrial production. Three experimentalprocedures have been investigated. The first one involves the fabrication of flat and hollow fibersmembranes by immersion/precipitation in a nonsolvent bath and by spinneret spinning process,respectively, adding the monomers directly in the polymeric solution and in the precipitation bath.The second and third procedure combined the classic concepts of interfacial polymerization with thetriple and quadruple spinning technique, respectively, using two immiscible liquid phases. Allmembranes were prepared from polyetherimide (PEI), polyvinylpyrrolidone (PVP) and N-methylpyrrolidone (NMP) (15/10/75%w/w) polymeric solution. 1-6 hexa-methylene diamine(HMDA), m-phenylenediamine (MPDA) and 1,3,5-benzentricarbonylchloride (TCM) were investigatedas the interfacial polymerization monomers. The produced membranes were characterized byscanning electron microscopy (SEM), by attenuated total reflectance/Fourier transform infraredspectroscopy (FTIR/ATR) and through their transport properties. Although the first procedure did notlead to the expected results, the second and third ones succeed in synthesizing the active layer ofpolyamide on the inner or outer side of the support, simultaneously with the phase inversion. Thespinneret design and the mass transfer kinetics between the watery and polymeric solution provedto be predominant factors for the skin adhesion.

Bio-Lubricant Production by Pervaporation-Assisted ReactionPaola Andrea Borda Díaz*, Frederico Kronemberger eAlberto Claudio Habert, Programa de Engenharia Química/COPPE,Universidade Federal do Rio de Janeiropdiaz@peq.coppe.ufrj.brThe use of bio-lubricants has been an alternative to problems that results from the use of minerallubricants. Today, approximately 50% of the waste lubricants are not properly disposed [1],causing pollution of soil, air, water and damage to many ecosystems. The Bio-lubricants mainadvantage rely on its biodegradability. In the synthetic base oil (precursors of lubricants) industry,much of the energy is consumed in the reaction, separation, concentration and purification stagesof their products [2]. For this reason, considerable effort has been dedicated to the improvementof existing separation processes and for the development of more efficient, and a less energyconsuming technology, as it is the case, for example, of the membrane separation processes.Da Silva (2012) developed a new bio-lubricant from the enzymatic transesterification of biodieselfrom castor oil and trimethylolpropane (TMP). In this work, it was seen that the time to obtain a93% conversion of the reaction is approximately 25 hours, and it is possible to increase thereaction yield with the continuous removal of the product in the reaction equilibrium. To achievethis, vacuum into the reaction mixture may be used. Generally, this method is not selective in theremoval of desired components, in this case, methanol. Pervaporation, which is a membraneseparation process, appears to be an alternative to carry out the methanol removal from thereaction mixture.In this work, results of the membrane evaluation in the pervaporation on a synthetic mixture arereported. Materials such as PVA, PU and PDMS were examined. PVA membranes showed lowfluxes in the permeate mixture. However, PDMS membranes obtained best fluxes and selectivitywhen the concentration of methanol in the mixture is about 5%. The use of PDMS membrane andthe influence of temperature and feed concentrations will be discussed when pervaporation iscoupled with the enzymatic reaction.[1]Potera, Carol (2009). MATERIALS SCIENCE: Bringing Biolubricants to Industry.E Environmental HealthPerspectives.[2]Da Silva, J. A. C. (2012). Obtenção de um lubrificante biodegradável a partir de ésteres do biodiesel damamona via catálise enzimática e estudos de estabilidades oxidativa e térmica. Tese de Doutorando aoPrograma de Pós-graduação em Engenharia Química, COPPE, Universidade Federal do Rio de Janeiro.

Feasibility and Metodology for the Reuse of Reverse Osmosis ModulesPaula Werneck Teixeira Reuther * , Cristiano Piacsek Borges, Frederico KronembergerChemical Engineering Program, COPPE/UFRJpteixeira@peq.coppe.ufrj.brScarcity of drinking water is a worldwide problem. A possibility for obtaining potable water is throughthe desalination of seawater, which can be accomplished through a variety of techniques. Reverseosmosis (RO) has been chosen in most new desalination plants for its lower energy demand. Thistechnique may also be used to make the reuse of industrial water feasible, reducing the capture offreshwater. RO membranes are typically composed of two polymers. A polymer constitutes themicroporous support and another is responsible for the selectivity, forming a dense layer. Theselective layer presents a life cycle of about 3-5 years, depending on the operating conditions. At theend of this time, the modules are replaced and must be disposed in a properly place. However, withthe increased number of desalination plants, the modules disposal is growing at the landfills makingthe reuse of these modules necessary. Recent studies are based only on the removal of themembrane selective layer, maintaining the integrity of the microporous support, allowing the use ofthe modules as ultrafiltration ones.The objective of this work is the evaluation of the reuse of reverse osmosis modules, through asurface modification with poly (vinyl alcohol) (PVA), used to form a new dense layer, for the recoveryof their initial properties, especially in terms of salt rejection. In order to remove the selective layer,RO modules were exposed to a solution of NaClO with 350 ppm (mg/L) concentration untilapproximately 50.000 ppm.h of degradation intensity. The NaCl rejection was reduced in 90% andthe permeability increased 84 %, demonstrating that the selective layer was removed. In order tocharacterize the porous support obtained, its retention to polyethylene glycol (PEG) with differentmolecular weights was evaluated. The nominal retention (cut-off) obtained was between 20 and 50kDa, confirming that the support has characteristics of an ultrafiltration membrane. It can beconcluded that it is possible, after the removal of the damaged selectively layer, to reuse the reverseosmosis modules as ultrafiltration ones. Since the objective was to investigate the recovery of the ROmodule, a new selective layer was placed using the dip coating technique with a PVA solution. Afterthe coating with the PVA solution, MgSO 4 rejection of 78.6% was obtained, indicating the actualpossibility of the recovery of RO modules, just through an optimization of the experimentalconditions.

Application of Ceramic Membranes for Oilfield Produced Water Treatment inOffshore PlatformsSilvio Edegar Weschenfelder* a, b , Ana Maria Travalloni Louvisse, Cristiano Piacseck Borges,Juacyara Carboneli CamposaPetrobras Research Centerb School of Chemistry, Inorganic Processes Department. Federal University of Rio de Janeiroc COPPE/Chemical Engineer Program, Federal University of Rio de Janeiro Rio de Janeiro*silvioweschenfelder@petrobras.com.brThe cost of managing and treating large volumes of oilfield produced water (OPW), generated in oilproduction units, is a key consideration to oil and gas producers. This water contains a complexmixture of organic and inorganic compounds, dissolved or not, that need to be removed to someextent before disposal or reinjection. The main quality requirements for OPW reinjection areconcerned to total suspended solids (TSS) and oil and grease (O&G) removal. These contaminantsmust be removed in order to keep from clogging the reservoir production zones and maintaining ahigher efficiency of injectivity. Conventional systems such as dissolved gas flotators andhydrociclones are not able to reach the quality requirements in most of the cases. Thus, membranetechnology has been pointed as a potential solution for treating efficiently the OPW, removingalmost completely TSS and O&G. This study shows the lab scale results with microfiltrationmembranes, using a polymeric membrane and two different ceramic membranes based on zirconiumoxide and silicon carbide. The membrane performance was evaluated as a function of permeability (J,L/h.m 2 ), rejection of O&G (R, in %), TSS content and silty density index (SDI). The synthetic producedwater used for the tests had drop sizes and oil and grease content similar to those obtained in anoffshore produced water treatment plant. Cleaning protocols were also tested in order to regeneratethe membrane. Good results were obtained for both, polymeric and ceramic membranes, concerningO&G rejection, TSS removal and permeability. However, much higher permeabilities were obtainedwith ceramics. It indicated that ceramic membranes system could be pointed as a possibletechnology for treating the OPW in an offshore platform, with the advantage of being a compact,resistant and a robust technology. Based on these evidences, longer trial will be carried out in a pilotplant that will be implemented to test different membranes, different operational conditions andalso varying OPW characteristic. The system shown in Fig.1 has a capacity of treating 10m 3 /h and willbe used for further trials to evaluate the technical feasibility of this technology for reinjectionpurposes.

Fig.1: Ceramic Membrane Pilot Plant.

Polyurethane Membranes to Remove Sulfur Compounds from Naphtha byPervaporation ProcessRafael Aislan Amaral*, Alberto Cláudio Habert, Cristiano Piacsek BorgesInst. Alberto Luiz Coimbra de Pós-graduação e Pesquisa de Eng., Univ. Fed. do Rio de Janeiro, Brasil*ramaral@peq.coppe.ufrj.brThe removal of sulfur in fuels has been an important issue in the refining industry. In Brazil, about70% of the gasoline pool is comprised of naphtha derived from the fluid catalytic cracking process(FCC, Fluid Catalytic Cracking) without any additional treatment. In general, this current can be founda high sulfur content (average 1.000 mg / kg), which directly contributes to SO 2 emission andcorrosion of equipment and pipelines.Separation processes with membranes (SPM), in particular the process of pervaporation has beenstudied in a growing number of articles and patents for the desulfurization of liquid hydrocarbonstreams. The advantages of this process are usually common characteristics of SPM, i.e., selectivity,low cost and simplicity of operation, modular and compact equipment and easy to scale up. Whencompared to the conventional hydrodesulfurization of FCC naphthas, the pervaporation enables toremoving organosulfur compounds without hydrogen consumption (lower operating costs andwithout loss of octane) operate at relatively low temperature and pressure, and dispense the use ofcatalysts . The efficiency of the pervaporation to desulfurization is related to the use of membraneswith affinity to sulfur compounds.The main objective of this research is the development of membranes with high affinity to sulfurcompounds present in naphtha. The polyurethane was selected as membrane material due to itsexcellent properties of chemical, mechanical and heat resistance, besides having an affinity for sulfurcompounds. The potential of polyurethane membranes have already been exploited for the removalof aromatic compounds, showing the feasibility of using for separating organic streams [1].In this study, membranes were prepared in flat sheet and hollow fibers geometry. As feed charge,was chosen initially a binary mixture containing 1,500 parts per million of 2-methyl thiophene (sulfurcompound more difficult to be removed in the traditional process) in iso-octane (the maincomponent of naphtha).The results os pervaporation showed high selectivity for sulfur compound with a relatively lowpermeate flux for the binary mixture. Currently, the work is focused on the preparation ofasymmetric membranes in order to increase the permeate flux, keeping the selectivity obtained.[1] V. S. Cunha, M. L. L. Paredes, C. P. Borges, A. C. Habert, R. Nobrega (2002), J. Memb. Sci., 206, 277-290.

R i X 10 11 (m -1 )R i x 10 11 (m -1 )Study of New Permeators for Membrane Bioreactors (MBR) Aiming at FoulingControlRobson Rodrigues Mororó*, Cristiano Piacsek Borges, Frederico de Araujo KronembergerPrograma de Engenharia Química – COPPE/UFRJ.robson@peq.coppe.ufrj.brThe conventional biological wastewater treatment is based on activated sludge process, followed bysedimentation. This approach, although effective in the removal of pollutant loading, requires largevolume settling tanks for the sludge removal of the treated effluent, to meet the standards set byenvironmental agencies. The membrane bioreactors (MBR) equipped with microfiltration (MF) orultrafiltration (UF) membranes are an alternative to replace the conventional processes, since theypresent smaller footprint and better quality of the final effluent. The main problem in operating MBRis the loss of productivity due to fouling and the key for its control lies in the hydrodynamics of thebioreactor. The design of new membrane modules is critical in this scenario. The present work aimsat studying new permeators for membrane bioreactors (MBR), with both hollow fiber membranesand air injectors attached to their base, in a uniform distributed manner, in order to investigatefavorable conditions for the permeation. For this purpose, permeation transport resistances wereassessed using modules with different number of holes in the air injector and different packingdensity, under several permeation conditions, with distinct yeast concentrations, superficial airvelocities and filtration pressures. Five new permeators were tested. Figure 1 presents the foulingresistance (R i ) in function of superficial air velocity and energy expended in aeration for each newpermeator tested. The lowest resistances were found for the permeator with 64 holes in the airinjector and fiber packing density of 650 m²/m³. Nevertheless, the variant with 32 holes in the airinjector and fiber packing density of 650 m²/m³ showed better or the same efficiency in the controlof fouling in relation to energy expenditure with aeration.2500.7 bar2500.7 bar20020015010015010050500 2 4 6U g (m.s -1 )00 2 4 6 8Energy expended (KJ)Figure 1. Comparison of the efficiencies of fouling control of each new permeator. R i as a functionof air velocity and anergy expended.

Mixed Matrix Membranes for Gas Separation: Morphological Characterization andTransport Properties for O 2 /N 2Sandro Eugenio da Silva*, Bruno da Silva Gonçalves Alves, Helen Conceição Ferraz, CristianoPiacsek Borges.Federal University of Rio de Janeiro/Chemical Engineering Program - COPPE.sandro@peq.coppe.ufrj.br.Some industrial processes are always improving their technologies, promoting the decreasing inproduction costs that are joined with energetic and environmental aspects. Among the separationprocesses, which need new technologies, are gas separation processes. Current technologies for gasseparation are cryogenic distillation and adsorption process for sieves molecular whose separationoccurs by phase shift of the components. An alternative technology is processes for gas separationusing membranes. But, for some gases separations, the conventional polymeric membraneproperties are not sufficient to apply for current technologies because of inverse relationshipbetween selectivity and permeability of them.In this context, the development of new membranes has been inquired, mainly mixed matrixmembranes (MMM). These membranes are prepared by addiction of inorganic particles in polymermatrix. With this, the junction of two materials with different diffusivity and solubility for gases canresult in a favorable effect, combining high flux and selectivity from inorganic particles (e.g, carbonnanotubes, silica and zeolites) with the facility of production of polymeric membrane [1]. Thus, thedevelopment of these membranes can promote the commercial applicability of the gas separationprocess competitively.From what has been explained above, the general objective of this work is the development andcharacterization of mixed matrix membranes for gas separation, with focus on the adhesion betweenpolymer matrix and inorganic particles, and the improvement of the transport properties for O 2 /N 2separation. MMM flat sheets were produced by the solution casting technique and subsequentformation of these one by solvent evaporation technique, using polyurethane polymer (PU) and asinorganic particles, zeolites 4A e 5A. Scanning electronic microscopy (SEM) was used to characterizeMMM morphology and transport properties (permeability and selectivity) were obtained bypermeation gas system, through O 2 and N 2 permeation tests.By SEM photomicrography of the MMM surface layer, it was observed good dispersion of zeolites inpolymer matrix, but still with the presence of agglomerates. In the cross section was visualizedaccumulation of inorganic particles on the bottom of MMM that was caused by decantation of theseparticles during formation membrane. This morphology reflected in the results of transportproperties, observing 140% increase in the O 2 /N 2 selectivity (from 3.72 in the PU pure membrane to6.55 in the MMM) in the MMM with 15%(m/m) zeolite 5A. MMM permeability values were 0.6-1.2barrer for N 2 and 3.2-4.3 barrer for O 2 .[1] T.-S. Chung, L. Y. Jiang, Y. Li, S. Kulprathipanja (2007), Mixed matrix membranes (MMMs) comprising organicpolymers with dispersed inorganic fillers for gas separation, Prog. Polym. Sci., 32, 483-507.

Study from Hydrodynamics Aiming to Reduce Fouling in MBRThaissa P. Silva*, Cristiano P. Borges, Frederico A. KronenberguerLaboratório de Processos de Separação com Membranas e Polímeros – PAM /Universidade Federal do Rio de Janeiro – UFRJ, Campus do Fundão, Rio de Janeiro – RJthaissa@peq.coppe.ufrj.brCurrently one of the major environmental concerns is related to the indiscriminate useof water. Due to this increasing concern about saving water and also legislation restrictions,the reuse of water has been the focus of global discussions. A process that allows the watertreatment for reusing would be the association of technology separation by membranes to theconventional activated sludge process. This set of processes is named Membrane Bioreactor(MBR).Compared to the standard techniques the membrane bioreactors produce betterquality effluent since they retain completely the biomass. Furthermore, the pollutantsdegradation is much more efficient due to the higher concentration of microorganisms in thesystem.Among all the advantages, the one that stands out most is the ability to obtain atreated effluent with an exceptional quality that can be reused in the productive process,reducing water abstraction and effluent generation.However, one of the major limitations from the processes separation by membrane isthe formation of fouling, which has as consequence a reduction in the permeated flux, a highpower consumption and the need of membranes cleaning or even their replacement. Theselimitations have provided the development of several studies and publications directed mainlyto the shift in the modules and operational parameters as well as the change in thehydrodynamics process.The main objective of this study is to evaluate the hydrodynamic in systems BRMpromoting oscillations within the liquid phase in order to minimize fouling and thus reduce theamount of air used in the process. The system was characterized by: (1) the hydraulicpermeability from the modules, (2) the permeate flux with different concentrations of biomassand air flow rate, and (3) the study of the oscillating system – by selecting the pump wavegenerator – from a relation between the amplitude and the frequency.The next stages are: (1) conducting experiments to ratify the oscillating systemperformance, (2) determining the guns designer – wave’s providers, (3) the coupling from theoscillating system to MBR and (4) technical and economic analysis.

Oily Wastewater Treatment by Membrane Separation Processes AimingReuse: Considerations Based on Experimental Data.Albérico Ricardo Passos da Motta 1 *, Cristiano Piacksek Borges 2 , Karla Patricia de OliveiraEsquerre 3 , Asher Kiperstok 3 , Rafaela Oliveira Flores 41 PETROBRAS, 2 COPPE/UFRJ, 3 EP/UFBA, 4 UFRJE-mail address: arpmotta@yahoo.com.brThe main advantages of membrane separation processes (PSM) in relation to the processes whichare widely used for oily effluents treatment are: retention of oil droplets with sizes below 10 µm,lower capital costs, the non-requirement of any chemicals addition and ability to generatepermeated with a very good quality [1].This paper presents technical considerations about oily effluents treatment by the PSM, for oilremoval, in order to reuse it in industrial processes.The tests were conducted on a bench scale microfiltration (MF) unit. The unit consisted of a 8 Lcapacity tank where the membrane element was submerged and which was continuously fed by theeffluents to be tested. The membrane used was a hollow fiber type, made from polyetherimide,having a total area of 0.5 m 2 and pore diameter average and maximum of 0.4 and 0.8 µm,respectively. The filtration was done by using a filtrate suction pump, in order to obtain the requiredpermeate flow rate. Two fouling mitigation techniques were used: air bubbling and periodicbackwashing. The bubbles prevented oil from adhering to the membrane surface by shaking thehollow fibers.The tests were carried out using synthetic oil in water emulsion (O/W) with oil and grease content(O&G) between 100 and 200 mg.L -1 and oil droplet diameter between 3 and 8 µm. The unitoperational parameters tested were: trans membrane pressure (TMP) between -0.12 and -0.30 bar,feed flow rate (Qf) between 30 and 120 L.h -1 and recovery factor (REC) of 0.75 and 0.90. Theparameters used for assessing the tests efficiency were the permeate O&G (O&Gp) and thepermeate flux (Jp) decline over the time.The results showed the backwash and air bubbling have successfully reduced the decrease ofpermeate flux, an inherent PSM problem which results in an undesirable increase in the frequency ofchemical cleaning. Another important result was the process efficiency, in terms of oil removal orpercent oil rejection (% R). In this study, the minimum efficiency found was 96%. In addition, theaverage O&G found in the permeate (O&Gp) was 5.6 mg.L -1 , which represents a very good quality forreuse purposes in several industrial processes, such as spare parts washing in mechanical garages,industrial vehicles washing, dust control and fire control.[1] B. Chakrabarty; A. K. Ghoshal; M. K. PURKAIT (2008), Journal of Membrane Science, 325, 427-437.

Copper Waste Recovery from Hydrometallurgical Industry by MembraneContactor SystemKleber Bittencourt Oliveira* 1,3 ; Helen Conceição Ferraz 2 ; Emanuel Negrão Macêdo 31Departamento de Engenharia Química - Universidade do Estado do Amapá2Lab. de Processos de Separação com Membranas – Universidade Federal do Rio de Janeiro3Laboratório de Simulação de Processos, Universidade Federal do Parákboliveira@ueap.edu.brThe treatment of effluents from hydrometallurgical industry aims at the recovery of wasted metalsand satisfying agency's legislation and regulations for mitigating environment impact. Membranecontactors have emerged as alternative to conventional liquid-liquid extraction and have proven itspotential since it requires a much smaller amount of reagents, avoids formation of emulsions,provides a large contact area and reduces equipment footprint [1,2].This study aimed to develop a membrane contactor system for the recovery of copper from wastewater generated in the process of solvent extraction of copper from a hydrometallurgical plantlocated in the North Brazil. After characterization of the residue, it were determined the keyparameters for the system design. Using direct contact, it was done a screening of best solvents andconditions for the extraction.The prototype consists of a continuous system extraction and stripping of metals in aqueous media,polymeric membranes of the hollow-fiber type (FiberFlo ®, Minntech Co. USA) with a pore size of0.03 microns, 240 microns inner diameter and 0.2 m 2 footprint, as shown in Fig. 1.(a) (b) (c)Fig. 1. Membrane contactor system; (a) Layout in 3D with their dimensions in millimeters, (b) Frontview of the assembled system, (c) Photograph of the commercial module of microporousmembranes.It was investigated the influence of type and concentration of extractants, solvents and strippingsolution, pH range and operating time on profile extraction kinetics. The following extractans wertested: Cyanex 272 (phosphinic acid bis (2,4,4 - trimethylpentyl)) and Lix-84IC (2-hydroxy-5-nonylacetophenone). As solvents, we tested kerosene, 1-octanol, decalin (decahydro-naphthalene ) and

Concentration of Copper (ppm)Percentage of Recovery (%)Exxol D80 (aliphatic hydrocarbon) and as stripping solution, sulfuric acid and hydrochloric acid wereemployed. Extractant concentration ranged from 5 to 20% (v/v), pH from 2 to 6 and the operatingtime from 30 to 80 minutes. Figure 2 show some tipical results.1200100100080800600400200Extraction of CuRecovery604020000 20 40 60 80Time (min)Fig.4. Change in concentration and recovery over time in the extraction of copper, using LIX84Iin kerosene (20% v/v), pH = 4, T = 25C, Cu = 1.194 g / L.[1] P.K. Parhi, K. Sarangi (2008), “Separation of copper, zinc, cobalt and nickel ions by supported liquidmembrane technique using LIX 84I, TOPS-99 and Cyanex 272”. Separation and Purification Technology., 59,169-174, Elsevier Science B.V.[2] E. Drioli, A. Criscuoli, E.Curcio (2006), “Membrane Contactors. Fundamental, Aplications and Potentialities”.Membrane Science and Technoloy, 11, chapter 5, Elsevier Science B.V.

J ( g / h m 2 )Ethanol dehydration through crosslinked PVA/PES composite membranes withplasma treated asymmetric supportBetina Villagra Di Carlo* a ,Elza Castro Vidaurre a , Alberto Claudio Habert b .a Instituto de Investigaciones para la Industria Química, CONICET, Universidad Nacional de Salta,Facultad de Ingeniería, CIUNSa, Salta- Argentina.b Universidade Federal do Rio de Janeiro, Programa de Eng. Química, COPPE, Brasil.* email: betinadicarlo@gmail.comPervaporation through membranes has potential advantages compared to the conventionalseparation technologies. A composite membrane involves a deposited dense active layer on a poroussupport film. The morphology of the membrane and the chemical properties of the polymericmaterial affect the membrane performance. The pervaporation performance of the compositemembrane also depends on operational conditions (temperature, partial pressure gradient, feedcomposition, etc.). Plasma treatment is a non-polluting and flexible technique to modify surfaceproperties of polymeric materials. It is particularly useful whenever surface adhesion and wettabilityhave to be increased. In this study, crosslinked PVA/PES composite membranes were prepared toinvestigate the pervaporation performance aiming at separating ethanol/water mixtures.8006002 coating steps3 coating steps4 coating steps400200020 30 40 50 60 70T (°C)Fig. 1. Effect of feed temperature on total flux of the crosslinked PVA/PES composite membranes forthe pervaporation of a 20/80 wt% water/ethanol mixture.Poly(vinyl alcohol) was chosen as active layer for the composite membrane due to its highhydrophilicity and thermal resistance. Support membranes were synthesized through the wet phaseinversion process. Polyethersulfone was selected to synthesize porous membranes.Polyvinylpyrrolidone was added as soluble component to promote porous structure whileN,Ndimethylformamide was chosen as solvent to prepare a solution for the casting process. Distilledwater was used as coagulating bath. A radio-frequency reactor (Harry-Plasma, Inductive, 8–12 MHz)was used for plasma treatment. The precursor was atmospheric air, fed at room temperature. Cross-

sections of membranes were observed by SEM (JEOL-JSM-6480 LV). Surface chemicalcharacterization was deduced from IR spectrums with attenuated horizontal total reflectancetechnique (FT-IR/HATR, Perkin-Elmer, Spectrum GX). Surface hydrophilic character was investigatedby the measurement of contact angle with a goniometer (Rame-Hart). The surface energy wascalculated by means of an iterative procedure proposed by Neumann [1]. The adhesion work wasestimated through a combination of Young and Dupre´ equations [2]. Permselective properties ofcrosslinked PVA/PES composite membranes were evaluated in a standard pervaporation lab set. Itwas fed with a liquid mixture of water/ethanol (20/80 wt%).Crosslinked PVA/PES composite membranes with controlled skin thickness were successfullyprepared and characterized. The hydrophilicity of the porous support membrane surface wassignificantly improved by plasma treatment (air, 29.6 W, 650 mTorr, 10 min). The FTIR spectra of PVAmembranes showed that thermally induced maleic acid chemical crosslinking of the PVA membraneoccurred through an esterification reaction. The separation factor increases with increasing numberof coating steps with PVA at the expenses of total flux (Fig.1).[1] Kwok D, Neumann A (2000) Surf A: Physicochem Eng Asp 161(1) 31–48.[2] Tabaliov N, Svirachev D (2007) Appl Surf Sci 253:4242.

Sulphate Removal Units MonitoringMartins Jr, Elpidio CorreaPETROBRAS/E&P-SSE/UO-RIO/IPP/PMFelpidio.quimico@petrobras.com.brOffshore platforms have great systems to treat seawater in order to supply water injectionwells. A critical analysis of information is given by monitoring instruments. Evaluation ofsulphate removal unit membranes performance is carried out by main related parameters:feed pressure, flow rates, differential pressures of the system. These parameter analysis leadto predicting uncommon situations, schedule cleaning procedures, and also candemonstrate operation problems like unbalanced flows, occurrence of scale, biofilmgrowing. The operation above recommended limits can lead to these and other problems,such as reduced time campaign operation, shorter lifetime of membranes too. The values offeed pressure and differential pressure are observed during the whole operation time, andthey are the main parameters for defining the saturation limits of pores, that will indicatechemical cleaning necessity for each package of the sulphate removal module.

CO 2 Separation from Natural Gas with Membrane Permeators and Gas-Liquid ContactorsJosé Luiz de Medeiros 1* , Ofélia de Queiroz Fernandes Araújo 1 e Wilson M. Grava 21. Lab. H2CIN da Escola de Química da UFRJ. Av. Horácio Macedo, 2030, Centro deTecnologia, Bl.E. Ilha do Fundão, Rio de Janeiro – RJ – Brazil. CEP: 21.949-9002. PROCO2-CENPES/PETROBRAS, Av. Horácio Macedo, 950 - Cidade Universitária.Ilha do Fundão - Rio de Janeiro – RJ – Brazil. CEP: 21.941-915*jlm@eq.ufrj.brCO 2 removal is an important unit operation in natural gas (NG) processing. Brazilian Pre-Saltreserves, where associated NG occurs in deep reservoirs distant from onshore facilities andexhibits high concentration of CO 2 , unit operations should have small footprint and minimizeequipment weight due to the high cost of ship hulls. Some of the most commonly usedtechnologies to remove CO 2 from gas streams are absorption by chemical and physicalsolvents, membranes, and cryogenic fractionation. The priory mentioned constraints,however, favor membrane separations for offshore processing of natural gas with high CO 2content. Project design and optimization of such innovative alternative demand rigorousmodels to predict equipment performance at various process configurations and operationalconditions (e.g. Figure 1 and 2). The work presents simulation results comparing membranepermeators to gas-liquid contactors employing aqueous solutions of ethanolamines. Wepresented a realistic model of Gas-Liquid Contactor for CO2 removal from NG using hollowfibermembrane percolated by aqueous amine solutions. For instance, membrane contactorsmodel considers compressible flow for a two-phase reactive permeate and for the gasretentate, taking into account momentum and energy effects in both streams so as to predicttemperature, pressure and composition profiles. The model was demonstrated via a simple NGflowsheet with membrane Contactor showing soundly results [1].Figure 1 – Process Configuration of a Membrane Permeator Alternative

Figure 2 – (a) Membrane Contactor, (b) Simulation Results for Equilibrium Mol Fraction ofCO 2 in Gas Phase x (P,T), and (c) Permeate Liquid Phase Mol FractionsReferences[1] de Medeiros, José Luiz ; Nakao, Andressa ; GRAVA, WILSON M. ; NASCIMENTO, JAILTON F. ;DE QUEIROZ F. ARAÚJO, OFÉLIA . Simulation of an Offshore Natural Gas Purification Processfor CO Removal with Gas Liquid Contactors Employing Aqueous Solutions of Ethanolamines.Industrial & Engineering Chemistry Research , 2013.

CO 2 Removal Systems with Membranes at Petrobras Offshore Units1. Leandro Fernandes Nolasco Quintanilha – leandro.quintanilha@petrobras.com.br *2. Paulo Roberto de Jesus – pauloroberto@petrobras.com.br3. Rafael Henrique Pecora Gomes – rafael.pecora@petrobras.com.brPETROBRAS – Petróleo Brasileiro S.A.In the oil and natural gas production, the CO 2 is one of the most common impurities at the producedgas from the wells. During the news Pre-Salt FPSOs design, this was a big issue to deal due to thecontent of this contaminant vary from 8 up to 60% v/v and the Petrobras specification, for thisprojects, requiring a CO 2 content of 3% v/v in the exportation gas. In order to attend this scenario,i.e. high CO 2 inlet, large range of CO 2 content and an exportation gas with CO 2 concentration of 3%,the membranes separation was the technology adopted to remove the CO 2 from the produced gas.The membrane material itself operates on the principle of different solubility rates and diffusivityamong the natural gas components. They operate on the principle of solution-diffusion through apolymeric membrane. The CO 2 first dissolves into the membrane and then diffuses through it.Therefore, the components dissolve and diffuse with different velocities across the polymeric film, soit is possible to separate the components that are presented at the feed stream. For instance, as ageneral view, the CO 2 permeates 30 times faster than the methane, therefore it is possible toseparate at the outlet a stream with high CO 2 content (membrane permeate) and another streamspecified regarding the contaminant content and rich in hydrocarbons (membrane non-permeate).The driving force required to have this separation are the different partial pressures of the gascomponents.The main advantages of this technology are the smaller footprint and less weight, which are keyscharacteristics at offshore units, comparing with other commercial technologies used at offshoreenvironment. Others interesting characteristics are the simple operation and the high flexibility todeal with the Pre-Salt range of CO 2 content. A disadvantage is the hydrocarbon loss to the Permeatestream (roughly 3 – 5%), since that some methane molecules are able to permeate the membranes.However, the adoption of this technology to remove the CO 2 from natural gas requires a robust andefficient pre-treatment upstream the membranes. The membrane damage is caused by watercondensation within the membrane elements, hydrocarbon condensation can be also harmful,depending on the chosen membrane technology. Therefore, it is vital to remove the water and heavyhydrocarbons in order to maintain the removal performance and lifetime of the elements. The pretreatmenthas 3 basic steps: dehydration, dew point adjust and a coalescer filter.This paper purpose is to present the pre-treatment and membrane configuration adopted to the Pre-Salt basic design, sizing criteria, some issues involved at the specification of this unit and acomparison with others conventional technologies used to remove the CO 2 .

Assessment of Membranes Potential for Ballast Water TreatmentRafael Ferreira de Jesus 1 , Ana Maria Travalloni Louvisse 1 , *Celso Alleluia Mauro 21 PETROBRAS/CENPES/PDEDS/Gerência de Tratamento e Reuso de Águas.2 PETROBRAS/CENPES/PDEDS/Gerência de Avaliação e Monitoramento Ambiental.cmauro@petrobras.com.brThe worldwide transfer and introduction of non-indigenous invasive aquatic organisms via ships’ballast water (BW) has been amply demonstrated to cause significant ecological, economic andhuman health impacts 1,2,3 . To prevent, reduce and control these impacts was adopted in a DiplomaticConference in 2004 the International Convention for the Control and Management of Ships’ BallastWater and Sediments 4 . This convention is divided into Articles and an Annex which includes technicalstandards and requirements regarding the Regulations for the control and management of ships’ BWand sediments. According to the Regulation D-2, discharges of ships shall comply with BWPerformance Standard. These regulations include two indicators concerning the size of the planktonorganisms, and three indicators concerning human health standards. BW exchange is currently theonly widely acceptable and suggested (sometimes even required) procedure to minimize the risk ofBW mediated invasions but operational limitations and variable effectiveness in meeting thestandard D-2 of this approach have led to significant financial investment in the research anddevelopment of more effective shipboard and shore based BW treatment technologies (5). The highBW flow rates and volumes that must be treated, the availability of space on board, and thepresence of sediment in the ballast tanks (providing habitat for resistant organisms such as restingstages of phytoplankton and zooplankton) 6, 7 reduce the efficacy of many treatment options andpose significant technological challenges to the millionaire market of BW treatment which has notyet been addressed from the Brazilian technological companies involved with water treatment. Thenthere is a strong need to address the various treatments technologies and available markettechnologies to solve the BW treatment onboard of the ships, therefore, technologies that do notdemand high electric power, produce chemicals or need to keep chemical substances on board are“well coming on board”. The main objective of this work was the assessment of microfiltrationmembranes potential for BW treatment especially regarding their ability to comply with thedischarge standards D-2 besides obtaining an estimate of the footprint and cost of a treatmentsystem to be installed on board a ship. The results obtained in bench scale study showed that: themicrofiltration membrane was able to effectively remove fecal and total coliforms possibly meetingmicrobiological indicators of Regulation D-2; large areas are required on board vessels for theinstallation of membrane system; and that the costs of deploying this system are high. There is aneed for more research to improve the knowledge in order to optimize the design arrange of themembranes to install on board, develop more appropriate material for this purpose and also to carryout trials on board to confirm it commercial applicability.References[1] J. T. Carlton (1993), Science, 261, 78-82.[2] G. M. Ruiz (2000), Nature, 408, 49–50.[3] D. Pimentel (2000), Bioscience, 50, 53-65.[4] IMO (2004), www.imo.org[5] M. Gregg (2009), Aquatic Invasions 4, 521-565

[6] V. Alekseev (2010), Mar. Poll. Bull. 61 254–258[7] T. F. Sutherland (2010) Mar. Ecol. Prog. Ser. 210, 139–148

Gigamem® : An Innovative Ultrafiltration Membrane ProcessApplication To Seawater Filtration For Injection On Large 250,000 bpd(10 Mgd) Oil PlatformsOlivier Lorain / Jean Michel Espenan (*)Polymem SA- Impasse de Palayré- F31100 Toulouse-France-jm.espenan@polymem.frPolymem is working since 2007 with Oil and gas companies to develop new applications ofUltrafiltration (UF) membrane into oil & gas industry. For this purpose, Polymem has developed andlaunched in 2009 the largest pressurized hollow fiber module available on the market forUltrafiltration and Microfiltration applications. The brand name is Gigamem ® . Unically with Polymemcompany, the membrane material can be chosen between several materials such as Polysulfone orPVDF based. Several oil and gas companies have now decided to move forward to these very largepressurized UF modules instead of convention media or sand filters. The Gigamem® module benefits,compared to conventional media or cartridge filtration, are numerous: significant reduction inoperation weight compared with traditional media; high quality treated water for injection ;membrane separation is independent of varying feed water quality ; UF reduces frequency ofcleaning and replacement of RO and NF membranes ; Simple maintenance procedures ; No need forconsumable cartridge filters ; Enhanced bio-contaminants and Suspended Solids reduction.Furthermore, Polymem has developed a specific operating process associated with the Gigamem®with no decrease of filtration flow during backwash. The unit is composed of several trains ofmodules. By increasing temporally the operating flow of the running trains, one train can bebackwashed while the flow of the unit keeps constant. Therefore, the process allows to work withoutpermeate storage tanks which is very important to save space and weight on offshore platforms andalso can be very interesting to save costs for in-shore applications too.The paper presents the case studies of a demonstration unit and 3 full scale large plants equippedwith these large modules, treating up to 250,000 bpd (10MGD). The designs of the plants aredescribed. Space and weight reduction is presented. Cost estimations are showing drastic CAPEX andOPEX cost saving. The consistent quality of the filtrate is presented.

Submitted to SIMPAM 2013www.peq.coppe.ufrj.br/simpam_2013simpam2013@peq.coppe.ufrj.brAdvances in polymeric membrane material technology open new options fornatural gas treatingAbstractBen Bikson, PhD and Yong Ding, PhDPoroGen Corporation,35 A Cabot Road, Woburn, MA, 01801, USAMembrane technology for natural gas processing has been considered extensively. Thetechnology holds much promise due to the inherent simplicity of the membrane process and modestoperating costs. Although the use of membranes in natural gas processing has grown significantly, it isperceived by the industry as a niche technology applicable to a narrow range of acid gas treatmentapplications. The current industry perception of the membrane technology can be summarized asfollows – extensive pretreatment is required for reliable operations; hydrocarbon recovery may belimited; it is applicable mostly for the CO 2 removal; in a limited set of circumstances the technology canbe used for the fuel gas conditioning and dehydration. The primary user concern continues to bemembrane durability and the separation efficiency. These concerns must be fully addressed by any newmembrane technology to breakout of the existing paradigm.PoroGen Corporation has recently introduced new PEEK-Sep membrane technology for abroad range of natural gas treatment applications. The technology is based on advance engineeringpolymer poly (ether ether ketone), PEEK. PEEK is a commercial engineering plastic with superior thermomechanicalproperties as compared to most engineering plastics and exhibits exceptional chemicalresistance. Membranes manufactured from PEEK are not soluble in solvents at conventionaltemperatures and PEEK-Sep membrane operation is not affected by components of natural gas orprocessing fluids including acid gases, aromatic and aliphatic hydrocarbons, methanol and amines. Themembranes are manufactured in a hollow fiber configuration to provide for a low cost compactpackaging and to optimize thermodynamic separation efficiency. The paper will address distinctperformance characteristics of PEEK-Sep membrane systems with focus on natural gas dehydration, acidgas removal and fuel gas conditioning. The paper will provide examples of commercial installations thatremove multiple impurities from the natural gas to meet pipeline specifications. The operational

advantages of this new membrane technology as compared to prior art membrane systems and glycoldehydration will be further outlined.

Characterization of the Pore Size of Polymeric Membranes by Capillary FlowPorometry and Comparison with other Characterization TechniquesLuc Stoops 1 , Chris Dotremont 1 , Danny Pattyn 2 and Angels Cano-Odena 2*1VITO, Boeretang 200, 2400 Mol, Belgium. 2 POROMETER n.v. Begoniastraat 17, 9810 Eke,Belgium. Corresponding author: Angels Cano-Odena (angels.cano-odena@porometer.com)Capillary Flow Porometry (CFP) is a fast, accurate and reproducible technique for the characterizationof pore size distributions in porous materials. It is based on the displacement of a wetting liquid fromthe through pores of a sample by applying an inert gas at increasing pressure. The pressure (P)required to expel the wetting liquid is used to calculate the pore diameter (D), based on the Young-Laplace equation P=4*γ*cos θ/D, where (γ) is the surface tension at the interface gas and liquid andθ is the contact angle of the wetting liquid. [1] The diameter measured in CFP corresponds to themost constricted part of the pore, which is the most challenging part and offers the highestresistance to evacuate the liquid. CFP widely used to measure minimum, maximum (or first bubblepoint) and mean flow pore sizes, and pore size distribution of through pores in membranes,nonwovens, papers, filtration and ultra filtration media, hollow fibers and ceramics in the range of 13nm-500µm.There are two methods to measure in CFP. The pressure step/stability method is specially indicatedfor research and development work. A certain pressure is applied and maintained for a certain time.A data point is acquired only when the stability criteria for both pressure and flow rate, defined bythe user, are achieved. This takes into account that materials have a complex pore structure andpores may have different tortuosity and pore length but still the dame diameter. The porometerdetects when a pore empties at a certain pressure and waits until all pores of the same diameterhave been completely emptied before accepting a data point and moving to the next pressure. Onthe other side, in the pressure scan method a single valve is opened during the measurement and thepressure and the resulting gas flow data points are acquired continuously. Therefore it permitsobtaining fast and very reproducible results and it is very suited for QC type of work and for sampleswhere all pores are identical.In the present work the pressure step/stability method is used in CFP was used to characterize thepore size distribution of commercial and research stage microfiltration and ultrafiltration polymericmembranes. The membranes are also characterized by Scanning Electron Microscopy (SEM) andMolecular Weight Cut-off (MWCO), based on the retention of Dextran and/or polyethylene glycolsolutes of different molecular weights evaluated by gel permeation chromatography (GPC). Theresults obtained by CFP, SEM and MWCO are compared. The objective of this work is to understandbetter the differences between different characterization techniques and to find a correlationbetween the results obtained. CFP appears to be a very powerful tool for the selection of a suitablemembrane for a particular application and for further membrane research and development.[1] S. Lowell; J. E. S. Martin; A. Thomas; M. Thommes. Characterization of Porous Solids and Powders: SurfaceArea, Pore Size and Density; Springer: Dordrecht, 2006.

Solvay Materials for UF/MF Membranes and Development TrendsAnna Maria Bertasa*, Pasquale Campanelli, Emanuele Dinicolo, Thomas Kohnert, TheodoreMoore, Aldo SanguinetiSolvay Specialty Polymers. Annamaria.bertasa@solvay.com.Solvay Specialty Polymers has strengthened its position in the Water Treatment market over lastyears, offering several high performance polymers for membranes.Some key features of standard sulfone polymers and fluoropolymers for membranes manufacturingwill be presented, together with an overview of the running R&D developments.Sulfone polymers, including Udel ® polysulfone and Veradel ® polyethersulfone have been used inmembrane applications for nearly 40 years. Because of their ease of formation into variousmembrane morphologies, excellent mechanical and thermal properties, and high chemicalresistance, they can be found gas separations, water purification (reverse osmosis, ultrafiltration, andmicrofiltration), hemodialysis. Sulfone polymers are also being considered for new applications inforward osmosis and pervaporation.Relevant information for processing of sulfone polymers, including suitable solvents, solutionviscosities, and chemical compatibility will be given.Fluoropolymers has received a large consideration for some specific segments in the market of lowpressure water treatment. Solef ® PVDF is often the first choice for manufacturing resistantmembranes for MBR application as well as durable UF filters by DIPS or TIPS processing. Theexcellent chemical resistance and hydrolytic stability combined with high strength make PVDF asuitable choice for membranes used in demanding end-use environments. Whenever exceptionalchemical resistance in harsh environment or highly hydrophobic materials is requested, it is possibleto select Halar ® ECTFE as raw material for manufacturing membranes by TIPS processing. Thismaterial may be especially suitable for filtration of highly aggressive media, distillation orpervaporation technologies. Besides, Solvay Specialty Polymers offers a family of Algoflon DFpowders for the manufacture of e-PTFE items through paste extrusion. Selection of the bestcandidate for evaluation is heavily dependent on the item that is going to be made, themanufacturing process, and service conditions. Relevant polymer properties and processingconditions will be presented.R&D resources of Solvay are constantly dedicated to provide innovative performing materials. A newlaboratory has been installed in Solvay Specialty Polymers headquarter in Bollate (Italy) for testingcommercial and experimental polymers. Manufacturing equipments for flat sheet and hollow fibermembranes and characterization capabilities will be illustrated together with innovativeexperimental grades.Open Innovation is an important part of Solvay strategy: research projects are active today withProfessor Lee at Hanyang University, with ITM-CNR in Italy and with Professor McCutcheon atConnecticut University.

Volume Fraction (φ)Volume Fraction (φ)Application of the UNIQUAC-HB Model in the Sorption Behavior ofEthanol/Water Mixtures into Polydimethylsiloxane Membrane at DifferentTemperatureAli Shokouhi 1 , Gholamreza Pazuki 1 *, Ahmadreza Raisi 1,2 , Mohammad Irani 11 Department of Chemical Engineering, Amirkabir University of Technology (TehranPolytechnic), Hafez Ave., P.O. Box 15875-4413, Tehran, Iran2 Food Process Engineering and Biotechnology Research Centre, Amirkabir University ofTechnology (Tehran Polytechnic), Hafez Ave., P.O. Box 15875-4413, Tehran, Iran*Author for correspondence, E-mail: ghpazuki@aut.ac.irPervaporation is a membrane process to separate a liquid mixture through partial evaporation acrossa nonporous membrane. The sorption and diffusion are two main steps during the transport ofpermeating components across the membrane. In this study, the classic UNIversalQUAsi Chemical(UNIQUAC) model is modified based on the hydrogen bonding concept accounting for the specificchemical effects. The modified UNIQUAC and UNIQUAC models are also employed to correlate thesorption behavior of ethanol/water mixtures into the polydimethylsiloxane (PDMS) membrane.According to the solution-diffusion mechanism, the thermodynamic equilibrium is assumed at theinterface between the feed mixture and the polymeric membrane. The activity of each permeatingcomponents is calculated using the UNIQUAC and UNIQUAC-HB models. Furthermore, the swellingexperiments were performed to determine the sorption levels of various ethanol/water mixturesinto the PDMS membrane at feed temperatures of 303, 318 and 333 K. The correlated ethanol andwater sorptions are compared with the experimental data. Fig. 1 indicates the effect of ethanol feedconcentration on the sorption behaviors of ethanol/water mixtures in the membrane at feedtemperature of 303 K. It can be inferred from this figure that the total and ethanol sorptions increaseas the ethanol concentration in the liquid mixtures increases. The correlated and experimentalresults also reveal the sorption levels of both permeate components enhances at higher feedtemperatures. Moreover, the UNIQUAC-HB model is found to be more accurate than the UNIQUACmodel to determine the volume fraction of the permeants in the PDMS membrane, because theUNIQUAC-HB model is able to predict the synergistic effect of ethanol on the solubility of water.(a)0,080,070,060,050,040,030,020,01UNIQUAC EtOH (T=30 ˚C)UNIQUAC Water (T=30 ˚C)UNIQUAC Total (T=30 ˚C)Experimental EtOH (T=30 ˚C)Experimental Water (T=30 ˚C)Experimental Total (T=30 ˚C)9E-170,0-0,010,1 0,2 0,3 0,4 0,5 0,6 0,7 0,8EtOH Concentration in Feed (%wt)0,000,0 0,2 0,4 0,6 0,8EtOH Concentration in Feed (%wt)Fig. 1: The effect of ethanol feed concentration on the sorption behaviors of ethanol/water mixturesin the PDMS membrane at feed temperature of 303 K: (a) the UNIQUAC model and (b) theUNIQUAQ-HB model.(b)0,080,070,060,050,040,030,020,01UNIQUAC-HB EtOH (T=30 ˚C)UNIQUAC-HB Water (T=30 ˚C)UNIQUAC-HB Total (T=30 ˚C)Experimental EtOH (T=30 ˚C)Experimental Water (T=30 ˚C)Experimental Total (T=30 ˚C)

Modification of Polyethersolfone Ultrafiltration Membrane by CoronaTreatment and Coating TiO 2 Nanoparticle on the SurfaceVahid Moghimifar 1 , Ahmadreza Raisi 1,2 *, Abdolreza Aroujalian 1,2 , Mohammad Irani 11 Department of Chemical Engineering, Amirkabir University of Technology (TehranPolytechnic), Hafez Ave., P.O. Box 15875-4413, Tehran, Iran2 Food Process Engineering and Biotechnology Research Centre, Amirkabir University ofTechnology (Tehran Polytechnic), Hafez Ave., P.O. Box 15875-4413, Tehran, Iran*Author for correspondence, E-mail: raisia@aut.ac.irIn membrane processes such as microfiltration, ultrafiltration and reverse osmosis, membranefouling and concentration polarization phenomena play important role in the flux decline andseparation performance. Various methods such as pretreatment of feed, optimization of operatingconditions, pulsatile flow, radiation and membrane modification were used to reduce the membranefouling. Surface treatment of the membrane is one of the methods employed to modify themembrane and increase the membrane hydrophilicity. The aim of this study is to reduce the foulingof polyethersulfone (PES) ultrafiltration membranes which used in separation of oil in wateremulsions via the surface modification of membrane by coating titanium oxide (TIO 2 ) nanoparticles.For this purpose, at first TiO 2 nanoparticles were synthesized by hydrothermal method usingmicrowave, then the PES UF membranes were fabricated by nonsolvent-induced phase inversionmethod and the membrane surface was modified by corona treatment, finally TiO 2 nanoparticleswere deposited on the membrane surface by a dip coating technique. The fabricated membraneswere used for treatment of a synthetic oily wastewater. The pure water flux and permeation flux ofthe oil/water mixture for the neat PES and TiO 2 coated membranes are shown in Fig. 1. It can be seenthat the pure water flux of the modified membrane was higher than the neat PES membranes. Thisimplies that the coating of TiO 2 nanoparticles on the membrane surface increases the hydrophilicityof the membrane and leads to higher water flux. Also, it was observed that the surface treatmentand modification of membrane by adding hydrophilic nanoparticles improved the permeation flux ofoil/water mixture and reduced the flux decline and membrane fouling.

Flux (kg/m 2 .hr) Flux (kg/m 2 .hr)302520(a)modified membraneneat membrane15105201500 10 20 30 40 50 60 70Time (min)(b)neat membranemodified membrane10500 20 40 60 80 100Time (min)Fig. 1: The pure water flux (a) and permeation flux of the oil/water mixture (b) for the neat PES andTiO 2 coated membranes.

Supported Ionic Liquid Membrane for CO 2 SeparationCinthia E. Sánchez 1* , Mirella Gutiérrez 1 , Sibele B. Pergher 2 Miguel Torres 11Laboratorio de Química Aplicada, Universidad Autónoma Metropolitana-Azcapotzalco,(México).2 Laboratório de Peneiras Moleculares, Universidad Federal do Rio Grande do Norte, Natal(Brasil).* sirerika86_@hotmail.comINTRODUCTIONLately, the supported ionic liquid membranes (SILMs) have gained significant attention for gasseparation [1-3], in the SILMs, the solute molecule dissolves into the membrane at thefeed/membrane interface, then it diffuses through the membrane and desorbs at the oppositemembrane surface. The applications of SILMs are attributable to the negligible vapor pressure andhigh stability of ionic liquids [4], a property that ensures no mass loss due to volatilization underthe conditions at elevated temperatures. Carbon dioxide exhibits relatively high solubility inseveral ionic liquids (ILs), leading to considerable attention focused on ILs based separationprocesses for carbon capture from flue gases generated in coal fired power plants. In this work,we report the facilitated transport of CO 2 through a supported ionic liquid membrane based onconventional ionic liquid (second generation) to separate CO 2 from gas mixture CO 2 / N 2 .METHODOLOGYPreparation of supported ionic liquid membrane (SILM)The supported ionic liquid membrane (SILM) was prepared using as ionic liquid 1-butyl-3-methylimidazolium tetrafluoroborate [bmim] [BF 4 ] which was synthesized and impregnated ontopores of α-alumina inorganic supports with 20nm of average pore diameter. Figure 1 presents thethickness and pore diameter dimensions of the commercial tubular membrane (tube of 15 cmlength, 0.7 cm ID, 1cm OD, glazed ends 2.5 cm) with an active layer of ᵧ-Al 2 O 3 in which the liquidionic is impregnated.Figure 1. Scheme of cross section ZrO 2 -Al 2 O 3 support, indicating thickness and average pore diameter of thevarious layers that comprise the support.

Characterization of ionic liquid and supported ionic liquid membrane (SILM)The ionic liquid 1-butyl-3-methylimidazolium tetrafluoroborate [bmim] [BF 4 ] was characterized byProton Nuclear Magnetic Resonance Spectroscopy (H-NMR). A scanning electron microscope(SEM) and an energy dispersive X-ray (EDX) analysis were used to study the membranemorphology, the overall chemical composition and the distribution of the chemical elements ofinterest in the supported liquid membranes.Single gas permeabilityThe single gas permeability was carried out at 24±1°C with pressure difference range from 0.5 to2.8 bar. In order to examine the reproducibility of the achieved permeability resulting fromincreased pressure, the CO 2 permeation was repeated three times. The permeability of the SILMwas expressed as Barrer (1 Barrer = 3.35 x 10 -10 mol/m 2 .s.Pa) [5]. The permeability of the CO 2 andN 2 was determined as follows:Where is the flow rate of permeation (cc/min), is the effective sectional area of the SILM(cm 2 ), and is the pressure trans-membrane (bar), while represents the thickness (cm) of theionic liquid.RESULTS AND DISCUSSIONSCharacterization of ionic liquid 1-butyl-3-methylimidazolium tetrafluoroborate [bmim] [BF 4 ]Figure 2 shows the spectra 1 H NMR spectrum of [bmim] which showed several signals. Threedeshielded ring protons were identified at δ 8.669 (A; singlet) and at δ 7.427 (C, D; twooverlapped doublets). The aromatic ring imidazolium produces great deshielded effects on theiradjacent protons, i.e., the external magnetic field induces a current in the aromatic ring which isopposed to the magnetic field, as result, the aromatic protons are deshielded and absorbed atlower values of applied magnetic field, hence most of the aromatic protons absorbed in the rangeof δ 7-8. The signal at δ 3.873 ((B; singlet) was assigned to protons of the methyl group attachedto the ring. The remaining signals were attributed to alkyl group protons, namely methylenegroups at δ 4.177 (E; triplet), at δ 1.834 (F; quintet), and δ 1.834 (F; quintet), and δ 1.304 (G;sextet), as well as the methyl group at δ 0.908 (H; triplet).

Figure 2. 1 NMR spectra of [bmim] [BF 4 ].Characterization of supported ionic liquid membrane (SILM)Figure 3a shows the cross section micrograph of the SILM [bmim] [BF 4 ], at 5000x magnification ofthe most superficial layer of the membrane (Fig. 3.4b) which corresponds to the mesoporous ZrO 2film and the EDX spectra of the SILM [bmim][BF 4 ] (Fig. 3.4c).Figure 3. a) Scanning electron micrographs of the SILM [bmim][BF 4 ], b) ZrO 2 -Al 2 O 2 membrane impregnatedwith [bmim][BF 4 ] (1000x) and c) EDX spectra of the SILM [bmim][BF 4 ].The EDX spectrum of the SILM [bmim] [BF 4 ] presented the characteristic peak assigned to fluor,the presence of this chemical element correspond to the chemical formulation of ionic liquid[bmim][BF 4 ]. The morphological study showed that the IL was homogeneously distributed in themesopores that corresponds to the ZrO 2 film.Studies of single gas permeabilityFigure 4 show the single CO 2 permeability relative to pressure, until 1.0 bar range of pressure, thepermeability was decreased from 73 933 to 41 314 barrer, after, the CO 2 permeability did notchange in response to increased pressure, i.e. the permeability remains constant, then itincreased slightly from 2 bar to 2.8 bar. This can be attributed to the fact that from 1 to 2 bar, thepartial pressure of CO 2 is sufficiently low; the concentration of CO 2 into the membrane is also low,resulting in a relatively smaller number of molecules of CO 2 with the ionic liquid being used forfacilitated transport.

Permeability [Barrer]7x10 46x10 45x10 44x10 43x10 42x10 40.5 1.0 1.5 2.0 2.5 3.0Pressure [bar]Figure 4. Permeability of CO 2 in the SILM [bmim] [BF 4 ] at 25°C as a function of transmembrane pressuredifferenceConsequently, the permeability through facilitated transport is the predominant stage. However,as the pressure of CO 2 increases, the concentration of complex CO 2 -IL used for facilitatedtransport also increases. When the complex CO 2 -IL into the membrane is saturated with CO 2 , thepermeability of CO 2 by facilitated transport does not increase with increased pressure.Regarding the values of CO 2 and N 2 permeability, are 6x10 4 and 3 x10 4 - barrer at roomtemperature, respectively (not shown). These results indicate that the carbon dioxidepermeability is higher than nitrogen. This can be attributed to the fact that the partial pressure ofCO 2 increases, the concentration of carriers used for facilitated transport dominated by solutiondiffusionmechanism, and the flux resulting bonding between CO 2 and ionic liquid also increase.CONCLUSIONThe permeability of CO 2 through the ionic liquid [bmim] [BF 4 ] in the SILM is higher than N 2 . Theseresults were favorably compared with results reported in the literature for gas separation in postcombustionsystem.REFERENCES[1] O. C. Vangeli., G. E. Romanos., K. G. Beltsios., D. Fokas., C. P., Athanasekou, N. K. Kanellopoulos (2010),Journal of Membrane Science., 365, 366-377.[2] M.A. Malik,., M.A. Hashim., F. Nabi (2011), Chemical Engineering Journal., 171, 242-254.[3] J.J. Close., K. Farmer., S.S. Moganty, R.E. Baltus (2012), Journal of Membrane Science., 390, 201-210.[4] P. Luis., L.A. Neves., C.A.M. Afonso., I.M. Coelhoso., J.G. Garea., A. Irabien (2009), Desalination., 245,485-493[5] D.D Iarikov., P. Hacarlioglu., S.T. Oyama, (2011).,Chemical Engineering Journal., 166, 401-406.

Polyimide Hollow Fiber Membranes which contribute to Energy CreationNozomu TANIHARA 1* , Nobuhiko FUKUDA 1 , Tomohide NAKAMURA 1 , and Tetsuo NAKAYASU 21 Specialty Products Development Center, Ube Industries, Ltd.,1978-10, Kogushi, Ube, Yamaguchi 755-8633, Japan.2 Specialty Materials & Products Business Unit, Ube Industries, Ltd.,Seavans North Buliding, 1-2-1, Shibaura, Minato-ku, Tokyo 105-8449, Japan.* Corresponding author’s email: 30492u@ube-ind.co.jp.Polyimide membranes applied to hydrogen recovery in the 1980s are still extending scope aboutgas separation and vapor permeation. Because, especially, polyimides from 3,3’,4,4’-biphenyltetracarboxylic dianhydride (BPDA) have excellent fiber-forming property with good thermal,chemical, and mechanical durability, they are prepared as asymmetric hollow fiber membranes andused. This presentation introduces about the polyimide hollow fiber membranes which contribute toenergy creation such as methane concentration, ethanol dehydration, humidification in fuel cell, etc.The methane concentration by membrane separation of carbon dioxide from biogas has attractedincreasing attention because of the energy creation from waste [1]. Table 1 shows an example ofmaterial balance about biogas upgrading by dual stages of polyimide hollow fiber membranemodules.In order to decrease energy consumption, it is necessary to use the modules having high selectivity.Operating pressure and energy consumption for a compressor in a system can be lowered by anincrease in the number of the modules.However, an initial cost becomes higher as the number of the modules becomes larger. Further,the excessive number of the modules causes large energy consumption because of recycling flowquantity from the modules for 2nd stage.It is important in system design to consider comprehensively the energy consumption, the initialcost, an operating cost, a methane loss, etc.[1] N. Tanihara and M. Hayashi (2010), Maku (Membrane), 35, 37-39.Table 1. Example of methane concentration about biogas upgrading.

Characteristic and Applications of Polyimide Hollow Fiber MembraneTetsuo NAKAYASU 1* , Nozomu TANIHARA 2 and Tomohide NAKAMURA 21 Specialty Materials & Products Business Unit, Ube Industries, Ltd.,Seavans North Buliding, 1-2-1, Shibaura, Minato-Ku, Tokyo 105-8449, Japan.2 Specialty Products Development Center, Ube Industries, Ltd.,1978-10, Kogushi , Ube, Yamaguchi 755-8633, Japan.* Corresponding author’s email: 27049u@ube-ind.co.jpMembrane technologies are being used for gas and vapor separation in many industries as energyefficientand cost-effective processes which contribute to conservation of working and livingenvironment. Most commercial membranes are made of polymer and polyimide-based polymer ismost excellent material for gas and vapor separation [1] [2].This paper introduces hollow fiber membranes made of polyimides from 3,3’,4,4’-biphenyltetracarboxylicdianhydride (BPDA) and other monomers demonstrate good performance for gas andvapor separation such as air separation generating nitrogen enriched gas, dehumidification,humidification, dehydration of organic vapor, separation for hydrogen, helium, carbon dioxide, andso on and their applications are promoting to expand as shown in figure 1 because BPDA-basedpolyimide has excellent thermal, chemical, and mechanical durability.Natural gas energy is known as a low environmental impact and recently its production amountand consumption are increasing, but one of major problems of natural gas production is how toremove CO 2 from natural gas, especially the durability of polymer membrane with high CO 2 contentin natural gas. The durability of polyimide hollow fiber membrane at high CO 2 partial pressure,3.2MPaG is shown in figure 2 and no degradation was observed for a long time. Another problem isdurability against heavy hydrocarbons and polyimide hollow fiber was also observed.Figure 1. Applications of Polyimide MembraneFigure 2. Durability of Polyimide Membrane[1] S. Sridhar, B. Smitha, and T.M. Aminabhavi, Sep. Purif. Rev., vol. 36(2), pp. 113-174, 2007.[2] Lloyd M. Robeson,Journal of Membrane Science, 320 (2008) 390-400.

Microfiltration and Ultrafiltration applied to Concentration of Pectinases Producedby Solid-State FermentationPatrícia Poletto*, Eloane Malvessi, Mára Zeni, Mauricio Moura da SilveiraUniversidade de Caxias do Sul, Caxias do Sul, RSppoletto@ucs.brIn this work, the steps to concentration of enzymatic extract produced in solid-statefermentation by Aspergillus niger LB23 were reported. The crude extract was obtained by extractionwith 1:10 solid:liquid (water pH 4.0) at 20°C for 60 min. In the sequence, the extract was treated with5 g/L of activated charcoal for 60 min. This treatment decolorized the crude extract in 72% (opticaldensity read at 630 nm) and reduced the protein concentration [1] in 23%.The charcoal-treated extract was then submitted to microfiltration (MF) to remove particlesbigger than 0.4 μm and to facilitate the next step that was the concentration by ultrafiltration (UF).The permeate flux presented a significant drop just after the beginning of the MF step. This behavioris probably due to the permeation resistance caused by membrane pore blocking [2]. The yield of MFstep was 94%, taking in account the pectinase activity that was determined by the reduction ofviscosity of a pectin solution.The permeate fraction obtained in MF was submitted to UF in a 10 kDa polyethersulfonespiral membrane (MILLIPORE). The total activity in concentrate stream (activity x volume) was lowerthan that measured in the feed stream. This loss can be owed to enzyme denaturation or retentionof the protein in membrane [3]. The results are summarized in Table 1.Table 1- Summary of purification of pectinase from Aspergillus niger produced by solid-state fermentationStepPectinaseSpecific Recovery FoldVolumeProteinFoldactivity(L)(U mL -1 (mg mL -1 activity yield concentration))(U mg -1 purification) (%) (enzyme activity)Crude extract 31.13 9.01 0.326 27.6 - - -ActivatedCharcoal30.7 9.17 0.281 32.6 100 1,01 1.18TreatmentMicrofiltration(0,4 µm)30.32 8.7 0.217 40.1 94.0 0.95 1.23Ultrafiltration(10 kDa)0.293 663 4.063 163.2 73.6 76.2 4.07Considering the total process, a final enzyme preparation 73.6-fold concentrated in relationto the original crude extract was obtained, with a total recovery yield of 69.2% and 5.91-foldpurification.[1] M.M. Bradford (1976), Anal. Biochem., 72, 248-254.[2] M. Cheryan (1998), Ultrafiltration and microfiltration: handbook. 2.ed. Boca Raton, E.U.A.[3] K.J. Hwang; P.Y. Sz (2011), Chem. Eng. J., 166, 669-677.

Remoção de Cor (%)Remoção de Turbidez (%)Purification of Protein Coagulant from Moringa oleifera Seed*Aline Takaoka Alves Baptista 1 ; Pedro Henrique Freitas Cardines 1 ; Carole Silveira 2 ; MarianaOliveira Silva 1 , Marcelo Fernandes Vieira 2 ; Rosângela Bergamasco 2 ; Angélica MarquetottiSalcedo Vieira 1 .1Programa de Pós-graduação em Ciência de Alimentos, Universidade Estadual de Maringá; 2Departamento de Engenharia Química, Universidade Estadual de Maringá.Av. Colombo, 5790. CEP: 87020900, Maringá, Paraná.Alinetakaoka_17@hotmail.comWater is an essential resource for life and to be within the standards of potability there is theneed for treatment with chemical coagulants. The Moringa oleifera can be a potential replacer forchemical coagulants because a protein with coagulant action, despite that, it must be elucidated ifthe isolated protein has the same coagulant potential of the aqueous extract. Therefore, this studyaimed to purify the protein found in the seeds of Moringa oleifera Lam by ultrafiltration andevaluates its power of coagulation compared to the aqueous extract unpurified.Moringa seeds were donated from Federal University of Aracaju-SE. The aqueous Moringa1% (w / v) [1] had a protein concentration of 689.2 mg / L according to Lowry et al. (1951) [2] and Itwas purified in tangential ultrafiltration module with hollow fiber membranes of polietersullfonawith 50 kDa, operating in 2 bar pressure. The coagulation assays were conducted in Jar test [1] usingwater of low turbidity to evaluate the removal of color and turbidity parameters [3], using ascoagulant different concentrations of aqueous Moringa before and after the UF process.After 50 min the UF permeate and concentrate flows presented 315mg of protein and 482,respectively, demonstrating that the proteins contained in the aqueous extract was permeatedthrough the membrane over time, and therefore, there is a need to evaluate other membranes withless molecular weight than 50 kDa. The percentages of color and turbidity removal are shown inFigure 1, to initial extract (initial MO), protein extract concentrated (MO concentrated) and proteinextract permeated (MO permeated) during the UF process.40353025605040203015105Mo inicialMO concentradoMO permeado2010Mo inicialMO concentradoMO permeado00 2 4 6 8 10 12 14 16Concentração de proteína (mg/L)00 2 4 6 8 10 12 14 16Concentração de proteína (mg/L)Figure 1. Percentage removal of color and turbidity using as coagulant different concentrations ofprotein coagulant.

Based on the presented results it can be seen that both of the solution of Moringa initial,permeate and the concentrate had higher percentages in removing turbidity and color at low proteinconcentrations, between 0.17 to 0.69 mg / L. A comparison between the two solutions of coagulationshows that the concentrate was more efficient, reaching 37% color removal with only 0.17 mg / L ofprotein. This is also reflected in low organic load added to the water to be treated. The same profilewas presented for turbidity removal. The concentrated solution was more efficient with reaching53% of removal, for the protein concentrations from 0.17 to 0.69 mg / L.Studies indicate that the use of coagulant protein in purified form is most efficient for thetreatment of water, because it uses less amount of coagulant, adding less organic load treated waterand achieving the best results for reducing color and turbidity in comparison with the coagulantunpurified. Additional studies are being conducted to confirm the results were obtained.Referências[1] G. S. Madrona; G. B. Serpelloni; A. M. S. Vieira; L. Nishi; K. C. Cardoso; R. Bergamasco (2010), Water Air SoilPollut (2010) 211:409–415.[2] O. H. Lowry; N. J. Rosebrough; A. L. Farr; R. J. Randall (1951), Journal of Biological Chemistry, 193, 265.[3] APHA - American Public Health Association.2005. Standard Methods for the Examination of Water andWastewater. 21 st , Centennial Edition, Washington.

Removal of Trihalometanes Precursors by Combined ProcessCoagulation/Flocculation/Membranes in water treatmentMilene Carvalho Bongiovani*, Franciele Pereira Camacho, Letícia Nishi, Karina CardosoValverde, Livia de Oliveira Ruiz Moreti, Driano Rezende, Carlos Henrique Furlan, AngélicaMarquetotti Salcedo Vieira, Rosângela Bergamasco. Corresponding author*milene.bongiovani@gmail.com.Universidade Estadual de Maringá, milene.bongiovani@gmail.com;franciele_camacho@hotmail.com; leticianishi@hotmail.com; karinacordeirocardoso@hotmail.com;li.moreti@hotmail.com; drirezend@hotmail.com; carloshenriquefurlan@gmail.com;angelicamsalcedo@hotmail.com; ro.bergamasco@hotmail.comThe chlorine used in the water disinfection step, has been responsible for forming byproducts in thepresence of organic substances in the water such as trihalomethanes (THM). For this reason severalstudies have been performed in order to find other treatment alternatives that cause less harm tohealth and minimize the formation of these compounds. Therefore, the objective of this study was toevaluate, on a laboratory scale, the efficiency of the combined process coagulation / flocculation +membrane filtration (MF and UF) + chlorination using natural coagulant Moringa oleifera Lam inreplacement to conventional treatment on the formation of THM. For the tests, it was used PirapóRiver Basin raw water, with low turbidity (50 NTU). To minimize the THM formation, optimization ofcoagulation/flocculation tests were initially performed in jar-test Nova Ética - Model 218 LDB withdosage of Moringa oleifera Lam (with oil extracted with hexane 1% m/v) ranged from 10 to 60 mg.L -1and of polyaluminum chloride (PAC) 1% with dosage ranged from 7 to 12 mg.L -1 . The conventionalfiltration consisted of rapid filtration descending of coagulated water in a dual layer filter (sand andanthracite), applying a flow rate of 240 L/m 2 *h for a period of 40 min. In membrane filtration step,microfiltration membrane modules of poly (imide) and ultrafiltration membrane modules of poly(ether sulfone) were used, these being in the form of hollow-fibers from engineering polymers,produced by the company PAM-Membrane Sectionals (COPPE-UFRJ, Rio de Janeiro-RJ/Brazil). Thedisinfection of filtered water was performed with sodium hypochlorite in a concentration of 1.5 mg.L -1 for contact times of 30 minutes to 8 hours. The parameters analyzed were color, turbidity, THMT,UV254nm, COD and free chlorine, and the detection of THM formed was performed by gaschromatography. Among the results obtained, the optimal dosage for PAC and Moringa coagulantswere 9,5 and 30 mg/L respectively. It could be seen that the membrane separation processminimized the formation of THM. For microfiltration and ultrafiltration process, before thechlorination it was not observed significative increase in THM formation (5 μg.L -1 ), however after thechlorination process, THM residual increased lower for Moringa (33 μg.L -1 ) than PAC (45 μg.L -1 ), beingaccording with legislation (100 μg.L -1 ). The coagulation/flocculation pre-treatment for bothcoagulants minimized the fouling formation in membranes process with average of 12%. Due to thefact that Moringa is a natural coagulant (produce less sluge, doesn’t alter the pH, etc) and reduceorganic matter and THM formation can be considered advantageous and a promising step towardsimproving the water coagulation/flocculation/micro and ultrafitration processes.

Future of Membranes for Greywater ReuseTaísa Machado de Oliveira*, Cláudia Telles Benatti**, Célia Regina Granhen Tavares*,Roberto Bentes de Carvalho***, Rafael Alberto Nishimura** Universidade Estadual de Maringá – UEM, ** Faculdade Ingá - Uningá, *** PAM MembranasSeletivastaisamachadooliveira@hotmail.comDomestic wastewater recycling is an attractive option due to a relatively high water consumptioncoupled with an intensive population [1]. Greywater is any type of domestic water that comes fromkitchen sinks, baths, washing machines and hand basins excluding black waters (toilets and urinals).The membrane separation process is a technology for treating such effluent. An important moderndevelopment in terms of filter media has been the microfiltration membrane, with an open structureenabling operation at relatively low transmembrane pressures. However, a relevant restriction to themembrane processes performance is the negative influence the permeate flow suffers from thetransient accumulation of a layer of rejected species in the membrane interface. Such phenomenonmakes the system less efficient and reduces the membrane commercial viability. Deposition andaccumulation of foulants such as particles and organics on the membrane surface not only causepermeate flux decline through time, but also deteriorate the permeate quality in many situations [2].According to such approach, this study aims at evaluating the applicability of the separation processof submerged membrane in greywater treatment for domestic reutilization. For such purpose, westudied a module of hollow fiber microfiltration membrane with pores of 0.4µm, effective surfacearea of 0.091m 2 and packing density of 500m 2 /m 3 .The greatest results regarding treated effluents quality and the decrease of permeate flow wereobtained through experiments at pressures lower than the critical pressure (0.15 bar) and aeration of50L/h. The physical cleanliness and the retro washing were both efficient to recover both thepermeate flow and the membrane hydraulic permeability. Both raw and treated effluentscharacteristics are demonstrated in Table 1.Table 1 – Greywater quality of influent and effluentinfluent effluent Efficiency (%)Colour, Pt/Co units 518 3 99.5Turbidity, FAU 71 2 97.9BOD 5, ppm 211 27 87.0COD, ppm 349.5 66.5 81.0Total Suspended Solids, ppm 30 0 >99.9thermotolerant coliforms, count/100mL 500 ND >99.9ND – not detectableThe results achieved reveal that the submerse microfiltration is presented as an efficient alternativeto treat greywater. The final effluent quality emphasized the possibility of secondary sewage

eutilization for domestic purposes. Such reutilization may lead to changes in hydric resources globalmanagement and a consequently a sustainable scenario.[1] JEFFERSON, B., LAINE A., PARSONS S., STEPHENSON T., JUDD, S.. Technologies for domestic wastewaterrecycling. Urban Water, 1, p.285-292. 1999.[2] HOEK, E.M.V., ELIMELECH, M., Cake-enhanced concentration polarization: a new fouling mechanism for saltrejectingmembranes, Environ. Science Technology. 37 p.5581–5588. 2003.

Electroflocculation and Reverse Osmosis in the Treatment of Oily WastewaterLeonardo Firmino da Silva, Patrícia Braz Ximango, Alexandre Andrade Cerqueira, MônicaRegina da Costa Marques, Fábio Merçon*.Instituto de Química, Universidade do Estado do Rio de Janeiro. * mercon@uerj.brThe uncontrolled discharge of wastewater into the environment over the last decades hasaccelerated the process of contamination and degradation of water bodies in the world. Thesewastes contain high amounts of contaminants and concentration of organic matter which leads tothe death of several species due to lack of oxygen and, in extreme cases, acceleration ofeutrophication processes.In the specific case of oily wastewater, the use of techniques such as chemical coagulation, dissolvedair injection, membranes, biochemical and electrochemical processes are described. However someof these processes have limitations which range from the concentration of the contaminant in theeffluent, limitations in the operating conditions and even cost constraints. Based in these facts, theaim of present work was the study of a hybrid system for treatment of oily wastewater. Thetreatment system was consisted of two stages: electroflocculation and reverse osmosis.Electroflocculation is a technique responsible for breaking stability of oil/water emulsions that’spossibility oil removal by flotation or sedimentation. Reverse osmosis provides the removal ofsoluble ions and dissolved oil.The oily wastewater consisted in a simulated dispersion prepared by adding specific lubricating oil inan aqueous solution with emulsifiers and supporting electrolyte. The electroflocculation system wasevaluated in relation to the use of iron and aluminum electrodes, in continuous and alternate modesand with electrical currents from 1 to 3 A. The results showed a higher apparent mass consumptionof electrodes when using direct current. Best removals were reached maximum 98% COD, 99,8%color removal and 99,8% turbidity removal for use alternating current and aluminum electrodeswhile were reached maximum 96% of COD, 99,5% color removal and also 99,8% to remove theturbidity with iron electrodes.In the second stage, it was used a reverse osmosis system with tangential flow in a fat-sheetmembrane module and plane module with a polyamide membrane (4040-X201-TSA produced byTrisep Corporation). Reverse osmosis provided removal of soluble components: 100% COD, 100%color, 100% turbidity, 99,1% conductivity, 99,5% aluminum ion and 98% salinity. Varying pressurefrom 10 to 30 bar, it was obtained an increase in permeate flow from 10,9 to 18,5 L.h -1 m -2 . Thecombination of electroflocculation and reverse osmosis was an effective technique for treating oilemulsions.

Comparative Analysis of electrodialysis Process Analytics as a Tool forReducing Energy Consumption of Brackish Water Desalination Process*Caio Cezar Neves Kunrath, Joao Thiago de Guimaraes Anchieta de Araujo Campos, EduardoBraga Costa, Franco Dani Rico Amado*.*Santa Cruz State University - UESC, caiokunratth@gmail.comThe need for alternative solutions on production of potable water becomes increasingly importantdue to, among other factors, water scarcity caused by climate change. Although water is the mostabundant element on Earth, only 3% of the total volume available is fresh water, and less than 1% isaccessible for human consumption [1]. In Brazil, access to clean water is a recurring problem,especially in areas affected by poor rainfall distribution. In the Northeast, the drought caused by lackof rain causes serious social and economic problems, making it necessary to develop methods for thetreatment of other sources. Among the currently methods used, desalination of water has beenhighlighted by the use of brackish water, this with little use on a commercial scale. By electrodialysismethod (ED), it is possible to remove salts and impurities from the water unfit for consumption,which in an electrochemical process, it uses selective membranes for separation of ions through anelectric potential [2,3,4] . However, the cost generated by the applied bias voltage shows theimportance to develop methods and research for reducing electricity consumption in the productionof potable water. Therefore, the study of methods for process optimization ED becomes necessary toreduce costs and consequently develop an optimized process for desalination accessible toconsumer.This paper analyzes the behavior of different concentrations of NaCl (sodium chloride) in ED under aconstant bias voltage. Three different concentrations (30 g/l, 25 g/l and 20g / l) of NaCl, under aconstant tension of 10 v were analyzed based on current variation, with a total duration of 8 hours(current records in 10 minutes interval). To analyze the behavior of the variation of the currentbetween selective membranes, the 0.42 A was used as the base point, named triple point. Theresulting graph shows that variation of current from the triple point is non-linear for all treeconcentrations, with a high current rate 20 g/l. At 30 g/l concentration, there is a low rate, differentefrom the two concentrations also studied. Thus, based on this study it is clear that the optimizationof the ED is a real solution for reducing energy consumption and thus ensure its viability for use insmall-scale production.

[1] SHIKLOMANOV, i. a. world water resources – a new appraisal and assessment for the 21 s t century . paris:united nations educational, scientific and cultural organization – unesco, 1998.[2]AMADO, F.D.R.; “Produção e Caracterização de Membranas Catiônicas para Eletrodiálise com PolímerosConvencionais e Polianilína Dopada com Diferentes Ácidos Orgânicos”, Dissertação de Mestrado. Programa dePós- Graduação em Engenharia de Minas, Metalurgia e dos Materiais. Porto Alegre – UFRGS, (2002).[3]KROL, J. J.; “Monopolar and Bipolar Ion Exchange Membranes”, Mass Transport Limitations, Ph.D., Universityof Twente, Germany, (1997).[4]MULDER, m., basic principles of membrane technology, kluwer academic publishers, enschede, thenetherlands, (1996) p. 1-557

Intensidade (u.a.)Preparation and characterization of MCM-22 type zeolite membraneAntonielly dos Santos Barbosa 1* , Antusia dos Santos Barbosa 1 , Meiry Gláucia FreireRodrigues 1 .Federal University of Campina Grande, Av. Aprígio Veloso 882, block CX, Campina Grande - PB, zipcode: 58429-970, contact: 55 83 2101-1488, Brazil. *antoniellybarbosa@yahoo.com.brMembrane technology is attractive from the point of view of both energy cost and separationselectivity and efficiency [1]. In particular, inorganic membranes such as those fabricated from zeolitematerials are especially fascinating because of their high thermal, mechanical, and chemical stability[2]. The secondary (seeded) growth method allows, among other advantages, the reduction of theinfluence of the support over the permeation properties of the resulting zeolite membrane [2].MCM-22 membrane was prepared on a porous α-alumina disk using a secondary growth techniqueconsisting of the deposition of seed crystals on a substrate followed by crystal growth underhydrothermal conditions. The membrane was measured by X-ray diffraction (XRD) and scanningelectron microscopy (SEM). As a result of these measures, X-ray diffraction (XRD) patterns (Figure 1)showed that MCM-22 membrane was the only zeolite material present in the membrane [3] andalumine. Morphologies of the MCM-22 membrane synthesized were illustrated by SEM images, asshown in Figure 2. Scanning electron microscopy (SEM) examination of the MCM-22 membranerevealed that the membrane has a rose like morphology with agglomerated by thin crystal sheets,which is quite similar to that previously reported [5].12001100MCM-22/-alumina100090080070060050040030020010005 10 15 20 25 30 35 40 45 502Figure 1. XRD patterns of the MCM-22membrane.Figura 2. SEM micrographs of the MCM-22membrane.High-quality MCM-22 zeolite membrane was successfully synthesized on long porous α-Al 2 O 3 disk bysecondary growth technique.Reference[1] J. Caro; M. Noack (2008), Microporous and Mesoporous Materials, 115, 215–233[2] A. Ayral, A. Julbe, V. Rouessac, S roualds, J. Durand (2008), Membrane Science and Technogy 13, 33-79.[3] A. S. Barbosa (2009), Dissertação de Mestrado. Universidade Federal de Campina Grande.[4] A. S. Barbosa, E. R. F. dos Santos, R. C. N. Leite, M. G. F. Rodrigues (2012), Revista Eletrônica de Materiais eProcessos, 7.3, 180–184.[5]Y. Wu; X. Ren; Y. Lu; J. Wang, Materials Letters, (2008), 62, 317–319.

Intensidade (u.a.)Intensidade (u.a.)(0 1 2)(1 0 4)(1 1 0)(1 1 3)Intensidade (u.a.)X-type zeolite membranes: preparation and characterizationAntusia dos Santos Barbosa 1* , Antonielly dos Santos Barbosa 1 , Meiry Gláucia FreireRodrigues 11 Development Laboratory of New Materials, Federal University of Campina Grande, Centerfor Science and Technology, Academic Unit of Chemical Engineering, Av. Aprígio Veloso 882,Block CX, Campina Grande - PB, CEP: 58429-970, Contact: 55 83 2101-1488, Brasil.*antusiasb@hotmail.comZeolites are microporous inorganic crystals that have a high surface area to volume ratio. They showgood mechanical strength, thermal stability and resistance to chemical corrosion (Breck, 1979). In thelast decade, zeolite membranes have attracted exhaustive research efforts due to their potentialapplications (Caro, 2008) and can be used for separation membrane, catalytic membrane reactor,chemical sensor (Caro, 2010). In the review entitled ‘‘Zeolite membranes – state of theirdevelopment and perspective” (Caro 2000) has been reported numerous zeolite membranepreparations and substantial progress can be stated. X-type zeolite membrane was prepared by asecondary (seeded) growth method on porous disk support (α-alumina). The X-type zeolitemembrane, porous disk support (α-alumina) and X-type zeolite were measured by X-ray diffraction(XRD). The XRD pattern of powder collected from the X-type zeolite is shown in Fig. 1. All peaksmatch those reported by Breck [1] for X-type zeolite crystals with respect to the positions andintensities of the verified reflections, and no additional peaks were observed. Fig. 2 shows the XRDpatterns of porous support. The XRD patterns of all six samples are nearly the same, so we suppliedonly one of them. After it was calcined up to 1200 C, γ-alumina was completely transformed tocrystalline α-alumina. No other Al 2 O 3 phase characteristic peaks were detected. The XRD pattern ofthe crystals rubbed the surface of X-type zeolite membrane (Fig. 3) demonstrated the presence ofboth zeolite X and Al 2 O 3 phases. The high intensity of the XRD lines and low background intensityindicate a high degree of crystallinity.24001200Zeolita X2000-alumina1000o X* - alumina*10001600800*8006006001200*400800400o*200400200o ooo o05 10 15 20 25 30 35 402Figure 1. X-ray diffractionpattern of zeolite NaX.010 20 30 40 502Figure 2. Diffractogram of theceramic support (α-alumina).00 10 20 30 40 502Figure 3. X-ray diffractionpatterns of zeolite membraneX/α-alumina.X-type zeolite membrane of high quality was synthesized on on porous disk support (α-Al2O3) usinga seeding technique (secondary growth method).Referências[1]. D.W. Breck, Zeolite Molecular Sieves, Wiley, New York, 1974.[2] Juergen Caro, Manfred Noack, Zeolite membranes – Recent developments and progress, Microporous andMesoporous Materials 115 (2008) 215–233.[3] Juergen Caro, Manfred Noack , Chapter 1 - Zeolite Membranes – Status and Prospective Advances inNanoporous Materials, Volume 1, 2010, Pages 1-96.[4] J. Caro , M. Noack, P. Kolsch, R. Schafer. Microporous and Mesoporous Materials 38 (2000) 3 – 24.

THE PERFORMANCE OF A SYSTEM OF WATER TREATMENT WITH MEMBRANES OFMICROFILTRATION (MF) AND NANOFILTRATION (NF), IN ORDER TO ACCESS THEIRDESALINATION POTENTIAL AND TO COMPARE THEIR PERMEATED QUALITY WITHTHAT OF THE REVERSE OSMOSIS SYSTEMFrancisco Rubens Macedo de Queiroz 1 , Emylle Laisa Santos Souza 1 ,Kepler Borges França 1(1)Universidade Federal de Campina Grande, Campina Grande, Brasil.franciscorubensmacedo@yahoo.com.br,emylle.souza@hotmail.com,kepler@labdes.ufcg.edu.brABSTRACTThe objective of this work is studying the performance of a system of water treatment withmembranes of microfiltration (MF) and nanofiltration (NF), in order to access theirdesalination potential and to compare their permeated quality with that of the reverseosmosis system. The system will contain two elements of membranes, one of those is a DowChemical Company – Filmtec model NF90 – 4040 with an area of 7,6 m 2 , and the other iscomposed of a PAM microfiltration membrane made of hollow fibers with measures ofdiameter 0,95 mm and area of 14 m 2 , whose capacity of production are of 500 L/h and 250L/h, respectively. As an instance of comparison with the reverse osmosis system, a brackishwater well was chosen, with a 2479.7 mg/L of TDS, has been being desalinized by a reverseosmosis system located at the Village of Uruçu of the São João do Cariri at Paraiba state, in theNortheast of Brazil. The salt concentration profiles of the microfiltration – nanofiltration andreverse osmosis system (MF-NF/RO), were done through physico-chemical analysis reaching anaverage rejection ratio for ions monovalent was 6,0% and for ions divalent was 20,7%.

Performance of flat UHMWPE membranes modified NaClJosé Stênio Sousa da Silva*, Addhyel Lopes Pontes Junior, Romulo Charles Nascimento Leite,Laura Hecker de Carvalho.Federal University of Campina Grande, Department of Materials Engineering, Academic Unitof Materials Engineering, steniosousa10@gmail.com *In industrial processes, such as production and petroleum refining, large volumes of oil are droppedinto water bodies, causing irreversible damages on local flora and fauna. Oil removal from theseeffluents is very important, since pollution caused by industrial wastes tend to increase withindustrialization. Membrane separation processes is one of the most popular forms of effluenttreatment. The pursuit of processes which are efficient, simple to operate and low in cost, hasmagnified the interest in the study and use of polymeric membranes. Among these membranes,those prepared from sintered high molecular weight polyethylene (UHMWPE) have found variousapplications. The use of these membranes to reduce pollution in various industries becomes viablewhen membrane pore size and porosity are suitable for separation process adopted. The presentstudy aims to verify the effect of adding a pore forming material (sodium chloride) on the porosityand selectivity of sintered UHMWPE membranes. The effects of particle size and NaCl concentrationon permeate flow and ability of theses membranes to selectively remove the oil phase present inoil/water emulsions with low oil contents was evaluated. A previous study has shown that saltaddition promoted higher sintering of UHMWPE and a reduction in permeate flow. In this work anew synthetic route and higher granulometric selected salt concentrations are investigated. Theeffects of this new route on water permeate flux were carried out and it was found a reduction inwater flow through the membranes with increasing levels of salt. This can be attributed to areduction in the average pore diameter of the membranes and, therefore, should increase theirselectivity in oil separation from water/oil emulsions. Characterizations in progress, such as flux andselectivity of separation of emulsions water/oil, mercury porosimetry, OM and SEM, shall confirm theefficiency of the method being studied.

Evaluating the Quality of treated wastewater for reuse by Ceramic MembraneMicrofiltration with Tangential FlowJulyanna Damasceno Pessoa*; Cristiane Rodrigues Macedo; Taline Sonaly Sales dos Santos;Kepler Borges França.Universidade Federal de Campina Grande/LABDES, julyanna_pessoa18@yahoo.com.br; UniversidadeFederal de Campina Grande/ LABDES; Universidade Federal de Campina Grande/ LABDES.Resume - Water is a form of energy essential to life and the maintenance of ecosystems. Due to the growingconcern with specific microorganisms, the use of membrane separation process becomes the treatment ofchoice for the production of drinking water. The filtration unit comprises a pilot reactor with a capacity of 10liters and a ceramic membrane, and monotubular 1 channel pore diameter of 0.20 micrometers. This studyaimed to extend the technology filtration membranes for water of inferior quality, evaluating the mainparameters of drinking water before and after treatment filtration with ceramic membrane microfiltrationstuffed by ion exchange resins. We tested four pressures from 1 to 3 bar. The system will be evaluated as afunction of permeate flow, turbidity, bacteria extract, color (actual and apparent), total coliform, totalsuspended solids and total dissolved solids of which. The results obtained showed that the crossflowmicrofiltration, presents itself as an effective alternative for the final treatment of sewage. The quality of thefinal effluent makes it possible to reuse this type of wastewater, be it in the agricultural, industrial or in themiddle.Keywords: ceramic membrane, water treatment, ion exchange resinIntroductionWater is a form of energy essential to life and the maintenance of ecosystems. Due to the growingconcern with specific microorganisms, the use of membrane separation process becomes the treatment ofchoice for the production of drinking water.The microfiltration process is a technique that has gained importance in the field of wastewatertreatment as with industrial development, population growth and land use in an intense and disorderly havecaused the impairment of available water resources for human consumption, increasing the risk of waterbornediseases in the transport of pathogenic microorganisms by the waters that spreads infectious processes inpopulations, especially when systems of water supply and sewage treatment are precarious. The systemssanitary sewage treatment generally results in good level of reduction of the organic load. However, onlyadvanced treatments lead to a significant reduction in sputum, and removal of contaminants allowing for reusepurposes nobler (STEPHEENSON, 2000; FANE et al. 2000). One of the main objectives of using the technique ofmembranes is the separation of substances of different properties (size, shape, diffusivity, among others). Theproduction of water which meets the standard for drinking water requires filtration, since only in this step is

that colloidal particles are removed, and suspended microorganisms in general, so that the final disinfection iseffective (Spinelli, 2001). Process uses membranes with surface water of good quality, now the goal is toextend to lower water quality for the removal of color, flavor, dissolved organic matter and disinfectionproducts (GUIGUI et al., 2002). According Lemanski (2004), the cross-flow filtration feed solution flows parallelto the membrane and the permeate flow, which permits the flow of large volumes of fluids, such as flow, athigh speeds, has the effect of dragging ae solids tend to accumulate on the membrane surface.This study aimed to evaluate the technology for water filtration membranes with lower quality,evaluating the main parameters of drinking water of an effluent before and after treatment filtration withceramic membrane microfiltration.ExperimentalThe membrane used was a ceramic composite plastic clay and alumina (Al2O3) tubular in shape, withsingle channel filtering area of 0.005 m2 and average porosity 0.2 micrometers. The tangential filtrationmembrane can be represented in Figure 1.Figure 1. Tangential filtration membraneCharacterization of MembranesAssays were performed to characterize the membrane under a pressure of 1, 2 and 3 bar. The feedtank was fed with deionized water for this filtration process, collecting the permeate in plastic cups with theirintervals at pre-determined. The temperature of the feed tank was monitored and maintained at (27 ± 1) ° C.The permeate samples were collected every five minutes in a period of two hours to a good determination ofthe permeate flow curve as a function of time. Between each membrane filtration process was changed.The raw water will be collected at the point of capture, Federal University of Campina Grande. Thecollected water will not receive any pretreatment. The same procedure will be done in testing of raw waterfiltration. Will be done color analysis (real and apparent), turbidity, total suspended solids and total dissolvedsolids were performed according to procedure recommended by Standard Methods (APHA, 1995).

To determine the permeate flux used to Equation 1:fPermeadom . tA.27 Cm(1)WherefPermeado is the permeate flow, m is the mass of water collected, is the density of27 Cwater at 27 ° C, Δt is the time interval in which the mass of water was collected andAm the membrane filterarea.Results and DiscussionInitial analyzes were performed with deionised water at pressures between 1 and 3 bar under thetemperature (27 ± 1) ° C. Figures 2 to 4 show curves characterizing the ceramic membrane with the permeateflux over time. The Figure 2 represents the curves characterization of membrane and permeate flow testing ofraw water in filtration operation pressure of 1 bar.Figure 2. Behavior of Permeate Flow for Time Trial Filtration at 1 barThe Figure 3 shows curves characterization of membrane and permeate flow testing of raw water infiltration operation pressure of 2 bar.

Figure 3. Behavior of Permeate Flow for Time Trial Filtration to 2 barThe Figure 4 represents curves characterization of membrane and permeate flow testing of raw waterin filtration operation pressure of 3 bar.Figure 4. Behavior of Permeate Flow for Time Trial Filtration to 3 bar

ConclusionsAt the present time, based on the results, the initial batch made with deionized water at all filtrationtests conducted for pressures between 1 and 3 bar, it can be seen that the proposed water treatment wasadequate. The treatment proved satisfactorily, being of economic interest and quality. In terms of flowfiltration test at 1 bar showed advantage over the filtration test on 2 and 3 bar, because fouling was smaller forthe former. The following procedure will be the characterization of wastewater to assess their quality afterfiltration by ceramic membrane microfiltration in order to obtain water fit for human consumption.References[1] APHA- AMERICAN PUBLIC HEALTH ASSOCIATION, 1995, Standard Methods for the Examination for Waterand Wastewater. 19th ed., Washington[2] GUIGUI, C., ROUCH, J.C., DURAND-BOURLIER, L., BONNELYE, V., APTEL, P., 2002, Impact of CoagulationConditions on the in-line Coagulation/UF Process for Drinking Water Production. Els. Sc. – Desalination, 147: 95- 100.[3] LEMANSKI, S.R., 2004, “Purificação e Concentração do Extrato Aquoso de Stévia Rebaudiana Bertoni Atravésdos Processos com Zeólitas e Membranas”. Tese de Doutorado. Departamento de Engenharia Química/UEM,Maringá, PR, Brasil.[4] SPINELLI, V. A. , 2001. Quitosana: polieletrólito natural para o tratamento de água potável. Dissertação(Mestrado em Engenharia Química), Universidade Federal de Santa Catarina – UFSC, Florianópolis, SantaCatarina.[5] STEPHEENSON, T. et all. Membrane Bioreactors for wastewater treatment. Publishing IWA, London, 179 p,2000.

Wastewater Treatment by Polyamide/Clay NanocompositesMembranesKeila Machado de Medeiros 1* ,Caio Henrique do Ó Pereira 1 , Luana Rodrigues Kojuch 1 , PaulaSimone Soares de Medeiros 1 , Edcleide Maria Araújo 1 , Hélio de Lucena Lira 11 Federal University of Campina Grande – UFCG- Department of Materials Engineering, AvenueAprígio Veloso, 882, Campina Grande – PB, Brazil, *keilamm@ig.com.brIn recent years, considerable attention has been given to the discharge of oily waste and its impacton the environment. Water pollution by oil is especially harmful to aquatic life, because it reduceslight penetration and disrupts the mechanism of oxygen transfer [1]. Consequently, the removal ofoil from wastewater is an important aspect in the control of pollution from various industries,especially the oil industry [2].The membrane separation processes (MSP) are relatively simple and easy to be operated, areenergetically economic, produce an effluent of good quality, facilitating their reuse in themanufacturing process [3-4]. These processes are presented as an alternative for the treatment ofoily wastewater, such as stable emulsions [5].This paper presents the development of microporous membranes of polyamide/clay nanocompositewith treated (organophilic) and untreated clay. The membranes in the form of thin films wereprepared by phase inversion technique, from the nanocomposites obtained by solution. These werecharacterized by scanning electron microscopy (SEM) and flow measurements. By SEM it wasobserved that the addition of small percentages of clay in the polymeric matrix provided a lowerthickness skin filter, directly influencing the flow measurements of these nanocompositemembranes. The water-oil separation tests in the concentrations of 100 and 300 ppm for polyamidemembranes with untreated clay (AST) showed a significant reduction in the concentration of oil inthe permeate, confirming the potential of these membranes to be applied for the treatment of oilywastewater from oil industry.Keywords: Membranes, Polyamide, Clay, Water-Oil Emulsions.[1] B. Braga, I. Hespanhol, J. G. L. Conejo, M. T. L. Barros, M. V. Vera, M. F. A. Porto, M. L. R. Nucci, N. M. A.Juliano, S. Eiger, Introdução à Engenharia Ambiental, 2ª edição, ed. Prentice Hall, São Paulo, 2005.[2] Conama, Resolução n° 430, de 13 de maio de 2011 que dispõe sobre as condições e padrões de lançamentode efluentes de óleos e graxas de origem mineral, proveniente do petróleo. Publicada no DOU n° 92, em16/05/2011, p. 89, 2011.[3] A. C. Habert, C. P. Borges, R. Nóbrega, Processo de Separação com Membranas. 1a ed. Rio de Janeiro. E-papers Serviços Editoriais Ltda. 2006.[4] P. Anadão, Ciência e Tecnologia de Membranas. Artliber Editora Ltda. São Paulo, 2010.[5] A. Hong, A. G. Fane, R. Burford (2003), Journal of Membrane Science, 222, p.19-39.

Analysis of Polymer Membranes Obtained From NanocompositesLuana Rodrigues Kojuch 1 *, Rodholfo da Silva Barbosa Ferreira 1 , Keila Machado de Medeiros 1 ,Edcleide Maria Araújo 1 , Hélio de Lucena Lira 1 .1 Federal University of Campina Grande (UFCG), 882, Aprígio Veloso Avenue, , Bodocongó , CampinaGrande/PB, *luanakojuch@yahoo.com.brResearches related with membrane separation processes has been increased considerable inrecent years and many ideas have emerged for their potential application [1]. The main reasons forthe advance in membrane technology are related to the fact that works without addition of chemicalagents, use of low consumption of energy, easy to process and compact design [2].Polymeric membranes has been developed and commercialized for a variety of industrialapplications such as microfiltration and ultrafiltration, often manufactured by the immersionprecipitation process. The morphology of the polyamide membranes prepared from inversion phasecan be controlled by precipitation in a soft coagulation bath [3].Nanocomposites are a new polymers materials category that contains relatively smallamounts of nanoparticles and are known by conferring material with combined characteristics, withthe aim to improve thermal, optical, and mechanical properties. Nanocomposites developed withsilicates in layers represent an alternative to the composites developed with conventional filler,because they use minimum amount of nanofiller [4-6].In this research, it was used bentonite clay from the state of Paraíba (Brazil), due to theoccurrence of great reserves, and to contribute to the economic and scientific development of thisregion. The use of nanocomposites membranes has attracted significant interest, because they canbe easily obtained through the addition of small amount of filler to a polymer matrix. In this work,microporous membranes were produced by immersion-precipitation technique with distilled water.This process is constituted by 3 main stages: preparation of a homogeneous polymeric solution,spreading the solution on a glass surface forming a film with a defined thickness e, finally, formationof the polymeric structure of the membrane by the separation of phases of the system [7]. Byscanning electron microscopy (SEM), it was observed that the membranes obtained by precipitationin a bath with water + acid showed a higher cell and better defined contour morphology whencompared to the membranes obtained by precipitation only with water.[1] A. J. BURGGRAAF; L. COT. Fundamentals of Inorganic Membranes, Science and Technology. Elsevier Scienceand Technology Series 4, Elsevier. Amsterdam, 1996.[2] W.B. Braga Junior. Tese de Doutorado/COPPE, Universidade Federal do Rio de Janeiro, 2011.[3] M. ZENI; R. RIVEROS; J. F. SOUZA; K. MELLO; C. MEIRELES; G. R. FILHO. Desalination. v. 221, p. 294-297,2008.[4] R. BARBOSA. Tese de Doutorado do Programa de Pós-Graduação em Engenharia de Processos, UniversidadeFederal de Campina Grande-PB, 2009.[5] L. F. BOESEL. Dissertação de Mestrado em Ciência e Engenharia de Materiais, UFSCar, São Carlos-SP, 2001[6] R. A. PAZ. Dissertação de Mestrado em Engenharia de Materiais - Universidade Federal de Campina Grande– UFCG, Campina Grande, 2008.[7] A. C. HABERT; C. P. BORGES, R. NÓBREGA. Processos de separação por membranas. Rio de Janeiro. E-papers, 2006.

Effect of internal surface modification on the performance of sintered UHMWPEmembranes for water/oil emulsion separationNilman Demetrius da Silva Gomes*, Addhyel Lopes Pontes Junior, Romulo CharlesNascimento Leite, Laura Hecker de Carvalho.Federal University of Campina Grande, Department of Materials Engineering, Academic Unitof Materials Engineering, nilmands@gmail.com *Stricter government regulations relating to the environment, including water resources, have led toincreased concerns for wastewater treatment. The pollution caused by oil contaminated fluids,harms the flora and fauna present in water bodies and industries which generate these dejects arefacing severe fines, which has fostered studies on ways to minimize and/or eliminate these impacts.Membrane (ceramic, metallic or polymer) separation processes have been able to meet thesecriteria. The effectiveness of membrane separation is related, among other factors, to the averagepore size and pore size distribution of the membrane after sintering. There are several studies whichaim to increase membrane selectivity through forms of modification. In the present work, a sinteredultra-high molecular weight polyethylene (UHMWPE) microporous membrane which allows partialseparation of the oil present in water/oil emulsions was developed. In an attempt to render thesemembranes more selective, their inner surface was coated with films of LDPE or LDPE/organoclay(Low density polyethylene and organophilic clay). The modifying films were obtained by dissolvingLDPE or a mixture LDPE/clay (produced by hot melting in an internal mixer) in toluene and thesolution used to coat the inner surface of the sintered UHMWPE membranes. The selectivity of themembranes were determined by analysis of permeate flux of water and of an oil/water emulsionwith oil concentrations below 100 mg/L. Partial results show that coating with LDPE film increasesthe selectivity of membranes. Studies on the performance of the coating LDPE-clay is underway. Themembranes produced are being characterized by XRD, SEM, DSC and TGA.

Performance and selectivity of LLDPE membranes modified with bentonite clay inwater/oil separationRaquel Araújo Nunes*, José Stênio Sousa da Silva, Eduardo de Mello Silva, Romulo CharlesNascimento Leite, Laura Hecker de Carvalho.Federal University of Campina Grande, Department of Materials Engineering, Academic Unitof Materials Engineering, raaquelnunes@hotmail.com *Minimization of environmental impacts caused by various production processes has been a constantconcern of humanity. Considerable attention has been paid to the environmental impact of dejectsfrom oil contaminated waters. Removal of the supernatant derived from large oil spills is relativelyeasy. However, the removal of small amounts of emulsified oil in water bodies is rather difficult, andconstitutes an important aspect in the control of environmental pollution caused by variousindustries. The use of membrane separation processess for these applications has been shown to bea promising cost-effective technique which presents a number of advantages over the classicprocesses for the separation of stable emulsions of oil in water. The development of processes forefficiently separating low amounts of oil from water emulsions which are fast and low in cost havebeen focused on the use of polymeric membranes. This work aims at the development, withdomestic technology, of low-cost membranes, able to guarantee the treatment of these emulsions.Films of linear low density polyethylene (LLDPE)/clay were prepared by flat die extrusion. Bentoniteclays in their pristine, purified and organophilic forms were incorporated (1% w/w) into LLDPEmatrix, resulting in a microcomposite. The membranes(films) manufactured were tested with respectto water permeate flux and selectivity in the separation the oily phase from water/oil emulsions. Ourresults indicated that it was possible to manufacture LLDPE based polymer membranes with distinctpermeations and selectivities by flat die extrusion.

Preparation of Y Zeolite for Synthesis of Zeolite MembraneAna Paula Araújo 1 *, Meiry Glaúcia Freire Rodrigues 2 André Luiz Fiquene de Brito 21 Estadual University of Paraíba/Federal University of Campina Grande 2,1* annpawla@yahoo.com.brAbstractThe synthesis of zeolite membranes can be classified into two categories: direct (in situ) andindirect (secondary growth). The template is used to direct the synthesis to a particular structure. Asan alternative to this, the addition of seed can be an effective route to direct the synthesis of aparticular structure, lowering the induction time for the formation of the desired structure, reducingthe cost of production of the membrane and subsequent treatment (calcination) for removing thetemplate [1,2]. The hydrothermal treatment time of Y zeolite was optimized for the purpose ofemploying it as a seed in the making of a zeolite membrane. So syntheses were carried out withdifferent times of hydrothermal treatment to obtain only the desired phase. Y zeolite membrane wasprepared by a secondary (seeded) growth method on porous disk support (α-alumina). The gel of Yzeolite was transferred into the polyethylene container to hydrothermal treatment. Crystallizationwas carried out at about 100° C for 24, 48 and 72 hours. An analogous procedure was used for Yzeolite membrane for 24 hours. Y zeolite (24, 48 and 72 h) and Y zeolite membrane, porous disksupport (α-alumina) were measured by X-ray diffraction (XRD). The effect of hydrothermal treatmenttime on crystallization was investigated. The Figure 1 show the x-ray diffraction patterns of Y zeolitesynthesized (24, 48 and 72 h). When the hydrothermal treatment time was changed from 72 to 48hours there was reduction in the intensity of all the peaks on the P zeolite and an increase in theintensity of the peaks of Y zeolite which, for example, the Miller indices (1 1 1), (2 2 0) and (3 1 1) forthe first three peaks of Y phase have intensities 680, 268 and 246 in the treatment of 72 h and beganto exhibit intensities of 1299, 368 and 305 respectively in the treatment of 48 hours. When thehydrothermal treatment time changed to 24 hours did not observe the presence of undesired phase(zeolite P), as reported by authors [3]. The XRD of Y zeolite membrane is presented in Figure 2, whereit is observed the presence of crystalline phases of Y zeolite and α-alumina showing a zeolite layerwas formed on the porous support. According to Chiang and Chao, 2001 once the support seeded gelis immersed in a reactive its pores are filled with liquid, then zeolite nucleation and deposition occuron both surfaces and within the pores. The results showed that the hydrothermal treatment time isimportant in synthesis of Y zeolite. It was possible to obtain the Y zeolite and eliminate the presenceof undesired phase with time of 24 hours. According to XRD result, Y zeolite membrane wassynthesized on porous support using a seeding technique (secondary growth method).

IntensityIntensityFigure 1. Effect of hydrothermal treatment time on the x-ray diffraction patterns of Y zeolitesynthesized.2000YTreatment - 24 hours15001000500YYYYYYYYY YY1500YTreatment- 48 hours1000Y50015001000500YY YYY YYYPP Y Y PP YY YPTreatment - 72 hoursP PPYPP YYY Y YYYY Y Y00 10 20 30 40 50Figure 2. X-ray diffraction pattern of Y zeolite membrane made from the use of seeds.2500Y zeolite membrane40030020010000 10 20 30 40 502References[1] D. Urbano; F. Vicente; C. Avelino (2006), Micro. Meso. Mater., 90, 73–80.[2] Z. Huo, X.; Xu, Z. J. Song; M. He; Z. Li; Q. Wangc; L. Yan (2012), Micro. Meso. Mater. 158, 137–140.[3] M. M. Htay, M. Mya (2008), Worl. Acad. Sci., Eng. Tech., 24, 114-120.[4] A. S. T. CHIANG; K. CHAO (2001), Phis. Chem. Sol., 62,1899-1910.

Evaluation of a Resin-Membrane System for the Production of LowConductivity Water.José Theódulo Fernandes Neto*Kepler Borges França***MSc in Chemical Engineering from the Federal University of Campina Grande.fernandoquimico@hotmail.com.br**Dr in Chemical Engineering from the Federal University of Paraiba. Kepler123@gmail.comABSTRACT: With the growing of good quality water, not only for human consumption, but also forsome industrial applications, several purification technologies on water has been implementedsuccessfully, such as desalination through reverse osmosis membranes, electrodialysis, thermalprocesses, ion exchange resins and others. The system aims the production of pure water, whit lowelectrical conductivity, which may be a research source for study and producing waters for hospitaland pharmaceuticals purposes. It is our understanding that these types of waters are very guardedby ANVISA and other federal agencies and their physico-chemical and biological properties aresubject to change by the treatments to assess the quality of the product and the proper functioningof the system. From the parameters of pH and electrical conductivity, we observed a considerabledecrease after regeneration of ion exchange resins within 30 to 80 minutes of operation. The pHvaried from 6.2 to 4.2 and after 40 minutes the electrical conductivity became constant, reaching 0.8μS.cm -1 , indicating the regeneration. It can be observed in the present study a low salt rejection in aresin column, to a pressure of 8.2 kgf.cm -2 , reaching a maximum of 30% indicating a little efficiency ofthe reverse osmosis desalinization systems, unlike the other studied pressures (2.2 and 6.2 kgf.cm -2 ),where a rejection rate of 90% for most ions was observed.Keywords: reverse osmosis membrane, ion exchange resin, electrical conductivity.

Sol-gel Processing of Titania Membranes: Correlation Between SynthesisConditions, Pore structure and Permeability Performance.1 Lecino Caldeira*, 1 Giuliana Xavier de Medeiros, 2 Eduardo Henrique de M. Nunes, 2 WanderLuiz de Vasconcelos.1 Instituto Federal de Educação,Ciência e Tecnologia do Sudeste de Minas de Gerais- Departamentode Educação e Tecnologia. Núcleo de Metalurgia, Juiz de Fora, MG *lecinocaldeira@yahoo.com.br.2Universidade Federal de Minas Gerais – Escola de Engenharia, Departamento de EngenhariaMetalúrgica e de Materiais. Belo Horizonte, MG.ABSTRACTA membrane can be seen as a barrier that acts on the separation of two phases and its function is torestrict, in total or partial manner, the transport of chemical species that comprise these phases. Themembrane separation process has a number of advantages over conventional methods [1]. Amongthem we can mention its relative simplicity and easy to use, low power consumption involved (lowercosts), its applicability in the separation of both gases and liquids, flexibility arrangements in severalprocess and the possibility of employing different materials. For these reasons, the membranetechnology in recent decades has acquired great strategic and commercial importance. Amongvarious systems that have been studied, the titania constitutes the most promising materials toreplace the silica and gamma-alumina, due to its superior chemical stability. Titania has beenconsidered as a good candidate to porous material due to its particular superficial properties,specially its capacity to work properly in harsh environments and thermal stability at hightemperature [2]. However, the procedures for synthesis of titania microporous membranes arehighly sensitive and case dependent of synthesis conditions. Although there are many reports in theliterature of successful fabrication and applications of such membranes, the means to achievecontrol of the pore structure in the nanometer range have yet to be fully understood [4]. Therefore,the aim of this work is to develop a porous inorganic membrane appropriate for separation of greenhousegases, especially CO 2 . For such application, it’s taken in to account its pore structure (porosity,average pore size and pore size distribution), considering that the average pore size must to be in ananoscale range (

Composite PDMS membranes for gas separationAlice Reis Brasil 1 , Dario Windmöller 2 , Katia Cecília de Souza Figueiredo 1,*1 - Chemical Engineering Department, Federal University of Minas Gerais. 2- Chemical Department,Federal University of Minas Gerais. Av. Antônio Carlos, 6627, Pampulha. CEP 31270-910. BeloHorizonte, Minas Gerais, Brazil.* katia@deq.ufmg.br.Dense composite membranes are efficient means of gas separation and pervaporation. Thesemembrane processes have potential to substitute the conventional separation methods used byindustry that usually consume large amount of energy. Such membranes have a broad range ofapplications like recovery of volatile organic compounds, separation of H 2 and N 2 in ammonia plants,recovery of CO 2 from natural gas and the removal of 1-butanol from water [1].Elastomeric polymers are usually responsible for high fluxes in membrane separation processes. Inthis work, the aim was the preparation of composite polydimethylsiloxane (PDMS) membranes inorder to provide high flux due to the mobility of its polymeric chains. The porous support wasinvestigated in order to increase membrane mechanical strength.Commercial silicon adhesive was dissolved in an equal toluene mass quantity and then casting overthe surface of a microfiltration acetate cellulose support (0.45 µm). The solvent was allowed toevaporate in a chamber for 48 hours. After that, the prepared membranes were characterized by gaspermeation tests with N 2 , H 2 , CO 2 , CH 4 and O 2 . Each individual gas was tested and the pressureincrease in permeate side was monitored with time. This procedure was repeated three times so thatthe reproducibility could be guaranteed. The results are presented in Figure 1.1210CO2CH4O2N2Permeate Pressure (Torr)864H2200 10 20 30 40 50 60 70Time (s)Figure 1 – Gas permeation data for Oxygen, Nitrogen, Hydrogen, Carbon Dioxide and Methanethrough the composite PDMS membrane.

All curves presented linear shape and the angular coefficient of the lines were almost exactly thesame for the same gas, showing reproducibility. The ideal selectivity for a pair of gases was 1.4 forO 2 /N 2 , 1.6 for H 2 /N 2 , 4.4 for CO 2 /N 2 and 2.3 for CO 2 /CH 4 . These results show that dense compositemembranes were successfully prepared. The addition of inorganic materials in the membrane will befurther investigated in order to increase membrane selectivity. The authors would like to thankFapemig for the financial support.[1] A. C. Harbert, C. P. Borges, R. Nobrega (2006), Processos de Separação por Membranas. Rio de Janeiro: E-Papers, 1-180.

Study of Filterability Methods for Quality Evaluation in Biological Sludge fromBRMAline Ribeiro Alkmim 1 , Paula Rocha da Costa 1 , Míriam Cristina Santos Amaral 1* , Luzia Serginade França Neta 2 , Ana Cláudia Cerqueira 3 e Vânia Maria Junqueira Santiago 31 Department of Sanitary and Environmental Engineering - Federal University of Minas Gerais - Brazil- Phone: + 55 31 3409-3669 - Email: miriam@desa.ufmg.br2 Chemistry Department - Federal Center of Technological Education of Minas Gerais - Brazil3Research Center of PETROBRAS - BrazilThe membrane bioreactors (BRM) are an efficient method for the treatment of domestic andindustrial effluents. However, due to the fouling formation, the transmembrane pressure increaseswith time, in order to keep the permeate flow constant. This increase in the transmembranepressure may cause an increment in the pumping costs and damage to the membrane due to morefrequent cleanings.The filterability of the sludge has been used for monitoring and controlling the fouling in MBR.Different methods have been used to measure the filterability, such as Capilarity Suction Time - CST[1], Time to Filter – TTF [2,3], Filter Test – FT [1] Sluge Filtration Index – SFI [4], Delft FiltrationCharacterization Method – DFCm [5]. The absence of a standard method of filterability precludes thecomplete understanding of the influence of this parameter in the performance of MBRs, and makesthe comparison of MBR systems with other alternatives more difficult.In this context, the present study aimed at comparing the three main different methods to measurethe filterability reported in the literature (TTF, FT and SFI) and observing which is the best to evaluatethe quality of biological sludge from BRM used to filter an effluent from oil refinery. Experimentswere conducted with 29 samples in triplicate in a period of 163 days amounting to 87 repetitions foreach method. The experimental apparatus used in the tests are presented in Figure 1:Time To Filter (TTF) Filter Test (FT) Sludge Filtration Index (SFI)(a)(b)(c)Figure 1 – Experimental apparatus used for determining the sludge filterability. (a) Time To Filter(TTF), (b) Filter Test (FT) and (c) Sludge Filtration Index (SFI). Source: THIEMIG, 2011a – adapted.Figure 2 shows the statistical analysis of the methods used during the monitoring period obtained forthe tested methods.

Figure 2 – Box-Plot – Coefficient of variation for the filterability methods.Through analysis of Figure 2, it is possible to observe that the values of the coefficients of variationfor the tests which used the TTF200 method had lowest median value of its coefficient. This meansthat this method presents a better result in respect of reproducibility.Comparing the results obtained by the three methods in the monitoring period, we observe in Figure3 that they are able to identify significant change in the filterability, the three methods can highlightit in your results. It can be observed that the "Filter Test" method has no sensitivity for detectingsmall variations in the sludge quality.Figure 3 – Comparison of methods TTF, FT and SFI.Based on the results obtained from the comparison of the three methods, we conclude that the TTFmethod proved to be most effective for the analysis of sludge filterability in BRM used for refinerywastewater treatment.

ACKNOWLEDGEMENTSThe authors would like to express gratitude to: Petrobrás, Conselho Nacional de DesenvolvimentoCientífico e Tecnológico (CNPq), Coordenação de Aperfeiçoamento de Pessoal de Nível Superior(CAPES) and Fundação de Amparo à Pesquisa do Estado de Minas Gerais (FAPEMIG) for theirpermanent support.REFERENCE[1] THIEMIG, C. (2011a) Die Bedeutung der Filtrationseigenschaften von belebten Schlämmen beim Betriebvon Membranbioreaktoren. Aachen.[2] SM-2710. (2004) Test on sludges.[3] APHA (2005), Standard Methods for the Examination of Water and Wastewater, 21th ed., American PublicHealth Association/American Water Works Association/ Water Pollution Control Federation, WashingtonDC.[4] THIEMIG, C. (2011b) The importance of measuring the sludge filterability at MBR – introduction of a newmethod. 6th IWA Specialist Conference on Membrane Technology for Water and Wastewater Treatment.[5] EVENBLIJ, H. ; GEILVOETA, S.; VAN DER GRAAFA, J..J.M; VAN DER ROESTB, H.F (2005), Filtrationcharacterisation for assessing MBR performance: three cases compared. Desalination.

Toxicity removal on leachate treatment using membranesBeatriz Gasparini Reis * , Miriam Cristina dos Santos Amaral, Liséte Celina LangeDepartamento de Engenharia Sanitária e Ambiental, Federal University of Minas Geraise-mail: bbiagasparini@yahoo.com.brToxicity is a very important tool as it´s consequence of the interaction of different pollutants presentson effluents, its synergic and antagonist effects and different physic-chemical properties [1, 2].Effluents containing toxic compounds, like leachate, can greatly complicate its treatment as toxicitymay hamper biological processes. Its persistence on the final effluent is also not desirable as toxiceffluents don’t meet release or reuse standards.Membranes are a very versatile and promising technology on effluent treatment as it can achieveseveral goals. They can be used alone or in association with different processes, like biologicalprocesses, originating membrane bioreactors – MBR. Membranes improve the overall process’efficiency and provide a better quality effluent. As membranes are a physical treatment it doesn’tsuffer influence from toxicity and can be widely used.In this study, we analyzed a route of leachate treatment using membranes (Fig. 1). Experiments wereconducted using the leachate of a 5 years old landfill of Minas Gerais (Brazil).Figure 1 – Route of leachate’s treatmentRaw leachate and samples of the different stages of treatment were analyzed to evaluate theirperformance. Physicochemical analyses included pH, color, conductivity, chemical oxygen demand(COD), total organic carbon (TOC), total nitrogen, ammonia-nitrogen, nitrites, nitrates, totalphosphorus, chloride and alkalinity. Bioassays with the bacteria Vibrio fischeri (Microtox®) and themacrophyte Lemna minor were performed to determinate the acute toxicity of the samples.The route of treatment showed satisfactory results on leachate treatment, with removal efficienciesof physicochemical parameters which mostly range from 80 to 99%. Treatment also achievedcomplete removal of toxicity (Fig 2 - the green line on graphic illustrates nontoxic zone, EC50 > 81,9).Figure 2 – Toxicity evolution during leachate’s treatment route using Microtox®

EC50 30min10080604020014,69,84,6Raw leachate Air-stripping MBR NanofiltrationAs shown above, there was a gradual removal of toxicity during treatment. Air-stripping phase is thefirst step to remove toxicity as it removes ammonia. After MBR it can be observed another increaseon EC50 that can be due to the degradation inside the bioreactor and microfiltration membrane’sselectivity. But the most significant step for toxicity removal is definitely nanofiltration. After thispolishing stage, the final effluent of the route presents as a nontoxic sample.Biological treatment is not capable of achieving high rates of toxicity removal [3], but its conjugationwith membranes makes the system more efficient and promising. Nanofiltration is a very versatileapproach [4] and its use as polishing stage allows membrane fouling control besides completeremoval of toxicity. Finally, the final effluent can either be discharged or reused in many differentways.AcknowlegmentsThe authors acknowledge the financial support provided by CNPq, CAPES and FAPEMIG and thestructural support of DESA-UFMG.[1] A. Pivato & L. Gaspari (2006) Waste Management, 26, 1148–1155.[2] S. K. Marttinen, R. H. Kettunen, K. M.Sormunen, R. M. Soimasuo, J. A. Rintala (2002) Chemosphere, 46, 851–858.[3] S. Renou, J. G. Givaudan, S. Poulain, F. Dirassouyan, P. Moulin (2008) Journal of Hazardous Materials, 150,468–493.[4] A. Z Gotvajn, J. Zagorc-Koncan, N. Cotman (2011), Desalination, 275, 269-275, 2011.

Poly(vinyl alcohol) and Chitosan Blended Membranes for Dehydration of 1-Butanolby means of PervaporationCarlos Eduardo Rinco 1 , Lucas Almeida Castro 1 , Pedro Garcia Ribeiro 1 , Sophia Cherem 1 ,Thomaz Antônio Perilli 1 , Walace Silva Bráulio 1 , Dario Windmöller 2 , Katia Cecília de SouzaFigueiredo 1,*1 - Chemical Engineering Department, Federal University of Minas Gerais. 2- Chemical Department,Federal University of Minas Gerais. Av. Antônio Carlos, 6627, Pampulha. CEP 31270-910. BeloHorizonte, Minas Gerais, Brazil.* katia@deq.ufmg.br.Biobutanol and bioethanol have proved to be promising alternatives to fossil fuels. Particularly, theproduction of butanol from biomass and its potential as a precursor to a set of products may reducethe petroleum dependence worldwide [1]. However, both the reaction to produce biobutanol andthe separation and purification steps are difficult to attain. One of the approaches to circumvent theproblem is the use of a membrane-assisted reactor. The idea is based upon the fact that the smallamount of alcohol can be continuously removed from the fermentation froth by means ofpervaporation. Another membrane based step to dehydrate the previous mixture may also be viable.This work is focused on the dehydration of 1-butanol from ethanol, 1-butanol and water mixtures.Our aim was the preparation and characterization of a poly(vinyl alcohol), PVA, and chitosan, CS,blended membrane to be used in dehydration of alcohols, namely, ethanol and 1-butanol, by meansof pervaporation.Membranes were prepared by varying PVA/CS mass ratio from 0 to 1. Aqueous solution of eachpolymer was prepared and mixed in the desired proportion, after filtration. The casting solution wasdegassed by using a vacuum pump and transferred to a plate. The solvent was allowed to evaporatein an oven at 60 o C for 24 hours. Membranes were immersed in the crossliking solution (aqueoussolution of acetone, 48% in weight, glutaraldehyde, 1% in weight and sulfuric acid, 1% in weight oraqueous sodium hydroxide 2% in weight, for the CS pure membrane) for 30 minutes and dried for 24hours. The characterization tests comprised water swelling, infrared spectroscopy, differentialscanning calorimetry, thermogravimetric analysis and pervaporation tests at room temperature of asolution containing 80% w/w 1-butanol, 15% w/w ethanol and 5% w/w water.Membrane corresponding to 75% of PVA and 25% of CS was selected from the characterization testssuch as water swelling, FTIR, DSC and TGA to be evaluated regarding its transport properties. Theseparation factor for water/ethanol and water/1-butanol were 152 and 281, respectively. Membraneflux was 401 g/m 2 h. The preparation of composite membranes is under evaluation in order todecrease membrane thickness (from 82 µm to 10 µm), which may increase the flux.The authors would like to thank Fapemig for the financial support.[1] B. G., Harvey, H. A., Meylemans (2011), J. Chem. Technol. Biotechnol., 86, 2-9.

Pressure / TorrGas separation with a nanocomposite membrane of polyurethane and carbonnanotube.Dario Windmöller* 1 , Kamila Silva Alves 1 , Rodrigo Lassarote Lavall 1 , Elisa Carvalho Castro 1 ,Juliana Aparecida De Sales 2 .1 - Chemical Department, Federal University of Minas Gerais. Av. Antônio Carlos, 6627, Pampulha.CEP 31270-910; 2 – FACET - Centro Universitário Newton Paiva. Belo Horizonte, Minas Gerais, Brazil.* dariow@ufmg.brThe separation of gases with rubbery membranes is widely used, polyurethane is a common materialemployed in this cases [1,2]. Nanomaterials, like carbon nanotubes, improve membrane fluxes andselectivities [3]. In this work we prepare the nanocomposite membrane with a multiwalled carbonnanotubes supplied by the Physical Department of UFMG. The nanotube was chemically modifiedwith strong acids. The nanotube was then mixed with a solution of THF and polyurethane (TPU 990R- Bayer Material Science). This solution was casting and allowed to evaporate the solvent. Weproduced membranes with 0; 0.02 and 0.5 weight percent of the nanotube. The polyurethane hasthe following structure:HHHH(C 4 H 8 ) m O C NN CO(CH 2 ) 4OCNNCOOOOOnThese membranes were tested with different gases in a constant volume variable pressure testsystem. The feed gas was pressured to a constant pressure of 1 atm, the pressure of the permeateside was monitored by one MKS Baratron capacitance sensor. The results of the three membranesare showed in figures 1 to 3.0.5CO 20.40.3H 20.2O 20.1N 20.00 200 400 600 800 1000Time / sFigure 1. Permeate pressure in the runs with the PU membrane.

Pressure / TorrPressure / TorrThis permeability order is in agreement with other works that also used polyurethane membranes of differentstructures [4].0.300.250.15CO 2H 2CH 40.200.10O 2N 20.050.000 50 100 150 200 250 300 350 400Time / sFigure 2. Permeate pressure in the runs with the PU 0.02 % nanocomposite membrane.1.61.41.2CO 2H 2CH 4O 2N 21.00.80.60.40.20.00 100 200 300 400 500 600 700Time / sFigure 3. Permeate pressure in the runs with the PU 0.5 % nanocomposite membrane.The additions of the nanotube at low concentration don’t change significantly the permeability of the testedgases as can be seen in the Table 1.Table 1 – Gas permeability of the membranesNanotube content / %Permeability / BarrerCO 2 CH 4 H 2 O 2 N 20 11.4 - 3.8 1.5 0.50.02 11.7 1.8 4.1 1.4 0.7

When the concentration of the nanotube is higher the membrane lost completely their selectivity, indicatingthat the nanotube introduces defects in the membrane structure; this result can be confirmed by increasedpermeability of this membrane.[1] M. Sadeghi et al (2011), J. Memb. Sci., 385, 76-85.[2] J. A. de Sales et al (2008), J. Memb. Sci., 310, 129-140.[3] K. Sears et al (2010), Materials, 3, 127-149.[4] M. A. Semsarzadeh (2012), J. Memb. Sci., 401-402, 97-108.Acknowledgment:Dario W. thanks the financial support of FAPEMIG for the costs of participation in this Symposium and KamilaS. A. the scientific initiation scholarship (PROBIC).

Vinasse Treatment by Anaerobic Membrane Bioreactor (AnMBR) with PhasesSeparationFábio Soares dos Santos*, Míriam Cristina Santos Amaral, Luzia Sergina de França Neta.Department of Sanitary and Environmental Engineering, Universidade Federal de MinasGerais. Av. Antônio Carlos, 6627 - Pampulha - Belo Horizonte – MG – Brazil. CEP: 31270-901.+55 (31) 3409-3669. fabiosoares04@gmail.comThe vinasse is an effluent of the distillation of fermented juice or molasses from sugarcane forethanol production. This effluent is characterized by high organic material concentration, low pH andhigh levels of suspended solids and nutrients (N, P and K) [1]. Currently, anaerobic membranebioreactors (AnMBR) are presented as promising in the treatment of this effluent. Beyond combiningthe advantages of the anaerobic processes, the use of membrane separation processes can preventloss of sludge, producing a solids-free effluent and prevent unintended sludge wasting. The phaseseparation may allow better conditions for acidogenesis and methanogenesis, important stages ofanaerobic digestion, promoting efficiency to the process. Thus, the aim of this study was to evaluatethe AnMBR with phase separation, acidogenic and methanogenic, for the treatment of sugarcanevinasse.The effluent used throughout this study was provided by the alcohol industry Irmãos Malossolocated in Itápolis - SP, Brazil. The AnMBR was operated for 75 days and consisted of two tanks,acidogenic (AR) and methanogenic (MR). The latter was equipped with microfiltration membrane,hollow fiber type, with surface area of 0.046 m 2 [2]. The permeate flux was kept constant (5.2L/m 2 .h) and feed controlled by level valves. The total HRT was 5.3 days and STR infinity. Feed andpermeate were characterized by COD, total solids (TS), total nitrogen (TN), NO 3 - , PO 4 3- , SO 42-e K + andMR sludge by solids according to Standard Methods and production SMP and EPS.The results showed good removal efficiencies of COD, SO 42-e PO 4 3- , considering a significance level of0.05 (Table 1). Other anions and cations important in agriculture, such as NO 3-e K + , and TN, were notsignificantly removed. The removal of TS was also considerable, and this is mainly due to thecontribution of microfiltration membrane on the MR.Table 1 - Characteristics of feed and permeate and removal percentThe system presented average permeability values around 19.7 L/m 2 .h.bar, and the highest valueswere observed when it was operated in lower pressures. The biological sludge (MLSSV) was veryimportant for the organic matter removal and its average concentration was 8011.0 mg/L

corresponding to a average F/M relation of 0.4 d -1 . Its stay in the reactor was ensured by themicrofiltration membrane, which contributed to the efficiency of treatment. It was observed a higherproduction of SMP in relation to EPS, and this mainly in the form of protein, which may be associatedwith high sludge age employed, that favors cell lysis.The results show that AnMBR was feasible for the treatment of effluent, achieving high efficiency inremoving organic matter (> 97%) and ensuring the stay of important ions for fertigation. The use ofmicrofiltration membrane in the treatment system was very important for the retention of biologicalsludge and solids allowing the effluent treatment be more efficient.[1] A. C. Van Haandel (2005), Water Science and Technology, 52(1-2), 49-57.[2] V. T. F. Mota, (2012) Biorreator com membranas anaeróbio de duplo estágio para o tratamento do vinhoto.Dissertação (Mestrado em Saneamento, Meio Ambiente e Recursos Hídricos) – DESA, UFMG.

Preparation and characterization of PVA and chitosan hydrophilic membranescrosslinked by glutaraldehydeFernanda Angélica Camilo Aguiar, Kátia Cecília de Souza Figueiredo * .Federal University of Minas Gerais. Chemical Engineering Department. Av. Antônio Carlos, 6627,Block 2, Room 5206. CEP 31270-910, Belo Horizonte, Minas Gerais, Brazil.* katia@deq.ufmg.br.Membranes separate two phases and restrict the flow of substances between them. The hydrophilicmembranes have been studied in recent years since they have a great importance for many industrialprocesses [1]. The pervaporation dehydration of organic solvents is an example, especially when themixture forms azeotropes with water, making it difficult to separate. Another use for suchmembranes is the separation of water vapor from natural gas and in dialysis processes.Polyvinyl alcohol (PVA) is a synthetic polymer, obtained by the hydrolysis of poly(vinyl acetate),widely used in composition of membranes for pervaporation dehydration industry. This is due to thehigh number of hydroxyl groups present in the polymer, which justifies its good interaction withwater. The recent use of chitosan (CS) for this type of membrane has great technological interest.Besides its high hydrophilicity due to the presence of hydroxyls and the amino groups, CS forms highmechanical strength and chemical resistance films [2]. Thus, the advantages of the two polymers canbe combined into one blended material.The use of a difunctional aldehyde, such as glutaraldehyde, GA, to crosslink blended membranes ofPVA and CS have proved to be very effective [2]. This is because the two carboxyl groups may attachto the amino groups of CS and the hydroxyl groups of the PVA. Thereby, GA consists of a verypromising crosslinker.The main objective of this work is the preparation and characterization of blended hydrophilicmembranes of PVA and CS for separation of water from various mixtures. Membranes wereprepared by mixing different proportions of PVA and CS brought to ultrasound to avoid defects in thefilm. The technique applied was solvent evaporation at room temperature and once dried, thecrosslinking was performed to a membrane of each composition. Water swelling tests wereconducted in the membranes of all proportions, with and without crosslinking. The results showedthat the crosslinked membranes with compositions of 75%CS/25%PVA and 75%PVA/25%CS showedthe lowest water swelling and are the most promising condition for the permeation of water.Other characterization tests are still being conducted in order to characterize the transport ratethrough these membranes, as well as FTIR, DSC and TGA. Our previous results showed promisingtransport and selectivity properties. The authors would like to thank Fapemig for the financialsupport.[1] A. C. Habert; C. P. Borges; R. Nobrega (2006), Processos de Separação por Membranas. Rio de Janeiro: E-Papers, 1-180.[2] A. Svang-Ariyaskul, R. Y. M. Huang, P. L. Douglas, R. Pal, X. Feng, P. Chen, L. Liu, (2006), J. Membr..Sci., 280,815-823.

Preparation and Characterization of a Catalytic Membrane for Biodiesel ProductionFernanda Teixeira da Silveira 1 , Dario Windmöller 2 , Katia Cecília de Souza Figueiredo 1,*1 - Chemical Engineering Department, Federal University of Minas Gerais. 2- Chemical Department,Federal University of Minas Gerais. Av. Antônio Carlos, 6627, Pampulha. CEP 31270-910. BeloHorizonte, Minas Gerais, Brazil.* katia@deq.ufmg.br.Biodiesel is an alternative fuel for diesel engines, but the lack of a cost competitive technology fortransesterification of vegetable oils or animal fats still limits the use of this product [1]. In order toreduce the cost of biodiesel production, the use of cheap feedstock has been investigated [2].According to this approach, waste cooking oil with high free fatty acid content may be used toproduce methyl or ethyl esters. Catalytic membranes, with strong acid sites and high hydrophilicity,can be an alternative for heterogeneous catalysis and water removal from de medium.Our aim in this work was the preparation and characterization of a catalytic membrane in order toproduce biodiesel from waste cooking oils. The experimental strategy comprised the use of poly(vinylalcohol), PVA, as the hydrophilic polymer, and Amberlyst 15, A15, (Rohm and Haas), as the protonicsites source. Glutaraldehyde, GA, was the crosslinking agent. Kinetic tests were conducted in order toevaluate the heterogeneous catalyzed reaction. Membranes were characterized by infraredspectroscopy, differential scanning calorimetry and thermogravimetric analysis, as well as transportproperties in pervaporation and gas permeation tests.Typically, GA aqueous solution (25% w/w) was added to 5% w/w aqueous PVA solution andhomogeneized. A15, previously dried, milled and degassed in an ultrasound bath, was added to thesolution. The suspension was cast into a plate and the solvent was evaporated in an oven at 60 o C,for 24 hours. This procedure was used to prepare integral dense membranes. Composite membraneswere also prepared by casting the suspension described above over a microfiltration celluloseacetate commercial membrane (0.45 µm).The addition of A15 to the films increased the thermal stability of PVA based membranes, accordingto TGA tests. It was also shown a high hydrophilicity of the membrane, as the result of TGA and DSCtests. Membrane chemical characterization confirmed the reaction between PVA and GA. Regardingmembrane transport properties, it was noticed that integral membranes were dense, with idealselectivity of 3.5 for N 2 /CO 2 . Future tests will comprise pervaporation of water/ethanol (5:95 inweight) as well as the reacting mixture, alcohol and waste cooking oil, in order to evaluate esterconversion.The authors would like to thank Fapemig for the financial support.[1] W. Shi, B. He, J. Ding, J. Li, F. Yan, X. Liang (2010), Bioresour. Technol., 101, 1501-1505.[2] M. Zhu, B. He, W. Shi, Y. Feng, J. Ding, J. Li, F, Zeng (2010), Fuel, 89, 2299-2304.

Microfiltration for Indigo Blue Dye Recovery from Textile WastewaterIgor Bernardes Oliveira¹, Laura Hamdan de Andrade 1 *, Míriam Cristina Santos Amaral 1 , LuziaSergina França Neta²1 Department of Sanitary and Environmental Engineering, Federal University of Minas Gerais² Department of Chemistry, Federal Center of Technological Education of Minas Gerais* Corresponding author: Av. Antônio Carlos, nº 6627 - Pampulha - Belo Horizonte – Minas Gerais –Brazil. Telephone: +55 (31) 34093669; Fax: +55 (31) 34091879; Email: lauraha@ymail.comIndigo blue is widely used in the textile industry, specifically for jeans manufacturing, however, 5 to20% of the this dye is lost during the fiber washing step [1]. In textile wastewater, indigo blue ispresented in an oxidized, insoluble form. Thereby, microfiltration (MF) can be used for the treatmentof indigo blue dye effluent, as it enables simultaneously the recovery of the dye and the reduction ofthe color and organic load of the effluent. Thus, the aim of the present study was to evaluate thefeasibility of using MF for the treatment of dyeing wastewater and indigo blue recovery.The effluent used in the experiments was the wash water from jeans dyeing process collected in atextile industry located in Minas Gerais, Brazil. It was used a sidestream microfiltration module(polyetherimide, average pore diameter 0.40 µm, membrane filtration area 0.0471m², modulepacking density 550 m²/m³).Tests of critical and limit flux were performed with permeate and retentate returned to the feedtank. In order to evaluate the permeate flux with increasing feed solute concentration and determinethe optimal recovery rate, another MF test was carried out returning only the retentate to the feedtank and monitoring the permeate flux and COD. The conditions applied were feed flow rate of 4.8L/min (Reynolds number of 3800) and pressure of 0,10 bar. MF feed, permeate and retentate werecharacterized regarding COD, color, conductivity and indigo blue concentration.The COD retention efficiency of the system was only 27% (Table 1), which shows that most of organiccompounds present in the effluent were constituted by soluble material. On the other hand, MF wasquite efficient for retaining suspended particles, since the retention efficiencies for color and indigoblue were 97% and 99%, respectively. The indigo blue was almost fully recovered in the retentate,which could be reused in industrial process after indigo reduction.Table 1 - Raw effluent, permeate and retentate characterization.Parameter Unit Feed Permeate RetentateCOD mg/L 1756 1316 2046Color mg/L 6072 172 11055Conductivity mS/cm² 2.73 2.21 2.16Indigo blue g/L 0.37 0.0044 0.81The measured critical flux was 31 L/h.m², which can be considered elevated. This was due to highfeed flow rate and high shear stress near membrane surface, which prevent foulant deposition. Thelimit flux was only slightly superior to critical flux (32 L/h.m²).

In Figure 1 it is shown results of the concentration test. After 5 hours of operation, the permeaterecovery rate was 68% and permeate flux was equal to 25% of the initial value. The permeate fluxdecreased about 40% during the first 10 minutes of permeation, however, after this initial period,the permeate flux decay was slow, indicating low fouling.Figure 1 – Permeate flux versus time for the concentration test.[1] J. Ji, J. Yang, W. Wang, Z. Wang. (1999) Treatment of dyeing wastewater with ACF electrodes. Water Res.,33, 881-884.AcknowledgementsThe authors acknowledge the financial support provided by CNPq and FAPEMIG.

PLGA Nanoparticles Containing Dexamethasone Acetate for ControlledReleaseIzabella Maria Ferreira Campos*; Kátia Cecília de Souza Figueiredo;Department of Chemical Engineering, School of Engineering, Federal University of MinasGerais, Pampulha Campus, CEP 31270-901, Belo Horizonte, MG, Brazil.* E-mail: izabellafcampos@gmail.comControlled release systems have been the subject of intensive research in recent years, aiming toincrease the absorption of the drug, provide protection and allow prolong drug exposure [1]. Theobjective of this study is the preparation of poly (lactic-co-glycolic acid), PLGA, nanoparticlescontaining dexamethasone acetate, in order to develop systems for controlled drug delivery.Nanoparticles were prepared by dissolving the PLGA (75:25) in acetone and subsequently dribbledout into a solution containing water, ethanol and Tween ® 80. The system was stirred by means of amagnetic bar for 5 hours.The operational conditions investigated during this process are shown in Table 1. The evaluation ofthese variables was carried out by means of an experimental plan. The results were analyzed andindicated the best conditions to prepare the nanoparticles containing the drug. The response was themean size and zeta potential of the particles.Table 1: Conditions investigated for the preparation of nanoparticles.Condition Minimum MaximumVolume fraction of ethanol in the solution ethanol / water 0.5 0.8Surfactant concentration (% w / v) 2 6Polymer concentration (g / L) 3.7 7.4Volumetric ratio of acetone / water 0.25 0.5The method of preparation of nanoparticles containing dexamethasone acetate was similar to thatdescribed above, except that the drug was added to the organic solution, already containing thePLGA and acetone. The concentration of the drug in the solution of nanoparticles was 200 g/mL.The results showed that nanometric particles were produced by using the experimental procedureproposed, in the absence of organochloride solvents. The 2 3 experimental plan showed the mostfavorable conditions for the preparation of nanoparticles containing the drug. The volumetric ratioof ethanol and water was set to 0.5, the surfactant was used in the concentration of 6%, PLGAconcentration was 7.4 g / L and the volumetric ratio between acetone and water was 0.25.The results obtained for the nanoparticles prepared under these conditions were 208 nm and -10mV, while the nanoparticles containing dexamethasone acetate had the following results: 540 nmand -2,5 mV.The authors would like to thank to Fapemig for the financial support.[1] S. K. Sahoo; F. Dilnawaz; S. Krishnakumar (2008), Drug Discovery Today[k1], 13, 146-151.

Advanced Oxidation Process, Microfiltration and Nanofiltration for Treatment ofLandfill LeachateLarissa M. Diniz 1 , Laura H. Andrade 1 *, Marco A. Herculano 1 , Eghon P. Rocha 1 , Thiago L.Massula 1 , Míriam C. S. Amaral 1 , Liséte C. Lange 11 Department of Sanitary and Environmental Engineering, Federal University of Minas Gerais.* Corresponding author: Av. Antônio Carlos, nº 6627 - Pampulha - Belo Horizonte – Minas Gerais –Brazil. Telephone: +55 (31) 34093669; Fax: +55 (31) 34091879; Email: lauraha@ymail.comThe treatment of sanitary landfill leachate is a problem in many countries. The existence ofincreasingly restrictive standards regarding the discharge of effluents on water bodies and the agingof landfills cause the conventional treatments not to provide adequate removal efficiencies anymore[1]. In this scenario, membrane technology and advanced oxidation processes appear as promisingtechnologies.The aim of this study was to evaluate the performance of a treatment system constituted ofadvanced oxidation process (AOP), microfiltration (MF) and nanofiltration (NF) for advanced landfillleachate treatment.In the proposed system (Figure 1), raw leachate was initially microfiltrated (MF1). The concentrate ofMF1 underwent the AOP-Fenton process and subsequently, a second MF for sludge removal (MF2).Permeates from both MF1 and MF2 were mixed and sent to a nanofiltration unit (NF). The permeatefrom the NF consisted of treated effluent, and the concentrated returned to the AOP-Fenton stage.Figure 1 - Scheme of the proposed treatment system for landfill leachate.The AOP-Fenton reaction was performed with the following operational conditions: 1.7g H2O2/1gCODraw leachate, [H2O2]/[Fe] molar ratio of 13, pH of 3.0 and reaction time of 30 minutes. MF1 wasperformed using a sidestream module (0,072 m²), and MF2, a submerged module (0,044 m²). Bothmodules were hollow-fiber type, made of polyetherimide, with average pore diameter of 0.4 µm. TheNF membrane used was the commercial NF90, which was cut and inserted into a filtration cell(0.0062 m²). A recovery rate of 60% was applied for all membrane process.To evaluate the proposed treatment system, the raw and treated effluent and intermediate streamswere analyzed in terms of COD, apparent color, total solids, ammonia nitrogen (N-NH3), totalphosphorus and chloride concentrations. For assessment of the stages with membranes, thepermeate flow decay was monitored during filtration time.

As can be seen in Table 1, the system showed high capacity for organic matter, solids and nutrientsremoval.Table 1 – Values of the principal physicochemical parameters for raw landfill leachate.ParametersRaw effluentPermeate Permeate OverallPermeateAOP-Fenton NF removalMF1+ MF2efficiencyCOD (mg/L) 3,702 2,971.4 832 211 94%Total solids (mg/L) 10,493 9,063 8,740 1,612 85%Apparent color (Hu) 1,689 1,110 135.2 14.7 99%N-NH3 (mg/L) 1,513 - - 461 70%Phosphorus (mg/L) 32 - - 3 90%Chlorides (mg/L) 2,699 - - 622 77%Figure 2 shows the membrane performance results. Note that the raw landfill leachatemicrofiltration (MF1) showed more significant fouling than MF applied after POA-Fenton (MF2).Although the post-Fenton effluent has many suspended solids, which could deposit over membranesurface, apparently the compounds of the raw leachate are more likely to cause fouling. For NF, itcan be observed that despite initial effluent permeability is 30% lower than clean membrane waterpermeability, which can be related to concentration polarization process, fouling could be partiallycontrolled by shearing.Figure 2 - Performance of the microfiltration and nanofiltration process.Preliminary results show the suitability of the proposed route for the treatment of landfill leachate.[1] S.RENOU; J. G GIVAUDAN; P. MOULIN. Landfill leachate treatment: Review and opportunity. Journal ofHazardous Materials, v. 150, p. 468–493, 2008.AcknowledgementsThe authors acknowledge the financial support provided by CNPq, FINEP and FAPEMIG

Pilot Scale Microfiltration and Membrane Bioreactor for Vinasse TreatmentLaura Hamdan de Andrade 1 *, Fábio Santos Soares¹, Míriam Cristina Santos Amaral 1 , LuziaSergina França Neta², Walter Bom Braga Jr³, Roberto Bentes de Carvalho³1 Department of Sanitary and Environmental Engineering, Federal University of Minas Gerais² Department of Chemistry, Federal Center of Technological Education of Minas Gerais³ Pam Membranas Seletivas Ltda.* Corresponding author: Av. Antônio Carlos, nº 6627 - Pampulha - Belo Horizonte – Minas Gerais –Brazil. Telephone: +55 (31) 34093669; Fax: +55 (31) 34091879; Email: lauraha@ymail.comVinasse is a residue from the distillation of alcohol. It is estimated that 15 liters of this effluent isgenerated per liter of ethanol produced [1]. One option for the disposal of this waste is theapplication on cane plantations, thus making use of the nutrients presented. However, besides theproblems of soil acidification, groundwater contamination and proliferation of insects, transport ofvinasse to disposal on sites distant from the industrial plant is costly.To reduce this cost, vinasse can be previous concentrated, improving product stability and reducingthe volume to be transported [2]. Microfiltration (MF) is presented as a good alternative for thisprocess, since it generates two streams: retentate, which could be used as fertilizer, and permeate,that may be post-treated and reused in distillery plant. For reduction of the organic load of MFpermeate, the use of membrane bioreactors (MBR) is promising, since they are capable to generatehigh quality treated effluent.Thus, the aim of this study was to evaluate the application of pilot-scale MF and MBR for thetreatment and reuse of vinasse.The pilot-scale MF and MBR systems (Figures 1, 2 and 3) were built by Pam Membranas SeletivasLtda. and are installed at a distillery, in Itápolis, São Paulo, Brazil.Figure 1 - Scheme of the vinasse treatment system.

231Figure 2 - Photograph of the pilot plant: 1 – MF permeate storage tank, 2 – raw vinasse storage tank,3 - biological tank.Figure 3 – Submerged MF unit.The MF system is equipped with three submerged hollow-fiber modules (6 m² per module). Thedesign flow of MF is 90 L/h, and the permeate flux, 5 L/h.m². The BRM also has two MF modulessubmerged in a tank external to the biological tank. The design flow of the BRM is 60 L/h, thepermeate flux, 5 L/h.m² and hydraulic retention time, 52 hours. Sludge is recirculated from thebiological tank to the membrane tank at a rate equivalent to five times the permeate flow.Figure 4 shows the results for the TPM-step test for determination of the critical flux for bothprocess. One can observe high values of critical flux, equal to 24 and 50 L/h.m² for MF and MBRsystems, respectively.

(a)Figure 4 – Critical flux test.(b)Figure 5 shows preliminary results regarding the performance of the membranes in both systems.(a)(b)Figure 5 - Pressure, permeate flux and permeability for MF (a) and MBR (b).The average COD retention by MF membrane was 25%. The concentration of COD in the retentatewas 79% higher than the raw vinasse. The MBR permeate COD concentration was close to 1,500mg/L, corresponding to a removal efficiency of 94%.Preliminary results show the suitability of the proposed route for the treatment and reuse of vinasse.The MF was effective to separate the effluent into two fractions, a retentate rich in suspended solidsand a permeate with reduced organic loading. The MBR was also able to remove significantly theCOD of the MF permeate. The unit monitoring will continue for more three months.[1] VAN HAANDEL, A. C. Integrated energy production and reduction of the environmental impact atalcohol distillery plants. Water Science and Technology. v. 52(1-2), p. 49-57, 2005.[2] SIMÕES, C.L.N; SENA, M.E.R.; CAMPOS, R. Estudo da viabilidade econômica da concentração devinhoto através de osmose inversa. XXIV Encontro Nac. de Eng. de Produção. Florianópolis, SC, Brasil,2004.

AcknowledgementsThe authors acknowledge the financial support provided by CNPq and FAPEMIG.

Treatment of Dairy Wastewater for Water Reuse: Membrane Bioreactor andNanofiltrationLaura Hamdan de Andrade 1 *, Flávia Danielle Santos Mendes 1 , Jonathan CawettiereEspindola 1 , Ariane Priscila Cota¹, Míriam Cristina Santos Amaral 11 Department of Sanitary and Environmental Engineering, Federal University of Minas Gerais.* Corresponding author: Av. Antônio Carlos, nº 6627 - Pampulha - Belo Horizonte – Minas Gerais –Brazil. Telephone: +55 (31) 34093669; Fax: +55 (31) 34091879; Email: lauraha@ymail.comAmong the food industries, the dairy industry is considered the most polluting one because of thelarge volume of wastewater generated and its high organic load [1]. Water reuse has become anincreasingly viable option for industries and one of the most promising technologies for wastewaterreclamation is membrane separation process and the combination of these systems with othertechnologies, such as membrane bioreactors (MBR) [2].Therefore, the aim of this study was to evaluate the application of MBR and nanofiltration (NF) forthe treatment of dairy wastewater, aiming at the reuse of the treated effluent.The wastewater used in this study came from a large dairy industry located in the state of MinasGerais, Brazil. Bench scale aerobic MBR and NF system were used for the experiments. The MBR wasequipped with a hollow fiber submerged microfiltration module. The operating conditions were:hydraulic retention time of 6 hours, solids retention time of 60 days, permeate flux and flow rate of18 L/h.m² and 0.80 L/h. The MBR permeate was passed through NF in order to generate final treatedwastewater with quality for reuse. It was used a NF90 commercial membrane from Dow-Filmtec. Thefeed flow rate was 7.8 m/s and pressure was 10 bar.The MBR operated with a mean MLVSS concentration of 19,500 mg/L. The system showed highcapacity for organic matter, color and nutrients removal (Table 1).Table 1 – Mean values of the physicochemical parameters of feed and permeate and the removalefficiencies of the MBR.ParametersRaw effluentMBRpermeate% RemovalCOD (mg/L) 2937 57 97.9%Color (Hu) 2316 27 98.7%Total nitrogen (mg/L) 50 7 86.1%Ammonia nitrogen (mg/L) 43 2 96.0%Phosphorus (mg/L) 36 2 89.0%Total solids (mg/L) 3,366 1,647 45.7%For NF, the effluent permeability (2,4 L/h.m².bar) corresponded to 97% of the clean membrane waterpermeability, indicating low fouling. The system also presented high pollutants removal efficiency(Table 2).

Table 2 – NF feed and permeate quality and retention efficiencies.Parameter Feed NF permeate % RetentionConductivity (mS/cm) 2.28 0.151 93.4%Color (Hu) 36.8 3.3 91.0%Total solids (mg/L) 1.482 488 67.1%Total organic carbon (mg/L) 24.9 0.5 97.9%Figure 1 presents the final result of the treatment path tested.Dairy WastewaterCOD = 3274 mg/LColor = 1802 Pt-Co unitsTS = 2323 mg/LNFMBR PermeateCOD = 34 mg/LColor =35,5 Pt-Co unitsTS = 1783 mg/LNF PermeateCOD = 4,0 mg/LColor = 15,0 Pt-Co unitsTS= 233 mg/LMBRNF RetentateCOD = 73,4 mg/LColor = 75,1 Pt-Co unitsTS = 3087 mg/LFigure 1 – COD, color and total solids of the MBR feed and permeate, and NF concentrate andpermeate.The quality of the NF permeate meets the standards for cooling water and water for low pressuresteam generation, enabling its reuse for such applications, as well as for washing floors, externalareas and trucks, which require a lower quality water.[1] M. Vourch, B. Balannec, B. Chaufer, G. Dorange (2005) Nanofiltration and reverse osmosis of model processwaters from the dairy industry to produce water for reuse, Desalination, 172, 245-256.[2] D. Bixio, C. Thoeye, J. De Koning, D. Joksimovic, D. Savic, T. Wintgens, T. Melin (2006) Wastewater reuse inEurope, Desalination, 187, 89–101.AcknowledgementsThe authors acknowledge the financial support provided by CNPq and FAPEMIG.

Membrane Bioreactor Applied to Treatment of Macaúbas Landfill LeachateMíriam Cristina Santos Amaral*, Wagner Guadagnin Moravia*, Mariana Moreira Zico**,Túlio Luís dos Santos**, Natalie Cristine Magalhães**Federal University of Minas Gerais (UFMG), **Federal Center for Technological Education of MinasGerais (CEFET-MG). miriam@desa.ufmg.brI- INTRODUCTIONThe leachate is the liquid resulting from the decomposition of waste in a landfill and it is a complexeffluent with high contents of organic and inorganic compounds [1,2].To improve the quality of the treated effluent through a biological treatment, an alternative is theuse of bioreactors with membranes (MBR), which has a better efficiency and removal of organicmatter if compared to conventional processes [3].This paper aims at framing the effluent according to current legislation and the possibility of reusingwater, through biological treatment combined with membrane separation processes.II-METHODOLOGY AND RESULTSThe treatment consists on the association of the stripping process of ammonia with MBR andnanofiltration as a polishing.The raw leachate from landfill Macaúbas has a high concentration of organic matter in terms of COD,about 3520 ± 750 mg/L (Figure 1). After the process of stripping of ammonia the value of CODleachate was increased to 4163 ± 828 mg/L. This increase may be related to the concentration of theorganic matter due to the evaporation process in the stripping operation.It is observed that after the leachate has passed through the biological treatment and the MBR tank,the value of COD of permeate was 2392 ± 951 mg/L. This step of biological treatment associated withthe MBR showed a mean removal of COD of 44 ± 18%. After the nanofiltration the permeate had adecrease of COD (482 ± 223 mg/L), which represents a removal of 82 ± 8% of organic matter (Figure2). Therefore, it is observed that this system showed a global mean removal of 87 ± 6% of organicmatter in terms of COD (Figure 3).

COD Feed (mg/L)COD Feed (mg/L)COD Permeate (mg/L)COD Permeate (mg/L)Raw Leachate Post Stripping Leachate Permeate60005000400030002000100008000700060005000400030002000100000 20 40 60 80 100 120 140 160 180 200 220Operation Time (days)Figure 1 – COD values according to the operation time of MBR.500040003000200010000MBR Permeate NF Permeate0 5 10 15 20 25 30 35 40 45 50Operation Time (days)1400120010008006004002000Figure 2 – COD values according to the operation time of nanofiltration (NF).

COD Removal (%)MBR Removal NF Removal Global Removal1009080706050403020100120 140 160 180 200 220Operation Time (days)Figure 3 – Global removal of COD throughout the treatment process of the landfill leachateMacaúbas.III-CONCLUSIONThe results showed that the use of BRM for the treatment of leachate from the landfill Macaúbaswas effective, removing much of the organic matter. By associating the MBR with nanofiltrationprocess for polishing the effluent it was obtained a global COD removal of 87 ± 6%. Moreover, theresulting permeate COD showed a value less than the amount required by law for the discharge ofeffluents into water bodies, according to Resolution No. 430, of May 13, 2011 of the National Councilfor the Environment - CONAMA [4].IV-ACKNOWLEDGEMENTSThe authors acknowledge the financial support provided by CNPq, CAPES and FAPEMIG and thesupport given by the Department of Sanitary and Environmental Engineering-DESA at UFMG.V- REFERENCES[1] EL-FADEL, M.; BOU-ZEID, E.; CHAHINE, W.; ALAYLI, B. Temporal variation of leachate quality from pre-sortedand baled municipal solid waste with high organic and moisture content. Waste Management, v.22, p.269-282,2002.[2] KJELDSEN P. I.; BARLAZ, M. A; ROOKER, A. P.; BAUN, A.; LEDIN, A.; CHRISTENSEN, T. H. Present and longtermcomposition of MSW landfill leachate: a review. Environmental Science and Technology, v.32, p.297-336,2002.[3] BUISSON, H.; COTE, P.; PRADERIE, M.; PAILLARD, H. The use of membranes for upgrading wastewatertreatment plants. In.: IAWQ CONFERENCE ON UPGRADING OF WATER AND WASTEWATER SYSTEM. Kalmar,1997.

[4] RESOLUTION Nº 430, OF MAY 13, 2011 – NATIONAL COUNCIL FOR THE ENVIRONMENT – CONAMA. Officialwebsite of the Ministry of Environment (http:// www.mma.gov.br). Accessed in July 2011.

Treatment of an Effluent from a Galvanizing Industry containing Chromiumand Zinc by Liquid Surfactant Membranes TechniqueVanesa da Silva Oliveira 1 , Fabrício Eduardo Bortot Coelho 1 , Julio Cézar Balarini 1,Estêvão Magno Rodrigues Araújo 1 , Cibele Konzen 1 , Adriane Salum 1 ,Tânia Lúcia Santos Miranda 1 *1 Universidade Federal de Minas Gerais, Chemical Engineering Department*tania@deq.ufmg.brThe galvanizing industry is responsible for the generation of a great amount of liquid effluents rich inheavy metals, including the ion Cr 6+ . According to CONAMA (Conselho Nacional do MeioAmbiente)[1], a Brazilian environmental agency, the permissible level to discharge Cr 6+ in the effluentis up to 0.1 mg/L. For this reason, it is indispensable for the galvanizing industries to treat theireffluents by using separation techniques in order to comply with the environmental regulations.Among the different methods used for the Cr 6+ removal, the liquid surfactant membranes (LSM)receive a special attention. Usually the LSM process has high extraction capability, high selectivity,especially in extraction of solutes from dilute solutions [2]. Considering the foregoing, the aim of thiswork was the determination of the extraction conditions of Cr 6+ by using LSM technique in order toreduce its concentration in the studied solutions. Initially, a synthetic solution of K 2 Cr 2 O 7 (353 mg/Lof Cr 6+ ) was investigated, and afterwards the same was done with a real effluent from a galvanizingindustry (77.4 mg/L of Cr 6+ and 1494 mg/L of Zn 2+ ) at the conditions established from the first study.It is worth to emphasise that the amount of chromium in the galvanizing effluents is variable, and thequantity of this metal in the synthetic solution and in the investigated effluent, both studied in thepresent work, is consistent with typical values. The membrane phase (MP) consisted of Alamine 336,the surfactant ECA 4360, 1-decanol and Escaid 110 and the internal phase is a KOH solution. In thebatch permeation tests with the synthetic solution, the influence of the following variables wasstudied: pH of the external or feed phase (EP); KOH concentration in the internal phase (IP); carrierconcentration in the MP and temperature. At the best operational conditions (carrier concentration= 5% w/w, pH = 1.5, temperature = 25°C and KOH concentration in the IP = 0.6 mol/L), 98% ofchromium were extracted from the external phase in a single stage. As a result, the final feed phasereached the concentration of 13 mg/L of Cr 6+ . In an attempt to comply the environmental laws, theprocess was conducted in three stages, reaching the concentration of 0.27 mg/L of Cr 6+ in the finalexternal phase. A decrease in the percentage of extraction of Cr 6+ (84%) and an extraction of 4% forZn 2+ was observed when the real effluent was used under the same operational conditions in a singlestage and pH 1.5. Moreover, if the pH of the external phase is lowered to 1.0, it is possible toselectively extract Cr 6+ compared to Zn 2+ (90% and 0%, respectively), and higher concentrations of H +(2.0 mol/L of HCl) allowed the extraction of 95% of Cr 6+ and 60% of Zn 2+ . Thus the use of the samereagent (Alamine 336) permits the selective extraction by varying the pH of the external phase.Firstly zinc is extracted, and, then chromium is extracted at higher pH values.[1] BRASIL, resolução CONAMA 430, 13 maio 2011, Conselho Nacional de Meio Ambiente - CONAMA – 2011.[2] PATNAIK, P. R. Liquid Emulsion Membranes: Principles, problems and application in fermentation processes.Biotechnology Advances, v. 13, nº 2, p. 175-208, 1995.

Synthesis and characterization of membranes made of Chitosan and Polyvinylalcohol blends for gas separationAlan Ambrosi*, Vanessa Finkler Caputo, Nilo Sérgio Medeiros Cardozo, Isabel CristinaTessaroLaboratory of Membrane Separation Processes (LASEM) – Department of Chemical Engineering –Federal University of Rio Grande do Sul - UFRGSaambrosi@enq.ufrgs.brThe removal of carbon dioxide from methane in natural gas (NG) is a featuring process in themembrane-based gas separation processes, growing significantly over the years due to the increasingdemand, which requires the increase of NG quality. Raw NG composition varies substantially fromsource to source; methane is the major component with more than 70% of the total, conferring highenergy power to the gas. Moreover, it can contain significant quantities of ethane, propane, butaneand other heavier components, besides water, carbon dioxide, nitrogen and hydrogen sulfide [1].Natural gas requires a process of purification or treatment to meet the standards andspecifications of the pipeline and the major application of membrane processes in this field is thecarbon dioxide removal. The presence of CO 2 reduces the calorific capacity of natural gas; also CO 2 ishighly corrosive, freezes at relatively high temperatures and may cause damage to pipelines andpumps [1, 2].Membranes employed in the separation of gas mixtures are usually polymeric and it is wellknown that there is a trade-off between the permeability and selectivity of gases, since theseparation factor generally decreases with the permeability increase to the more permeablecomponent. This occurs because of the differences in mobilities of each permeant through thepolymeric matrix [3, 4]. The performance of current polymeric membranes has reached a level ofstagnation in which is hard to achieve a significant improvement. Thus, the study of mixed matrixmembranes, where deficiencies of an individual material can be overcome with the blending ofmaterials with different properties, has been well accepted.Chitosan (CH) and Polyvinyl Alcohol (PVA) are polymers studied with success in the synthesis ofpervaporation membranes for the separation of water and organic compounds, as alcohols [5-11].Pervaporation and gas permeation processes have similarities, as membrane morphology andtransport mechanism, which makes the investigation of using CH/PVA blends for the gas separation apromising study.In this work, CH/PVA blends with proportions of 9:1 and 1:9 were prepared to synthesizedense membranes for gas separation. Maleic acid and acetaldehyde were used as crosslink agents toimprove membrane characteristics. Permeabilities of pure N 2 , CO 2 and CH 4 gases, determined in abench scale unit, and membrane morphology, observed by Scanning Electron Microscopy, werestudied to evaluate permeation properties of membranes, as permeance and selectivity.Preliminary results showed high variation of membranes performances: permeance variedfrom 0.0073 to 107.89 GPU for CO 2 , 0.007 to 87.77 GPU for CH 4 and 0.0055 to 54.87 GPU for N 2 . Bestresults were obtained for the membrane with composition of 9:1 wt. of CH:PVA cross-linked with

acetaldehyde, which presented selectivity of 2 for the pair CO 2 /N 2 and 1.2 for the pair CO 2 /CH 4 .[1] R.W. Baker, K. Lokhandwala (2008), Natural Gas Processing with Membranes: An Overview, Ind.Eng. Chem. Res., 47, 2109-2121.[2] D. Dortmundt, K. Doshi (1999), Recent developments in CO2 removal membrane technology, in,UOP LLC, Des Plaines, Illinois, 31.[3] L.M. Robeson (2001), Polymeric Membranes for Gas Separation, in: K.H.J. Buschow, W.C. Robert,C.F. Merton, I. Bernard, J.K. Edward, M. Subhash, V. Patrick (Eds.) Encyclopedia of Materials: Scienceand Technology, Elsevier, Oxford, 7629-7632.[4] L.M. Robeson (2008), The upper bound revisited, J. Membr. Sci., 320, 390-400.[5] FENG, X., HUANG, R. Y. M. (1996), Pervaporation with chitosan membranes. I. Separation of waterfrom ethylene glycol by a chitosan/polysulfone composite membrane. J. Memb. Sci., v. 116., p. 67-76.[6] WANG, X.P., et al. (1996), A novel composite chitosan membrane for the separation of alcoholwatermixtures. J. Memb. Sci., 119, 191-198.[7] HUANG, R. Y. M., PAL, R., MOON, G. Y. (1999), Cross-linked chitosan composite membrane for thepervaporation dehydration of alcohol mixtures and enhancement of structural stability ofchitosan/polysulfone composite membranes, J. Memb. Sci., 160, 17-30.[8] BURSHE, M. C., et al., (1997), Sorption and permeation of binary water-alcohol systems throughPVA membranes crosslinked with multifunctional crosslinking agents, Sep. Pur. Tech., 12. 145-156.[9] NAM, S. Y., LEE, Y. M., (1999), Pervaporation separation of methanol/methyl t-butyl ether throughchitosan composite membrane modified with surfactants, J. Memb. Sci., 157, 63-71.[10] HYDER, M. N., CHEN, P., (2009), Pervaporation dehydration of ethylene glycol with chitosan–poly(vinyl alcohol) blend membranes: Effect of CS–PVA blending ratios, J. Memb. Sci. , 340, 171-180.[11] ZHANG, W., et al., (2010), Improving the pervaporation performance of the glutaraldehydecrosslinked chitosan membrane by simultaneously changing its surface and bulk structure, J. Memb.Sci., 348, 213-223.

Ultrafiltration/Nanofiltration for Polyphenols Recovery in Winery EffluentsAlexandre Giacobbo 1,2 , Andréa Moura Bernardes 1 , Maria Norberta de Pinho 2,*1 Programa de Pós-Graduação em Engenharia de Minas, Metalúrgica e de Materiais(PPGE3M), Universidade Federal do Rio Grande do Sul (UFRGS), Porto Alegre, Brazil.alexandre_giacobbo@yahoo.com.br, amb@ufrgs.br.2 Instituto de Ciência e Engenharia de Materiais e Superfícies (ICEMS), Instituto SuperiorTécnico, Technical University of Lisbon, Lisbon, Portugal. marianpinho@ist.utl.pt.The winemaking process involves two operations of solids separation that are designated by first andsecond racking. They generate large volumes of effluents with high fractions of suspended solids anda high pollutant charge. The present work addresses the treatment of the effluents from the secondracking that have a total solids content of 17.7 g L -1 and a chemical oxygen demand of 27.6 g L -1 withthe simultaneous recovery of polyphenols. For that, a sedimentation pre-treatment is followed bytwo ultrafiltration operations.The first ultrafiltration (UF) is carried out in a Lab-Unit M20 from Alfa Laval – Denmark, with aGR95PP membrane with molecular weight cut-off (MWCO) of 7.6 kDa, 0.072 m² of membranesurface area at the transmembrane pressure of 4.0 bar and at the feed circulation velocities of 0.87m s -1 [1]. The UF is run in concentration mode up to a concentration factor of 2 to yield 5 L ofpermeate. This is the feed of a second UF that is carried out in a flat sheet cell [2] with an ETNA01PPmembrane with MWCO of 1 kDa and a membrane surface area of 13.2 cm 2 . The transmembranepressure is 20 bar which is a value in the range of nanofiltration.The UF permeates of the first operation have a total polyphenols content of 53 mg L -1 (gallic acid) andits processing in the second UF operation yields permeate fluxes of 106 kg h -1 m -2 with a 72% passageof the polyphenols to the permeate stream.References[1] A. Giacobbo, M. Oliveira, H. Mira, E. Duarte, A. M. Bernardes, M. N. Pinho (2013), Ultrafiltration BasedProcess for the Recovery of Polysaccharides and Polyphenols from Winery Effluents, Separation Science andTechnology, 48, 438-444.[2] M. D. Afonso, M. N. Pinho (1990), Ultrafiltration of bleach effluents in cellulose production, Desalination,79, 115-124.

Influence of the pH on the Recovery by Electrodialysis of Zirconium andFluoride from Wastewaters of Nanoceramics Process.Carolina de Moraes da Trindade 1, *, Vicente Guedes Ferreira 1 , Andréa Moura Bernardes 11 Universidade Federal do Rio Grande do Sul (UFRGS), PPGE3M*cmtrindade@yahoo.com.brThe industrial application of nanoceramic coatings is increasing because they are free ofpotentially toxic components, present fewer steps and are performed at room temperature, thuspresenting lower energy consume. The nanoceramic is a pre-treatment of the metal surface,obtained by a conversion reaction which results in a protective oxide. The process is based onhexafluorzirconium acid [1]. Considering that this is a process applied for less than ten years in theworld market, there is not a systematic study of the treatment for generated effluents. Therefore,this work attempted to perform the recovery of chemicals from the bath and water through theelectrodialysis process (ED).A laboratory electrodialysis cell made of five compartments acrylic cell with ion exchangemembranes, cationic and anionic, arranged alternately, was used for the tests. The working solutionwas an acidified nanoceramic bath. Sodium sulfate was used as conductive solution for ED. Duringthe ED tests pH and conductivity were monitored in order to assess the influence of theseparameters on the efficiency of the treatment.At ED occurs the migration of ions from one compartment to another and the formation ofH + and OH - , promoting pH changes of the whole system. Any small change in the pH of the workingsolution produces the formation and precipitation of hydrolysaded Zr compounds [2], as it is show onthe Figure 1. This precipitation, besides hindering the recovery of Zr in the solution, also preventesthe recovery of F - , since the channels of the ion exchange membranes were clogged. Thus, the pHcontrol is an extremely important parameter to be controlled, if ED is to be used on the treatment ofnanoceramic effluents.Figure 1: Behavior of chemical species Zr and F outside a pHrange of 0 to 14 (Hidrameduza Software).REFERENCES[1] DRONIOU, P., Nanoceramic-based conversion coating: ecological and economic benefits position process asa viable alternative to phosphating system. Organic Finishing. 2005.[2] JORGENSEN, K. Inorganic Complex. Academic Press. 220p. London. 1963.

Preparation of Electrodialysis Membranes Applied for Metal Recuperationfrom Eletronic WasteTatiane Benvenuti 1* , Thaís Macedo 2 , Guilherme Lazzaretti 2 , Aline de Moura Reis 2 , Raquel SantosMauler 3 , Fabrício Celso 2 , Marco Antônio Siqueira Rodrigues 1,21Programa de Pós-Graduação em Engenharia de Minas, Metalúrgica e de Mateiais - UFRGS – RS*(tati.eng.biobio@gmail.com)2Instituto de Ciências Exatas e Tecnológicas - Universidade Feevale – RS3Instituto de Química - UFRGS – RSIn this work two membranes based on sulfonated poly (ether ether ketone) (SPEEK) were preparedand applied in electrodialysis with the aim of evaluate the performance of SPEEK membranes inmetallic ions transport.SPEEK was prepared by PEEK sulfonation using sulfuric acid [1, 2] due to easy of functionalization to adesired sulfonation degree (SD) and promissing properties when used to cast membranes [3, 4].Membranes were obtained by dissolving SPEEK in n-methilpirrolidone (NMP) and casted onto a glassplate. In this work were used SPEEK of SD 56 and 67.Conductivity was calculated from resistivity measurements using a potentiostat in scanningfrequency mode in the range of 10 Hz to 1 MHz, at room temperature and 100% R.H. As shown inFigure 1, it can be noticed that membrane conductivity raise with increase on SD, once at humidifiedmedia there is a direct relationship of ionic conductivity and sulfonic acid amount available toperform the ionic transport. [5].Figure 1. Conductiovity of evaluated membranes in compasion with Nafion 117 commercial membrane.

Electrodialysis (ED) consists in an electrochemical technique that applies ion-selective membranes asseparation agents [6]. SPEEK membranes were applied in ED to treatment of a solution deriving fromleaching out of metal rich printed circuit boards. The ED cell used in this work is built in fivecompartments separated by alternating cationic and anionic membranes, each with area of 16 cm 2 .SPEEK cationic membranes of SD 56 and 67 were used together with commercial HDX anionicmembranes. As conductive solution was used Na 2 SO 4 1gL -1 and as electrodes, titanium plates(Ti/Ti0.7Ru0.3) De Nora® of 16 cm 2 . A constant potential of 5 V was applied during 17 h, periodicallymonitoring solution pH and conductivity. After ED treatment, solutions were analyzed by flameatomic absorption spectroscopy to metal quantification, allowing comparative evaluation ofefficiency between membranes of the two SD prepared in laboratory. Figure 2 shows the expectedtransport of the species in solution.Figure 2. Expected transport of the species in solution (Where: M x+ indicates Metals; A and C areanion and cations exchange membranes, respectively).Evaluated metals showed in Table 1 are arranged in decreasing order of concentration from theprinted circuit boards solution. Sn presented higher transport to SPEEK membranes, followed by Ag.Except to Cu, SPEEK membrane of 67 SD performed higher metal transport.Table 1. Metal transport measured for each membrane according to SD.MetalEvaluated MembranesSPEEK SD=67%SPEEK SD=56%Cu 0.09% 0.20%Sn 1.93% 1.45%Ni 0.38% 0.21%Ag 1.93% 1.06%Considering that the SPEEK membranes prepared in laboratory were made firstly to protonic (H + )transport and here is described the first attempt to characterise them to electrodialysis applicationwith no specific preparation to such condition. Another properties and formulation of thesemembranes will be studied to anable it application in electrodialysis.References[1] S.D. Mikhailenko; K.P. Wang; S. Kaliaguine; P. Xing; G. Robertson; M.D. Guiver (2004) J. Membr. Sci. 233, 93.[2] S.D. Mikhailenko; G. Robertson; M.D. Guiver; S. Kaliaguine (2006) J. Membr . Sci. 285, 306.[3] S. Bose; T. Kuila; T.X.H. Nguyen; N.H. Kim; K.T. Lau; J.H. Lee (2011) Prog. Polym. Sci.36, 813.

[4] E. Sgreccia; M.L. Di Vona; P. Knauth (2011) Int. J. Hydrogen Energy 36, 8063.[5] S.M. Javaid Zaidi (2003) Polymer Sulfonation – A Versatile Route to Prepare Proton-Conducting MembraneMaterial for Advanced Technologies. The Arabian J. Sci.& Eng. 28 (2B), 183-194[6] T. Benvenuti; G. Haubert; G. Fensterseifer Jr.; M.A.S. Rodrigues; A.M. Bernardes; J. Zoppas Ferreira; (2012)Electrodialysis for the nickel electroplating industry from Sinos River Basin. In: 3 rd International Conference onIndustrial and Hazardous Waste Management, Chania. 3rd International Conference on Industrial andHazardous Waste Management. Chania, Creta: Technical University of Crete, Greece.

Evaluation of Ion-Selective Membranes in the Electrodialysis for Treat NickelPlating EffluentTatiane Benvenuti 1, *, Marco Antônio SiqueiraRodrigues 2 , Andréa Moura Bernardes 1 , Jane Zoppas Ferreira 11 Universidade Federal do Rio Grande do Sul (UFRGS), PPGE3M2 Centro Universitário FEEVALE, ICET*tati.eng.biobio@gmail.comThe electrodialysis (ED) is becoming a good alternative, when it is compared to the traditionaltreatments for electroplating effluent, because it presents the advantage of allowing the recoveryand reuse of water and chemicals used in the process [1,2].This work addresses the ED treatment of a bright nickel electroplating effluent, comparing theeffectiveness of different membranes: Italian Membranes Resindion IONAC® MA-3475 (anionic) andMC-3470 (cationic) membranes in ED1 test, as well as Chinese membranes HDX 100 (cationic) andHDX 200 (anionic) provided by HIDRODEX (Brazil) in ED2 test.Electrodialysis systems were compared under similar operating conditions: current density of2.8mA.cm -2 and time of 240 h for treat real and synthetic nickel effluent (E). The ED system and theexpected transport for ions are presented in the Figure 1.Figure 1. Expected ion flux during the ED process.Table 1 shows the results obtained for Ni extraction (%pe) and concentration (%pc) in the ED.

Table 1. Evaluation of solutions obtained after 240h of ED for the treatment of real and syntheticnickel effluent.Solution Parameter ED1 Real ED1 Synthetic ED2 Real ED2Synthetic%pe 41% 74.9% 69.6% 88.9%ETransport rate 49.3 42.8 71.64 30.4(mg(h.A) -1 cm -2 )PPT** No Yes No YesCC PPT Yes No No No46.3% 54.6% 53.8% 88.9%AC 0.06% 0.13% 0.19% 0.20%%pcAn 0.006% 0.29% 0.01% 0.18%Cat 0 0 0 0.01%**Precipitated material.Regarding the extraction, both membranes were effective, but pH control was the key factor forjustifying differences between the tests. The pH monitoring indicated a large pH variation in theeffluent and CC solutions and it led to the formation of nickel precipitate on the membranes, whichprejudice the Ni transportation. Then, the pH control is required.It was verified that both anionic membranes let the transport of low Ni concentrations to the anionconcentrated compartment (AC) and to the anode one (An). This unexpected transport by anionicmembranes seams to be related to the effluent composition instead of the possible failure in themembranes selectivity. Future studies should consider the composition of the effluent to identify thereasons for this transport.REFERENCES[1] K. Dermentzis. Removal of nickel from electroplating rinsewaters using electrostatic shieldingelectrodialysis/electrodeionization. J. Hazard. Mater. 173 (2010) 647–652.[2] M. A. S. Rodrigues, F.D.R. Amado, J. L. N. Xavier, K. F. Streit, A. M. Bernardes, J. Z. Ferreira. Application ofphotoelectrochemical-electrodialysis treatment for the recovery and reuse of water from tannery effluents J.Clean. Prod. 16 (2008) 605-611.ACKOWLEGMENTSThe authors thank CAPES and CNPq- Brazil for financial support.

Characterization of Poly (ether imide) Microfiltration MembraneCarine Pertile 1* , Camila Baldasso 2 , Mara Zeni 2 , Isabel C.Tessaro 11 Chemical Engineering Department, Federal University of Rio Grande do Sul (UFRGS)2 Center of Exact Sciences and Technology, Caxias do Sul University (UCS)*e-mail: carine.pertile@gmail.comCrossflow microfiltration (MF) is widely used as a polishing step in leachate treatment [1].Informations of membrane characteristics such as permeability have direct effects on the processefficiency. The evaluation of compaction characteristics of the membrane avoids experimentsinterpretation errors, because compacting effects could be confused with others phenomena thatcould cause flux reduction, such as concentration polarization and fouling.The aim this work is to characterize the MF membrane by water permeability, compaction existenceand retention measurements.A commercial MF poly (ether imide) membrane, supplied by PAM Membranas Seletivas with100 kDa and effective membrane area of 0.064 m 2 was characterized with different solutions ofdextrans.Experiments were performed to evaluated water permeability, compaction and retention. Distilledwater flux was measured as a function of transmembrane pressure (0.5 to 1.4 bar) at the followingconditions: temperature of 25°C and crossflow velocity of 8.9 m s -1 . The compaction was alsodetermined by maintaining the transmembrane pressure at 1.5 bar until a constant permeate fluxwas achieved. In these tests a total recycle operating mode was adopted.In order to investigate membrane retention characteristics, different solutions of dextran withmolecular weights of 150, 200 and 500 kDa, supplied by Sigma Chemicals, were recirculated throughthe system. The observed retention was calculated by determining of the soluteconcentrations in the feed solution and in permeate stream.Experimental results revealed that the water permeate flux increased linearly with the increase oftransmembrane pressure. The pure water permeability, obtained by linear regression was95.89 L m -2 h -1 bar. The higher membrane permeability could be attributed to hydrophiliccharacteristics.Compaction test showed flux reduction from 296 L m -2 h -1 to 187 L m -2 h -1 , which represents anaverage reduction of 37%. The results show a highly asymmetric and compactable structure. Theretention, at operating pressure of 0.5 bar, was 43%, 59% and 66% for dextran with molecularweights of 150, 200 and 500 kDa, respectively. It was also observed the decrease in dextranobserved retention coefficients with increasing transmembrane pressure probably due to theincrease of concentration polarization.[1] L. M. Diniz, L. H. Andrade, T. L. Manssula, E. P. Rocha, M. C. S. Amaral, L. C. Lange, M. Machado (2012),Advanced oxidation process associated with membrane separation for the treatment of sanitary landfillleachate, Procedia Engineering 44, 1951–1955.

Concentration of ovine cheese whey proteins by ultrafiltration/diafiltrationNataly Leidens 1 *, Camila Baldasso 2 , Isabel Cristina Tessaro 1 .1 Universidade Federal do Rio Grande do Sul, 2 Universidade de Caxias do Sul.*natalyleidens@yahoo.com.brWhey is the remaining liquid of the cheese manufacture and it contains about 50 % of the milkconstituents, including proteins, lactose and minerals. To produce 1 kg of cheese, 5 L of ewe’s milk isrequired, generating 4 L of whey [1] [2] .In comparison to bovine whey, the ovine whey has a higher content of proteins, being a potentialsource of these components for the formulation of several foods [3] . One promising technology forconcentration and fractionation of cheese whey constituents are the membrane separationprocesses [4] [5] [6] .Aiming the use and development of new products from the ovine cheese whey, experiments wereconducted to concentrate the whey proteins by ultrafiltration/diafiltration (UF/DF). In this system,lactose, minerals and water permeate through the membrane while the proteins are retained. Thecontent of lactose and minerals in the concentrate can be reduced by DF, where water is added andthese smaller constituents are removed to the permeate [5] [7] [8] .The ovine cheese whey was supplied by Confer Alimentos (Viamão, RS) and has pH of 6.1 and totalsolids, protein and lactose concentration of 71.8 g.L -1 , 10.5 g.L -1 and 54.7 g.L -1 , respectively.In the UF experiment, it was used a spiral module membrane manufactured by Koch MembraneSystems with MWCO of 10 kDa and permeation area of 0.28 m 2 . The permeation of whey was carriedout at a transmembrane pressure of 3 bar, since above this value the limit flux was reached, andtemperature of 50 °C, which is adequate for the processing of whey [9] .The whey (12 L) was recirculated in the feed tank until a volumetric concentration factor of 4 wasreached. After the UF stage, 2 DF were applied using 1.3 L of water each. The permeate flux wasmeasured each 15 minutes and samples of concentrate and permeate were collected each 30minutes for the analysis of pH, total solids content, protein and lactose concentration.The results revealed that the permeate flux decreased with the time of the operation and with thevolumetric concentration factor, as in other studies [9] [10] [11] ; the initial flux was 20.1 L.m -2 .h -1 , itdropped to 9.85 L.m -2 .h -1 at the end of the UF stage and, at the end of the second DF, the final fluxwas 3.35 L.m -2 .h -1 . The reduction of the permeate flux was due to the fouling and concentrationpolarization phenomena [10] .In Fig. 1 is shown the concentrate protein and lactose content on dry basis versus time during thestages of UF and DF.

Fig. 1. Concentrate protein and lactose content on dry basis versus time during the UF/DFexperiments.In the beginning of the experiment, the protein content of the concentrate was 14.7 %; at the end ofthe UF, it increased to 32.5 % and after the second DF, the final protein concentration was 42.7 %.The content of lactose dropped in the stage of UF, from 76.1 % to 60.9 %; during the DF this valuewas further reduced to 46.3 %. Concerning to the permeate protein concentration, the values weresignificantly low, showing that proteins were completed retained by the membrane.From this study it can be concluded that the concentration of ovine cheese whey proteins can beachieved using the process of UF/DF, however other experiments using different conditions andmembranes should be tested to optimize the fractionation of whey components.[1] G. Bylund (1995), Dairy processing handbook, Tetra Pak Processing Systems.[2] Y. Berger; P. Billon; F. Bocquier; G. Caja; A. Cannas; B. Mckusick; P. Marnet; D. Thomas (2004), Principles ofsheep dairying in North America, Cooperative Extension Publishing: University of Wisconsin.[3] B. Hernández-Ledesma; M. Ramos; J.A. Gómez-Ruiz (2011), Small Ruminant Research, 101, 196-204.[4] Z.T.C. Leite; D.S. Vaitsman; P.B. Dutra (2006), Química Nova, 29, 876-880.[5] A.L. Zydney (1998), International Dairy Journal, 8, 243-250.[6] A.S. Jönsson; G. Trägardh (1990), Desalination, 77, 135-179.[7] G. Brans; C.G.P.H. Schroën; R.G.M Van der Sman; R.M. Boom (2004), Journal of Membrane Science, 243,263-272.[8] A.D. Giraldo-Zuñiga; J.S.R. Coimbra; J.C. Gomes; L.A. Minim; E.E.G. Rojas; A.D. Gade (2004), Rev. Inst. Latic.“Cândido Tostes”, 59, 53-66.[9] R. Atra; G. Vatai; E. Bekassy-Molnar; A. Balint (2005), Journal of Food Engineering, 67, 325-332.[10] A. Macedo; E. Duarte.; M. Pinho (2011), Journal of Membrane Science, 381, 34-40.

[11] A. Chollangi; M. Hossain (2007), Chemical Engineering and Processing, 46, 398-404.

Quality Evaluation of Jaboticaba (Myrciaria Jaboticaba) Juice Concentrated byForward OsmosisVoltaire Sant’Anna, Poliana Deyse Gurak, Natieli Souza de Vargas, Mauricio Kipper da Silva*,Ligia Damasceno Ferreira Marczak, Isabel Cristina TessaroMembrane Separation Laboratory, Chemical Engineering Department, Universidade Federal do RioGrande do Sul, Porto Alegre, Brazil. Email: kippertt@yahoo.com.br.Jaboticaba (Myrciaria jaboticaba) is a Brazilian native plant and cultivated all over the country. Thefruit has a dark, thin and fragile skin, with a white pulp slightly acid and sweet, which presents anadstringent flavor. This natural source has a high nutrition value that comes from polyphenols,vitamins and minerals. Thermal processing is still widely employed in the field of preservation, shelflifeextension and concentration. However, heat treatments may cause a severe impact on nutritionvalue and organoleptic factors. Thereby, forward osmosis (FO) shows up as a promising membranetechnology, in which the osmotic pressure difference () between two solutions (feed and generallya brine solution) works as the only driven force. Thus, FO presents the advantages of working atroom temperature, no requesting of high hydraulic pressure, low fouling tendency and an ease scaleup.At this present work, the concentration of jaboticaba juice by FO was evaluated. Sodium chloridecomposed the draw solution because it is widely used in FO procedures, it is water-soluble, not toxic,non-expensive and presents high osmotic pressure. A 2 2 factorial design was used to analyze theeffect of the in the interval of 7.03-27.80 atm (the solutions flow rate in the range of 50-200 mL min -1 on the water) and the salt transmembrane flux performances. The process wasevaluated for 5 h, while temperature was kept at 25 o C. The water flux ranged between 2.36 and3.59 L m -2 h -1 , meanwhile salt flux, ranged about 63.2 to 384.2 mg Na m -2 h -1 . The statistical analysispointed that both process parameters have presented significant effect (p < 0.05) on the water flux,meanwhile only has affected (p < 0.05) the salt transport. Higher implies on enhance of waterand salt fluxes, the increase of the solution flow rate leads only to an increase of the water transport.Jaboticaba juice was concentrated up to a 2-fold concentration factor by FO and by thermal process(90 o C with vacuum of 50 mmHg), the quality of these beverages can be compared to the nonindustrializedjuice. In relation to the fresh juice, FO preserves the anthocyanin content, that wasmeasured in spectrophotometer, and the antioxidant properties, what can be proved by measuringthe scavenger activity of the ABTS. The fresh juice presents sodium content of 1.7 mg Na L -1 , while ahigh transport of sodium was observed in the reconstituted juice when concentrated by FO, reachingvalues of 12.9 mg Na L -1 . A thermal process for jaboticaba juice concentration implied on decrease ofanthocyanins and antioxidant activity, besides a change of coloration (a non-enzymatic browning anda decrease in the density and intensity of color). Results showed that FO presents high potential tobe used as an alternative to heat treatments in the food industry, although new researches mustevaluate other solutes to compose the draw solution, since a high content of sodium was transferredto the juice.

Biofilm Formation on Laboratory Nanofiltration MembranesFrancisca Pessoa de França * , Daniel Serwy Braz, Juliana Domingues Sampaio, Renata Oliveirada Rocha CalixtoEscola de Química - Centro de Tecnologia - Universidade Federal do Rio de Janeiro, RJ, Brasil,fpfranca@eq.ufrj.brThe filter membrane technology has been widely used in water treatment, however, theaccumulation of material on its surface known as inlay (6), resulting in the undesirable decrease ofthe flow, speed and pressure (4). The main cause of fouling is the adhesion of chemicals onmembrane surface (8,9) that was determined both by the membrane properties such ashydrophobicity, and chemical interactions of the substances in the flow (7,3,5). The biofouling and itseffects are observed through their initial processes, such as recognition of the location, explorationand surface adhesion by microorganisms. This colonization occurs through sensory structures at themolecular scale and it depends on the adhesion of chemicals in marine environments, promotinginitial formation of biofilm, composed by bacteria and microalgae (1). The biofouling occurs despitethe use of pre-treatment systems and the addition of disinfectants such as chlorine. Biofilmsoccurring in the membrane filtering systems can cause loss of performance of the process, oftenresulting in the use of cleaning procedures to maintain the quality and where the diaphragm isrequired in the process (2). The present work aimed to study the action of the formation ofbiofouling on the surface of laboratory nanofiltration membrane, taking into account the activity ofmicro-organisms present in seawater. Flat membranes produced were tested in the laboratorycontaining PVA. Assays were performed in a static system to verify biofilm formation in the samplesover a period of 8 days. Counts were made in water microbial groups used as inoculum at the start ofthe experiment. At the end of those 8 day new counts carried out to quantify microorganismsplanktonic and sessile. Results showed that there was biofilm formation in all samples tested,consisting of aerobic and anaerobic bacteria. Results also showed that the sample containing PVAmicrobial quantification is presented in smaller numbers, particularly for aerobic bacteria.Acknowledgments: The authors wish to thank CNPq, CAPES, CENPES/Petrobras for financial support.Referências:[1] A. Rosenhahn, S. Schilp, H. J. Kreuzer, M. Grunze. Phys. Chem. Chem. Phys., 12 (2010): 4275-4286.[2] J.S. Baker, L.Y. Dudley. Desalination 118 (1998): 81-90.[3] C. Bellona, J.E. Drewes. J. Membr. Sci., 249 (2005): 227–234.[4] K. Boussu, B. Van der Bruggen, A. Volodin, C. Van Haesendonck, J.A. Delcour, P. Van der Meeren, C.Vandecasteele. Desalination, 191 (2006): 245–253.[5] A.E. Childress, M. Elimelech. Environ. Sci. Technol., 34 (2000): 3710–3716.[6] D.B. Mosqueda-Jimenez, P.M. Huck, O.D. Bazu. Dessalination, 230 (2008): 79-91.[7] W.H. Peng, I.C. Escobar, D.B. White. J. Membr. Sci., 238 (2004): 33–46.[8] B. Van der Bruggen, C. Vandecasteele. Environ. Sci. Technol., 35 (2001): 3535–3540.[9] B. Van der Bruggen, L. Braeken, C. Vandecasteele. Desalination, 147 (2002): 281–288.

Synthesis of BaCeO3 Nanoparticle by EDTA-CitrateAngélica Belchior Vital 1* , André Luis Lopes-Moriyama², Carlson Pereira de Souza³1 Programa de Pós Graduação em Ciências e Engenharia de Materiais (PPGCEM-UFRN)angelica.vital@outlook.cm2 Programa de Pós Graduação em Engenharia Química (PPGEQ-UFRN)allmoriyama@gmail.com3 Programa de Pós Graduação em Ciências e Engenharia de Materiais (PPGCEM-UFRN)carlson@ufrnet.brThe Brazil has deposits of rare earths, including cerium compounds, which possess interestingcatalytic properties. These can be used as raw materials for the production of ceramic membraneswith catalytic properties. In this context, this article aims to present the synthesis process ofnanostructured BaCeO3.The BaCeO3 sample was synthesized by an EDTA-Citrates complexing process, in which the heatingrate and the pH of the precursor were controlled, being subjected to heat treatment at 1000 ° C for 5hours. The resulting powder was characterized by X-ray diffraction (XRD) to identify the crystallinephase of barium and cerium oxide are arranged in the orthorhombic form; Rietveld refinement wasused to verify crystallite size; scanning electron microscopy (SEM) to investigate the morphology;thermogravimetry for calcination temperature.Keywords: Powder; BaCeO3, EDTA-citrate, X Ray Diffraction.

Removal of nitrate in aqueous effluents by catalytic membraneVilma Araújo da Costa Braz* 1 , Sibele Berenice Castellã Pergher 1 , Dulce Maria de Mello 1, ,Miguel Torres Rodrigues 2 .1 UFRN - Universidade Federal do Rio Grande do Norte, PPGCEM-Programa de Pós-Graduação em Ciência e Engenharia de Materiais – Natal – RN – Brasil.2 UAM - Universidade Autônoma Metropolitana - Azcapotzalco,Cidade do México –DF –México.*vilmacostabio@gmail.comIntroduction.The need to protect the environment has led to the search of new methods for efficient removal ofchemical compounds that alter the stability of natural resources. Currently, the contamination ofgroundwater by nitrate occupies the attention of many investigations. This type of contaminationis due particularly to the use of fertilizers and biocides in excess and other organic wastes. Thefertilizer is rich in nitrogen leached reaching being water reservoirs [1, 2].In order to minimize the concentrations of nitrate, alternatives have been sought for removal inwater. The use of alumina has been a promising alternative route for the removal of pollutingcompounds due to their adsorption properties [2].Recently, an alternative system is to use a catalytic membrane that acts as interface between areducing gas (H 2 ) and the aqueous solution to provide a concentration of NO 3 [3].The catalyticalumina membrane with nanoparticles of Pd/Ni can be an efficient alternative for the eliminationof NO 3 in polluted water.For this reason, the aims of this study was to investigate the adsorption of nitrate in aqueousmedium using commercial alumina as adsorbent and then engage a system of separationmembranes for catalytic reaction.MethodologyWe used three types of activated aluminas supplied from Merck Chemicals Company (particle sizefrom 0.063 to 0.200 mm) commercially knoen as acidic, basic and neutral. This designation is dueto the pH of preparation of these materials and surface properties, however in this study wereused at neutral pH aluminas. Furthermore, an asymmetric microfiltration membrane commercialalumina IT-70 (exekia) of cylindrical geometry mono-channel average pore diameter of 100 nmcomposed of three layers, where the support is alpha-alumina and active layer of gamma-alumina.The sound dimensions: 15 cm length, 0.7 cm inside diameter and outside diameter of 1.0, figure 1.

Figure 1 catalytic ceramic membraneCharacterizationAluminas were characterized by X-Ray Diffraction (Simens equipment. Filter Model D5000 using Niand Cu-kα radiation (λ = 1.54 Å), Scanning Electron Microscopy SEM (JEOL JSM-5900) and BETspecific area held porosimeter used in the NOVA brand 2200 – Quantchrome.Adsorption test and the adsorption isotherms of aluminaThe adsorption experiments were conducted in batch mode using shaker table rotating with thealumina mass of 100 mg under the conditions of 200 rpm at 25 °C and volume of 50 mL solutionwith 700 ppm sodium nitrate for different times of 30 minutes to 48 hours. After the elapsed time,the suspensions were filtered and the liquid reserved for analysis.To obtain the isotherms other experiments were conducted by fixing time of 30 minutes byvarying the initial concentration of nitrate (from 0.2 to 1000 ppm). For such procedures, analysesof nitrate content were performed on a spectrophotometer UV - VIS-SHIMADZU - Model 36000,the wavelength of 220 nm. The catalytic membrane was prepared by wet impregnation bybimetallic nanoparticles, follow by drying and reduction under hydrogen atmosphere a400 °C.Results and discussions.X ray diffractionThrough analysis of X - ray diffraction (Figure 2) showed that all the samples showed characteristicreflections at 2θ of phase γ = 36.35 °, 60.55 ° and 45.5 ° in the Bragg angle range and the transitionphase and crystallinity η and lacking intensity modulations weak and diffuse.

(aFigura 2. Difratograma das aluminasScanning Electron Micrographs - SEMFigures 2 (A), (B) and (C) identified below, show the micrographs obtained by scanning electronmicroscopy for acidic aluminas (ALOA), Basic (ALOB) and neutral (ALON), respectively. It can be seethat morphology and the difference in sizes of the clusters.ABCFigura 2. (A) ALOA, (B) ALOB and (C) ALONAnalysis BETThe specific area of alumina’s shows these are relatively low compared to the clay minerals alsoused in adsorption processes [3]. However, showed a considerable adsorption capacity of nitratewith values of specific areas and pore volume near showing a similarity for the different types (seeTable 1).

Table 1. Specific area and pore volume of the alumina calculated from the adsorption dataAl 2 O 3A BET(inidades)V Total(Unidades)V BJHAcidic1520 ,2300,250Basic1410,2300,270Neutral1270,2400,250It was observed also a Type IV isotherm characteristic of mesoporous material in which thephenomenon of capillary condensation (Figure 5).Figura 5: Isotermas de adsorção de N 2 das aluminasThrough the adsorption tests of nitrate, it was observed that the alumina already within 30minutes adsorb a considerable amount of nitrate (each approximately 350ppm, corresponding toa 50% removal). It was also noted that the linear regression results obtained following theLangmuir model at least in the concentration ranges studied.Conclusion.From the results achieved to date, it was found through experiments that the simpleadsorption of nitrate on alumina (powder) adsorption capacity thereby study the elimination ofnitrates in aqueous effluents using transition metal catalysts supported on a porous support ofalumina and installing a catalytic membrane reactor. Due to the characteristics of the membranereactor is expected to reduce further the contamination or the use of milder conditions ensuring aclean and efficient alternative technological, competitive costs and income, within the broadspectrum of existing waste water treatment.

AcknowledgementsReferencesWe gratefully acknowledge by financial support from CAPES ( BEX 0367-13-3)[1] Kappor, A; Viraraghavan, T. J. of Environm.Eng. 1997,123, 371.[2] Smith, R. L.; Buckwalter, S. P.; Repert, D. A.; Daniel Miller, D. N. Water Research. 2005, 39.[3] Pergher, S.B.C. ; Oliveira Luiz C. A. ; Smaniotto Alessandra ; Petkowicz Diego I. Quím. Nova. 2005.[4] Ward D.A., Ko E.I., 1995. Preparing Catalytic Materials by the Sol-Gel Method. Ind. Eng. Chem. Res. 34,421-433.

Characterization of Ultra filtration Ceramics Membranesfor Wastewater Treatment of Oil RefineryAna Paula Soares de Lima*Regina de Fátima Peralta Muniz MoreiraThaís Appelt PeresJéfersson BakkarUniversidade Federal de Santa Catarina/Departamento de Engenharia Química e Engenhariade Alimentos.apaulasl.ufsc@gmail.com*The process of membrane separation by tangential ultrafiltration (UF) offers the advantage ofoperating the system at low pressures being effective on the separation of particles, microorganismsand certain organic compounds of high molecular weight. Therefore, the UF has been widely appliedfor advanced treatment of wastewater [1, 2].The aim of this study was to experimentally characterize the permeate flux, hydraulic permeability(Lp), retention and fouling tendency of tubular ceramic membranes for UF to be used on wastewatertreatment of oil refinery.The hydraulic permeability, which is the angular coefficient of the linear regression plot of permeateflux versus transmembrane pressure was determined via the permeate flux at different pressures0,5; 0,8 and 1,0 Bar, using water solutions distilled and synthetic wastewater oil refinery [3].The evaluation of the permeate flux and hydraulic permeability produced results similar to thosedetermined in other studies with UF membranes. However, it is noteworthy that the hydraulicpermeability cannot be compared with experiments of other authors, since each membrane hasdifferent characteristics from each other, such as porosity, tortuosity, pore size, membrane thickness[4].By using synthetic wastewater oil refinery in the experiments, the fouling phenomenon occurred atthe membranes, which causes a decrease in the permeate flux, although through regular cleaningand proper choice of experimental conditions of operation this phenomenon can be minimized. Inorder to investigate the fouling phenomenon, experiments were performed to measure thepermeate flux at the same pressure on different days. The result was the reduction of the permeateflow as the membrane was used [5].It is concluded, therefore, that the functional characterization of ceramic membranes is veryimportant in determining best operation conditions and thus more efficient processes because itenables proper use of the membrane in the separation process, and enables the previousdetermination of behavior and interaction of the membrane with the feed solution [6].

[1] COTE, P.; BUISSON, H.; PRADERIE, M. (1998), Water Science and Technology, v. 38, n. 4, p. 437-442.[2] BAKER, R. W. (2004), 2nd Edition. John Wiley e Sons Ltd.[3] PERSSON, K. M.; GEKAS V.; TRAGARDH, G. (1995), Journal of Membrane Science, v. 100, p. 155 – 162.[4] DIEL, J. L. (2010), Dissertação de Mestrado, Porto Alegre, UFRGS.[5] JUANG, L. C.; TSENG, D. H.; LIN, H. Y. (2007), Desalination, 202, 302-309.[6] NOBLE, R.D. e STERN, S.A. (1995), Elsevier Science B. V., Netherlands.

PEI/PEIS blends reinforced with sepiolite Clay for fuel cell polymeric electrolytes:evaluation of applicabilityAna C. O. Gomes 1 , Fernando N. S. Monteiro 1 , Caio M. Paranhos 2 , L. A. Pessan 1,*1 Laboratory of Permeation and Sorption, Department of Materials Engineering, UFSCar, São CarlosBrazil. 2 Laboratory of Polymers, Department of Chemistry, UFSCar, São Carlos, Brazil.*pessan@ufscar.brFuel Cells based in polymeric membranes are an alternative for the conventional energetic matricesbased on fossil fuel and generation of energy with minimum environmental impact [1,2]. However,polymer membranes available nowadays for this specific use have some disadvantages, like lowefficiency and cell durability [3]. This work presents preliminary studies of hybrid polymericmembranes for application as hydrogen fuel cell polymeric electrolytes. Poly (ether imide) (PEI) waschemically modified with sulphone groups for increasing its ionic conductive property [4]. Theincorporation of the mineral nanoclay sepiolite aims the increasing of its mechanical and thermalproperties. The nanoclay was also chemically modified with silane groups for better interaction withthe matrix. Poly(ether imide)/sulphonated poly(ether imide) blends-based nanocomposites wereprepared using natural and modified nanoclay and the nanocomposites were evaluated by FTIR,WAXD, DSC and TGA, besides water vapor transmission rate (WVT) and ionic migration resistance(MR). The DSC (Figure 1) and FTIR (Figure 2) results confirm the matrix sulphonation and its betterinteraction with modified sepiolite. The differences between processing methods seems to be mainlyin the permeation processes (ionic and water vapor – Table 1), probably due to morphologicaldifferences. These differences are under investigation by transmission electronic microscopy. Theresults so far in this work lead to a better structure versus properties balance, aiming the highperformance of obtained membranes.Figure 1: Tg values obtained by DSC for PEI,sulphonated PEI and nanocomposites blendsFigure 2: FTIR curve for sulphonated PEI,x axis is wave length (cm -1 ) and y axis isTransmitance (%)Table 1: WVT and IM results for PEI/PEIS nanocomposites blendsPEI PEIS PEI/PEIS PEI/PEIS1,5 sepPEI/PEIS3 sepPEI/PEIS1,5 sepmodPEI/PEIS3 sepmodWVT17.4 19.7 18.4 18.6 25.0 15.6 14.6[g/(day*m 2 )]Ionic Migration[Km]- 108 8433 109 150 33300 17660

[1] Larminie, J., Dicks, A. Fuel cell systems explained. 2nd ed. John Wiley: Chichester, 2003.[2] O´Hare, R.P., Cha, S.W., Colella, W., Prinz, F.B. Fuel cells Fundamentals. John Wiley: New York, 2006.[3] Loredo, D. E. S. ,Paredes, M. L. L., Sena, M. E. Materials Letters v.62, p. 3319-3321, 2008.[4] Pinto, B. P., Santa Maria, L. C., Sena, M. E. Materials Letters, v. 61, p. 2540-2643, 2007.

PC/PCS blends reinforced with sepiolite clay for polymeric PEMFC electrolyte:Evaluation of applicabilityAna C. O. Gomes 1 , Eduardo Backes 1 , Caio M. Paranhos 2 , L. A. Pessan 1,*1 Laboratory of Permeation and Sorption, Department of Materials Engineering, UFSCar, São CarlosBrazil. 2 Laboratory of Polymers, Department of Chemistry, UFSCar, São Carlos, Brazil.*pessan@ufscar.brIon conductive polymer membranes have been studied in recent years for use in fuel cellsapplications [1,2]. One of the main goals in these studies is to develop new materials with improvedproperties compared to the materials available in market [3]. In this workpolycarbonate/sulphonated polycarbonate/sepiolite nanocomposites were tested for ion conductivemembranes applications. The use of nanoclay sepiolite aimed the increase of mechanical andthermal resistance, which can be reduced by polymer sulfonation. The membranes were evaluatedby WAXS, DSC, TGA and DMA analyses, besides water vapor transmission rate (WVT) and ionicmigration resistance (MR). The DSC results (Figure 1) showed the decrease of T g of polycarbonatedue to the sulfonation reaction [4]. The DMA results (Figure 2) show the development of two phasesin the blends, and the interaction of sepiolite with the matrix by changes in transitions under T g . Thedifferences in WVT and MR results seems to be mainly due to morphological differences. Theexperimental results pointed to a better structure versus properties balance, aiming the highperformance of obtained membranes.Figure 1: DSC results for PEI, sulphonated PEIand nanocomposites blendsFigure 2: DMA results for PEI, sulphonatedPEI and nanocomposites blendsTable 1: WVT and IM results for PC/PCS nanocomposites blendsPC PC/PCS PC/PCS1,5 sepPC/PCS3 sepPC/PCS 1,5sepmodPC/PCS3 sepmodWVT18 16.6 15.2 15.2 17 13.6[g/(day*m 2 )]Ionic Migration[MWm]- 300 400 224 411 0,117[1] Larminie, J., Dicks, A. Fuel cell systems explained. 2nd ed. John Wiley: Chichester, 2003.[2] O´Hare, R.P., Cha, S.W., Colella, W., Prinz, F.B. Fuel cells Fundamentals. John Wiley: New York, 2006.[3] Loredo, D. E. S. ,Paredes, M. L. L., Sena, M. E. Materials Letters v.62, p. 3319-3321, 2008.[4] Pinto, B. P., Santa Maria, L. C., Sena, M. E. Materials Letters, v. 61, p. 2540-2643, 2007.

Magnetic Field Influence on Cleaning of Ultrafiltration Membranes Applied toTreatment of Textile WastewaterFranciele Carlesso, Selene M. A. G. U. Souza, Antônio A. U. Souza, J. Vladimir de Oliveira,Marco Di Luccio*Departamento de Engenharia Química e Engenharia de Alimentos,Universidade Federal de Santa Catarinae-mail: fccarlesso@gmail.com, *diluccio@enq.ufsc.brMembrane technology has become one of the best alternatives for the textileindustry wastewater management [1]. However, the efficiency of the process can be greatlyaffected due to membrane fouling. In this work, membrane fouling in a tangential flowultrafiltration of a model textile industry wastewater is studied, assessing the use of a staticmagnetic field as an alternative to improve flux recovery in membrane cleaning.A model wastewater constituted of carboxymethylcellulose and sodium sulfatesolutions in different concentrations was permeated through an ultrafiltration polysulfonemembrane with MWCO 30,000 Da, with and without the presence of a static magnetic fieldof 0,41 T. The magnetic field was perpendicular to the membrane surface. Magnetic memoryof the feed solution was also investigated by the recirculation of the feed stream throughthe magnetic field for 3h. The flux of ultrapure water was determined with the clean (new)membrane at different pressures. Then the permeate flux of the model wastewater wasmeasured at 2 bar. After each batch of ultrafiltration process, the membrane was rinsed outwith clean water. The water permeability was then measured and a chemical cleaning stepwas carried out.The magnetic field proved to be effective on the reduction of the irreversible fouling.According to the results in Fig.1a, when the feed solution was magnetically pre-treated, thereduction in water flux is half the one obtained when the system was operated without themagnet. Although the system presents magnetic memory, a more effective foulingminimization was obtained when the magnetic field is applied during the ultrafiltration (andnot only in the feed solution previously to the UF). The effect of the magnetic field is evidentin membrane cleaning by simple water rinse and by chemical treatment. The magnetictreatment proved to be an attractive alternative to reduce the membrane fouling. This noninvasivetechnique would enhance process economy by reducing the use of chemicals inmembrane cleaning, and by the consequent improvement of membrane lifetime.Acknowledgements: CAPES, CNPq

Figure 1 - Relative water flux reduction for different solutions. (a) After physical cleaning and (b) After chemicalcleaning.

Influence Of Pretreatment On The Permeability Of Polymeric UltrafiltrationMembranes To Non-Aqueous SolventsFrederico Marques Penha* 1 ; Kátia Rezzadori 1 ; Guilherme Zin 1 ; Vanessa Zanatta 1 ; Marco DiLuccio 1 ; José Carlos Cunha Petrus 11 Department of Chemical and Food Engineering, UFSC, Florianópolis/SC, 88040-900, Brazil.e-mail adress*: fredmpenha@gmail.comThe solvent recovery step is the most critical process in vegetable oil extraction, due to theireconomic, environmental and safety implications. Thus, many recent studies on the application ofmembrane technology to edible oils industry are focused on solvent recovery [1,2].Nevertheless, advances in this field are slow, due to the fact that commercially available membranesare mainly produced for aqueous systems. Studies suggest that polymeric membranes pretreatmentby immersion in organic solvents can prevent the pores collapse and ensure full membrane-solventcontact, which facilitates the permeation, increases permeate flow and guarantees the structuralintegrity of the membrane.The present work tested four pretreatments in commercial polymeric membranes (UH004, UP005,UP010 and UH050 – Microdyn-Nadir) with different pore sizes (4 kDa, 5 kDa, 10 kDa and 50 kDa,respectively), in order to evaluate their efficiency during hexane permeation. The treatmentsconsisted on the sequential immersion of membranes into two solvents: firstly ethanol, for 2 or 12hours; and then hexane, for 2 or 12 hours. The experiments were performed with a dead-endfiltration cell, pressurized with nitrogen. Permeate fluxes were measured from 1 to 6 bar, aftermembrane compaction at 8 bar for 45 minutes. The determination of hexane fluxes on pretreatedmembranes allowed the calculation of permeability and evaluation of the influence of theconditioning in solvent flux.Regardless of the pre-treatment, fluxes increased with transmembrane pressure. A strong correlationcan be noted between the conditioning time and the permeate flux and permeability. The longer theexposure time to the solvent, the greater the flux and the permeability. The time of exposure to n-hexane did not cause great changes in permeate flux. However, there are noticeable differences influxes with the exposure time to ethanol. Thus, it can be inferred that the time of exposure toethanol, rather than to hexane, determines the increase in permeability and consequently theefficiency of the pre-treatment. The results suggest viability in the use of these membranes for therecovery of solvents in the oil industry, if adequate process parameters are chosen, and membraneintegrity is monitored.Acknowledgements: CAPES and CNPq for financial support.[1] COUTINHO, C.M.; CHIU, M.C.; BASSO, R.C.; RIBEIRO, A.P.B.; GONÇALVES, L.A.G.; VIOTTO, L.A. (2009). Stateof art of the application of membrane technology to vegetable oils: A review. Food Research International,v.42, p.536-550.[2] Koseoglu, S.S.; Engelgau, D.E. (1990). Membrane applications and research in the edible oil industry. Journalof American Oil Chemists’ Society. 67, 239-249.

Permeation Of Non-Aqueous Solvents Through Ultrafiltration CommercialPolymeric MembranesFrederico Marques Penha 1 *; Kátia Rezzadori 1 ; Guilherme Zin 1 ; Vanessa Zanatta 1 ; Marco DiLuccio 1 ; José Carlos Cunha Petrus 11 Department of Chemical and Food Engineering, UFSC, Florianópolis/SC, 88040-900, Brazil.e-mail adress*: fredmpenha@gmail.comIn non-aqueous systems, the membrane’s lack of stability due to changes in its structure caused bythe solvent are some drawbacks to industrial implementation of this technology. When it comes tomembrane process in non-aqueous systems, important characteristics are the resistance of themembrane material to solvents, and reasonable solvent fluxes and rejection coefficients. Thus, thechoice of suitable membranes should be performed for each process [1].Furthermore, the lower the surface tension, less polar is the solvent and thus, the lower the solventflux through hydrophilic membranes and higher in hydrophobic membranes [2].Pretreatment ofpolymeric membranes induces a gradual change of the surface polarity and promotes the grouping ofhydrophilic and hydrophobic sites, which can contribute to the reduction of the hydrophilicity and ofthe risk of pore degradation and polymer matrix rupture [3].Commercial ultrafiltration polymeric membranes with different molecular weight cut-off (4 kDa, 5kDa, 10 kDa and 50 kDa) from Microdyn-Nadir were evaluated, regarding permeability in water,ethanol, iso-propanol and n-hexane. Permeation tests were conducted in a dead-end stainless steelfiltration cell at room temperature. The membranes were previously compacted to preventinterference in the results. Fluxes were collected at transmembrane pressures from1 to 6 bar every 5minutes.It was possible to verify that, independent of the solvent, the larger the membrane’s pore size, thegreater is the flux. The water flux was higher than the flux of all other solvents, except for the 5 kDamembrane, in which the ethanol is higher than the water flux. This behavior may be due tomembrane conditioning that rearranged the hydrophilic and hydrophobic sites in the polymer matrixand thus, increasing ethanol permeability. Only the 4 kDa membrane showed the expectedcorrelation with the theoretically predicted flows (water> ethanol>iso-propanol> hexane). In theother tested membranes, the flux of iso-propanol was the lowest, with values up to 7 times lowerthan the hexane flux. The results prove that application of commercial polymeric membranes in thepermeation of non-aqueous streams should follow a detailed investigation of the behavior of suchmembranes in the different solvents, for the choice of the membrane more suitable to the process.The permeation of organic solvents through microporous membranes depends not only on pore size,but also on the interaction between the solvent and membrane material.Acknowledgements: CAPES and CNPq for financial support.[1] Bhanushali, D.; Kloos, S.; Kurth, C.; Bhattacharyya, D. (2001). Performance of solvent-resistantmembranesfor non-aqueous systems: solvent permeation results and modeling. Journalof Membrane Science, 189, 1–21.[2] Van der Bruggen, B.; Genes, J.; Vandecasteele, C. (2002). Fluxes and rejections for nanofiltrationwith solventstable polymeric membranes in water, etanol and n-hexane.ChemicalEngineering Science 57, 2511-2518.

[3] Shukla, R., Cheryan, M. (2002) Performance of ultrafiltration membranes in ethanol-water solutions: efectof membrane conditioning. Journal of Membrane Science, v.198, p.75-85.

Effects of Magnetic Field on Ultrafiltration of Protein SolutionsGuilherme Zin*¹, Frederico Marques Penha¹, Vanessa Zanatta¹, José Vladimir De Oliveira¹,José Carlos Cunha Petrus¹ e Marco Di Luccio¹¹Department of Chemical and Food Engineering, UFSC, Florianópolis, 88040-900, SC, Brazil.e-mail address: guilhermezin@gmail.comThe separation and purification of bioproducts as proteins, polysaccharides, vitamins and aminoacids is an important bioprocess step in the food industry due to its large number of applications[1,2]. Precipitation, crystallization and centrifugation may not result in good selectivity, while moreselective methods as electrophoresis and chromatographic separations are often costly. Thus, thedevelopment of separation processes that combine high selectivity and throughput with low costcomprises an attractive research topic. In this context, membrane separations may be potentiallyviable for separation and purification of food and bioproducts [3-5].The use of membrane processes for concentration and purification of protein in industrial scale is stillchallenging, due mainly to factors that cause the decrease in permeate flux as concentrationpolarization and fouling [6]. A number of solutions to overcome this drawback have been proposedtoward minimizing fouling and polarization. Among them, the application of magnetic, electric, sonicand centrifugal fields for such purpose should be highlighted.In this context, the aim of this study was to assess the effect of a permanent magnetic field on thefouling caused by proteins on ultrafiltration membranes. The behavior of permeation of bovineserum albumin through ultrafiltration membranes was followed at different pH and ionic strengthunder regular permeation conditions and under the influence of a permanent magnetic field.Different magnetic field intensities (0.1 to 0.5 T) were tested. The recovery of water flux afterphysical and chemical cleaning procedures was evaluated and resistances to permeation wereestimated.Acknowledgements: CAPES and CNPq for financial support.[1] Lin,S.H.; Hung, C.L.; Juang,R.S.(2008) Effect of operating parameters on separation of proteins in aquoussolutions by dead-end ultrafiltration.Desalination, 234, 116-125.[2] Tung,K.L.; Hu,C.C.; Li,C.H.; Chuang,C.J. (2007) Investigating protein crossflow ultrafiltration mechanismsusing interfacial phenomena. Journal of de Chinese Institute of Chemical Engineers, 38, 303-311.[3] Huang,R.; Kostanski,L.K.; Filipe,C.D.M.; Ghosh,R. (2009) Environment- responsive hydrogel-basedultrafiltration membranes for protein bioseparation. Journal of Membrane Science, 336, 42-49.[4] Ibáñez,R.; Almécija,M.C.; Guadix, A.; Guadix, E.M. (2007). Dynamics of the ceramic ultrafiltration of modelproteins with different isoelectric point: Comparison of β- lactoglobulin and lysozyme. Separation andPurification Technology, 57, 314-320.[5] Yunos,K.F.M. e Field, R.W. (2008) Rejection amplification in the ultrafiltration of binary protein mixturesusing sandwich configurations.Chemical Engineering and Processing, 47, 1053-1060.[6] Babu, P.R., Gaikar, V.G. (2001) Membrane characteristics as determinant in fouling of UF membranes.Separation and Purification Technology, 24, 23-34.

Separation of Mixtures of Soybean Oil and Organic Solvents by CeramicMembranesJonas R. M. de Melo 1 , Ricardo Verlindo 1 , Ana Paula Picolo 1 , Diane Rigo 1 1 ,Marcus V. Tres 1 , Juliana Steffens 1 ; J. Vladimir Oliveira 2 , Marco Di Luccio* ,21 Department of Food Engineering, URI Erechim, Av. Sete de Setembro, 1621, Erechim,99700-000, RS, Brazil.* ,2 Department of Chemical and Food Engineering, UFSC, Caixa Postal 476, Florianópolis,88040-900, SC, Brazil. e-mail: diluccio@enq.ufsc.brMembrane separations have advantages over conventional separation processes, including energysavings, selectivity, possibility of separation of thermolabile compounds, simple operation and arelatively easy scale up from lab to industrial scale. In the conventional processing of vegetable oils,distillation units operated under vacuum and other auxiliary equipment are used in the process. Apossible thermal degradation of oil and an incomplete elimination of n-hexane are majordisadvantages of this technology, besides the large amount of energy used in these processing steps.In contrast to the conventional refining process, solvent recovery by membrane separations can beconducted at mild temperatures, preserving the heat sensitive components of technological interestof the oil, such as natural antioxidants. A more stable product, with thus better quality can beobtained. The soybean oil extraction process is based in the solvent percolation to the cake and theseparation of the oil from solvent by evaporators, which represent 2/3 of the industry energyrequirement. Solvent recovery energetics could also be enhanced by membrane technology, whichmay reduce up to 50% of the solvent sent to the evaporator. In this study, ceramic membranes withdifferent molecular weight cut-offs (5, 10 and 20 kDa) were used to separate soybean oil mixtures inorganic solvents like n-hexane, ethanol, isopropyl alcohol, and azeotropes of ethanol in n-hexane andof isopropyl alcohol in n-hexane. The mixture mass ratios investigated were 1:4, 1:3 and 1:1. The20 kDa membrane was preconditioned in n-butyl alcohol to increase the flux, achieving 275 L/m 2 h at1 bar. Decreasing the membrane molecular weight cut-off, and increasing the content of oil in themixture led to a significant decrease in the membrane permeate mass flux. Highest oil retentionswere obtained using ethanol as solvent. The azeotropes showed characteristics that changed theoriginal solvent behavior. The isopropyl alcohol showed a peculiar behavior, many times presenting aflux independent of pressure, possibly due to the chemisorption of this component by -alumina andzirconia that composes the membrane and capillary effects. The cleaning strategy was based on alkaliand acid sequential washes. The cleaning was improved when higher temperatures and tangentialvelocities were used.Keywords: ceramic membranes, separation, mixture, vegetable oil, organic solvents.Acknowledgements: CNPq, CAPES

Pretreatment Influence on Hexane Permeability in Nanofiltration and ReverseOsmosis Commercial Polymeric MembranesKatia Rezzadori, Frederico M. Penha, Mariane C. Proner, Lara Fogaça, José C. C. Petrus,Marco Di Luccio*Departamento de Engenharia Química e de Alimentos, Universidade Federal de SantaCatarina, UFSC, Florianópolis, SC, 88040-900.e-mail: katia.rezzadori@gmail.com; *diluccio@enq.ufsc.brMembrane technology application in non-aqueous systems is not yet fully established, although itspotential for technological innovations in the food, chemical and pharmaceutical industry isrecognized [1]. The development of this technological alternative is related to the chemical stabilityof the membranes, since the exposition of these to organic solvents can cause physicochemicaland/or morphological changes on the membranes, affecting process performance. Studies indicatethat pre-treatment of polymer membranes, by immersion in organic solvents, can ensure themembrane’s contact with the solvent and modification of the selective surface, providing bettersolvent permeation and increasing the performance of the membrane [2].In this context, the aim of this study was to define a pretreatment for commercial polymericmembranes and to characterize these membranes, before and after the pretreatment, usingdifferent techniques. Two reverse osmosis (RO) membranes (BW30 and ORAK, BW30 e ORAK –rejections of 99,5 e 99 % to NaCl, respectively) and two nanofiltration (NF) membranes (NF270 –rejection of 97 % to MgSO 4 and NP030 rejection of 80-97% to Na 2 SO 4 ) were characterized by contactangle, FTIR (Fourier Transform Infrared Spectroscopy) and SEM (Scanning Electronic Microscopy). Themembrane conditioning was studied using distinct solvents (n-hexane, ethanol, n-propanol, isopropanoland n-butanol) in intervals of 2, 8, 12, and 24 hours. After the pretreatment, the n-hexaneflux was measured on each pressure (0-35 bar), at room temperature. A resistance test on n-hexanewas performed for 8 hours at 15 bar for the NF and 20 bar for the RO membranes.The conditioning with ethanol enabled higher hexane fluxes in the membranes ORAK, NF270 andBW30, while NP030 did not presented increases in permeability after the different conditionings. Theconditioning time has no significant effect (p > 0.05) on the process. Thus, a pretreatment for 2 hourswas chosen for further essays. An increase in the contact angle after the conditioning of themembranes was detected, which reflects changes in hydrophilicity of the surface. The FTIR spectraindicated the presence of polyamide and polysulfone of the membranes ORAK, BW30 and NF270.The membrane NP030 showed consecutive and sharp peaks of sulfone. After hexane permeation, adecrease in FTIR transmittance was noticed, which suggest the occurrence of swelling. SEM analysisdid not show any visible changes in membrane structure, except for the NF270 membrane, whichpresented pore compaction, probably due to applied pressure or to the solvent’s action.The results obtained in this work with commercial membranes of RO and NF, normally used inaqueous solutions separations, indicate that these membranes can be used in separation of nonaqueousmixtures without structural degradation, measurable with the techniques applied in thepreliminary tests.[1] S. Darvishmanesh, J. Degrève, B. Van Der Bruggen (2010), Ind. Eng. Chem. Res., 49, 9330-9338.[2] M.S. Araki, C.M. Coutinho, L.A.G. Gonçalves, L.A Viotto (2010), Sep. Purif. Technol., 71, 13-21.Acknowledgements: CAPES and CNPq

Effect of Dense CO 2 on Polymeric Commercial MembranesKatia Rezzadori, Josamaique G. Veneral, Lucas Pires, J. Vladimir Oliveira, José C. C. Petrus,Marco Di Luccio*Departamento de Engenharia Química e de Alimentos, Universidade Federal de SantaCatarina – UFSC – Florianópolis/SC - 88040-900.e-mail: katia.rezzadori@gmail.com; *diluccio@enq.ufsc.brCoupling supercritical CO 2 (SC-CO 2 ) extraction with membrane separation can lead to energy savings.Also, when pressurized fluids are considered for oil extraction, membrane separation could beprofitably used for minimizing the need of solvent recompression [1]. However, high pressureconditions may cause physicochemical and morphological changes in polymeric membranes, whichcan negatively affect membrane performance [2]. Moreover, since most of the information oncommercial membranes is provided by manufacturers, further investigation on their structure wouldbe beneficial for the selection of proper membranes, especially for processes involving non-aqueoussolvents, as SC-CO 2 .In this context, the aim of the present work was to study the behavior of two commercialmembranes, one reverse osmosis (RO) membrane (BW30 – rejections of 99 % to NaCl) and onenanofiltration (NF) membrane (NP030 rejection of 80-97% to Na 2 SO 4 ) upon static exposure toSC-CO 2 . The static process was carried out with dense CO 2 in two subcritical and two supercriticalconditions (80 bar and 100 bar/20°C; 100 bar and 200 bar/ 80°C) for 8 hours. The performance wasinvestigated based on changes in physicochemical and morphological properties. These propertieswere studied using contact angle, ATR-FTIR (Fourier Transform Infrared Spectroscopy) and SEM(Scanning Electronic Microscopy).Dense CO 2 exposure caused an increase in contact angle, which was higher in elevated pressures,indicating changes in membrane hydrophilicity. The FTIR spectra indicated the presence of polyamideand polysulfone, proving the thin film composite formation of the membrane BW30. The membraneNP030 showed consecutive and sharp peaks of sulfone. After dense CO 2 permeation, a decrease inFTIR transmittance was noticed, which suggests the occurrence of swelling. After contact with denseCO 2 , membrane BW30 showed structural changes on the active layer, while the membrane NP030remained unchanged.The results obtained in this work suggest that the commercial RO and NF membranes can be appliedin the permeation of dense CO 2 , with small changes in their properties, which did not causestructural degradation, measurable with the techniques applied in these preliminary tests.[1] C.B. Sprícigo, A. Bolzan, R.A.F. Machado, L.H.C. Carlson, J.C.C. Petrus (2001), J. Membr. Sci., 188, 173-178.[2] O. Akin, F. Temelli (2011), J. Supercrit. Fluids, 60, 81-88.Acknowledgements: CAPES and CNPq

Recovery and Concentration of Isoflavones of Tofu Whey Using theNanofiltrationSilvia Benedetti 1* , Lara Alexandre Fogaça 1 , Guilherme Zin 1 , ElaneSchwinden Prudêncio 2 ,Rodrigo Santos Leite 3 , José Marcos Gontijo Mandarino 3 , José Carlos Cunha Petrus 11 Department of Chemistry and Food Engineering, Technology Center, Federal University ofSanta Catarina, Florianópolis, SC.2 Department of Food Science and Technology, Agricultural Sciences Center, University ofSanta Catarina, Florianópolis, SC.3 Embrapa Soja, Londrina, PR.*silviabene@gmail.comThe tofu is a nutritious food produced from the hydro soluble extract of soybean. Among theproduction steps, a large volume of whey is eliminated during the pressing step. The tofu whey ischaracterized by high values of Chemical Oxygen Demand (COD) and Biochemical Oxygen Demand(BOD), considerable protein content, substantial sugars and minerals (coagulants) concentrations ,besides presenting low molecular weight molecules as peptides, lipids, and some functionalcompounds such as isoflavones and oligosaccharides.The objective of this study was the use of tofu whey, using nanofiltration (NF) for concentration ofisoflavones. Initially, the influence of pressure, temperature and tangential velocity during theprocess was evaluated. The experiments were carried out in duplicate at 6 bar, 28 °C and 0.3 ms -1until reaching a volume reduction factor (VRF) of 4.5. The VRF was calculated as the ratio betweenthe initial volume (L) of the tofu whey used in the feed and the final volume (L) of the concentrateafter NF. The quantification of isoflavones was performed using High Performance LiquidChromatography (HPLC) with photo diode array detector (Model 996) and automatic sample injector(Model 717 Plus) of WATERS ® (Milford, USA). It was used a reverse phase column (YMC Pack ODS-AM ®, 250 mm x 0.4 mm diameter) [1].Throughout the nanofiltration process of tofu whey, a reduction in the permeate flux with time wasobserved, typical of membrane separation processes. Concerning the concentration of isoflavones, itcan be observed through Figure 1 a significant increase (p

Whey VRF1,5 VRF2 VRF 2,5 VRF 3 VRF 3,5 VRF 4 VRF 4,5Figure 1- Results of isoflavones concentration in the tofu whey and concentrates obtained bynanofiltration process.[1] M.A. BERHOW (2002). Modern analytical techiniques for flavonoid determination. In: BUSLIG, B.S.;MANTHEY, J.A. Flavonoids in the Living Cell. New York: Klusher, 2002. 505 p.[2] W.J. KIM; H. H. KIM; S.H.,YOO (2005), Food Sci Biotechnol, 14 (3), 380-386.

Preparation of oil-in-water emulsions by membrane emulsificationVanessa Zanatta *1 , Guilherme Zin 1 , Frederico Marques Penha 1 , José Carlos Cunha Petrus 1 ,Marco Di Luccio 11 Department of Chemical and Food Engineering, UFSC, Florianópolis/SC, 88040-900, Brazil.e-mail address * : zanattavane@gmail.comEmulsions are commonly found in food, cosmetics and pharmaceutical industry. They play animportant role in food formulations like dairy products, creams, salad dressings, soups, proteinproducts, etc. The interest in alternative emulsification techniques has been currently increasing fordifferent applications, since the method used for emulsification greatly influences the physicochemicalproperties of the final product [4]. The droplet size (d 23 ) and the span of size distribution arethe most important parameters that should be considered when preparing an emulsion. Membraneemulsification is a simple method with potential application in several areas. The main advantage isthe good control of droplet size distribution, for the size of droplets is directly related with themembrane pore size distribution. Low energy demand is also listed as an advantage of membraneemulsification [3].In the present study simple oil-in-water emulsions were prepared by membrane emulsification.Ceramic tubular membranes were tested, with pore size ranging from 0.2 to 3 µm. The model systemchosen was sunflower oil and water, for its good nutritional characteristics, aiming at application ofthe emulsions in food formulations. Three food grade surfactants (Tween 20, Tween 80 and casein)were investigated. Critical micellar concentration was measured for each surfactant and used forformulation of the emulsions. The oil was pumped through the bore of the tubular ceramicmembrane by pressurization with gaseous nitrogen, while water with the surfactant was recirculatedthough the shell side of the module by a gear pump. The effect of the flow rate of water on theemulsion characteristics was also investigated. Droplet mean size and size distribution wasdetermined for all the emulsions prepared. Emulsions prepared by sonication and by an ultraturraxwith the same system were prepared as a control. Emulsion stability was followed up to 15 days.Acknowledgements: CAPES and CNPq for financial support.[1] TRENTIN A., et.al (2012). Cleaning protocols for organic microfiltration membranes used in premixmembrane emulsification. Separation and Purification Technology 88: 70–78.[2] CATHERINE Charcosset (2009). Preparation of emulsions and particles by membrane emulsification for thefood processing industry. Journal of Food Engineering 92: 241–249.[3] JOSCELYNE SM, Tragardh G (2000). Membrane emulsification— A literature review. Journal of MembraneScience 169: 107–117.[4] VLADISAVLJEVIC G. T and R.A. Williams (2005). Recent developments in manufacturing emulsions andparticulate products using membranes. Advances in Colloid and Interface Science 113(1):1 {20.[5] VLADISAVLJEVIC G. T, et. al (2004). Production of O/W emulsions using SPG membranes, ceramic-aluminiumoxide membranes, microfluidizer and a silicon microchannel plate—a comparative study. Colloids and SurfacesA: Physicochem. Eng. Aspects 232: 199–207.

A Study of the Resistances During Permeate Flux Decline in CrossflowMicrofiltration of Passion Fruit Juice1* Rui Carlos Castro Domingues, 2 Miria Hespanhol Miranda Reis, 3 Vicelma Luiz Cardoso1 Federal University of São João del-Rey, 2 Federal university of Uberlândia* Corresponding author: ruidomingues@ufsj.edu.brMembrane processing can be an alternative for conventional stabilization methods of fruit juices,since does not involve the application of heat, conserving its sensorial properties. One of the majorconstraints is the decrease of permeate flux, which can be a critical point in the feasibility of theprocess. Permeate flux during pressure-driven membrane processes depends on transmembranepressure, viscosity and resistance of permeation. The aim of this work was to compare and quantifythe major fouling mechanisms during crossflow microfiltration of passion fruit juice with differentpretreatments using hollow fiber polymeric membranes. Two pretreatments of passion fruit juicewere evaluated: A combination of centrifugation and enzyme treatment, and pre-clarification usingchitosan. The mathematical model proposed and revised by Field et al. (1995) [1] and Field et al.(2011) [2] was used in order to determine the major fouling mechanisms during the experiments.The associated resistances during crossflow filtration were described as follows: The total resistance(R T ) is defined as a combination of a resistance of the clean membrane (R M ), polarized concentrationlayer (R PC ), gel layer on the surface of membranes (R G ), pore blocking (R B ) and adsorption (R A ).Resistances were determined from the values of water flux after four cleaning procedures describedas follows: Physical cleaning with water recirculation, alkaline cleaning with a 5% NaOH solution,enzyme cleaning and backwashing.Regarding to the first evaluated pretreatment, the stabilized permeate flux observed was. The best adjustment for main fouling mechanism found was cake formation. Values of, , , ,andwere found. R CP and R M were the major components, responsible for35,72 and 33,96% of total resistance. The second evaluated pretreatment resulted in a stabilizedpermeate flux of presented internal pore blocking and values of ,, , , andwere found. R A and R M were the major components, responsible for 18.36 and63.09% of total resistance.The results indicates that chitosan pre clarification showed to be a promising alternative for thepretreatment of passion fruit pulp as induced higher permeate fluxes in comparison to traditionalpretreatments and not influenced the quality of the clarified juice. The mathematical modelproposed by Field et al. was suitable to describe major fouling mechanisms. Cake formations iswidely reported as the major fouling factor during microfiltration of enzyme treated juices([3],[4],[5],[6] and [7]), and chitosan pretreatment was capable to avoid cake formation as the majorfouling factor. This information can be useful during optimization of microfiltration systems duringmembrane cleaning procedures in future studies.References:[1] Field, R.W., Wu, D., Howell, J.A., Gupta, B.B., (1995). Critical Flux Concept for Microfiltration Fouling. Journalof Membrane Science 100(3), 259-272.

[2] Field, R.W., Wu, J.J., (2011). Modelling of permeability loss in membrane filtration: Re-examination offundamental fouling equations and their link to critical flux. Desalination 283, 68-74.[3] Rai, P., De, S., (2009). Clarification of pectin-containing juice using ultrafiltration. Current Science 96(10),1361-1371.[4] Barros, S. T. D.; Andrade, C. M. G.; Mendes, E. S.; Peres, L., (2002).Study of fouling mechanism in pineappleclarification by ultrafiltration. Journal of membrane science 215, 213-224.[5] Jiraratananon, R., Chanachai, A., (1996). A study of fouling in the ultrafiltration of passion fruit juice. Journalof Membrane Science 111(1), 39-48.[6] de Oliveira, R.C., Doce, R.C., de Barros, S.T.D., (2012). Clarification of passion fruit juice by microfiltration:Analyses of operating parameters, study of membrane fouling and juice quality. Journal of Food Engineering111(2), 432-439.[7] Nandi, B.K., Das, B., Uppaluri, R., (2012). Clarification of Orange Juice Using Ceramic Membrane andEvaluation of Fouling Mechanism. Journal of Food Process Engineering 35(3), 403-423.[1] R. W. Baker (2002), Ind. Eng. Chem. Res., 41, 1393-1411.

Characterization of Cellulose Acetate Membranes Produced from RecyclingCorn Husk for Application in Ultrafiltration.Elaine Angélica Mundim Ribeiro 1* , Carla da Silva Meireles 2 , Guimes Rodrigues Filho 1 , JuliaGraciele Vieira 1 , Rosana Maria Nascimento Assunção 3 , Jocelei Duarte 4 , Mara Zeni 41 Chemistry Institute (UFU), Uberlândia, Minas Gerais, Brazil2 Departamento de Ciências Naturais -CEUNES-UFES São Mateus-ES,Brasil3 College of Integrated Sciences, (UFU), Ituiutaba, Minas Gerais, Brazil.4 Department of Physical and Chemistry, (UCS), Caxias do Sul, RS, Brazil*eamundim@yahoo.com.brIn this study corn husk (CH) was used as an alternative source of cellulose for the productionof cellulose acetate (CA). Cellulose extracted from the CH was acetylated [1] to obtain of celluloseacetate with degree substitution (DS) of 2.78 (cellulose triacetate (CTA)) and 2.49 (cellulose diacetate(CDA)). The viscosity average molecular weight of the cellulose acetates were of 98,313 and 41,130g.mol -1 , for CTA and CDA, respectively. The results were compared with the commercial diacetateRhodia with DS of 2.45 and molecular weight of 46,000 g.mol -1 . Membranes were prepared fromcellulose triacetate (M-CTA), and polymeric mixture of M-CTA/CDA-CH and M-CTA/CDA-Rho by theinversion of phase method. The solvent system used CA/dioxano/acetone. The membranes werecharacterized by Scanning Electron Microscopy (SEM). They were evaluated based on their transportproperties by pure water flux and ultrafiltration (UF) trails, which were conducted under a pressureof 100 KPa. The egg albumin (EA) was used to determine the molecular weight cut-off (MWCO)membranes. In the cross-sectional microscopy (Fig. 1) exhibit different morphologies are mainly dueto the difference in viscosimetric molecular weight and degree of substitution of CA used.(A) M-CTA(B) M-CTA/CDA

(C) M-CTA/CDA-RhoFigure 1: SEM cross section of the membranes (1000x), highlighting the top layer formed “skin”(3000x) to membranes: (A) M-CTA, (B) M-CTA/CDA and (C) M-CTA/CDA-Rho.According to Wienk et al. [2] the addition of a high molecular weight component to thepolymer solution changes drastically the structure of the membranes; the porosity is higher, poresand well interconnected and macrovoid formation is suppressed. Still suggested that microphasedemixing between the two polymers takes place which prevents the formation of the dense toplayer. As noted in the cross-sectional microscopy (Fig. 1) is also observed an increase of microporesand micropores decreased to membranes and M-CTA/CDA and M-CTA/CDA-Rho. The results for thetransport properties showed that the membrane M-CTA/CDA obtained a flow of pure water of 20.37L.m -2 .h -1 and the best result of rejection of 87.39% for egg albumin (EA). The M-CTA/CDA-Rhoshowed 80.50% rejection to EA and greater flow of pure water to 67.63 L.m -2 .h -1 . The M-CTApresented a flow of 7.54 L.m -2 .h -1 and rejection of 79.13% for EA. Thus both membranes preparedfrom the polymer mixture obtained rejection above 80% protein, determining MWCO the relative EA(45kDa) and can be used in UF processes for retaining solutes of molecular weight greater than 45kDa.Bibliographic Reference[1] D. A. Cerqueira, G. Rodrigues Filho, C. S. Meireles (2007), Carbohydr Polym., 69, 579-582.[2] I.M. Wienk, R. M. Boom, M. A. M. Beerlange, A. M. W. Bulte, C. A. Smolders, H. Strathmann(1996), J Membr Sci, 113, 361-371.

Characterization of Cellulose Acetate Membranes Produced from Mango SeedCarla S.Meireles 1* , Sabrina D. Ribeiro 2 , Elaine A. Mundim 2 , Guimes Rodrigues Filho 2 , JoyceRover Rosa 2 , Rosana M.N.Assunção 3 , Mara Zeni 4 , Aldo Bottino 5 , Gustavo Cappanelli 51 Departamento de Ciências Naturais -CEUNES-UFES São Mateus-ES,Brazil2 Chemistry Institute (UFU), Uberlândia, Minas Gerais, Brazil.3 College of Integrated Sciences, (UFU), Ituiutaba, Minas Gerais, Brazil.4 Department of Physical and Chemistry, (UCS), Caxias do Sul, RS, Brazil5 Dipartimento di Chimica e Chimica Industriale, Università di Genova,Genova,Itália* carlameireles@ceunes.ufes.brCellulose acetate membranes obtained from cellulose extracted of the mango seed have beenevaluated with respect to its properties of transport in separation processes [1]. In this study themembranes were produced, from a solution of cellulose acetate in the solvent system dioxane /acetone (D / A = 2.5), using the phase inversion technique[2,3]. In the preparation, the parametersevaluated were the temperature of the coagulation bath, 24 and 4 °C and time of solventevaporation, 30, 90 and 120 seconds. All membranes produced were evaluated as retention of saltsolution with NaCl 1000 mg L -1 conducted at 25 °C in a tangential flow membrane module, effectivearea of 66 cm 2 and a transmembrane pressure of from 5 to 30 bar. The membranes produced werealso evaluated relative its morphology by scanning electronic microscopy (SEM). The results revealedthe influence of the temperature of coagulation bath in the formation of the structure of themembranes. The temperature of 4 °C favors the formation of dense structures which allowincreased retention of salt as demonstrated by the result of retention of 78% compared to 70% ofthe membrane produced in the coagulation bath temperature of 24 °C. The microscopies of thesurface and cross section corroborate these findings, Figure 1, (M-24 °C and M1-4 °C). The increase inevaporation time also showed results of enhance in the % retention of salt of the membranes thatwith 120 seconds obtained retention of 84.3% and 82% in 90 seconds. The microscopies alsorevealed changes in the surfaces, that become denser with increasing time of evaporation, and thecross section with the formation of a dense layer over a porous support. This structure formed isresponsible for the enhance in the retention of the membranes. To evaluate the selectivity of themembrane was carried out an experiment under the same conditions, using the membranes 120seconds to measure the retention of a solution of MgSO 4 1000 mg L -1 . The result obtained was 94%for this solute indicating that this membrane has the best performance for ions larger. These samemembranes are being evaluated against different solutes and molecular masses.M(a)M(b)

M1(a)M1(b)M2(a)M2(b)M3(a)M3(b)Figure 1: SEM of the membranes M(24ºC-30 sec.), M1(4ºC-30 sec.), M2(4ºC-90 sec.), eM3(4ºC-120 sec.), (a) cross section and (b) surface of the membranes. 5000X.Bibliographic Reference1. Meireles et. al., (2010). Carbohydrate Polymers, 80, 954–961.2. S.V.Joshi, A.V. Rao, (1984)Desalination, 51, 307-3123. R.Chi Ong, T-S.Chung., (2012). J. Membr. Sci. 394-395 , 230-240.

Monitoring the Shelf Life of Microfiltered WheyMaura Pinheiro Alves 1 , Renam de Oliveira Moreira 1 , Guilherme Mendes da Silva 1 , RafaelOliveira Bento 1 , Cláudia Lúcia de Oliveira Pinto 2 , Antônio Fernandes de Carvalho 1 *1 Department of Food Technology, Federal University of Viçosa, Viçosa, Minas Gerais, Brazil2 Agricultural Research Company of Minas Gerais - EPAMIG, Viçosa, MG*Corresponding author: Antônio Fernandes de CarvalhoE-mail address: afc1800@yahoo.comThe development of alternatives to a suitable utilization of whey is extremely important because thetransformation of the whey in a number of products decreases environmental problems and enablesthe development of new products and increased profits in dairy industries. This study aimed toevaluate the application of the microfiltration technology as alternative to thermal treatment forimproving the microbiological quality of whey. Whey samples were subjected to the operations ofmicrofiltration (membranes with pores of 0.8 and 1.4 μm in diammeter), pasteurization (72 ºC for 15seconds) and thermization (65ºC for 15 seconds) and potted into bottles sterile of 200 ml. Thesesamples and the control (raw whey) were storage for 20 days at 4 ºC for the evaluation of their shelflife by monitoring their pH and acidity, and the number of mesophilic aerobic and psychrotrophicmicroorganisms. These data were evaluated using a split-plot model with five levels of treatmentsapplied to whey, randomized in plots with five replications, and assessments throughout the 20 daysof storage were the subplots, which were studied by analyzing regression. The whey sample whichwas microfiltered using the 0.8 μm-pore membrane presented longer shelflife, with constant countsof mesophilic aerobic and psychrotrophic microorganisms smaller than 1 CFU.mL -1 and 10 CFU.mL -1 ,respectively, beyond constant values for acidity and pH during the 20 days of storage at 4 °C. The useof membrane technology using microfiltration of 0.8 μm pore showed to be a viable alternative tothermal treatment by allowing obtain whey stable of microbiological point view and in relation tothe acidity and pH, resulting in a product with longer shelf life. The absence of thermal treatmentwith use of this membrane technology allows still maintaining the nutritional and sensorycharacteristics of the product.

Parametric Analysis of a Ethylbenzene Dehydrogenation Model carried on aMembrane Reactor with heat and mass transferGermano Possani*, Roger J. Zemp.Faculty of Chemical Engineering at State University of Campinas - UNICAMP.germano.eq@gmail.comThe Process Intensification aims the development of smaller, cleaner and more energeticefficienttechnologies [1] and inside this field lies the membrane reactor processes. The processanalyzed in this work refers to a mathematical model for dehydrogenation of ethylbenzene tostyrene, which is the desired product. The advantage of the a membrane reactor instead of packedbed reactors is the shift of the thermodynamic equilibrium, Le Chatelier's principle, due to thehydrogen removal by membrane [2].An inorganic composite membrane module is used. This membrane has two distinguishedlayers, one is the Porous Stainless Steel (PSS) support and another is a thin Palladium film coatedover the support [3]. As the above process occurs close to 620 °C [4], the temperature resistantsupport material has to be used (PSS), whereas the palladium film is used due to its uniquecharacteristic of be permeable only to the hydrogen [5]. The dehydrogenation is carried out insidethe packed bad, while the sweep gas passes in the permeate side to remove hydrogen.The temperature, pressure and concentration ODE equations were calculated in axialdirection using a Runge-Kutta method. In radial direction the ODE equations were turned in algebraicequations and the resulting system of equations was solved by a multivariate Newton-Raphsonmethod.For the parametric analysis conditions such as temperature, pressure, porous support size,concurrent or countercurrent flow directions, and steam to oil ratio were analyzed. The resultsindicate that is possible to achieve new improved values of conversion of ethylbenzene andselectivity and yield of styrene making some adjustments in the membrane configuration and theoperational conditions. This improvements are important accomplishments in Process Intensificationbecause they are an alternative way to reduce the energy consumption in the dehydrogenation ofethylbenzene process and the use of less and smaller equipments in the plant.[1] A. I. Stankiewicz, J. A. Moulijn (2000), Chem. Eng. Prog., January 2000,22-34.[2] N. S. Abo-Ghander, J. R. Grace, S. S. E. H. Elnashaie, C. J. Lim (2008), Chem. Eng. Sci., 63, 1817-1826.[3] J. Tong, H. Suda, K. Haraya, Y. Matsumura (2005), Journal of Membrane Science, 206, 10-18.[4] Ch. Hermann, P. Quicker, R. Dittmeyer (1997), Journal of Membrane Science, 136, 161-172.[5] Y. She, J. Han, Y. H. Ma (2001), Catalysis Today, 67, 43-53.

Clarification of Artichoke By-product Extract by Membrane Process:Membrane Selection Criteria and Fouling Mechanism Modeling DuringFiltrationMariana Teixeira da Costa Machado*, Miriam Dupas Hubinger.Department of Food Engineering, School of Food Engineering,University of Campinas, Campinas, SP, Brazil.e-mail: marifea@fea.unicamp.brArtichoke by-product originated from canning industry (bracts of heads) represents a hugeamount of discarded material and could be considered a promising and cheap source ofpolysaccharides, mainly inulin. After the extraction process, an initial clarification can removethe components responsible for turbidity and instability of the product. The objectives of thisstudy were: the selection of an appropriate membrane and identification of the flux declinemechanism during filtration of artichoke by-product extract using three different membranes.Artichoke bracts were homogenized with distillated water (1:40). The mix was continuallystirred at 85 °C during 3 h. Then, the extract was filtered to remove rough particles. Three flatsheet membranes manufactured by Microdyn-NADIR (Piracicaba, SP, Brazil) were used: one ofmicrofiltration (MF, polyethersulfone, 0.05 μm) and two of ultrafiltration (U100, cellulose, 100kDa, and U10, cellulose, 10 kDa). A dead-end stirred cell (effective membrane area of 50.24cm²) was used to conduct the trials in the open mode. The filtrations were performed at 25 °Cand 2 bar for microfiltration and 8 bar for ultrafiltration. Permeate was removed untilobtaining a volume reduction factor (VRF) of 4.0. Performance of membranes was studied interms of permeate flux, identification of flux decline mechanism during filtration [1], mass ofsolute adsorbed [2] and permeate quality: recovery of polyssacharides, reducing sugar, inulin,soluble and total solids and color parameters.The permeate flux decline was the more pronounced in MF and U100 membranes (Figure 1).And, for these membranes, the mass of adsorbed solute on the membrane surface and poreswas higher. The best prediction of the permeate flux was provided by cake layer formationfollowed by the intermediate blocking model to all the membranes.In general, the membranes rejected a big amount of soluble solids and low amount of totalsolids content. The recovery of total carbohydrate and inulin in permeate (77%) was the lowestfor MF membrane. But the highest rejection coefficient (35%) towards reducing sugar wasobtained for this membrane. In general, permeates were more diluted and clearer than feed.Microfiltration was found to be the most suitable process to clarify aqueous by-productartichoke extract. The results obtained motive the continuity of researches on the applicationof membrane technology to treat the aqueous by-product artichoke extract.

(a)(b)(c)(d)Figure 1. Permeate flux and calculated values according to the fouling models of the extractfrom artichoke bracts determinate with (a) MF, (b) U100 and (c) U10 membranes, and (d) VRFalong filtration.TBM= Total pore blocking model; SBM= Standard pore blocking model; IBM= Intermediate pore blocking model;CLM = Cake layer formation model.[1] J. Hermia (1982), Chem. Eng. Res. Des., 60, 5.[2] B. Díaz-Reinoso et al. (2011), Chem. Eng. J., 175(0), 95-102.

WATER TREATMENT TO HEALTH CLINICSAnna Lecticia Martinez Toledo 1 , Maria Eugênia Sena 2 .1,2UNIVERSIDADE FEDERAL DO ESTADO DO RIO DE JANEIRO/UNIRIO-CCBS/DCNAV. PAUSTER 458, Room 412, URCA- RIO DE JANEIRO. 1- Anna_tldc@yahoo.com.brAccording to the OMS, diarrheal diseases are responsible for the deaths of 1.8 million people everyyear and sums up to an estimated 4.1% of the total world DALY, the number of years lost due to illhealth,premature death or disability. It was estimated that 88% of this burden is attributable tounsafe water supply, sanitation, personal hygiene, and it is mostly concentrated on children fromdeveloping countries [1] .With those numbers, the need to create effective and cheaper means topurify water in a potable level, to avoid waterborne diseases, becomes clear. The UN estimates thatsimply meeting the Millennium Developing Goals related to water and sanitation would save $7.3billion per year in health care costs [2] .The SMEWW (Standard Methods for the Examination of Water and Wastewater) defines the coliformgroup as aerobic bacteria or facultative anaerobic bacteria, gram negative, non sporulating and inrod-shape form. They should also be lactose fermentative, with the production of gas in 48h at 37 °C.This group is composed by organisms that differ in their biochemical habitats and serologicalcharacteristics. They can be classified as Escherichia, Aerobacter, Citrobacter, Klebsiela, amongstothers that are not so common to turn up in stool test [3] .In Brazil, the Ordinance n o 518/GM on March 25 th of 2004 [4] establishes the standards for waterquality, vigilance and potability, as shown below:Water for human consumption must be devoid of E. coli or thermotolerant coliforms in100ml.Water in the exit of a treatment site must be devoid of total coliforms in 100ml.Water treated at distribution systems such as reservoirs must be devoid of E. coli orthermotolerant coliforms in 100ml. For systems that analyze 40 or more samples per month,95% of the 100ml samples should be devoid of total coliforms and, for systems which analyzeless than 40 samples per month, only one sample each month can present a positive resultfor total coliforms test.The goal of this work was to test a small module with specific microfiltration membranes. Themicrofiltration membranes are hollow fibers, made from a polymer material with pores which have awidth of 0.0002 millimeters. These pores were responsible for the rejection of microorganisms andsuspended particles. This hollow fiber membrane was chosen for this work based on its properties,such as higher permeation, low use of energy and the possibility of retro-washing, diminishing thecost of the system by avoiding a constant replacement of the module during its life span.The process uses porous membranes that have their selective capacity directly associated to the sizeof the species present on a sample and the size of the membrane pore. That’s the case withprocesses like microfiltration, which were used on this project. Besides that, the species present at

effluents should have an affinity as low as possible with the material of the membrane, just as thematerial from the membrane should be as hydrophobic as possible.Depending on the pressure, the water flows in a convective way through the membrane pores [5] . Inthis case, the microfiltration had a pressure gradient along the membrane in a range from 0.1 to 0.6bar at the max.The hollow fiber membranes, which will retain microorganisms bigger than 0.0002 millimeters, canalso reject organic species without affinity with the membrane material, avoiding the formation of abiofilm around the fiber.The characterization of the effluent, before and after the permeability tests, was made to show thedifferent concentration of Coliforms and Salmonella sp. The tests were carried out using directculture on petri dishes with Nutritive Agar, since the species that are most preferred in the findings isthe E. coli, which grows in this type of medium [6] , and quick tests for Salmonella sp. made byTECNOBAC®, all to assure that the result of this project is a potable water and that this system can beapplied in many places such as clinics, dentist’s offices and hospitals, in order to lower the numberof patients who are afflicted by waterborne diseases .Bibliography[1]Burden of disease and cost-effectiveness estimates. World Health Organization. Available at[2]Water Pollution and Contamination. World Savvy Monitor. Available at< http://worldsavvy.org/monitor/index.php?option=com_content&view=article&id=709&Itemid=1195>[3] [CETESB] Companhia Estadual de Tecnologia e Saneamento Ambiental. Controle da qualidade da água paraconsumo humano: bases conceituais e operacionais. São Paulo; 1997. 152-4.[4] BRASIL. Ministério da Saúde. Portaria nº 518/GM, de 25 de Março de 2004.[5]A.C. Habert, C. P. Borges, Nóbrega R (2003). Processos de Separação com Membranas, 1, 4.[6]S. Mims, M.H. Dockrell, R.V. Goering, I. Roitt, D. Wakelin, M. Zuckerman (2005). Microbiologia Médica, 643.We would like to thank FINEP for their support of this work.

PAPER TITLE: ULTRAFILTRATION AS PRETREATMENT IN RIVER WATER DESMINERALIZATIONBY REVERSE OSMOSISAUTHOR: Eng. Manuel García de la Mata, Product Manager at Unitek S.A. and ADRA’s (AsociaciónArgentina de Desalinización y Reuso) Pro-SecretarioE-MAIL ADRESS: garciadelamata@unitek.com.arPOSTAL ADRESS: República de Cuba 1034, Mar del Plata (B7608EBV)TELEPHONE NUMBER: +54 223 4825888FAX NUMBER: +54 223 4812182TYPE OF PRESENTATION: oral / poster

SUMMARYReverse osmosis has been widely used for well water treatment in Argentina since many years ago andthere has been a rapid expansion in the market in the last 15 years. However, the use of reverse osmosistechnology for desmineralization of river water has not been still accepted. Considering the location ofmany industries and power plants close to Paraná and Río de la Plata rivers in Argentina and the highoperative cost of ionic exchange nowadays, the use of reverse osmosis should be common. Badexperiences due to inappropriate pre-treatment explain the lack of diffusion of reverse osmosis for riverwater treatment.This paper is focused on the use of ultrafiltration as pre-treatment for river water treatment by reverseosmosis. Some basics concepts are developed as introduction to ultrafiltration technology and asuccessful case of river water (Río de la Plata) desmineralization trough ultrafiltration + reverse osmosis ispresented.OUTLINEThe production of desmineralizated water (DW) is a key factor for power stations and many processindustries. In Argentina most industries and many power plants are located close to rivers, mainly Paranáand Río de la Plata rivers.For the production of desmineralizated water from river water in Argentina reverse osmosis (RO) is almostnot used even though is extensively used in the production of DW from well water. Two main factorsexplain the lack of diffusion of the RO for river water treatment in Argentina:• In the past ion exchange (IX) was competitive from an operative cost (OpEx) stand point due tolower chemical prices and low salinity of the river water.• Very bad experiences in the use of RO for river water treatment due to high fouling rates.However, in the last years there were two important changes. The prices of the chemical products used forIX have highly increased and new membrane technologies are available for RO pre-treatment. In this newscenario added to the industry tendency of avoiding the use of hazardous chemical products, RO appearsas the best option for DW production.This paper presents basic concepts of the ultrafiltration (UF) technology as RO pre-treatment for surfacewaters and a successful case of UF+RO for DW production from Rio de la Plata water. The case studiedis a DW plant installed in a power plant in the city of Buenos Aires after one year of operation with thefollowing process stages:• Conventional clarification• Ultrafiltration• Reverse osmosis• Continuous electrodeionization (CEDI)It is important to point out that the use of CEDI as final stage of the process (polish) reduces the use ofchemicals in the DW production to a minimum.After one year of operation without any fouling in the RO membranes (no chemical cleaning wasnecessary yet) this case demonstrates that UF allows treating river water with RO in a reliable and costeffective way.

Continuous Production of Biodiesel using a Liquid-Liquid Film Reactor packedwith Hollow Fiber MembranesAderson Imbachi 1 , Nevardo Bello Yaya 1 , Luz Dary Carreño Pineda 1 , Juan Guillermo CadavidEstrada 1 , Alberto Claudio Habert 2 , Paulo César Narváez Rincón 11. Grupo de Procesos Químicos y Bioquímicos, Departamento de Ingeniería Química.Facultad de Ingeniería, Universidad Nacional de Colombia, Bogotá, Colombia.2. Laboratório de Processos de Separação com Membranas e polímeros PAM,Universidade Federal do Rio de Janeiro, Río de Janeiro, Brazil.* pcnarvaezr@unal.edu.coProcess intensification in biodiesel production has been a very active research field duringthe last decade. Among the alternatives evaluated, reactive distillation and extraction, microreactors, microwave and ultrasound have been widely investigated [1-3]. The use ofmembranes has been studied mainly in the separation and purification steps, in order toremove the remaining monoglycerides, diglycerides, triglycerides and glycerol in theproduct, in the reaction stage as support for heterogeneous catalysts, and, to a lesser extent,as media for the simultaneous reaction and separation [4-7]. Carbon and ceramicmembranes are the most studied, regarding some limitations of polymer membranes,mainly about chemical resistance to methanol and to the typical homogeneous basiccatalysts (sodium and potassium metoxide and hydroxides), affecting the membranestructure [8]. This paper present some results of a new development about the continuousproduction of biodiesel from Jatropha oil in a falling film reactor [9], using ultrafiltrationhollow fibers as packing material. Methanolysis and glycerol separation occursimultaneously, aiming at shifting the reaction equilibrium to the product side, increasingthe conversion of oil and the yield to methyl esters when compared to conventionalreactors. In addition to the evaluation of chemical resistance of commercialpolyethersulfone (PES) and polyetherimide (PEI) membranes to methanol, glycerol,methanol-NaOH, and jatropha oil methyl esters, transport properties were evaluated.Results showed that the PES membrane was more efficient. A bench level experimentalmodule was designed to study the continuous production of biodiesel exploring themembrane liquid-liquid falling film concept and will be presented.[1] N. Da Silva, M. Santander, C. Batistella, R. Maciel, M. Maciel (2010), Appl Biochem Biotechnol, 161, 245-254.[2]G. Kraai, B. Schuur, F. van Zwol, H. van de Bovenkamp, H. Heeres (2009), Chem. Eng. J, 154, 384-389.[3] S. Unker, M. Boucher, K. Hawley, A. Midgette, J. Stuart, R. Parnas (2010) Bioresource Technol, 101, 7389-7396.[4] M. Dubé, A. Tremblay, J. Liu (2007), Bioresource Technol. 98, 639-647.[5] J. Saleh, A. Tremblay, M. Dubé (2010), Fuel, 89, 2260-2266.[6] M. Gomes, N. Pereira, S. De Barros (2010), J. Membrane Sci. 352, 271-276.[7] S. Baroutian, M. Aroua, A. Raman, N. Sulaiman (2011), Bioresource Technol., 102, 1095-1102.[8] R. Othman, A. W. Mohammad, M. Ismail, J. Salimon (2010), J. Membrane Sci, 348, 287-297.[9] P.C. Narváez, F. J. Sánchez, R. D. Godoy (2009), J. Am Oil Chem Soc, 86, 4, 343-352

Measurement of the solubility of water - ethanol mixtures in PDMSmembranesAndrea Fuertes*, Mario Noriega, Miguel Ángel Gómez García, Javier FontalvoFacultad de Ingeniería, Universidad Nacional de Colombia, Manizales, Colombiaandreafuertesr@gmail.com*The measurement of the solubility of the ethanol - water mixture into the PDMS polymermembranes is necessary to describe the flux of these components through the membrane; howeverlittle information is reported in the literature relating to such measurement [1,2,3]. This paperdevelops an experimental technique for the determination of the solubility in polymer membranes ofPDMS which is based on the quantification of the phase dispersion through photography, theexperimental technique was used for the evaluation of the solubility of ethanol - water mixturesthrough PDMS membrane, the results have good reproduction and appears to fit well with theresults reported in the literature.[1] J. Hauser, G. Reinhardt, F. Stumm, A. Heintz. (1989), J. Membr. Sci., 47, 261-276.[2] A. Heintz, W. Stephan. (1994a), J. Membr. Sci, 89, 143–151.[3] A. Heintz, W. Stephan. (1994b), J. Membr. Sci, 89, 153–169.

Performance of Liquid Membranes in the Taylor Flow regimeJuan David García-Mahecha, Alan Didier Pérez-Ávila, Miguel Ángel Gómez-García, JavierFontalvo-Alzate *Universidad Nacional de Colombia - Sede Manizales – Facultad de Ingeniería y Arquitectura -Departamento de Ingeniería Química – Laboratorio de Intensificación de Procesos y SistemasHíbridos – G.I.A.N.T.: Grupo de Investigación en Aplicación de Nuevas Tecnologías -Cra 27 No. 64 – 60, Manizales, Apartado Aéreo 127 - Colombia* jfontalvoa@unal.edu.coSeparation processes using liquid membranes are advanced techniques for recovery, purification andabatement of substances in liquid or gas streams that can be integrated to other separation orreactive processes in order to increase productivity and performance. This integration can beimplemented using the Process Intensification Philosophy. This kind of membranes technology hasbeen intensively studied [1]. The non-supported liquid membranes are more attractive than thosethat are supported, because in the former the mass transfer rate is higher and there is a bettercontrol on the liquid membrane losses. However, the non-supported liquid membranes require theformation of emulsions that can be easily broken, reducing the separation efficiency or, on thecontrary the emulsion is very stable and consequently inhibits the phase splitting between the feedand strip phases [1]. Usually, in order to improve the emulsion stability, surfactants are used.However, they pollute the feed or strip phases and they can reduce the mass transfer rate [2].Figure 1. Diagram of a liquid membrane in the Taylor flow regime.This work proposes a new type of contact for liquid membranes by using the Taylor flow regime.Thereby the feed and strip phases are located in the same tube in drops or Taylor "bubbles", whilethe continues phase, that forms liquid slugs, constitutes the liquid membrane itself (Figure 1). Themass transfer start at the feed phase, continues through the liquid membrane and finishes at thestrip phase. This study experimentally studies the transport rate in liquid membranes in the Taylorflow regime for separation of lactic acid at several speeds of the feed and strip phases and analysesthe effects that the drop length has on mass transfer. The low layer thickness around the drops, thehigh liquid speed in this layer and the turbulence at the drop tail (von Kárman vortices) produce highmass transfer rates. This type of liquid membrane avoids the contact between the feed and stripphases overcoming the coalescence and improving the phase splitting. This kind of liquid membranepreserves the advantages of conventional emulsion liquid membranes while overcomes the stabilityproblems of emulsion systems.[1] V. S. Kislik, Liquid Membranes Principles & Applications in Chemical Separation & Wastewater Treatment,Elsevier B.V., Amsterdan, 1st Ed., 2010.[2] M. Aguilar and J. L. Cortina, Solvent Extraction and Liquid Membranes Fundamentals and Applications inNew Materials, Taylor & Francis Group, London, 1st Ed., 2008.

Modeling and Simulation of Membrane Reactor for BiodieselProductionMario Noriega 1 , Anderson Imbachi 1 , Nevardo Bello Yaya 1 , Luz Dary Carreño Pineda 1 , JairoErnesto Perilla Perilla 1 , Juan Guillermo Cadavid Estrada 1 , Alberto Claudio Habert 2 , PauloCésar Narváez Rincón* 11. Grupo de Procesos Químicos y Bioquímicos, Departamento de Ingeniería Química.Facultad de Ingeniería, Universidad Nacional de Colombia, Bogotá, Colombia.2. Laboratório de Processos de Separação com Membranas , COPPE,UniversidadeFederal do Rio de Janeiro, Río de Janeiro, Brazil.* pcnarvaezr@unal.edu.coBiodiesel is an important renewable fuel whose production has been limited mainly by highresidence times in the reaction and separation sections due to the presence of soaps and highviscosity gels. This work studies the possibility of reducing this problem by implementing a falling filmreactor integrated whit hollow fiber membranes. This reactor takes advantage of both systems: whileproduction of biodiesel using a falling film reactor is characterized by high reaction rates andproductivity and a positive effect on separation stages because interfacial mass transfer area isachieved without mixing [1], the integration of a membrane system would lead to higher yields tofatty acid methyl esters as well would perform the simultaneous purification of the biodiesel [2,3,4].In this work a mathematical model to predict the behavior of a falling film reactor assisted bymembranes was developed. The model describes a PFR reactor [2,5] and the flux through themembrane by the transport equations of Maxwell-Stefan [6]. A sensitivity analysis was performed toanalyse the operation of the membrane reactor and identify the main variables of the system. Themodel predicts the appropriate operating conditions range for experimental evaluation. Simulationof the process allows us to conclude that there is a strong drag effect exerted by methanol on theglycerol, and that both the conversion and yield in the reactor increase with the biodiesel andglycerol permeated fluxes, but decreases with the flux of methanol, a clear indication that theamount of methanol fed to the reaction system is a main operating variable because it stronglyaffects transport through the membrane.[1] P.C. Narváez, F. J. Sánchez, R. D. Godoy (2009), J. Am Oil Chem Soc., 86, 4, 343-352.[2] S. Baroutian, M. Aroua, A. Raman, N. Sulaiman (2011), Bioresource Technol., 102, 1095-1102.[3] P. Cao, M. Dubé, A. Tremblay (2008), Fuel., 87, 825-833.[4] L. Cheng, Y. Cheng, S. Yen, J. Chen (2010), Bioresource Technol., 101, 6663–6668.[5] L. Cheng, Y. Cheng, S. Yen, J. Chen (2012), Chemical Engineering Science., 69, 81–92.[6] P. Izak, L. Bartovska, K. Friess, M. Sipek, P. Uchytil. (2003), J. Membr. Sci., 14, 293–309.

Performance of Batch Pervaporation Membrane Reactorfor Isoamyl Acetate SynthesisWilmar Osorio-Viana a , Jesús David Quintero-Arias a , Javier Fontalvo a ,Izabela Dobrosz-Gómez b , Miguel Ángel Gómez-García a,*Grupo de Investigación en Aplicación de Nuevas Tecnologías, Laboratorio de Intensificaciónde Procesos y Sistemas Híbridos. a. Departamento de Ingeniería Química, Facultad deIngeniería y Arquitectura, b. Departamento de Física y Química, Facultad de Ciencias Exactasy Naturales. Universidad Nacional de Colombia, Sede Manizales. Campus Palogrande,Cra 27 64 – 60, Apartado Aéreo 127, Manizales, Caldas, Colombia* magomez@unal.edu.coBatch Pervaporation Membrane Reactor (BPVMR) is a promising technology for equilibrium limitedreactions. The concept of esterification reactions carried out in pervaporation membrane reactorwith in-situ or ex-situ water removal for a favorable shift in the equilibrium has been proved, e.g. inthe formation of ethyl and butyl acetates [1], ester of hexanoic acid [2], tartaric acid [3]. Productionof value added chemicals from agricultural residues like fusel oil (mainly constituted of isoamylalcohol) can be a potential field for BPVMR industrial commercialization. Low energy requirementsof membrane separation, reduction in plant equipment and in operational costs as well asproductivity enhancement can be mentioned as its main theoretical advantages. However, the majordrawbacks for a particular industrial application are: synthesis/selection of a suitable selectivemembrane and its evaluation at operational conditions.In this work, catalytic esterification of acetic acid with isoamyl alcohol, using Amberlite IR-120 ionexchange resin as catalyst, was conducted in a laboratory scale BPVMR. Two different membraneswere tested: a hydrophilic homemade silica membrane, with in-situ separation; and commercialHybSi® ceramic one, with ex-situ separation. The experiments were performed under stoichiometricfeed and isothermal conditions. The obtained results show that the homemade silica membrane hasa maximum water flux of 0.8 kg/m 2 .h and a mean water selectivity of 140, leading to a permeatestream with water at 75 wt./wt.% and a total conversion of 87% over the 69% equilibrium conversionexpected in a conventional reactor. Observed reactor productivity is as high as 1.75 kg ester /kg acid .The comparison between experimental data and simulation results (using previously validatedthermodynamic [4], kinetic [5] and permeation [6] models) shows reasonable agreement. Basing onexperimental results, pros and cons of tested homemade silica and commercial membranes arehighlighted. To guide the industrial implementation of a continuous BPVMR process for isoamylacetate production, suggestions are established for process conditions (e.g., operation mode,membrane area/catalyst mass and membrane area/reactor volume ratios).Acknowledgments: ECOPETROL-COLCIENCIAS-UNIVERSIDAD NACIONAL DE COLOMBIA, SEDEMANIZALES are gratefully acknowledged for financial support (Project number: 1119-490-26022).References[1] S.Y. Lim et al. (2002) Chem. Eng. Sci., 57, 4933 - 4946.[2] A. E. W. Beers et al. (2001) Catal. Today, 66, 175-181.[3] J. T. F. Keurentjes et al. (1994) Chem. Eng. Sci., 49, 4081-4089.[4] W. Osorio- Viana et al. (2013) Fluid Phase Equilibria, 345, 68 – 80.[5] M. Duque-Bernal, et al. (2013) Int. J. Chem. Kinet. 45, 10–18.[6] W. Osorio- Viana et al. (2013) Deswater, 51, 2377 – 2386.

Isoamyl Acetate Production - Membrane Reactor Design GuidelinesWilmar Osorio-Viana a , Jesús David Quintero-Arias a , Javier Fontalvo a ,Izabela Dobrosz-Gómez b , Miguel Ángel Gómez-García a,*Grupo de Investigación en Aplicación de Nuevas Tecnologías, Laboratorio de Intensificaciónde Procesos y Sistemas Híbridos. a. Departamento de Ingeniería Química, Facultad deIngeniería y Arquitectura, b. Departamento de Física y Química, Facultad de Ciencias Exactasy Naturales. Universidad Nacional de Colombia, Sede Manizales. Campus Palogrande,Cra 27 64 – 60, Apartado Aéreo 127, Manizales, Caldas, Colombia* magomez@unal.edu.coAs a new field for chemical technology development, processes intensification must deal with moretight requirements in performance, environmental impact, safety, product quality, energyconsumption and industrial competitiveness. Process intensification by membrane reactors isreceiving increasing attention to accomplish these necessities. However, the lack of systematic set ofchemical engineering tools for its optimal design and operation is observed.The application of agro-industrial residues to obtain valuable chemicals is of the main importancedue to the observed worldwide rapid growth of biofuels markets. Fusel oil is a liquid residue from thebioethanol production, mainly constituted of isoamyl alcohol. It can be converted, throughesterification to isoamyl acetate, to a compound with plenty of applications in the food and cosmeticindustry, among others. Low conversion and high energy consumption, problems frequentlyobserved in current production technologies, can be overcome using pervaporation membranerectors for simultaneous product removal.In this work, mathematical modeling and simulation using thermodynamic [1], kinetic [2] andmembrane transport [3] models developed for this process are used to analyze differentpervaporation membrane reactors schemes. The application of chemical equilibriumthermodynamics let to predict the possible products of the reaction as well as to obtain themembrane residue curve map for the reactive mixture. The performance of the process is evaluatedfor several types of membrane reactors: continuous stirred, plug flow, recycle plug flow and recyclecontinuous stirred, in terms of key design variables related through dimensionless numbersaccounting for reaction rate/residence time ratio, recycle ratio, reactor size/membrane area ratioand membrane flux and selectivity.The obtained results for maximum ester yield and maximum water separation shows that plug flowtype units presents better performance than sequential perfect mixing schemes. Several designheuristics are developed and a graph-numeric pervaporation membrane reactor map for analysis anddesign is presented. These tools can be used to define the optimal process conditions for furtherindustrial implementation.Acknowledgments: ECOPETROL, COLCIENCIAS and The UNIVERSIDAD NACIONAL DE COLOMBIA,SEDE MANIZALES, are gratefully acknowledged for financial support (Project number: 1119-490-26022).References[1] W. Osorio- Viana et al. (2013) Fluid Phase Equilibria, 345, 68 – 80.[2] M. Duque-Bernal, et al. (2013) Int. J. Chem. Kinet. 45, 10–18.[3] W. Osorio- Viana et al. (2013) Deswater, 51, 2377 – 2386.

Demineralization of waste waters containing phenol by electrodialysisH. Roux-de Balmann * 1,2 , F.J. Borges 3 , R. Guardani 31 Université de Toulouse; INPT, UPS; Laboratoire de Génie Chimique; France2 CNRS ; Laboratoire de Génie Chimique, Toulouse, France3 Chemical Engineering Department, University of São Paulo; SP- Brazilroux@chimie.ups-tlse.frRecalcitrant organic pollutants, like phenol and phenolic compounds, common contaminants inindustrial wastewater, have been recognized as an issue of growing importance in recent years. Sinceconventional wastewater treatments are hardly capable of removing such pollutants, oxidationprocesses are generally used for their degradation. However, such processes can be inhibited by thepresence of ionic compounds, like sodium chloride, often associated with these pollutants inwastewater.In order to fit with the salt content acceptable for the oxidation treatment of the organic matter,electrodialysis can be used to demineralize the waste water. The objective is then to decrease thesalt content down to a given value while minimizing the transfer of the organic pollutant to keep it asmuch as possible in the desalted stream to be further treated by oxidation.An experimental study was carried out with synthetic waste waters containing phenol and sodiumchloride, the experimental conditions and characteristic parameters being obtained by anexperimental design. A pilot plant (EURODIA) was used equipped with AMX and CMX membranes.The phenol and salt concentration variations in the ED compartments were monitored over time. Thedependence of the process performances, characterised by the demineralisation factor and theorganic matter recovery, i.e. the phenol transfer through the membranes, with respect to theoperating parameters was investigated. Experiments were also performed without current, in orderto determine the possible phenol transfer due to diffusion, which represents the minimum phenolloss expected during the desalination. A phenomenological approach, based on irreversible

thermodynamic models, was used to relate the phenol, salt and water fluxes with the driving forces(concentration and electric potential gradients) [1].Concerning the water transfer, the contribution of electrososmosis due to the water transportaccompanying the migration of salts was found to be predominant over that of osmosis as far as acurrent is applied. In the same manner, for the salts, the transfer due to migration was foundpredominant compared to that due to diffusion. Then, the current intensity can be considered as themost significant variable affecting both water and salt transfer in the ED system. Concerning thephenol transfer, a convective contribution was pointed out during ED experiments in addition to theminimum expected one coming from diffusion. This convective contribution, that increases thephenol loss during the desalting process, was correlated to the electroosmosis flux.For the conditions of this study, i.e. for the solutes and membranes used, the characteristicparameters of the equations relating the different contributions to the mass transfer were alsodetermined. This was done by fitting experimental results with the ones calculated by the model.Mass balance equations were proposed to describe the evolution of the volumes and the salt andphenol concentrations in each compartment as a function of their initial values and of the currentdensity. These equations depend basically on the transport parameters that have to be estimatedexperimentally for each membrane system. Then, the ED performances, i.e. the loss of phenol andthe salt concentration in the demineralized wastewater, can be calculated as a function of theoperating parameters, like the current density or the initial salt concentration in the feed.Concerning the process performances, it was demonstrated that despite that, high demineralisationfactors can be reached while maintaining the phenol yield at a reasonable level for further treatmentby oxidation. The relationship between the demineralisation factor and the phenol yield can also betuned according to the operating conditions. ED is then an interesting means to treat saline wastewaters containing organic pollutants, like phenol, prior to the chemical treatment.[1] F.J. Borges et al. / Journal of Membrane Science 325 (2008) 130–138This work was carried out in the frame of the PhD of F. Borges, funded by the CAPES, which is acknowledged

Electrodialysis for food and environmental applicationsScientific targets and industrial realizationsHélène Roux-de BalmannUniversité de Toulouse; CNRS ; INPT, UPS; Laboratoire de Génie Chimique; FranceElectrodialysis is a recognized technology in the tool box of engineers interested in the developmentof efficient and environmental friendly processes. Starting from the desalination of sea water for theproduction of drinking water in Japan in the 1960’s, electrodialysis is now currently used in the foodindustry, in the field of whey processing, sugar and beverage industries, wine making, and organicacid production from fermentation. Most of the time, electrodialysis is used in combination withother downstream operations, like ion exchange with resins or nanofiltration for instance. Suchincreasing applications of electrodialysis were made possible thanks to an improvement of thetechnology itself (membranes, stacks, ..) as well as to a better understanding of the mass transferthanks to which selectivity, between the ions or between organic solutes and ions, can be nowassociated to desalination.A sustainable process developed for the production of organic acids in collaboration with EURODIAindustry will be presented. This process includes a concentration step by conventional ED followed bya conversion step carried by bipolar membrane ED. The different steps of the investigation strategyas well as the resulting process improvements, like the integration of a nanofiltration step, will bediscussed.Electrodialysis can also be used to improve the treatment of different kinds of waste waters, moreespecially saline waste waters the treatment of which is still very problematic. Indeed, oxidationeither biological or chemical is currently used for the treatment of the organic pollution, but suchoxidation processes are inhibited in the presence of salts. A combined process, including ED as apretreatment for oxidation, will be presented.In any situation, the scientific targets which were investigated and the resulting scientific knowledgewill also be discussed.

Rejection (%)Characterization of RO90 membrane using saline solutions.Application of Spiegler-Kedem-Kachalsky modelA. Hidalgo 1 , G. León 2 , M. Gómez 1 , M.D. Murcia 1 , M.A. Guzmán 2 , C. Guardiola 21 Departamento de Ingeniería Química. Universidad de Murcia. Murcia. Spain. ahidalgo@um.es2 Departamento de Ingeniería Química y Ambiental. Universidad Politécnica de Cartagena. Cartagena.Spain.IntroductionPhysical-chemical processes based on membrane technology have demonstrated to be viablealternatives in the fields of desalination and wastewater treatment. The first steps in the design ofsuch processes are to check and characterise the membranes and to develop mathematical to, bothto predict the efficiency of the processes. In this work, a low reverse osmosis polyamide membrane(RO90) has been characterized using two saline solutions (sodium chloride and magnesium chloridesolutions) in order to ascertain the optimal operation conditions. The results have been processedthrough the graphic resolution method of the Spiegler-Kedem-Katchalsky model [1-4]. Theparameters of the model have been obtained and used to predict the membrane behaviour andperformance.Materials and MethodChemicals: sodium chlorine and magnesium chlorine were purchased from Aldrich and Panreac,respectively. Experimental tests were performed in an MMS Tryple System Model F1 flat membranetest module. The membrane module provides 13.97x10 -3 m 2 of active surface area. Salts aqueoussolutions of concentrations between 1 and 2 g/L were treated in the test module using the RO90membrane purchased from Alfa LavalResultsFigure 1 shows the rejection percentage obtainedfrom sodium chloride ( ) and magnesium chloride( ) using RO90 membrane in the pressure rangeassay (8-16 bar). Using the experimental results,model parameters P S (3x10 -9 and 9x10 -11 m/s) and σ(0.994 and 0.998) were determined. Values of theseparameters were similar to those described in theliterature [5]. From these values, the theoreticalrejections and fluxes were calculated. Goodagreement between the experimental and modeldata have been obtained.100806040200Sodium chlorine0 5 10 15 20Pressure (bar)Magnesium chlorineFigure 1. Variation of rejection coefficientwith applied pressureReferences[1] Pontié, M.; Dach, H.; Leparc, J.; Hafsi, M.; Lhassani, A. (2008). Desalination, 221, 174-191.[2] Ben-David, A.; Bason, S.; Jopp, J.; Oren, Y.; Freger, V. (2006). J. Membr. Sci., 281, 480-490.[3] Kedem, O.; Katchalsky, A. (1962). Biophys. J., 2, 53-78.[4] Spiegler, K. S.; Kedem, O. (1966). Desalination, 1, 311-326.[5] Hidalgo, AM., Gómez, M., Murcia, MD., Serrano, M., Otón, J. (2013). Afinidad, in press.

Optimizing Cobalt (II) Removal from Aqueous Solution by Bulk LiquidMembranes Containing D2EHPA. Study of Transport ParametersG. León 1 *, A. Hidalgo 2 , M. Gómez 2 , M.D. Murcia 2 , B. Miguel 1 , M.A. Guzmán 11 Departamento de Ingeniería Química y Ambiental. Universidad Politécnica de Cartagena. Cartagena.Spain. Gerardo.leon@upct.es2 Departamento de Ingeniería Química. Universidad de Murcia. Murcia. SpainHeavy metal pollution of industrial effluents and waste waters is a very important environmentalproblem. As heavy metals are not biodegradable, they tend to accumulate in living organisms causingvarious diseases and disorders. Cobalt is one of the heavy metals associated to industrial activities,being present in effluents and waste waters of a wide range of industries, such as mining,hydrometallurgy, electroplating, painting, etc. Toxicological effects of cobalt (II) make necessary toreduce its concentrations in those aqueous effluents.An optimizing approach of cobalt (II) removal from aqueous solutions by bulk liquid membranesthrough the study of some transport parameters is carried out in this paper. A facilitated countertransport mechanism, using D2EHPA as carrier and protons (H 2 SO 4 ) as counter-ions, has beenemployed and the effect of different operational variables (carrier and striping agent concentration,organic phase volume, emulsifier concentration in the membrane phase and stirring rate) has beenanalyzed. Membrane fluxes, membrane permeabilities and transport efficiencies were determined inorder to optimize the conditions of the removal process.Experimental studies were carried out applying the bulk liquid membrane technique, by using astirred transfer Lewis type cell with bulk liquid membrane layered over feed and product phases.0.025 M cobalt (II) sulphate solutions in 0.05 M formic acid, adjusted to pH 4.0 with sodiumhydroxide, were used as feed phase. The membrane phase was constituted by varying proportions ofD2EHPA and Span in kerosene, while sulphuric acid solutions of different concentrations were usedas product phase. Effect of stirring speed and membrane phase volume were also analyzed. Cobalt(II) ion concentrations in feed phase was determined by UV spectrophotometry using an Unicam UV2instrument, measuring the absorbance of the colour developed by the product of the reactionbetween cobalt (II) and xylenol orange. Membrane fluxes and membrane permeabilities weredetermined by monitoring cobalt (II) concentration in the feed phase (C f ) and ln(C ft /C f0 ), respectively,as the function of time, based on the followings equationsJV dCftCftlnAP tA dtCf0Vwhere C ft is the concentration of cobalt (II) remaining in the feed solution at a certain time t, C fo is theinitial concentration of cobalt (II) ions in the feed solution before extraction, V is the volume of thefeed phase, A is the surface area of the membrane and P is the permeability coefficient of themembrane. Extraction efficiency was determined as E(%)= 100·(C f0 -C ft )/C fo .Results show that flux, permeability and extraction efficiency increase with the increase of carrierconcentration in membrane phase, with the striping agent concentration in the product phase, withthe stirring speed and with the increase of volume of the membrane phase, while they decrease withthe increase of the Span concentration in the membrane phase.

Effect of Particle Diameter on the Permeability of Polypropylene/SilicaNanocompositesDiego Bracho, Moisés Gómez, Humberto Palza, Raul Quijada*.Departamento Ingeniería Química y Biotecnología, Facultad de Ciencias Físicas y Matemáticas,Universidad de Chile. Santiago, Chile. raquijad@ing.uchile.clIntroduction:Polymer-silica nanocomposites have been widely studied. Low loadings of silica nanoparticles (~2wt%) in polymer matrices can considerably improve the performance of these materials, such asits barrier and mechanical properties [1].Synthetic particles have grown interest over the past decade, especially for food packaging andmedicine applications, due to the absence of heavy metals and toxins in the particles. The sol-gelmethod is a good alternative for silica nanoparticle synthesis, being able to tailor the particlesgeometry and size [2, 3].The main goal of this work is to synthesize silica nanoparticles of different sizes to be used as fillerin polypropylene nanocomposites, in order to study the permeability of these materials.Results:Silica nanoparticles were previously synthesized in a previous work via the sol-gel method, usingtetraethylorthosilicate (TEOS) as the precursor [3]. Figure 1 shows results for oxygen and watervapor permeability of the nanocomposites, as well as the predicted values for the permeabilityusing the Maxwell and Pall prediction [4].The Maxwell prediction is based on a tortuosity mechanism of an ordered regular arrangement ofthe dispersed phase on the polymer matrix. The Pall prediction in based on a three-phase matrix,filler and interphase region, this last one with an increased permeability.Figure 1: Permeability of polypropylene/silica nanocomposites: (A) Oxygen Permeability (P O2 ); (B) WaterVapor Permeability (WVP)

The permeability of the material showed an increase in the relative permeability of the materialwhen using silica nanospheres as filler, both for oxygen and water vapor, especially for the smaller20 nm particles due to the higher specific surface. This increase seems to be well fitted with thePall prediction at low loading of silica content (10-20 wt%), as the hygroscopic silica and thehydrophobic PP matrix repel each other. Nevertheless, when more silica is added (30 wt%) thepermeability of the material is considerably increased, probably due to agglomeration of thedispersed silica, which can lead to channel formation. In this case the permeability mechanismcannot be explained by a solution-diffusion mechanism, and other mechanisms such a Kudsenpore diffusion must be taken into account [5].Conclusions:Oxygen and water vapor permeability of polypropylene/silica nanocomposites was studied.Relative permeability was increased both for oxygen and water vapor, especially for the smallerparticles due to the higher specific surface. Interphase void formation is expected to occur, thusincreasing the relative permeability of the composite. When silica loading is large enough (30wt%), channel formation can occur, thus considerably increasing the relative permeability.Acknowledgements:The authors would like to thank project FONDECYT N° 1130446 for financial support.References:[1] Choudalakis, G., Gotsis, A.D. (2009), European Polymer Journal, 45, 967-984.[2] Brinker, C.J., Scherer, G.W. (1990), San Diego, CA: Academic Press INC.[3] Bracho, D., et al. (2012), Journal of Nanomaterials, Article ID 263915.[4] Hashemifard, S.A., et al. (2010), Journal of Membrane Science, 347, 53-61.[5] Merkel, T.C., et al. (2002), Science, 296, 519-522.

Extraction of the light lanthanide metal ions by means of emulsified liquidmembranes using several kinds of organophosphorus extractants as carrierC. Basualto F. * , F. Valenzuela L., L. Molina C. and J. Sapag H.Universidad de Chile/Facultad de Ciencias Químicas y Farmacéuticas, Laboratorio de OperacionesUnitarias e Hidrometalurgia. Santos Dumont 964 2do piso, Independencia, Santiago, Chile.* cbasualt@uchile.clThe demand for lanthanide metals is growing during last years owing to their unique physical andchemical properties and to the developing of new materials, such as new constituents in electronic,optical and magnetic devices. Commercially available rare earth materials have been used asadditives in steels or other alloys, permanent magnets, among others. Lanthanide metals presentextremely similar chemical and physical properties, and therefore they are very difficult to separate.Their Therefore, their separation requires costly and fractionation processes.The family of extractants obtained as by-products of phosphoric, phosphonic, phosphinic anddithiophosphinic acids, commercially known as D2EHPA, PC-88A, CYANEX 272 and CYANEX 301,respectively, seems to be the most promising extractants in the achievement for recovering of rareearth metal ions from aqueous solutions by solvent extraction. This work aims to contribute toknowledge on the extraction behavior of the lighter lanthanide ions La, Ce, Pr and Nd by means ofliquid emulsified membrane (LEM) using the organophosphorus family extractants as carrier andSPAN 80 as surfactant.In a previous work the acid-base behavior of the four extractants were studied allowing to know theirapparent pKa and through it the availability to react with the rare earth ions (RE) at certain pH. Thespeciation curves for aqueous solutions of La, Ce, Pr and Nd were obtained in order to determine themost suitable pH range of the feed solution for the extraction of each one. From this knowledge andtheir correspondent chemical extraction reactions it was possible to propose the use of buffered feedaqueous phase with 3-cloropropionic acid at pH 4 for all experiments.From the liquid membrane stability study it was observed that the concentration of SPAN 80surfactant in the organic phase showed the most significant effect. If were insufficient cause the lossof the internal aqueous phase, decreasing the efficiency of extraction. If an excess of surfactant wereused a swelling degree of the primary emulsion is produced.From the solvent extraction experiments and preliminary extraction by LEM, it was determined thatthe most appropriated extractant for the process was CYANEX 272, owing to its high extractioncapacity and better selectivity for the four RE ions. Preliminary experiments were performed withmonometallic feeds, being employed afterward solutions containing all the RE. The results wereconsistent with the individual extraction experiments of the RE ions, wherein lanthanum is the lesserextracted ion compared with the other three ones. On the other hand, the backextractionexperiments showed that the cerium ion had the lowest degree of transference toward the internalaqueous phase. All this generated knowledge revealed that the pair Nd-Pr was the most difficult toseparate at the established conditions.

1D and 2D Approach for Modelling Hollow-fiber and Spiral-wound PermeatorsFor Gas SeparationDavide Bocciardo, Maria-Chiara Ferrari * , Stefano BrandaniScottish Carbon Capture and Storage, School of Engineering, University of Edinburgh,Edinburgh EH9 3JL, UKM.Ferrari@ed.ac.ukThis work presents the analysis carried out in order to analyse the separation through the mostcommon configurations adopted for gas separation membrane modules.A 2D cross-flow model is presented with the aim of describing the separation through spiral-woundmodules. In the case of hollow fiber, both a 1D formulation and a 2D compartmental model areimplemented and compared.The implementation is carried out in C language and solved by using the Orthogonal Collocation onFinite Elements Method (OCFEM).The cross-flow analysis starts from the work by Pan [1], with the aim of predicting the separationthrough spiral-wound permeators. The implemented model implemented is bi-dimensional: the feedside is considered as surrounded by two selective membrane layers while the permeate flow isperpendicular to the retentate flow. In order to account for pressure drops, Darcy’s law is includedon both sides.Hollow fiber permeators are commonly used in industrial gas separation: the analysis started fromthe one-dimensional models available in the literature [2], where the only design parameter is themembrane area. However, with the aim of obtaining more detailed simulations, a 1D formulation isimplemented: the design parameters are the fibre radius, the area density and the fraction occupiedby the fibers. Pressure drops are assumed on both sides related to the module geometry.A bi-dimensional compartmental model is also implemented [3], with the aim of evaluating theeffect of combined cross-flow and countercurrent flow pattern, as shown in Figure 1.SweepyRetentateFeedPermeateFigure 1: hollow fiber module with comparmentsz

Simulations are carried out, in order to compare the prediction among the different models.The effect of possible module defects on the performances is also investigated: variable fiber radius(hollow fibre), membrane and channel thickness (spiral-wound) are assumed and statistical analyseson sets of simulations are performed.References:1. Pan, C.Y., Gas Separation by Permeators with High-Flux Asymmetric membranes. AIChE Journal, 1983.29(4): p. 545-552.2. Li, K., D.R. Acharya, and R. Hughes, Mathematical Modelling of Multicomponent MembranePermeators. Journal of Membrane Science, 1990. 52: p. 205-219.3. Wang, K., L.; Cussler, E., L., Baffled membrane modules made with hollow fiber fabric. Journal ofMembrane Science, 1993. 85: p. 265-278.

Multi-stage Design for Carbon Capture from Coal-fired Power Plants:From Process Design to Economic AnalysisDavide Bocciardo, Maria-Chiara Ferrari * , Stefano BrandaniScottish Carbon Capture and Storage, School of Engineering, University of Edinburgh,Edinburgh EH9 3JL, UKM.Ferrari@ed.ac.ukThe aim of this work, funded by Scottish Power and Energy Technology Partnership Scotland (ETP), isto investigate the application of membrane gas separation to post-combustion CO 2 capture fromcoal-fired power plants.A multi-stage process simulation is linked to a rigorous economic analysis: detailed cost models are infact required to compare membrane separation with amine absorption, the conventional carboncapture solution.The base-case power plant is the DOE case 9 – subcritical 550 MW coal-fired power plant [1]: thetarget is to produce a CO 2 high purity (> 0.95) stream at 150 bar with an overall CO 2 recovery of 90%.A hypothetical material combining high CO 2 permeance and selectivities over the other componentsis assumed. However, a comparison with commercial materials is carried out.The key step of the multi-stage analysis is the implementation of a completely automatedcustomised unit operation into UniSim Design®, the Honeywell process simulator.Two multi-stage designs including cross-flow and countercurrent with sweep stages are proposed [2]:Retrofit: the flue gas is sent to a dual-stage system followed by a compression andrefrigeration system.Boiler: part of the CO 2 is recovered into an additional countercurrent stage with air as sweepand its resulting permeate stream (~3 % CO 2 ) is sent as feed to the boiler.As a result of the higher CO 2 content in the flue gas, the boiler option results in the best solution interms of membrane area (–30%) and energy consumption (–10%) compared to the retrofit case.A key part of the work presented is a rigorous economical analysis linked to the process simulations,based on the Levelised Cost Of Electricity (LCOE) estimation [3], as shown in Figure 1.A sensitivity analysis with respect to material and process parameters is presented and the carbonmarket contribution is also investigated since CO 2 price will be a key feature for CCS applications.

Dimensionless LCOE [-]1.51.00.5Emission costStorageFuelO&MCAPEX0.0Base Case Retrofit Boiler Amines*Figure 1: LCOE comparisonBoth avoidance and capture costs are also evaluated and compared with the available literature onmembranes and amines [3, 4].References:1. NETL, Cost and Performance Baseline for Fossil Energy Plants. 2007, US Department Of Energy.2. Bocciardo, D., M. Ferrari, C., and S. Brandani, Modelling and multi-stage design of membraneprocesses applied to carbon capture in coal-fired power plants. Energy Procedia, 2013. In press.3. The Costs of CO 2 Capture. 2009, European Technology Platform for Zero Emission Fossil Fuel PowerPlants.4. Merkel, T.C., et al., Power plant post-combustion carbon dioxide capture: An opportunity formembranes. Journal of Membrane Science, 2010. 359(1-2): p. 126-139.

Membrane Fouling Control using High Voltage Impulse (HVI) TechniquesJi-Sun Lee and In-Soung Chang *Dept. of Environmental Engineering, Hoseo University, Asan, 336-795, South Korea, cis@hoseo.eduAbstract A high voltage impulse (HVI) technique was examined to mitigate the membrane foulingoccurring in membrane bioreactors (MBRs). After the activated sludge was filtrated through anmembrane, the cake layer was removed by either water-washing cleaning (control) or HVI cleaningwith an electric field of 4-20kV/cm and a pulse duration of 20~70 microseconds. The flux recoveriesafter HVI induction ranged from 24 to 44% were always higher than those of the control. Todetermine the exact mechanism of the enhanced flux recovery of the HVI cleaning, the change insludge properties after HVI induction was examined. The mixed liquor of suspended solidsconcentration decreased with increasing HVI contact time, while the concentrations of solublechemicaloxygen demand, -total nitrogen, -total phosphorus, -polysaccharide, and -protein in thebulk solution increased, indicating that the flocs and cells were damaged and burst due to the HVIinduction. These results suggest that the HVI induction led to sludge solubilization, which loosenedthe tightly deposited cake layer on the membrane surface, enabling it to be easily dislodged from themembrane surface. Consequently, the HVI technique could be an alternative strategy for foulingcontrol and sludge solubilization in MBRs.

Light Olefin/Paraffin Separation Using Polymeric Ionic Liquid MembranesContaining Ag + -IL as CarrierLiliana C. Tomé 1,2 , David Mecerreyes 3 , Carmen S.R. Freire 2 ,Luís P.N. Rebelo 1 , Isabel M. Marrucho 1,2*1 Instituto de Tecnologia Química e Biológica, Universidade Nova de Lisboa, Av. República,2780-157 Oeiras (Portugal)2 CICECO, Departamento de Química, Universidade de Aveiro, Campus Universitário deSantiago, 3810-193 Aveiro (Portugal).3 POLYMAT, Institute for Polymer Materials, University of the Basque Country UPV/EHU, JoxeMari Korta Center, Avda Tolosa 72, 20018 Donostia-San Sebastian (Spain).imarrucho@itqb.unl.ptLight olefins are usually obtained as a mixture with paraffin hydrocarbons by steam crackingprocesses and their separation is one of the most important and challenging processes in thepetrochemical industry since olefins are essential building blocks for several products and chemicals[1]. Since conventional processes like low-temperature distillation are quite expensive and energyintensive,research targeted at developing new saving and cost-effective processes have beenundertaken.In this context, membrane-based processes have been considered as viable alternative.Particular attention has been paid to supported ionic liquid membranes (SILMs) containing silversalts, not only due to the well-known ability of olefins to react selective and reversibly with the Ag +via a π-bond complex formation but also because ionic liquids offer high olefin retention capacity andstability to the solubilised metal cation [2]. Nevertheless, SILMs stability under industrial processesconditions (high pressures and temperatures) is of concern [3]. It has been shown that the best wayto approach ionic liquids for industrial gas separation is to use polymeric ionic liquid membranes,since they combine some of the unique properties of ionic liquid with the improved mechanicalstability of polymers [4].In order to evaluate the viability of using polymeric ionic liquids as alternative materials for lightolefin/paraffin separation, free standing membranes of poly([pyr 11 ][NTf 2 ]) combining differentamounts of the ionic liquid ([pyr 14 ][NTf 2 ]) and the silver salt AgNTf 2 were prepared by the solventcasting method. Gas permeation experiments using ethane and ethylene were performed in all theprepared materials using a time-lag apparatus and the gas permeation properties (permeability,solubility and diffusivity) and ethylene separation performance of the prepared membranes will bepresented.References[1] R. Faiz, K. Li (2012), Chem. Eng. Sci. 73, 261-284.[2] M. Fallanza, A. Ortiz, D. Gorri, I. Ortiz (2012) Sep. Pur. Technol., 97, 83-89.[3] P. Scovazzo (2009), J. Memb. Sci. 343, 199-211.[4] R. D. Noble, D.L. Gin (2011), J. Memb. Sci., 2011, 369, 1-4.

AcknowledgmentsL.C. Tomé is grateful to FCT (Fundação para a Ciência e Tecnologia) for her PhD research grant(SFRH/BD/72830/2010). I. M. Marrucho acknowledges FCT/MCTES (Portugal) for a contract under CIENCIAprogram. This work was partially supported by FCT through the projects PTDC/QEQ-FTT/1686/2012, Pest-OE/EQB/LA0004/2011 (ITQB) and Pest-C/CTM/LA0011/2011 (CICECO).

Ionic Liquids and Polymeric Ionic Liquids Membranes for CO 2 SeparationLiliana C. Tomé 1,2 , Luís P.N. Rebelo 1 , Carmen S.R. Freire 2 ,David Mecerreyes 3 , Isabel M. Marrucho 1,2*1 Instituto de Tecnologia Química e Biológica, Universidade Nova de Lisboa, Av. República,2780-157 Oeiras (Portugal)2 CICECO, Departamento de Química, Universidade de Aveiro, Campus Universitário deSantiago, 3810-193 Aveiro (Portugal).3 POLYMAT, Institute for Polymer Materials, University of the Basque Country UPV/EHU, JoxeMari Korta Center, Avda Tolosa 72, 20018 Donostia-San Sebastian (Spain).imarrucho@itqb.unl.ptThe development of carbon dioxide (CO 2 ) capture processes is becoming increasingly important asconcerns on the rising anthropogenic CO 2 levels, leading to global warming and unpredictableclimate changes, are being widely expressed. Therefore, the design of materials with the ability toefficiently separate CO 2 from other gases is of vital importance.The use of ionic liquids for CO 2 separation has received growing attention in recent years, not onlydue to the high levels of solubility and selectivity of CO 2 in these fluids relative to other gases, butalso because of the ability to tailor many of their physical and chemical properties by combiningdifferent anions and cations or by adding functional groups. A large amount of work addressing theuse of ionic liquids for separating CO 2 has been published, particularly in applications involvingmembrane technology. These data clearly show that the endless combination of cations and anionsallows the development of new membranes for more efficient processes. Nevertheless, the best wayto approach ionic liquids for industrial gas separation is to use polymeric ionic liquids to preparemembranes, because they present fundamental engineering advantages [1].All the above mentioned aspects motivate us to explore new possibilities of designing improved CO 2separation membranes based on polymeric ionic liquids. In this work, we focus on the separation ofCO 2 from power plants exhausts (CO 2 /N 2 ) and natural gas streams (CO 2 /CH 4 ) using several strategiesfrom supported ionic liquid membranes [2] to polymeric ionic liquid membranes [3,4]. The aim is toshow the versatility of these materials in the development of new highly efficient engineeredmembranes.[1] R.D. Noble, D.L. Gin (2011) J. Membr. Sci.369, 1-4.[2] L.C. Tomé, D.J.S. Patinha, C.S.R. Freire, L.P.N. Rebelo, I.M. Marrucho (2013) RSC Adv. 2013, in press.[3] L.C. Tomé, D. Mecerreyes, C.S.R. Freire, L.P.N. Rebelo, I.M. Marrucho (2013) J. Membr. Sci. 428, 260-266.[4] L.C. Tomé, M.A. Aboudzadeh, L.P.N. Rebelo, C.S.R. Freire, D. Mecerreyes, I.M. Marrucho (2013) J. Mater.Chem. A 2013.AcknowledgmentsL.C. Tomé is grateful to FCT (Fundação para a Ciência e Tecnologia) for her PhD research grant(SFRH/BD/72830/2010). I. M. Marrucho acknowledges FCT/MCTES (Portugal) for a contract under CIENCIAprogram. This work was partially supported by FCT through the projects PTDC/QEQ-FTT/1686/2012, Pest-OE/EQB/LA0004/2011 (ITQB) and Pest-C/CTM/LA0011/2011 (CICECO).

Treatment of Kraft Pulp Mill (EPO) Bleaching Plant Filtrates Using MembraneTechnologyRafael Quezada Reyes*, Claudio Mudado SilvaUniversidad Federal de Vicosa, Minas Gerais, Brazil.Rafael.Reyes@ufv.brDue to the continuous increase of environmental concern of the pulp industry, it is necessary to findoptions that minimize the water consumption, and enhance the effluent quality [1]. The treatment ofspecific in-plant stream seems to be an attractive technical and economical approach because of thelarge final effluent volume which would not be compatible with some technologies such as the use ofmembranes [2,3]. The purpose of this study was to evaluate the use of membrane technology in ahighly contaminated stream from bleaching plant, the alkaline extraction (EPO) filtrate. This stream ischaracterized by a high load of organic compounds (COD of 1.800 mgl -1 and colour of 900 mgl -1 ).The work was carried in three phases. In Phase 1 it was evaluated three membrane configurations: i)tight ultrafiltration (UF) (ESP04 and XP197); ii) open UF + nanofiltration (NF) (FP200 + AFC30) and iii)NF (AFC30). It was determined the separation performance of these membrane configurations forthree filtrate quality parameters: AOX, COD and colour. The results indicate that the best option fortreatment of (EPO) filtrates was, according to operational simplicity and cost, the tight UF (ESP04).This configuration obtained a removal of 64% of COD, 87% of colour and 60% of AOX.In Phase 2 it was carried out experiments in the pilot plant to confirm the separation performance ofESP04 membrane and determine the flux rate and optimal transmembrane pressure (TMP). In thisphase, it was also identified if any immediate or irreversible fouling of the membranes occurred. Theresults confirmed the performance of the membrane and indicated that the best operating conditionwas achieved at the low TMP (1.7 bars) and the flux of 24 lh -1 m -2 (Table 1). No irreversible fouling wasobserved. The first two phases was carried by the simulation in membrane batch fed pilot plant.Table 1: Results of phase 2.Flux(l/min m 2 )151924ColorCODVCF Fed(mg/l)Filtrate(mg/l)Reduction(%)Fed(mg/l)Filtrate(mg/l)1,9 34,0 989 74 93 2080 779 634,7 42,0 712 84 88 1638 769 546,6 32,5 645 66 90 1772 767 57Pressure(bar)Reduction(%)4,4 31,2 996 106 89 2050 869 586,5 71,0 955 76 92 2004 906 551,7 10,8 795 58 93 1995 690 654,4 95,0 859 102 88 2028 932 54

In Phase 3 it was determined the effect of UF of (EPO) filtrate in the effluent treatment plant.Biological treatment was simulated in sequential batch reactors (SBR) and tertiary treatment using aJar test. Two scenarios were evaluated: in Scenario 1, all UF permeate was sent to the EffluentTreatment Plant. The results showed a 10% reduction of the COD and a 30% reduction in tertiarysludge. Scenario 2 considered the reuse of the UF permeates within the bleaching plant. In thisscenario there was an increase in efficiency of COD reduction of 7%, a 20% reduction of biologicalsludge and a 45% reduction of tertiary sludge. In both Scenarios the use of coagulant reduced in thetertiary treatment plant. The results indicated that treatment of the filtrate (EPO) with UF is feasibleand allows reducing the production of solid waste and water consumption, and increasing theefficiency of the effluent treatment plant.[1] Zadorecki, P., Selection of Membranes for Treatment of Bleaching Effluent. Desalination, 1987(62): p. 10.[2] Jonsson, A.S., Ultrafiltration applications. Desalination, 1990. 77: p. 135-179.[3] Nordin, A.J., AS., Case study of an ultrafiltration plant treating bleach plant effluent from a pulp and papermill. Desalination, 2006. 201(1–3): p. 277-289.

Comparison of the Performance of Membranes in Treatment from IndustryTannery Wastewaters.Estela María Romero-Dondiz a* , Jorge Emilio Almazán a , Verónica Beatriz Rajal a,b and Elza FaniCastro-Vidaurre a .a Instituto de Investigaciones para la Industria Química (INIQUI-CONICET, UNSa), Facultad deIngeniería, Universidad Nacional de Salta (UNSa), Avenida Bolivia Nº 5150, Salta, Argentina.b Fogarty International Center, University of California in Davis, USA.*eromerodondiz@yahoo.com.arThe leather tanning industry consumes large amounts of water and produces, consequently,significant volumes of wastewater with high concentration of chemicals and organic matter. One ofthe main chemicals present in effluents is the vegetable tannin, which causes a severe environmentalimpact [1]. A possible alternative to solve this problem is the implementation of membranetechnology. In recent years, processes with membranes have been increasingly used in severalindustrial applications and in wastewater treatment [2-4].Commercial polymeric membranes were used, an ultrafiltration (UF) membrane OT050 (Pall LifeSciences) with a transmembrane pressure (TMP) of 5 bar and two nanofiltration (NF) membranes:MPF-36 (Koch Membrane) and DL (GE Osmonics) with a TMP of 15 bar. The morphologicalcharacterization of the membranes was performed: contact angle, thickness, porosity and scanningelectron microscopy (SEM). An equipment crossflow filtration was used to test the membranes. Thisequipment had a stainless steel flat cell and an effective membrane area of 0.004 m 2 . All tests wereperformed with an effluent coming from the vegetable tanning step from the tanning industry.The results indicate that all membranes have a similar average of permeate flux, showing that theMPF-36 membrane has the highest flow (18.10 ± 6.10 L/m 2 h). Regarding observed rejection oftannins, OT50 and MPF-36 membranes have similar rejections (74% and 78% respectively), while DLmembrane presented an excellent rejection of 98%. The three membranes can be feasibly to use inthe treatment of wastewater from the leather industry.[1] A. Cassano, J. Adzet, R. Molinari, M.G. Buonomenna, J. Roig, E. Drioli (2003), Membrane treatment bynanofiltration of exhausted vegetable tannin liquors from the leather industry, Water Res., 37, 2426-2434.[2] C. Conidi, A. Cassano, E. Drioli, A membrane-based study for the recovery of polyphenols from bergamotjuice (2011), J. Membrane Sci., 375, 182-190.[3] H.A. Mousa, Investigation of UF membranes fouling by humic acid (2007), Desalination, 217, 38-51.[4] C.J. Huang, B.M. Yang, K.S. Chen, C.C. Chang, C.M. Kao (2011), Application of membrane technology onsemiconductor wastewater reclamation: A pilot-scale study, Desalination, 278, 203-210.

Preparation and evaluation of ciprofloxacindelivery from poly(3-hidroxybutirate) membranesJosé M. Bermudez, Analía I. Romero, Mercedes Villegas, M. Florencia Dib Ashur, Mónica L.Parentis y Elza F. Castro Vidaurre*Instituto de Investigaciones para la Industria Química (INIQUI, UNSa-CONICET). Av. Bolivia5150, 4400 Salta, Argentina. email: elza@unsa.edu.arPolymeric membranes are being investigated and used in pharmaceutical technology as controlledrelease systems to modulate body drug release. In this study we have evaluated the potentialapplication of novel membranes constituted of poly (3-hydroxybutyrate) (PHB). PHB is anintracellular polyester synthesized by certain bacteria as a carbon and energy storage compound andshows promising applications in medicine due to its biodegradability and biocompatibility.Ciprofloxacine hydrochloride (Cipro) was the model drug used for the release studies. Cipro is asecond-generation fluoroquinolone antibiotic, valued for its broad spectrum of activity and excellenttissue penetration. Composite membranes loaded with 5 (PHB-Cipro-5) and 15%wt Cipro (PHB-Cipro-15) were synthesized.Pure PHB polymeric membranes and PHB-Cipro loaded membranes were characterized usingdifferential scanning calorimetry (DSC), electron scanning microscopy (SEM) and Fourier transforminfrared spectroscopy (FTIR).Homogeneous composite membranes were obtained. FT-IR and DSC showed an interaction betweenCipro and PHB, demonstrating that there is not only a physical mixture. SEM micrographs (Fig.1)provided evidences of a smooth and uniform structure.(a) (b) (c)Fig. 1. SEM micrographs of (a) Ciprofloxacin, (b) PHB-Cipro-5 cross section and (c) PHB-Cipro-15 crosssection.Cipro release was measured in three different media: water, saline solution and a pH 6.8 buffersolution. From release profiles, kinetic parameters and release mechanism were determined. It wasobserved that PHB membranes modulate Cipro release with appropriate release profiles; drugrelease was over 50% and followed Fickian release mechanisms according to the model applied forthe kinetic analysis.

These novel membranes are potentially useful platforms for formulating drug delivery systems.

Ultrafiltration Membranes Modified by Plasma and Its Application in The ViralRemoval In Water TreatmentMercedes L. Méndez 1 *, Verónica Rajal 1,2 , Elza F. Castro 11. Facultad de Ingeniería - UNSa – Instituto de Investigaciones para la Industria Química, CONICET.Av. Bolivia 515, 4400. Salta-Argentina.2. Fogarty International Center - University of California at Davis, USA. mmendez@unsa.edu.arCurrently the plasma treatment is a tool widely used in surface modification of different materials tooptimize their properties in order to a particular application. In the present work, low temperatureplasma technique was used to modify ultrafiltration (UF) membranes using an inductive reactor. Theaim was enhance hydrophilicity and uniform surface pores of the UF membranes leading to lessfouling and subsequent flux enhancement. The UF membranes were of Polyethersulfone (PES) andsynthesized for the phase inversion method. Additionally, polyethylene glycol (PEG) of molecularweight 10.000 was used as additive, dimethylacetamide (DMAc) and water as solvent and the nonsolvente,respectively. The modification was made in two consecutive treatments, first with argonplasma (Ar) followed by polymerization with acrylic acid (AA). The pre-treatment with Ar plasma wasperformed for 2, 5, 10 and 15 minutes at a pressure of 200 mTorr, with the goals of cleaning thesurface and improve adhesion between the substrate and plasma polymerised acrylic acid coatings.In the plasma polymerization was used a mixture of AA with Ar at a pressure of 300 mTorr by 30minutes. The radio frequency power source (8- 13.56 kHz) was 10,2W for all case.The characterization of the membranes before and after the surface modification was done usingcontact angle to determine its effect on the surface hydrophilicity. Also SEM and AFM images havebeen used to know the membrane morphology and Liquid-liquid Displacement Porosimetry (LLDP)was used to quantify the pore size distributions. The pure water permeability and tests of retentionof viral model, bacteriophage PP7 using the host Pseudomonas aeruginosa, were measured showinga proper performance. Finally, the fouling was evaluated by measuring the relative water reduction(RFR).As of analysis of the properties of the modified membranes the changes observed on the surface ofthese were reduction and uniformity of the surface pores and increase hydrophilicity, and in terms ofperformance of ultrafiltration membranes were observed increasing its permeability and smaller RFRvalues after filtration with PP7, with respect to unmodified membranes.

Polycarbonate Modified Membranes With Silanized Clays For UseIn Ethanol / Water Pervaporation.L. Dada 1 , M. Toro 1 , C. Carrera 2 , E. Erdmann 3* , C. Paranhos 4 , L. Pessan 4 , H. Destéfanis 21 Consejo de Investigaciones-CIUNSa, Facultad de Ciencias Exactas, Universidad Nacional deSalta, UNSa. Salta, Argentina.2 Instituto de Investigaciones para la Industria Química- INIQUI-CONICET, Consejo deInvestigaciones-CIUNSa, Facultad de Ingeniería, Universidad Nacional de Salta, UNSa, Salta,Argentina.3 Instituto Tecnológico de Buenos Aires-ITBA, Instituto de Investigaciones para la IndustriaQuímica –INIQUI (UNSa-CONICET); Buenos Aires, Argentina.4 Laboratório de Permeação e Sorção (LAPS), Departamento de Engenharia de Materiais-DEMa, Universidade Federal de São Carlos - UFSCar, São Carlos–SP, Brasil.* erdmann@itba.edu.arThe pervaporation technique is considered as a process of energy saving and has gained increasinginterest in the separation of azeotropic mixtures (such as water/alcohol), mixtures of close boiling orisomers, and disposal or recovery of trace substances. In recent years, pervaporation has establisheditself as one of the most promising membrane technologies for the treatment and recycling ofvolatile organic compounds and pollution prevention [1]. In the field of study of membranes forseparation processes efforts have focused on issues such as forming processes of the membrane, γray irradiation, 60 Co or plasma grafting, the polymer mixture, chemical grafting, and preparation newpolymers [2].This paper shows the effect of the incorporation of various clays silanized withdichlorodimethylsilane (DMS), diphenylsilane (DPhS) and methylphenylsilane (MPhS) with a load of 3wt % to a polycarbonate matrix [3] for use in pervaporation of alcohol / water mixtures [4]. MaterialsPolycarbonate (PC) / modified clay were prepared by casting. The structure and morphology of thematerials was determined by XRD and SEM, the thermal resistance by thermogravimetric analysis,surface properties by determination of contact angle (with polar and non polar solvents) andtransport properties by pervaporation experiences using water as solvent.Figure 1 shows X-ray diffraction diagrams of PC/organoclay modified membranes. The typicaldiffractogram of PC is not modified by presence of clays silanized perhaps by underload added.Figure 1. XRD of Films of: PC, PC/MMT DMS ,PC/MMT DPhS and PC/MMT MPhS .

However the crystallinity of the polycarbonate is affected by the incorporation of different clayssilanized as PC/MMT MPhS material, it has a more intense peak indicating higher crystallinity comparedto the other two composites materials.We observed a significant increase in contact angle in materials modified with DPhS and MPhS incomparison to pure PC, so there is a decrease for their affinities towards water (Table 1).Table 1. Contact angle of films with water and diiodomethaneFilm Water DiiodomethanePC 88.66 22.85PC/MMT DMS 3% 85.79 21.89PC/MMT DPhS 3% 95.34 30.6PC/MMT MPhS 3% 95.36 26.95Results of pervaporation using water as solvent indicate that flux through composites materialsdecreases compared to pure PC, but there is not significant differences between fillers. So, thesematerials with a small charge into the polymer matrix has achieved significant barrier to the passageof water in the membranes which would be applicable for separating alcohol/water mixtures.ReferencesTable 2. Flux of water in films.Film J: Flux [g/h.m 2 ]PC puro 2774,6PC/MMT DMS 3 % 25,6PC/MMT DPhS 3 % 37,9PC/MMT MPhS 3 % 20,0[1] F. Lipnizki et al. (1999), Journal of Membrane Science, 153, 183-210.[2] M. Müller, B. Elkin, D. Hegemann, U. Vohrer (1999), Surface and Coatings Technology, 116, 25–35.[3] M. Alkan; G. Tekin; H. Namli (2005), Microporous Mesoporous Mater,84, 75-83.[4] Y. Wang, M. Teng, K. Lee, J. Lai (2005), European Polymer Journal, 41, 1667-1673.

Industrial Application of Membranes for CO 2 Removal from Natural GasWilliam I. EchtUOP, A Honeywell CompanyWilliam.Echt@Honeywell.comThe use of cellulose acetate membranes for CO 2 removal from natural gas has grown significantlyover the past 30+ years. Both hollow fiber and flat-sheet, spiral-wound membranes have been usedin this service.This presentation will briefly review the positives and negatives of each type of membrane elementand then focus on experience with UOP Separex membrane elements. Several case studies arepresented and the use of Separex membrane systems offshore Brazil is covered in detail.

Use of Precipitation and Ultrafiltration to Purify Inulinase Obtained by Solid StateFermentation of Sugarcane BagasseSimone Maria Golunski 1 , Helen Treichel 2 , Marco Di Luccio 3 *1 Departamento de Engenharia de Alimentos, URI-Campus de Erechim, Erechim-RS, Brasil2 Universidade Federal da Fronteira Sul- Campus de Erechim; 3 Departamento de EngenhariaQuímica e Engenharia de Alimentos, UFSC, Florianópolis-SC, Brasil. *diluccio@enq.ufsc.brInulinases are 2,1-β-D fructan furohydrolases (EC 3.2.1.7.) that convert inulin to fructose. Theseenzymes can be applied to the production of high fructose syrups and fructooligosaccharides, whichare extensively used in the food and beverage industry [1]. The isolation and purification of anenzyme produced by microorganisms is a challenging task, taking into account both economical andtechnical aspects, since the purification steps can account with 70-90% of the total production costs.The use of precipitation and membrane processes for purification of inulinases can be of greatinterest to research and technology development for applications in food industry [2,3]. In this sense,this work presents a systematic investigation on isolation and purification of inulinases produced bysolid state fermentation using precipitation with ethanol (a food grade solvent) coupled toultrafiltration. The effects of the concentration of ethanol and the rate of addition of ethanol to thecrude extract on the purification yield and purification factor were assessed using the experimentaldesign technique. Precipitation caused an activation of enzyme and allowed purification factor up to2-fold. Maximum recovery of inulinase by precipitation was obtained with ethanol 55% at a flow rateof 10 mL/min. The summary of inulinase purification strategy proposed in this work is presented inTable 1. After precipitation, the pre-purified enzyme was concentrated and fractioned byultrafiltration using a 100 kDa membrane, which was the best membrane for increasing thepurification factor from a range of molecular weight cut-off from 30 to 100 kDa. The UF step caused alittle drop in activity yield due to loss of enzyme on the membrane surface, by fouling or gelformation. Membrane retention based on activity was 95%, while total protein retention was 43%. Agood purification factor could be obtained (5.5-fold) after UF. These results are encouraging whencompared to literature, proving that a simple two-step purification technique can be even moreeffective than some chromatographic techniques. The results of retention suggest that thecontaminant proteins preferably permeate the membrane, while the inulinase was retained,increasing its purity.Table 1. Summary of purification steps of inulinase from K. marxianus NRRL Y-7571Purification steps Total Protein(mg)Total Activity(U)Specific activity(U/mg)Enzyme Yield(%)PurificationfactorCrude enzyme 108 7944 73,56 100,0 1,0extractEthanol56,0 9560 170,71 120,3 2,3precipitationUF retentate 16,1 6484 402,73 81,6 5,5[1] M. Ettalibi, J.C. Baratti (2001), Enzyme Microb. Technol., 28, 596–601.[2] R. Ghosh (2003), Imperial College Press, London, UK.[3] I.Y. Galaev, B. Mattiasson (2001), Membrane Separations in Biotechnology, 2nd ed., Marcel Dekker Inc.ACKNOWLEDGEMENTS: CAPES, CNPq

Production of Filtrating Membranes from the Components of Sugarcane BagasseGuilherme Gonçalves de Godoy*, Rafael Garcia Candido, Adilson Roberto GonçalvesEscola de Engenharia de Lorena – EEL/USP – Departamento de BiotecnologiaEstrada do Campinho s/n – Lorena – SP - Brasilguilhermeggodoy@gmail.comIn the early 70's, in addition to the classical separation processes, a new class of processes emerged,known as membrane separation processes, which use synthetic membranes as selective barriers.These synthetic membranes arose as an attempt to mimic the natural membrane, particularlyregarding its unique selectivity and permeability. Cellulose acetate is a versatile material used in thepreparation of membranes and has attracted attention because of its excellent performance andfeatures, such as high hardness and biocompatibility, good desalination capacity and low cost. Insome cases, it is used some components as reinforcements aiming to improve the mechanicalproperties of the membrane.Sugarcane bagasse is one of the most generated co-products in the sugarcane processing and thetotal utilization of the sugarcane bagasse components is economically and environmentally desirable.In this context, this work aimed to produce filtrating membranes using sugarcane bagasse. Cellulosewas utilized in the production of cellulose acetate and lignin was utilized as reinforcement in themembranes preparation.Cellulose and lignin were extracted through a sequence of chemical treatments. After this stage,cellulose was acetylated and lignin was chemically oxidized. It was prepared two membranes, onewithout lignin and other with lignin. Cellulose acetate was dissolved in dichloromethane in a ratio of6% (w/w). The solution was stirred during 5 h. Then, the solution was spread on a glass plate forsolvent evaporation for 5 minutes. After this time, the glass plate was immersed in water at 4ºC inorder to promote the phase inversion and withdraw of the membrane from the glass plate surface.In the case of the membrane with lignin, the lignin was added after 4 h of acetate/dichloromethanesolution stirring. The solution containing lignin was stirred for 1 h, totalizing 5 h of stirring.The cellulose extracted from sugarcane bagasse presented purity higher than 90%, what leading toobtain a cellulose acetate with high substitution degree, 2.62. The lignin oxidation was effective.Infrared analysis of this material showed the disappearance of OH groups that were replaced bycarbonyl groups. The addition of oxidized lignin represented an improvement in the mechanicalproperties of the membrane, besides higher steam water flux. The next stage of this work is to applythese membranes in the desalination process.

Membrane Distillation Process Design Applied to Highly Concentrated Brines:Mathematical Model and Operating Conditions AnalysisCarlos Eduardo Pantoja*, Marcelo Martins Seckler, Yuri NariyoshiDepartment of Chemical Engineering, Polytechnic School, University of São Paulo,cepantoja@usp.com.brWater scarcity is an important problem in many countries that is expected to worsen withdemographic increase. The world population should increase by 2.5 billion people by the year 2050[1], and considering that about 70% of all freshwater withdrawn from natural resources around theglobe is destined to agriculture [2], the cost of freshwater for the chemical processing industry (CPI)is going to experience a steep increase in the next decades. To illustrate the magnitude of thisproblem, a modern petroleum refinery consumes about 1 to 2.5 m 3 of water for each cubic meter offinished products produced [3]. For that matter, a large number of aqueous effluent reductiondischarge projects are being implemented throughout the CPI.The aqueous waste stream of a well-designed effluent treatment plant in the CPI, after theconventional primary, secondary and tertiary processing steps, is comprised mainly of inorganicspecies (salts) dissolved in water. Partial recovery of the water content in these saline effluents isfrequently achieved by means of desalination processes like reverse osmosis and electrodialysis.However, 20 to 40% of the water is not recovered by such processes and comprise concentratedbrines that are normally disposed in evaporation ponds, deep wells and coastal waters [4]. Not onlyis this water wasted but the disposal of concentrated brines imposes hazards to the environment [5]and is becoming very restricted by environmental protection agencies worldwide. Therefore, zeroliquid discharge (ZLD) is becoming a necessary objective of many water recovery initiatives.Recovery of the water contained in concentrated brines is, on the limit of a ZLD objective, aseparation problem that will most likely consider a crystallization step. A prerequisite to promotecrystallization of saline species dissolved in water is the supersaturation state, which may beachieved either by cooling or solvent evaporation, depending on the solubility behavior of the saltswith respect to temperature variations. For brines containing significant amounts of sodium chloride(it is the case of industrial effluents in many CPIs), which display a high and temperature invariantsolubility, conventional thermally driven crystallizers are the most suitable choice (forced circulationand draft-tube-baffled crystallizers have been widely used for production of sodium chloride fromseawater [6]). These conventional technologies require relatively hot heat sources as evaporationtakes place at the boiling point of the saline solution, and although the boiling point is occasionallylowered by means of vacuum application, evaporative crystallizers generally operate at temperatureshigher than 70 o C, with specific energy consumptions in the range of 30 kWh/m 3 of distillate produced[7].Membrane distillation (MD) is an alternative thermally driven process that was developed in the late1960s but did not attain commercial status at the time, mainly because of difficulties to obtainsuitable membranes at reasonable costs [8]. Recent developments in membrane manufacturingtechnology allied to the research of less energy intense processes favored a rebirth of the MDprocess. The use of MD as the supersaturation promoter in a crystallization system was firstproposed by Curcio et al. [9] in a process named membrane distillation crystallization (MDC). In MDC,

the high contact area provided by hollow fiber microporous hydrophobic membranes allows theachievement of reasonable evaporation fluxes at moderate temperatures (40-60 o C) at atmosphericpressure, with an average energy consumption that ranges from 15-20 kWh/m 3 [7]. Also, themoderate temperatures involved in MD processes allow the utilization of low-grade waste energysources (frequently readily available at oil refineries and petrochemical processing complexes)and/or alternative sources such as solar, wind and geothermal energy [10, 11].The aim of the present work was to develop a mathematical model to assist the design and theestablishment of optimum operating conditions of MD processes in applications where well solublesalts like sodium chloride are involved, which implies in concentrated solutions that require arigorous approach for the water activity prediction in order to correctly estimate the vapor pressuredepletion in the retentate side. The direct contact membrane distillation (DCMD) configuration wasmodeled because it is the most simple, economical and efficient configuration for the concentrationof aqueous inorganic streams [9, 12, 13]. Also, regarding the membrane module geometry, thehollow fiber type was modeled due to its large specific contact area (about 10 4 m 2 /m 3 ) andconsequent better suitability for industrial applications when compared to its flat sheet typecounterpart, normally found in laboratory apparatus [9, 10].In DCMD, as depicted in Figure 1, hot saline solution is fed to one side of a microporous hydrophobicmembrane (normally made of polymeric materials). The other side of the membrane is fed with purecold solvent (in the present case, water). The vapor pressure difference established across themembrane air-filled pores drives the evaporation of solvent from the hot side to the cold side, withsubsequent vapor condensation. The small size of the pores, in the range of 0.1 to 1.0 μm, preventsliquid to flow across the membrane pores (due to surface tension). Hence, only vapor is transferredfrom the hot side to the cold side, which causes the saline solution to become more concentrated inthe hot side (the so-called retentate) and pure water to be recovered in the cold side (permeate).Fig. 1: Temperature and vapor pressure profiles across a hydrophobic membrane in a DCMD configuration.In order to model the simultaneous heat and mass transfer phenomena that take place across thehydrophobic microporous membrane, the theory developed by Schofield and co-workers [14] forDCMD was employed. The water activity in the retentate side was rigorously modeled according to aPitzer-based thermodynamic method [15], due to the significant role that water activity plays in thevapor pressure depletion of the resultant highly concentrated solution, specially in MDC applicationswhere the retentate operates close to saturation or even at supersaturated conditions. The modelalso accounted for the temperature polarization effects due to heat transfer resistance across themembrane, which ultimately influences the process driving force (the temperature differencebetween the hot and cold fluids fed to the membrane module). Likewise, concentration polarization

that takes place on the hot side of the membrane is estimated by the model and considered in thenet vapor flux calculation. A differential mass and energy balance performed for the hollow fibermodule, which is similar to a shell and tube heat exchanger configuration, allowed the model topredict the concentration and temperatures profiles along the module and ultimately predict therequired module dimensions (length, number of tubes, total area) and most suitable fluid dynamics(circulation flowrates, pressure drop, liquid entry pressure) for a given set of conditions (availablefeed temperatures of the hot and cold fluids, feed solution concentration, available commercialmembrane characteristics as pore size, thickness, material etc.). Figures 2, 3 and 4 are model outputsfor an arbitrary design case.Fig. 2: Concentration profile across a DCMD membrane module.Fig. 3: Temperatures profiles across a DCMD membrane module.The knowledge of concentration and temperatures profiles along the membrane module might benecessary, for example, in a MDC process design where the degree of saturation or supersaturation

of the retentate must be closely controlled in order to prevent crystallization on the membranesurface (which could cause its clogging).Finally, as the present model is intended to assist the process design of membrane distillationprocesses as a whole, which comprises not only the determination of the membrane moduledimensions but also the optimum process conditions (although both tasks are related), as previouslymentioned, a hierarchical design approach [16] based on heuristics, experimental information andqualitative theoretical considerations was developed in order to be used alongside the model itself asa design tool. The full paper will present both the model and the hierarchical design approach indetail.[1] United Nations (2007), Press Release POP/952.[2] United Nations (2012), United Nations Educational, Scientific and Cultural Organization.[3] USEPA (2012), Water and energy efficiency by sectors.[4] D.H. Kim (2011), Desalination, 270, 1-8.[5] A. Pérez-González, et al. (2012), Water Research, 46, 267-285.[6] J.W. Mullin (2001), Crystallization, 4th. ed., Elsevier Ltd.[7] X. Ji, et al. (2010), Sep. & Purif. Technology, 71, 76-82.[8] A. Alklaibi, N. Lior (2004), Desalination 171, 111-131.[9] E. Curcio, A. Criscuoli, E. Drioli (2001), Ind. Eng. Chem. Res., 40, 2679-2684.[10] E. Curcio, E. Drioli (2005), Sep. & Purif. Review, 34, 35-86.[11] M.S. Bourawi et al. (2006), J. Membr. Sci., 285, 4-29.[12] A. Alklaibi, N. Lior (2004), Desalination, 171, 111-131.[13] A. Alkhudhiri et al. (2012), Desalination, 287, 2-18.[14] R.W.Schofield et al. (1987), J. Membr. Sci. 33, 299-313.[15] J.F. Zemaitis Jr. et al. (1986), Handbook of Aqueous Electrolyte Thermodynamics, AICHE.[16] M.M. Seckler et al. (2013), Ind. & Eng. Chem. Res.

Study of integrated use of Coagulation / Flocculation and Membrane SeparationProcesses Microfiltration and Ultrafiltration in WheyPaulo Ricardo Amador Mendes 1 *, Júlia de Goes Monteiro Antônio 1 Luís Fernando FigueiredoFaria 11 Escola de Engenharia de Lorena/USP. paulo_ricardo_am@yahoo.com.brThe emplacement of whey is one of the greatest issues that have been faced by dairy industries. Theannual worldwide production of whey is 190 million tons, being only 50% of this total processed andthe remnant represents a great nuisance, thus becoming a problem to the industries because of itstreatment [1]. The effluents from dairy industries pollute mainly because of its high amount oforganic material, and due to it they must be previously treated before of its disposal [1].There are many physical, chemical and biological techniques for treating effluents. Moreover, thesetechniques can be also used mixed in order to improve the treatment, considering that eachtechnique has both costs and efficiency limitations. Consequently, in order to reduce the disposalimpacts to attend the environmental demands, this present work proposes an alternative for treatingthese residues, aiming a reduction of organic contaminants and an increase of the wheybiodegradability, according to a treatment sequence for the effluent.The first stage of the suggested sequence is the coagulation/flocculation which uses coagulates fromnatural sources (tannin and Moringa Oleifera seeds extract) to remove suspended materials thatprovide both turbidity and organic material reductions.In the second stage, membrane separation processes (MSP) have been used, employingmicrofiltration (MF) (0,40 µm in polyetherimide of hollow fibre type) and ultrafiltration (UF) (50 kDaem polyethersulfone of hollow fibre type). Some response variables, such as total organic carbon(TOC), chemical oxygen demand (COD) and turbidity, have been evaluated to optimize thecoagulation/flocculation stage. An response surface methodology with 2 control variables (Tanninconcentrations and moringa extract) was stated, in coagulation pH equals 8,3.In an optimal condition, the coagulated/flocculated whey has been treated by (MSP), beingevaluated according to permeation flow and permeated quality to both membranes. The MFmembrane has shown the best results, due to its higher permeated flow compared to UF at similarlevels of organic material removal. Using these processes was to obtain reductions of 14.61% and89.83% for COD and turbidity, respectively.[1] C. Baldasso, T. C. Barros, I. C. Tessaro (2011), Desalination, 249, 381-386.

Polymeric nanofiltration Membranes based on PVC and C-butylPyrogallol[4]arene or C-butyl Resorcin[4]areneSilvânia Marilene de Lima* and Grégoire Jean-François Demets.Universidade de São Paulo, Faculdade de Filosofia, Ciências e Letras de Ribeirão Preto. Avenida dosBandeirantes, 3900, Monte Alegre, Ribeirão Preto, SP. CEP: 14040-901. *slima@lmim.orgThis communications present a new application for two type of organic molecules: pyrogallolarenes 1and resorcinarenes 2 as ionophores in semipermeable membranes. These compounds can beprepared by acid condensation of pyrogallol, or resorcinol, with functionalized aldehydes to formcavitands with an adequate size to allow the passage of small chemical species through a solidmedium. The scheme represents the general synthesis of PGLs and RCNs:RHOOHOHOROH+4R'H + (Catal)HR = OH or HR' = Alkyl or ArylRHOHOR'R'R'R'OHOHRC-butil pyrogallol[4]arene, 1a, and C-butil resorcin[4]arene, 2a, dispersed in PVC matrix led toflexible, resistant and defined pore-size membranes, which may be classified as nanofiltrationmembranes 4 .HOROHHere, PVC were dissolved in tetrahidrofuran and mixed with 1a, or 1b in 10, 20 and 40% mass/mass.SEM images reveal that the thickness of the membranes prepared by this method is quitereproducible, despite the manual pulverization to be used. B image shows a kind of plastic andporous surface from 1a, 20% membrane; A image, lateral of 1a, 10% prepared with 10mL of theconcentrated solution and C, prepared with 20 mL.Membranes based on PGLs and RCNs are described and tested in assays of permeation ionic speciesin aqueous solution 3 . Natural diffusional measurements using acid and saline solutions as hypertonic,demonstrated that the flux of protons are bigger if the counter-ion have a low hydrated radii, the fluxis proportional of the size of the specie.

Method to obtain data fromconductivity, which can become influx and diffusional coefficientapplying Second Fick Law.Some typical results demonstrated that the quantity of ionophore determine the permit bigger fluxof species. On the left, membranes of resorcinarenes tested with HNO 3 0,5 M, in three differentperceptual. The flux reached with 40% 2a membrane. On the right, the comparison between thesame membrane of 1a, treated with and acid solution of HNO 3 and HCl.To retain salts, our membranes seem to be quite efficient. When the membrane of 1a, 20%, wastested at the same conditions to permeate NaCl and KCl the diffusional coefficients found we muchlow than that obtained with testes to proton permeation. To NaCl the DC reached was a plateau in2,03E -10 m 2 .s -1Mechanical resistances are influence by the percent of ionophore in membranes, more PVC becomethe membranes more elastic. The curves Strain versus stress attest this.[1] T. Gerkensmeier, W. Iwanek, C. Agena, R. Frolich, S. Kotila, C. Nather and J. Mattay (1999), Eur. J. Org.Chem., 2257-2262.[2] A. G. Sverker Högberg (1980), J. Am. Chem. Soc. 102, 6046-6050.[3] T. M. B. Teodósio, L. V. Jardim, T. S. Cavallini and G. J. –F. Demets (2011), Orbital, 3, 4, 2-8.[4] R. W. Baker (2000), Membrane Technology and Applications,[5] H. D. Correia and G. J. –F. Demets (2009), Electrochem. Commun., 11, 1928-1931.

Diffusion of Monovalent Cations through Membranes Based on Polymers andcucurbituril Ionophores.Tiago Mateus B. Teodósio 1 , Gregoire Jean-Françóis Demets 1(1)Faculdade de Filosofia Ciências e Letras de Ribeirão Preto, Universidade de São Paulo,Brasil.tiagomateus@pg.ffclrp.usp.br,greg@usp.brSynthetic ionophore like cucurbiturils are obtained by condensation of glycoluril and formadhyde inacid medium 1 . For their barrel shape, these cavitands are important and versatile building blocks forSupramolecular Chemistry. Many examples of usage of these compounds can be found in theliterature, in the form of rotaxanes, pseudrotaxanes and inclusion complexes, as they are studied bymany researchers all around the world 2 .Figura 1: Cucurbit[6]urilFigura 2 :Hemicucurbit[6]urilRecently the cucurbiturils family got one more member: hemicucurbit[6]uril (figure 2), its structure ishalf of cucurbit[6]uril (figure 1), and can be obtained at cone conformation or alternating. Accordingto Myahara and co-workers 3 , the solubility of hemiCuc6 increases in the presence of metal orammonium thiocyanates. In this communication we show by using of this new macrocycle,hemicucurbit[6]uril, acting as an ionophore, that it is possible to prepare polymeric membraneswhich are permeable to ions, and also we use new polymers with the cucurbit[6]urils, who alsosatisfactory results. We developed polimeric composite with synthetic ionophore typecucurbit[6]uril, hemicucurbit[6]uril and various polymers as poly-vinyl chloride (PVC Solvay-Indupa),poly-vinylidene fluorid (PVDF Solvay-Indupe), and the poly-urethane (PU-Basf), thusgenerating assim membranes semi-permeable for nanofiltration. The objective of this work is creatematerials capable of lead ions through small channels created by lumen ionophore in polimericmatrix. The permeability to ions of the membranes with different gradients of ionophores (10,20 and43%), were quantified under gradients of concentration variables, using a glass cell of two separatecompartments, separated by the same membranes. The results indicated a direta relationshipbetween the flow of ions by the material with the load of ionophore in polymer, confirming that thecucurbitands and hemicucurbitands act directly in transport of mass by membranes. Measure ofdiffusion with the cucurbit[6]utils the ion as H + , Li + , Na + and K + , demonstrated be greater permeability

to the protons of which the other cations. The analyzes by conductivity with hemicucurbit[6]urilsdemonstrated also be pemeable to ions as H + ,Li + , Na + , e K + . Tests liquid permeation with poly-vinylcloride (PVC) and the salts as NaCl and Na 2 SO 4 , results showed, that there was not any permeabilityfor the membrane of pvc-pure, the membranes of 20% showed excellent rejections to the salts,therefore the cucurbit[6]urils are directly linked to liquid permeability. The rheologicas propertiesand structural of polymers were studied by scanning electron microscopy. In terms of applicationswe can think about these memebranes for dialysis, sensors, fuel cell, filtres, among other markets.The low cost of production makes these membranes very competitive. We thank the reserach groupof professor A. C. Habert (Coppe-UFRJ) for the tests of liquid permeability.[1] W. A. Freeman; W. L. Mock; N. Y. Shih (1981), J. Am. Chem. Soc. 103(1981) 7367.[2] G. J. -F. Demets (2007), Química Nova, 30, 5, 1313-1322.[3] Y. Miyahara , K. Goto, M. Oka, T. Inazu (2004), Angew. Chem. Int., 43, 5019-5022.

Effect of the UF-Membrane Cut-off on the Invertase ActivityFrancesco Di Addezio 1 , Ester Junko Yoriyaz 2 , Maria Cantarella 1 and Michele Vitolo 2*1 University of L’Aquila, Italy. 2 University of São Paulo, School of Pharmacy, Dept. of Biochemical andPharmaceutical Technology, São Paulo, Brazil, e-mail: *michenzi@usp.br.Invertase [EC.3.2.1.26] hydrolyses sucrose, originating the inverted sugar syrup, which is used,mainly, as a food composition in industries. To carry on the hydrolysis properly, the invertase (MW200kDa) should be recovered after the reaction as well as maintaining its full activity in the solubleform through a considerable reaction period. Then, the best way would be conduct the reaction in amembrane reactor (MR) – which is a continuous stirred tank reactor coupled with an UF-membrane(UFM) -, because it presents: a good diffusion as well as high activity per unit of volume. The cut-offof UFM for retaining soluble invertase must be up to 100kDa. As invertase is the main element forthe process, this work was focused on the role of the UFM cut-off on its activity.Invertase and the UFM (cut-off: 10, 30, 50 and 100kDa) were purchased from FLUKA ® andMILLIPORE ® , respectively. A 10mL Bioengineering ® -Enzyme Membrane Reactor (RM), describedpreviously [1], was purchased from BIOENGINEERING AG (Wald, Germany).Ten milliliters of 0.05Macetate buffer (pH 5.0) containing soluble invertase (1.53x10 -5 mg e /mL) were poured into the MR,which was operated at 45 o C and 140rpm for 30h. The RM was coupled with an UFM and fedcontinuously with a 200mM sucrose solution at a feeding rate of 1h -1 . During the tests, the internalpressure of the RM remained invariable at 0.7atm. Aliquot samples taken every 1h from the outletsolution were measured for the concentration of total reducing sugar, expressed as µmol of glucose,by using the Somogyi’s method. The invertase activity was expressed as µmol gluc /min.mg e .A steady-state regimen occurred in all tests (data not shown), leading to the calculation of the meanvalues of the specific invertase activity (r sp ) (TABLE 1). It can be noted from TABLE 1 that: a)the r spwith the 10kDa-UFM (6027 µmol gluc /min.mg e ) was about eleventh, sixteenth and sixteenth timeshigher than those obtained with 30kDa, 50kDa and 100kDa, respectively. All UFM employed differedonly on the cut-off parameter. The different r sp observed might result from differences on theinvertase adsorption intensity on each membrane due to the fact that the enzyme molecules and themembrane surface/matrix have charged chemical groups. The higher the membrane cut-off, themore deeply into the polymeric matrix the enzymes molecules may insert itself. This should promotea kind of “steric hindrance” of the invertase active site leading to a less efficient sucrose-invertaseinteraction. An electrostatic charge interaction among ionized groups of both invertase andmembrane surface/matrix could also occur; b) the fluoropolymer UFM (cut-off=20kDa) allowedattaining an r sp equal to 400 µmol gluc /min.mg e , i.e., a value 23% lower than that attained withpolyethersulfone 30kDa-UFM. It would be expected that the r sp had a value between 528 and 6027µmol gluc /min.mg e , if the cut-off were the only parameter affecting the invertase specific activity.TABLE 1. Variation of invertase specific activity (r sp ) regarding the UFM cut-off.CUT-OFF (kDa) 10 20* 30 50 100r sp (µmol gluc /min.mg e ) 6027 400 528 379 371*FS61PP/DDS-Alfa Laval UF-membrane (fluoropolymer)[1] E. J. Tomotani and M. Vitolo (2010), BJPS, 46, 571-577.

River Water Treatment by Microfiltration with Sedimentation Pretreatment with anAlternative CoagulantAline Neher, Lucila Adriani Coral, Fatima de Jesus Bassetti*Universidade Tecnológica Federal do Paraná. Department of Chemistry and Biology, Deputado HeitorAlencar Furtado Street, 4900 - Ecoville, 81280-340, Curitiba, Paraná, Brazil. Phone: + 55 48 3279-4575.* Corresponding author: bassetti@utfpr.edu.brTechnological developments, particularly in chemical and pharmaceutical industries, havecontributed to the increase in concentration and in the number of micro-pollutants that reach thewater body due to their difficult removal in wastewater treatment systems. Also, the pollution ofwater bodies by untreated sewage tends to increase the termotolerant bacteria in the water.Although with high capacity in the removal of water contaminants, conventional water treatmentprocesses (coagulation, flocculation, sedimentation/flotation and filtration) are sometimes limited toremoval some micropollutants. Aiming to improve the quality of treated water, the membranefiltration technology has been increasingly studied with complementary method to conventionalprocesses for water treatment, with satisfactory results when applied. Thus, this study aimed toevaluate the applicability of the association of microfiltration technology in the treatment ofPassaúna River water with sedimentation pretreatment by the conventionalcoagulation/flocculation/sedimentation, considering also a comparative evaluation of aluminumsulfate coagulant and Tanfloc (natural coagulant) in the quality of treatment. A flat sheetmicrofiltration membrane of polyethersulfone and N'N'Dimetilformamida (10%:90% inconcentration) was used at pressures between 0.4 and 2.0 bar. Were considered physical-chemicaland microbiological (Escherichia coli) analysis to characterize the treatment efficiency. The resultsindicated similar values for removal of physical and chemical parameters for both coagulants, beingobserved less influence of Tanfloc in the alkalinity of the water. Microfiltration was always efficient inretaining E. coli, yielding the complete removal of these bacteria. Preliminary tests of bacteriaretention with deionised water contaminated with E. coli were performed for all pressures indicated,in order to assess the permeate flux and indicate a better working pressure for natural water. Fromthe results, it was found the use of pressure of 0.8 bar for subsequent experiments because of theirhigher permeate flux (~350 L m -2 h -1 ). When filtration of river water were performed, with previouslytreatment, there was a significant decrease in permeate flow rates, with average permeate fluxes of115 and 130 L m -2 h -1 for Tanfloc and aluminum sulphate, respectively. Although the flow rates canbe low for the pressure used, which indicates the existence of a high organic load in the water evenafter the previous treatment, it was not verified the presence of E. coli in treated water, indicatingthe effectiveness of microfiltration membrane.

Saxitoxins Removal by NF270 e NF90 Nanofiltration MembranesLucila Adriani Coral (a) *, Fatima de Jesus Bassetti (a) , Flávio Rubens Lapolli (b)(a) Universidade Tecnológica Federal do Paraná. Department of Chemistry and Biology, DeputadoHeitor Alencar Furtado Street, 4900 - Ecoville, 81280-340, Curitiba, Paraná, Brazil. Phone: + 55 483279-4575.(b) Universidade Federal de Santa Catarina, Department of Sanitary and Environmental Engineering,Water Reuse Laboratory, Technological Center, Campus Trindade, PO Box 476, 88040-970,Florianópolis, Santa Catarina, Brazil. Phone: +55 48 3721-7744.* Corresponding author: lucilacoral@utfpr.edu.brSaxitoxin (STX) and its analogues are a group of neurotoxic alkaloids, also known as "ParalyticShellfish Poison" (PSP), due to its association with events of toxicity in seafood. These toxins arehydrophilic molecules, positively charged and are characterized for a high solubility in water [1].Brazilian law recommends as a maximum concentration for saxitoxin and its analogues, expressed interms of equivalent STX, value of 3 µg L -1 [2]. Nanofiltration membranes have proved to be effectivefor some cyanotoxins removal. Some studies show a high removal level of dissolved cyanotoxins,mainly microcystins, by nanofiltration membranes [3-7]. In this paper, two flat sheet nanofiltrationmembranes (NF270 and NF90) were studied to evaluate the retention of PSP toxins. A solution oftoxin used in the tests was obtained from a laboratory culture of Cylindrospermopsis raciborskii cells,after consecutive freezing/drawing cycles and previous filtration. The nanofiltration tests wereperformed in a bench scale filtration unit, with volumetric capacity of 450 mL, operating inperpendicular flow and pressure constant (5/6 - 15 bar). The identification and quantification oftoxins was performed by High Performance Liquid Chromatography (HPLC) with post-columnderivatization and fluorimetric detection. The permeate flux and membrane permeability were alsoevaluated. For cyanotoxins removal, five toxin variants were identified as produced by C. raciborskiilaboratorial culture (neoSTX, dcSTX, STX, dcGTX-2 and GTX-2). The percentages of toxins removal forNF270 membrane were varied depending on the type of toxin. For the STX group, the grater removalwas observed for neoSTX and similar values of removal for dcSTX and STX. This behaviour can beassociated in a first moment to the different molecular weight for the toxins (neoSTX: 317 Da; dcSTX:258 Da; STX: 301 Da) [8] in relation to the WMCO of NF270 membrane (300 Da) [9], characterizing aneffect of size-exclusion. The same consideration can also be used to explain the completely retentionof dcGTX-2 toxin (353 Da) [8]. For NF90 membrane, all toxins of STX group and dcGTX-2 werecompletely removed, and the effect of size-exclusion can be also considered as responsible for thetoxins retention, since the WMCO of the membrane is about 200 Da [9]. Nevertheless, the toxin GTX-2, that has a molecular weight higher than other toxins (396 Da) [8] was poor removed by the NF90membrane and this behaviour can be attributed to the electrostatic interaction membrane (chargenegative) - GTX-2 toxin (charge positive). From the results obtained in this study, it can be consideredthat NF90 membrane was more efficient to PSP toxins removal and that the effect of size-exclusion isnot the only mechanism active in the process.

References[1] L. E. Llewellyn (2006), Nat. Prod. Rep., 23, 200-222.[2] Brasil. Ministério da Saúde (2011).[3] M. R. Teixeira, M. J. Rosa (2005), Separation and Purification Technology, 46, 192-201.[4] M. R. Teixeira, M. J. Rosa (2006), Water Research, 40, 2837-2846.[5] A. J. Gijsbertsen-Abrahamse et al. (2006), Journal of Membrane Science, 276, 252-259.[6] M. B. Dixon et al. (2010), Water Science and Technology, 61(5), 1189-1199.[7] M. R. Teixeira, V. S. Sousa (2013), Desalination, 315, 149-155.[8] G. M. Hallegraeff et al. (2003), Manual on harmfull marine microalgae. Paris: UNESCO, 793 p.[9] M. J. López-Muñoz et al. (2009), Separation and Purification Technology, 66, 194-201.

Effect of Plasma Activation on Polyamide Reverse Osmosis Membrane forImproved Chlorine ToleranceRackel REIS*, Ludovic Dumée 1,2 , Mary She 2 , John ORBELL 1 , Mikel DUKE 11 Institute of Sustainability for Innovation, College of Engineering and Science, Victoria University,3030 VIC, Australia.2 Institute for Frontier Materials, Deakin University, Waurn Ponds, 3216 VIC, Australia*rackel.reis@live.VU.edu.au (Rackel Reis)The chlorine oxidation effect of commercial brackish water polyamide RO membranes was investigated aftersurface activation with oxidative (CO 2 and H 2 O) and inert (He) plasma. The plasma treatment was optimized toavoid compromising bench mark membrane performance. He and H 2 O modified membranes exhibited saltrejection by 98% and 95% for CO 2 plasma treated membrane. FT-IR (Figure 1) showed of peak enhancement inthe vicinity of amide vibration for all plasma treated membranes suggesting a change of the nature of thefunctional groups attached to the secondary amides. Water contact angle tests showed a 6% decreaseindicating increased hydrophilicity. SEM shown in Figure 2 showed a strongly reduced surface roughness of theplasma treated membranes when compared to un-treated membranes. Moreover, the chlorine oxidation effectto membrane performance was investigated. The membranes were immersed in chlorine solution (100ppm,pH4) and compared with non-modified membranes. The salt rejection of control membrane dropped from 99%to 94%. He and H 2 O modified membranes successfully exhibited antioxidant property with salt rejectiondropping from 98% to 97%. After chlorine exposure, all membranes were soaked overnight in sodiummetabisulfite followed by salt rejection measurements. As a result, all membrane salt rejections recovered to99% except for the CO 2 modified membrane, which maintained salt rejection at 96%. These results showed thatthe effects on polyamide structure can be via plasma and also exhibit improved chlorine resistance. Meanwhilebisulphite treatment of all chlorine exposed membrane restored salt rejection to the original value.1556cm-1Figure 1 ATR-FTIR spectra for BW30 membrane modified byplasma with peak enhancement in 1556.62 cm -1 , over 1680 –1480 cm -1 obtained by Shimadzu IR FFinity-1 spectrometerequipped with variable angle specular reflectance assessorATR model Vee Max II. All the spectrums were equallynormalized, smoothed and were performed with total of 20scans and 4 cm -1 of resolution.Figure 2 SEM images of DOW FILMTEC BW30 membranes before and afterwater plasma treatment was obtained by Zeiss Supra 55VP FEG withresolution of 5keV, 5cm working distance and 30 µm aperture size. Nanocracksfound on the plasma treated membrane surface are related to thedrying process of sample preparation for SEM analysis (membrane stillexhibited >98% salt rejection and were therefore intact).