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<p>Kvalitetno me&scaron;anje pra&scaron;kastih materijala, čestica ili granula je od izuzetnog inženjerskog, energetskog, ekonomskog i ekolo&scaron;kog značaja u raznim granama industrije: prehrambenoj, procesnoj, hemijskoj, farmaceutskoj industriji. Efikasnost me&scaron;anja, dizajn opreme i parametri procesa me&scaron;anja imaju značajan uticaj na kvalitet i cenu poluproizvoda ili finalnog proizvoda.<br />U ovoj tezi, prikazana je upotreba metode diskretnih elemenata (DEM) na modelovanje me&scaron;anja granula i/ili pra&scaron;kastih materijala (granulisani zeolit ili kukuruzna prekrupa) u različitim konfiguracijama statičkih me&scaron;ača Komax i Ross, kao i za modifikovane pužne transportere / predme&scaron;alice. Primenjen je i metod računske dinamike fluida (CFD) za modelovanje protoka fluida u Ojlerovom vi&scaron;efaznom modelu, za predviđanje pona&scaron;anja čestica unutar različitih konfiguracija statičkih me&scaron;alica.<br />Ispitivano je petnaest horizontalnih pužnih transportera sa nepromenljivog koraka, sa modifikovanom geometrijom, različitih dužina pužnice, sa dodatnim elementima na pužnoj spirali, radi istraživanja mogućnosti me&scaron;anja granulisanog materijala, tokom transporta materijala (granulisani zeolit).<br />Rezultati matematičkog modeliranja i numeričke simulacije su upoređeni sa odgovarajućim eksperimentalnim rezultatima na osnovu stepena pome&scaron;anosti me&scaron;avine, primenom kriterijuma relativne standardne devijacije (RSD). Zahvaljujući ovde postavljenim modelima moguće je uraditi optimizaciju geometrije i parametara sistema me&scaron;anja uzimajući u obzir kvalitet procesa me&scaron;anja i cenu finalnog proizvoda.</p> / <p>The quality mixing of powders, particles and/or granules obtain an engineering, energetic, economic and ecological importance of various technologies, food industry, pharmaceutical and chemical industry. The mixing efficiency, the design of equipment and mixing parameters exert a strong impact on quality and the price of intermediate or final product. In this thesis, the use of Discrete Element Method (DEM) is shown for modeling of granular and/or powder flow in various multiple Komax and Ross mixing applications, as well as for the modified screw conveyors premixers . Computational Fluid Dynamic (CFD) method was used for modeling of fluid flow through Eulerian multiphase model, for the prediction of particle displacement within the various static mixers configurations. Fifteen horizontal screw conveyors with invariant pitch, with modified geometry and different screw length , with some additional elements welded on the helix were tested for the possibility of granular material mixing during the material transport (granulated zeolite).<br />The results of the numerical simulation are compared with appropriate experimental results, according to relative standard deviation criterion (RSD). Application of this model provide the optimization of the geometry and parameters of mixing systems taking into account the quality of the mixing process and the cost of the final product.</p>

Un grand nombre d’industries (chimiques, pharmaceutiques et agroalimentaires) utilisent, produisent ou transforment des fluides complexes. Ce sont des fluides à viscosité élevée, souvent de comportement non-Newtonien. Leur préparation nécessite souvent une étape de chauffe suivie d’une étape de refroidissement. La chauffe est indispensable afin de faciliter la fabrication (réaction chimique et/ou transformation physico-chimique). Le refroidissement, ou encore l’étape de finition, consiste à amener les fluides jusqu’à une température proche de la température ambiante pour aborder l'étape de conditionnement. Le refroidissement est le plus souvent réalisé « in situ » dans la même cuve agitée, équipée d’une double enveloppe (utilisée pour la fabrication), mais des technologies en continu peuvent également être envisagées. Ces travaux de thèse portent sur la mise en place d’une méthodologie de pilotage de la vitesse d’agitation lors du refroidissement de fluides complexes dans des cuves agitées, ainsi que sur la comparaison des performances de la cuve agitée avec celles du mélangeur statique. Deux fluides de travail sont testés : Newtonien et viscoplastique, en régime d’écoulement laminaire et transitoire. Nous déterminons les limites de l’influence de l’agitation sur le transfert thermique, la durée de l’opération et la quantité d’énergie consommée. En premier lieu, le refroidissement est étudié à l’échelle laboratoire (réacteur de 0,6L). Il a été constaté que le changement de la vitesse d’agitation au cours du refroidissement affecte le profil de température. Cela a un impact avantageux sur le coût énergétique et/ ou la durée de refroidissement. Les tendances observées à l’échelle laboratoire sont transposées et validées à l’échelle pilote (réacteur de 60L). Puis deux types de mélangeurs statiques sont étudiés comme technologie en continu. Nous établissons des modèles de perte de charge que nous utilisons dans la détermination de l’énergie dépensée pour le refroidissement. Ensuite nous réalisons une comparaison de leurs performances en fonction des facteurs d’efficacité de transfert thermique et de consommation énergétique. Enfin, une brève analyse comparée est exposée, présentant les divers critères de choix entre la cuve agitée et la technologie en continu. / Highly viscous Newtonian and non-Newtonian fluids are frequently encountered in the process industries (like pharmaceutical, food and cosmetics). The preparing of such products involves heating and cooling steps. The heating stage is essential in order to facilitate the production (chemical reaction and/or physico-chemical transformation). The cooling step, named also final stage, leads the fluids to ambient temperature and prepares them for the conditioning. The cooling is mostly realized "in situ" in the same double jacketed stirred vessel, (used for the manufacturing), but continuous technologies may also be employed. This study aims to investigate the cooling of highly viscous fluids, and intends to define the best conditions for controlling the impeller speed (constant or variable) in a stirred vessel, as well as to compare the performances of the stirred vessel with those of the static mixer. Two fluids are tested: a Newtonian and a Non-Newtonian yield-stress fluid, in laminar and transitional conditions. The limits of the influence of the impeller speed on the heat transfer, the duration and the energy consumption are determined. In a first approach, the cooling is studied at small scale (0,6L vessel). The variation of the impeller speed during the cooling, affects the profile of temperature. This type of procedure has an advantageous impact on the energy cost and / or the duration of the cooling. The observed tendencies at a small scale are transposed and validated at a pilot scale (60L vessel). Two types of static mixers are studied as continuous technology. Models of pressure drop are established, which are used further in the determination of the energy consumption for the cooling. The performances of these two static mixers are compared, according to the factors of heat transfer efficiency and energy consumption. Finally, a brief comparative analysis is exposed, presenting diverse criteria of choice between the stirred tank and the continuous technology.

Made available in DSpace on 2014-12-17T15:01:15Z (GMT). No. of bitstreams: 1 GustavoSM.pdf: 1835864 bytes, checksum: 70b860b47845b368d78b14132da46ee6 (MD5) Previous issue date: 2008-05-30 / In the oil industry the mixture oil/water occurs in the operations of production, transportation and refining, as well as during the use of its derivatives. The amount of water produced associated with the oil varies and can reach values of 90% in volume in the case of mature phase of the production fields. The present work deals with the development of new design of the Mixer Settler based on Phase Inversion (MDIF&#61666;) in a laboratory scale. We envisage this application in industrial scale so the phases of project, construction and operation are considered. The modifications most significant, in comparison with the original prototype, include the materials of construction and the substitution of the equipment used in the mixing stage of the process. It was tested the viability of substitution of the original system of mechanical mixing by a static mixer. A statistical treatment by means of an experimental design of composed central type was used in order to evaluate the behavior of the main variables of the separation process as function of the efficiency of separation for the new device. This procedure is useful to delimit an optimal region of operation with the equipment. The variables of process considered on the experimental design were: oil concentration in the feeding water (mg/L); Total volumetric flow rate (L/h); Ratio organic/water on volumetric basis (O/A). The separation efficiency is calculated by comparison of the content of oil and greases in the inlet and outlet of the equipment. For determination of TOG (Total Oil and Grease), the method used was based in the absorption of radiation in the infra-red region. The equipment used for these determinations was InfraCal? TOG/TPH Model HATR-T2 of the Wilks Enterprise, Incorporation. It?s important to stand out that this method of measure has being used by PETROBRAS S.A. Results of global efficiency of separation oil/water varied from 75.3 to 97.7% for contaminated waters containing up to 1664,1 mg/L of oil. By means of tests carried out with a real sample of contaminated water supplied by PETROBRAS we have got an effluent specified in terms of the legal standards required for discharging. Thus, the new design of equipment constitutes a real alternative for the conventional systems of treatment of produced water in the oil industry / Na ind?stria do petr?leo a mistura ?leo/?gua (?gua oleosa) ocorre nos est?gios de produ??o, transporte e refino, bem como durante a utiliza??o de seus derivados. A quantidade de ?gua produzida associada com o ?leo varia muito, podendo alcan?ar valores da ordem de 90% em volume ? medida que se caminha para a fase madura dos campos de produ??o. O presente trabalho trata do desenvolvimento de um novo projeto de um Misturador- Decantador a Invers?o de Fases (MDIF&#61666;) em escala de laborat?rio visando aplica??o em escala industrial abrangendo as fases de projeto, constru??o e opera??o. As modifica??es mais significativas, em compara??o ao prot?tipo original, abrangem os materiais de constru??o e a altera??o do equipamento usado na etapa de mistura do processo. Testou-se a viabilidade de substitui??o do sistema original de mistura mec?nica por p?s por um misturador est?tico ou em linha. Realizou-se um tratamento estat?stico atrav?s de um planejamento do tipo central composto a fim de avaliar o comportamento das principais vari?veis de processo em fun??o da efici?ncia de separa??o para o novo projeto do aparelho, com o prop?sito de se delimitar uma regi?o ?tima de opera??o para o equipamento. As vari?veis de processo contempladas no planejamento experimental foram: concentra??o de ?leo na ?gua de alimenta??o (mg/L); vaz?o volum?trica total (L/h); raz?o volum?trica org?nico-aquoso (O/A). A efici?ncia de separa??o ? calculada a partir da medida do teor de ?leo e graxas (TOG) na alimenta??o e na sa?da do equipamento. Para determina??o do TOG, utilizou-se o m?todo de determina??o por absor??o de radia??o na regi?o do infravermelho. O equipamento utilizado para estas determina??es foi o InfraCal? TOG/TPH Modelo HATR-T2 da Wilks Enterprise, Inc. Vale ressaltar que este m?todo de medida vem sendo empregado pela PETROBRAS S.A. para medidas de TOG. Os resultados de efici?ncia de separa??o global ?gua/?leo variaram entre 75,3 e 97,7% para ?guas contaminadas contendo at? 1664,1 mg/L de ?leo. Atrav?s de testes realizados com amostra real de ?gua produzida fornecida pela PETROBRAS, conseguiu-se enquadrar o efluente dentro dos padr?es exigidos pelo CONAMA Resolu??o 357/05 para descarte. Sendo assim, o novo projeto do equipamento constitui uma alternativa real para os atuais sistemas de tratamento de ?guas produzidas na ind?stria de petr?leo

Orientador: Jose Roberto Nunhez / Dissertação (mestrado) - Universidade Estadual de Campinas, Faculdade de Engenharia Quimica / Made available in DSpace on 2018-08-06T09:02:08Z (GMT). No. of bitstreams: 1 Fernandes_LuisAntonioGalhego_M.pdf: 1106385 bytes, checksum: 6b2e2fa17d2a53c5051005b064878165 (MD5) Previous issue date: 2005 / Resumo: Com aplicações nos mais variados ramos industriais, tais como o alimentício, o químico, o farmacêutico, o de bebidas e o de toucador, entre outros, a operação unitária de agitação ou mistura de fluidos desempenha importante papel nos processos industriais. Os misturadores estáticos constituem uma alternativa aos vasos agitados tradicionais, sendo aplicados em processos contínuos. Os atuais fabricantes nacionais de misturadores estáticos têm apresentado dificuldade em definir o tipo adequado de misturador para as aplicações de um modo geral, como selecionar um misturador que, apesar de promover a mistura apresenta um alto consumo de energia para a aplicação. A constante preocupação em se reduzir o consumo de energia exige um cuidado especial com relação à escolha do misturador adequado ao processo. Dois misturadores denominados ALETAS e EDA foram selecionados de um trabalho anterior que desenvolveu e otimizou misturadores estáticos, utilizando a ferramenta fluido-dinâmica computacional (CFD), sendo que um destes se opera em regime laminar (ALETAS) e o outro em regime turbulento (EDA). O presente estudo buscou complementar o desenvolvimento destes novos tipos de misturadores estáticos, sob a forma de ensaios experimentais, em regimes laminar e turbulento. Como resultado dos ensaios experimentais pôde-se concluir que o misturador tipo ALETAS é adequado para se operar em regime laminar e o EDA pode ser utilizado em ambos regimes, laminar e turbulento, com alguns cuidados especiais para o caso de regime laminar. Os mesmos foram comparados com misturadores bastante estudados na literatura (Kenics e Sulzer SMX) apresentando desempenho similar a estes dois misturadores comerciais / Abstract: Mixing is a unit operation with applicability in many industrial fields, such as food, chemical, petrochemical, beverages and pharmaceutical, just to say some fields. The static mixers appear with an alternative to the traditional agitated vessels. They could be used such in batch mixing operation as in continuous processes, but mainly in continuous processes. The Brazilian suppliers had some problems in choosing the adequate equipment, and it is not rare that they choose an equipment that really does the proper mixture, but with a very high consumption of energy. The recently concern about saving energy demands a special care about the choosing of the best static mixer for the particular task.It was selected two models (ALETAS and EDA) from another work that developed static mixers using computational fluid-dynamic (CFD) method, the ALETAS mixer for laminar mixing and EDA for turbulent mixing. This work searches to complete this study, by experimental tests in laminar and turbulent mixing conditions.The results show that ALETAS static mixer can be used in laminar mixing, as the EDA static mixer but the EDA can be used in laminar mixing with some particular cares. The EDA can also be used in the turbulent mixing. Both models of static mixers were also compared with the Kenics and Sulzer SMX commercial static mixers using the data available in the literature with very similar results / Mestrado / Desenvolvimento de Processos Químicos / Mestre em Engenharia Química

This work is focused on computational modelling of mixing fluids in pipeline with static mixers. Main objective is to analyze several selected static mixers in a particular industrial application, namely dosing of the aluminium sulphate solution in the clarification process for potable water treatment. The analysis focuses on the degree of mixedness and pressure loss of individual mixers. Further, the aim of this work is to process the search of available types of static mixers. The benefit of this work is at least an effort to motivate the reader to deeper understanding of the mixing fluids, especially by static mixers.

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La modélisation des phénomènes de brisure de gouttes lors d’opérations d’émulsification par bilan de population (PBE), a pour but de suivre l’évolution de la distribution des tailles de gouttes (DSD). Ceci a fait l’objet d’un grand nombre d’études au cours des deux dernières décennies. Une approche multiéchelle, couplant la modélisation des phénomènes de brisure à l’échelle d’une goutte avec les phénomènes agissant à l’échelle du champ d’écoulement est nécessaire pour simuler correctement les procédés d’ émulsification dans des géométries complexes tels que des mélangeurs statiques ou des homogénéisateurs à haute pression. Une telle approche est présentée dans cette thèse par l’emploi d’un couplage entre PBE et mécanique des fluides numériques (CFD). Trois types de procédés d’émulsification huile dans l’eau ont été étudiés : une cuve agitée de deux litres,équipée avec d’une hélice Mixel-TT générant un écoulement axial de la phase continue, pour deux systèmes modèles : Di-Stereate d’éthylène Glycol (EGDS) dans l’eau d’une part, huiles silicones de différentes viscosités d’autre part. Un montage expérimental sur mesure a été conçu pour l’émulsification d’huiles silicones dans eau basé sur l’emploi de mélangeurs statiques de type SMX+. Des expériences d’émulsification des huiles végétales de qualité alimentaire dans un homogénéisateur à haute pression (HPH) ont été réalisées dans le laboratoires d’UNILEVER R&D à Vlaardingen, Pays-Bas. Deux techniques d’analyse granulométrique in-situ ont été comparées aux résultats obtenus par la technique ex situ de diffraction laser : une sonde vidéo avec traitement automatisé d’images (basé sur la transforméecirculaire de Hough), et une sonde de réflectance laser « Focused Beam Reflectance Measurement »(FBRM), qui mesure la distribution de cordes (CLD). Les sondes ont été introduites dans la cuve agitée et une cellule de mesure a été conçue spécialement pour implanter en-ligne la sonde video et mesurer ainsi la DSD en amont et en aval des mélangeurs statiques. La technique FBRM n’a pas permis de détecter les plus grosses gouttes et la transformation de la CLD en DSD donnait une sous-estimation de la taille des gouttes. Cette méthode n’est par conséquent pas adaptée à l’analyse granulométrique des gouttes transparentes, telles que les huiles silicones. Par contre, la détection des gouttes sur les images prises par la sonde vidéo, permet de produire des mesures fiables de la DSD pour des concentration dephase dispersée faible (≤ 10 %). L’algorithme de détection a été amélioré pour être capable de mesurerla DSD des émulsions avec 10 – 20 % de phase dispersée. La partie modélisation de cette thèse se compose premièrement de l’élaboration d’un nouveau modèlede brisure qui est capables de représenter l’effet de la viscosité de la phase dispersée. Ce modèle est une amélioration du modèle phénoménologique proposé par Luo & Svendsen (1996). Deuxièmement le couplage entre des PBE discrétisées par volumes finis avec la CFD en régime turbulent a été réalisé, dans le code open-source OpenFOAM (OpenCFD). / The modelling of breakage phenomena with the goal to simulate the evolution of drop size distributions(DSDs) in turbulent emulsification by Population Balance Equation (PBE) modeling has been an activearea of research over the last decade. A multi-scale approach, combining the breakage phenomena on the droplet scale with the larger scale flow-field characteristics is necessary to accurately simulate emulsification in complex geometries such as High-Pressure homogenizers and static mixers. Emulsifications were performed for Ethylene Glycol Di-Stearate-in-water and Silicone oil-in-water systemsin a stirred tank reactor, using an axial-flow Mixel-TT impeller, as well as SMX+ (Sulzer) static mixers for the silicone oil system at the LAGEP, Lyon, France. Emulsifications of food-grade vegetableoils in a High-pressure Homogenizer were performed at UNILEVER R&D, Vlaardingen, Netherlands. Two in-situ DSD measurement techniques were compared to results obtained form laser diffraction measurements of samples. Focused Beam Reflectance Measurement (FBRM), which generates achord length distribution was found give an under-prediction of the DSD and failed to detect the largerdroplets of the transparent silicone oils. This technique, while providing a continuous, in situ measurement of the DSD is not reliable for measuring transparent droplets. An in situ video probe with off-line droplet detection via Hough transform, developed at LAGEP, was found to give reliable and traceable DSD measurements for dilute emulsions. The image detection algorithm was improved to be capable of measuring droplets in emulsions with 10 – 20 % dispersed phase hold-up fraction.The modelling part of this thesis consists of the development of a framework for the coupling of PBEand CFD modelling, as well as a significant improvement to the well-known Luo & Svendsen (1996)breakage model. Different breakage models were compared for their applicability to emulsification ofEthylene Glycol di-Stereate (EGDS) and silicone oil in water emulsions in a 2-L stirred tank reactor. This analysis revealed the need for a phenomenological breakage model which does not rely on system dependent parameters and is able to accurately take the dispersed phase viscosity effects into account.Such a model was proposed, based on the Han et al. (2011) to the Luo & Svendsen (1996) framework. A dispersed phase viscosity term was added to the surface energy opposing breakage. This was validated by experimental data from emulsification of silicone oils with varying viscosities (20, 50, 100, 350 mPa.s). The new model was found to provide better predictions than the Alopaeus et al. (2002) and Vankova etal. ( 2007) breakage models, without the need for empirically determined parameters. The one-way coupling of CFD and PBE modelling was implemented in the open-source finite volumes software package OpenFOAM. This was applied to emulsification of vegetable oils with varying viscosities(25, 50, 100 mPa.s) in a Niro-soave bench-scale HPH. The new model was found to deliver good predictions for the drop size distribution after three consecutive passes through the HPH valve at the three different viscosities and varying pressure drops (200, 400, 600 bar).

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