Cette étude porte sur la dynamique instationnaire d'une bulle de Taylor dans un tube vertical en repère oscillant. L'objectif est de réaliser une étude expérimentale quantitative plus détaillée de cet écoulement instationnaire, très peu abordé dans la littérature. Les résultats expérimentaux sont obtenus pour des grands nombres de Reynolds pour comprendre les effets d'inertie. Deux configurations différentes sont étudiées : 1) tubes avec deux diamètres internes différents (9,8 mm et 20 mm) remplis d'eau, 2) le tube de diamètre D=9,8 mm rempli de quatre fluides peu visqueux. Le nombre de Bond Bo, basé sur la vitesse ascendante en cas stagnant, varie alors entre 13 et 57, où les effets de la tension superficielle peuvent être pris en compte. La bulle est suivie à l'aide d'une caméra rapide. les vitesses moyenne et fluctuante et le déphasage avec le plateau oscillant sont obtenus par traitement d'images et traitement numérique des données. Les résultats principaux montrent que pour les faibles accélérations la vitesse moyenne diminue et la vitesse fluctuante augmente lorsque l'accélération relative augmente. Au delà d'une accélération critique, la vitesse moyenne augmente et l'augmentation de la vitesse fluctuante semble ralentir. Ce changement de comportement semble être lié à la déformation de l'interface (courbure modifiée, ondes de surface) qui devient significative aux accélérations élevées. De plus, les comparaisons avec les résultats numériques obtenus en négligeant les effets capillaires sont effectuées. Des corrélations permettant de calculer les vitesses moyenne et fluctuante sont proposées. L'évolution temporelle de rayon de courbure au voisinage du nez de la poche est également étudiée pour les différentes accélérations et les résultats sont comparés avec le cas stagnant. Pour les accélérations élevées, la formation et la propagation des ondes oscillantes qui affectent la dynamique de l'écoulement sont quantifiées / The present work deals with the motion of a Taylor bubble rising through vertical oscillating pipes. The aim is to perform a more detailed and experimental quantitative study of this unsteady flow, still seldom addressed in the literature. The investigation is restricted to high Reynolds numbers to understand inertia effects. Experimental results are provided for two different configurations : 1) pipes with two different inner diameters (9.8 mm and 20 mm) filled with water, 2) the thinner pipe (D=9.8 mm) filled with four low viscous fluids. So the Bond number Bo, based on the steady rise velocity varies from 13 to 57, where the effects of surface tension can be considered. The bubble trajectory is tracked by using a high-speed video camera. The average terminal and fluctuating velocity, as well as the phase shift with the oscillating plate are obtained by using image processing. The main results show that for weak acceleration, the mean velocity decreases with the relative acceleration as the fluctuating velocity increases in proportion to this acceleration. Beyond a critical relative acceleration, the average velocity increases and the fluctuating velocity increase seems to slow down. This behavior change seems to be related to the interface deformation (modified curvature, surface waves) which becomes significant in high accelerations. Additionally, comparisons are made with the numerical results obtained by neglecting the capillary effects. Correlations allowing the prediction of mean and fluctuating velocities depending on the Bond number and relative acceleration are proposed and compared with our experimental results. The time evolution of the radii of curvature in the vicinity of the bubble nose is also studied for different relative accelerations and the results are compared with the stagnant case. In high accelerations, the formation and propagation of surface waves which may influence the bubble dynamics are quantified

Made available in DSpace on 2014-06-11T19:23:38Z (GMT). No. of bitstreams: 0 Previous issue date: 2007-12-27Bitstream added on 2014-06-13T18:50:59Z : No. of bitstreams: 1 mendes_faa_me_ilha.pdf: 2673818 bytes, checksum: 120558e9283b734ad04dda5b07ec06d0 (MD5) / Coordenação de Aperfeiçoamento de Pessoal de Nível Superior (CAPES) / O princípio de funcionamento de um sistema gas-lift é bastante simples, baseando-se na injeção de um gás inerte próximo à extremidade submersa de um tubo utilizado para ascensão do líquido (riser). Esse sistema tem sido utilizado em diversos setores da indústria, dentre os quais se destaca o setor petroquímico. Apesar de ter sido concebido há mais de um século, e a despeito do considerável número de artigos publicados sobre o assunto, vários aspectos relativos às características do escoamento bifásico dentro do riser e ao funcionamento do sistema são, ainda, pouco conhecidos. No presente trabalho, um sistema air-lift de pequeno porte foi inteiramente desenvolvido e testado, permitindo observar o comportamento do sistema quando submetido a variações na vazão de ar, na razão de submersão e na geometria do injetor – contendo três (3F) ou quinze furos (15F). Ensaios de visualização foram conduzidos, possibilitando a caracterização do escoamento bifásico no interior do riser. Medições experimentais foram, também, realizadas para a obtenção da eficiência e das curvas características do sistema. Os resultados quantitativos foram interpretados em associação com imagens estáticas do escoamento, capturadas com uma câmera fotográfica digital, e com imagens dinâmicas, tomadas com o auxílio de uma filmadora de alta velocidade. A partir destas imagens, foi possível, ainda, a estimativa de alguns importantes parâmetros característicos do escoamento pistonado, associados ao deslocamento da chamada bolha de Taylor. Os dados assim obtidos foram comparados com valores oriundos de correlações empíricas propostas por outros autores, apresentando boa concordância. Com relação aos resultados quantitativos, observou-se que, sob determinadas condições de operação, o injetor 3F é capaz de atribuir ao sistema um rendimento significativamente maior... / The operation principle of a gas-lift system is very simple: it is based on the injection of an inert gas close to the immersed edge of a tube, which is used for the rising of the liquid (riser). This system has been used in several industrial areas and more often in the petrochemical industry. Despite the fact that it was conceived over a century ago and that there have been a considerable amount of articles published on the subject, several aspects concerning the two-phase flow characteristics inside the riser as well as its operational system are still not very well known. In the present work, a small size air-lift system was thoroughly developed and tested, which facilitated the visualization of the system behavior when submitted to variations in the air flow, the immersion ratio and the injector geometry – containing three (3H) or fifteen holes (15H). Observation experiments were carried out making it possible to characterize the two-phase flow inside the riser. Experimental measurements were also taken in order to obtain the system characteristic efficiency and slopes. The quantitative results were analyzed together with the statistic images of the flow - taken by a digital photo camera, and with the dynamic images – taken by a high-speed filming camera. Through these images, it was also possible to estimate some important characteristic parameters of the slug flow associated to the displacement of the so-called Taylor bubble. The data obtained this way were compared to the figures originated from experimental correlations proposed by other authors, and they showed a fine agreement. Regarding the quantitative results, it was observed that under certain operation conditions the 3F injector is able to give the system a significantly greater efficiency than when the 15F injector is used

Resumo: O princípio de funcionamento de um sistema gas-lift é bastante simples, baseando-se na injeção de um gás inerte próximo à extremidade submersa de um tubo utilizado para ascensão do líquido (riser). Esse sistema tem sido utilizado em diversos setores da indústria, dentre os quais se destaca o setor petroquímico. Apesar de ter sido concebido há mais de um século, e a despeito do considerável número de artigos publicados sobre o assunto, vários aspectos relativos às características do escoamento bifásico dentro do riser e ao funcionamento do sistema são, ainda, pouco conhecidos. No presente trabalho, um sistema air-lift de pequeno porte foi inteiramente desenvolvido e testado, permitindo observar o comportamento do sistema quando submetido a variações na vazão de ar, na razão de submersão e na geometria do injetor - contendo três (3F) ou quinze furos (15F). Ensaios de visualização foram conduzidos, possibilitando a caracterização do escoamento bifásico no interior do riser. Medições experimentais foram, também, realizadas para a obtenção da eficiência e das curvas características do sistema. Os resultados quantitativos foram interpretados em associação com imagens estáticas do escoamento, capturadas com uma câmera fotográfica digital, e com imagens dinâmicas, tomadas com o auxílio de uma filmadora de alta velocidade. A partir destas imagens, foi possível, ainda, a estimativa de alguns importantes parâmetros característicos do escoamento pistonado, associados ao deslocamento da chamada bolha de Taylor. Os dados assim obtidos foram comparados com valores oriundos de correlações empíricas propostas por outros autores, apresentando boa concordância. Com relação aos resultados quantitativos, observou-se que, sob determinadas condições de operação, o injetor 3F é capaz de atribuir ao sistema um rendimento significativamente maior... (Resumo completo, clicar acesso eletrônico abaixo) / Abstract: The operation principle of a gas-lift system is very simple: it is based on the injection of an inert gas close to the immersed edge of a tube, which is used for the rising of the liquid (riser). This system has been used in several industrial areas and more often in the petrochemical industry. Despite the fact that it was conceived over a century ago and that there have been a considerable amount of articles published on the subject, several aspects concerning the two-phase flow characteristics inside the riser as well as its operational system are still not very well known. In the present work, a small size air-lift system was thoroughly developed and tested, which facilitated the visualization of the system behavior when submitted to variations in the air flow, the immersion ratio and the injector geometry - containing three (3H) or fifteen holes (15H). Observation experiments were carried out making it possible to characterize the two-phase flow inside the riser. Experimental measurements were also taken in order to obtain the system characteristic efficiency and slopes. The quantitative results were analyzed together with the statistic images of the flow - taken by a digital photo camera, and with the dynamic images - taken by a high-speed filming camera. Through these images, it was also possible to estimate some important characteristic parameters of the slug flow associated to the displacement of the so-called Taylor bubble. The data obtained this way were compared to the figures originated from experimental correlations proposed by other authors, and they showed a fine agreement. Regarding the quantitative results, it was observed that under certain operation conditions the 3F injector is able to give the system a significantly greater efficiency than when the 15F injector is used / Orientador: Sérgio Said Mansur / Coorientador: Edson Del Rio Vieira / Banca: André Luiz Seixlack / Banca: Ricardo Augusto Mazza / Mestre

Multiphase flows in chemical reactors with micro- and millimeter-size channel structures such as monolith froth reactors, compact heat exchangers and fuel cells have received great attention in the last years. They are considered as a promising alternative to conventional reactors, such as fixed bed reactors and bubble columns which are mainly used for gas absorption, catalytic hydrogenation and biochemical conversions. Slug or Taylor bubble flow is a desired operating state for this type of contactors due to the frequent change of efficient gas-liquid contacting in the film around the bubbles and the enhanced mixing in the liquid slugs behind the bubbles. Consequently, capillary Taylor flow is currently a target of intensive investigations. However, a full understanding of design parameters and optimum operating conditions are still lacking. For milli- and microreactors mass transfer between gas and liquid phases depends upon various parameters such as bubble shape, relative velocity between the two phases, degree of liquid contamination and many more. To further advance the fundamental understanding of micro- and milli-channel reactors with Taylor flow, main design parameters and operating conditions were investigated, which include (a) the effect of bubble size, channel diameter and cross sectional shape of channel on the mass transfer coefficient of dissolving bubbles, (b) the influence of the presence of surface active agents on the bubble shape, velocity and also on the mass transfer rate of bubbles and (c) the intensification effect of oscillation of channels on the mass transfer performance of Taylor bubbles. For the study of gas-liquid mass transfer high-resolution X-ray radiography and tomography were used as measurement techniques. The X-ray imaging methods were chosen as their accuracy is less affected by changes in the refractive index, as it is the case for conventional optical methods. The mass transfer was calculated by measuring the changes in the size of the bubbles at constant pressure. The utilization of X-ray visualization enabled the acquisition of a series of radiographic images of bubbles. The images gave the volume, interfacial area and length of the bubble with high accuracy as a function of time and were used to evaluate the mass transfer coefficient using the mass conservation equations. In case of circular channels, the results show that Sherwood numbers have a large dependency on the bubble length and also equivalent diameter which is in accordance with previous results for larger channel diameters. However, the values of measured Sherwood numbers could not be predicted by available correlations which are valid only for larger pipes. As a result, a new mass transfer correlation in the form of Sherwood number as a function of Peclet number as well as bubble size ratio was derived. The proposed correlation is applicable for a large range of bubble sizes with high accuracy. The comparison of the results for the square and circular channels showed that despite the fact that the rise velocity of bubbles in the square channel is about three times higher than in the circular channel, the mass transfer coefficient is about the same. Furthermore, the results show that in square channels the dissolution curves are relatively even, while the dissolution curves of circular channels exhibit some distinguishable change in the slope. In addition, the results show that the calculated mass transfer coefficient based on the measured data show good agreement with the data predicted by the penetration theory. Regarding the influence of surfactants on the mass transfer in small channels with Taylor flow, it was shown that a small amount of surfactant reduces the mass transfer and its impact is more pronounced on small bubbles. Furthermore, it was demonstrated that the presence of surfactants causes the change of the bubble shape and leads to a slight increase of the liquid film thickness around the bubble and as a result the elongation of contaminated bubbles. Intensification of mass transfer in small channels with Taylor bubbles was investigated by measuring the motion, shape and dissolution rate of individual elongated Taylor bubbles of air and CO2 in water. The comparison of the results for the stationary and oscillating channel showed that mechanical vibration of the channel is able to enhance the mass transfer coefficient from 80% to 186%. Moreover, the mass transfer rate positively correlates with frequency and amplitude of oscillation, which is more pronounced at higher amplitudes. In addition, it was shown that the intensification of mass transfer with increase of amplitude/frequency of vibration is mainly attributed to the increase of bubble surface wave oscillations that causes an enlargement of contact area between the phases and also a reduction of mass transfer resistance in the liquid-side boundary layer.

Les réacteurs-échangeurs à plaques (HEX) sont une technologie clé en intensification des procédés. Cependant, la plupart des recherches existantes portant sur ce type d'équipement ont été réalisées dans le cas d’écoulements monophasiques. Pour les réactions gaz-liquide, peu d'études ont été conduites. Cette thèse a pour objectif d’étudier localement le transfert de matière gaz-liquide autour de bulles de Taylor en écoulement dans des canaux millimétriques droits et ondulés par une méthode dite colorimétrique. Ceci constitue une étape préliminaire indispensable avant la mise en œuvre de systèmes réactifs diphasiques. Il a d’abord déterminé si une possible accélération du transfert de matière gaz-liquide pouvait avoir lieu en présence de la réaction chimique utilisée. La deuxième phase de ce travail s’est focalisée sur l'étape de formation des bulles de Taylor dans un microréacteur. Ensuite, l'hydrodynamique gaz-liquide a été caractérisée et les effets des coudes sur le mécanisme de transfert de masse ont été étudiés localement dans un canal carré millimétrique ondulé. Enfin, une comparaison rigoureuse a pu être effectuée entre les différentes géométries de canaux (ondulé et droit). Elle a permis de montrer comment et pourquoi une géométrie ondulé permet d’intensifier le transfert de masse gaz-liquide (notamment en terme d’efficacité de transfert). L’ensemble de ces résultats ont conduit à la formulation une loi d'échelle, exprimée en termes de nombres de Sherwood, de Graetz et de Péclet, capable de décrire l'évolution du transfert de matière gaz-liquide en fonction de la position axiale dans le canal et des conditions opératoires mises en œuvre. / Compact Heat-EXchanger reactors (HEX) are an important part of process intensification technology. However, most of the existed research dealing with such type of equipment has been focused on the application of one-phase reactive flows. For gas-liquid reactions, few investigations have been out carried. This thesis aims at locally studying gas-liquid mass transfer around Taylor bubbles flowing in straight and meandering millimetric channels using a colorimetric method; this is a preliminary step essential before implementing two-phase reactive systems. Firstly, the occurrence of a possible enhancement of the gas-liquid mass transfer by the chemical reaction involved was investigated. Secondly, the gas-liquid mass transfer occurring in Taylor flows right after the bubble formation stage in a microreactor was studied. Thirdly, the gas-liquid hydrodynamics were characterized and the effects of bends on the mass transfer mechanism were locally investigated in a millimetric meandering channel. At last, a rigorous comparison could be made between the meandering and straight channels. It showed how and why the meandering geometry leads to intensify gas-liquid mass transfer. All these findings enabled to formulate a scaling law, expressed in terms of Sherwood, Graetz and Péclet numbers, able to describe the evolution of gas-liquid mass transfer as a function of axial position and operating conditions.

Cette thèse porte sur l’étude des écoulements de Taylor (ou poche/bouchon) gazliquide en microcanal. Ces écoulements où les effets de tension de surface sont prépondérants ont été étudiées expérimentalement et numériquement pour des géométries rectangulaires avec divers rapports d’aspects. Une première partie expérimentale a consisté à caractériser la formation de bulles (taille, fréquence) en fonction des conditions opératoires, des propriétés des fluides (notamment à travers le nombre capillaire) et du mode de mise en contact des fluides. La dynamique de l’écoulement établi a par la suite été étudiée à l’aide du code JADIM. La simulation de ces écoulements dominés par la tension de surface a nécessité de lever les limitations liées à la prise en compte de la force capillaire. En effet des courants parasites numériques sont créés à proximité de l’interface lors de la simulation d’écoulements capillaires. Une méthode Level Set a été implémentée et comparée à la méthode Volume of Fluid d’origine en termes de courants parasites. Des simulations numériques 3D ont permis l’étude des effets du nombre capillaire et de la géométrie sur la dynamique des bulles de Taylor (vitesse, pression et formes de bulles). Les effets inertiels souvent négligés ont été considérés et leur influence, notamment sur les sauts de pression à l’interface, a été mise en évidence. Le mélange dans le bouchon liquide a également été étudié. / This thesis focuses on the hydrodynamics of gas-liquid Taylor flow (or slug flow) in microchannels. These flows, which are generally dominated by surface tension forces, have been investigated in rectangular channels of various cross-sectional aspect ratios by means of both experimental visualizations and numerical simulations. The first experimental part aims at characterizing the bubble generation process (bubble length and frequency of break-up) depending on the operating conditions, the fluid properties, as well as the junction where both fluids merge. Numerical simulations of fully developed Taylor flow have been carried out with the JADIM code. The computation of such surface tension dominated flows requires an accurate calculation of the surface tension force. Some limitations of the Volume of Fluid method have been highlighted and a Level Set method has been developed in order to improve the calculation of capillary effects. Both methods have been compared in detail in terms of spurious currents. 3D numerical simulations have been performed and the influence of the capillary number, as well as the effects of geometry have been highlighted. Inertial effects have been taken into account and their influence on the pressure drop has been shown to be non-negligible. Mixing in the liquid slug has also been studied.