Дисертації з теми "Newtonian bubble"

Dans les procédés gaz-liquide, l'efficacité des transferts de matière et de chaleur est essentiellement contrôlée par la dynamique des bulles dans la phase liquide. L’étude du comportement des bulles de gaz dans un milieu liquide est donc d'un intérêt certain, tant sur le plan fondamental que sur le plan industriel, surtout lorsque le milieu liquide est non-newtonien. Notre étude a révélé que les propriétés rhéologiques de la phase liquide et la fréquence d'injection du gaz dans la colonne ont une influence importante sur la vitesse d'ascension des bulles. Dans les milieux viscoélastiques, des bulles de volume identique coalescent en ligne à partir d'une certaine hauteur de la colonne. Comme le confirme la simulation rhéologique, la coalescence en ligne des bulles est induite par la présence de contraintes résiduelles dans le fluide. L’utilisation des techniques spécifiques à l'analyse des systèmes dynamiques dissipatifs a montré que la coalescence en ligne est de nature chaotique déterministe. Enfin, un modèle de formation de bulle a été élaboré dans le but de prédire le volume et la forme des bulles au moment du détachement pour diverses conditions expérimentales

Dans le cadre de la production de bio-carburants, les fermenteurs agités aérés sont utilisés la culture de micro-organismes car ils permettent d’assurer un bon transfert d’oxygène entre gaz et liquide, tout en homogénéisant de manière efficace la concentration en substrats. Dans le cas de la production d’enzyme par le champignon filamenteux Trichoderma reesei (une étape clef de la production d’éthanol 2G), le transfert d’oxygène est dégradé par la rhéologie non-newtonienne du moût fermentaire. Par ailleurs, les volumes fermentaires nécessaires aux futures unités de production de bioéthanol sont tellement élevés, de l’ordre de plusieurs centaines de m3 ou plus, que l’homogénéité des substrats n’est plus assurée.Dans ce contexte, la finalité des travaux présentés était de développer un outil de prédiction de performances et d’extrapolation des fermenteurs aérés, basé sur la mécanique des fluides numériques (ou CFD : Computational Fluid Dynamics), et permettant de coupler l’hydrodynamique, la rhéologie, le transfert de matière ainsi que le métabolisme simplifié des microorganismes. Pour arriver à cela, plusieurs étapes expérimentales ont été préalablement menées.Les tailles de bulles présentes dans divers milieux (filtrat fermentaire, milieux modèles) ont été caractérisées à l’aide d’une technique de sonde optique développée à IFPEN lors de travaux antérieurs, mais encore jamais appliquée aux milieux non-newtoniens. Ces mesures inédites de tailles de bulles ont été complétées par la caractérisation du transfert gaz/liquide (kLa) dans chaque système étudié, et la combinaison des différents résultats a permis de développer un modèle de coefficient de transfert (kL) à implémenter dans le modèle CFD. Par ailleurs, des caractérisations hydrodynamiques de type Temps de mélange (par colorimétrie et traitement d’image) et Vélocimétrie (par tube de Pavlov) ont été menées dans les milieux visqueux aérés pour valider les simulations hydrodynamiques.Le modèle développé, basé sur une approche diphasique Eulérienne, et une description moyennée des champs de vitesse (approche dite RANS : Reynolds Averaged Navier-Stokes équations) est utilisé pour illustrer la dégradation du mélange lors de l’extrapolation de la production d’enzymes. Ce phénomène se traduit par l’apparition de gradients de concentrations en substrats (sucres, oxygène dis- sous). Les résultats issus du modèle seront utilisés pour guider les futurs développements technologiques de fermenteurs, ainsi que pour mener des cultures biologiques représentatives de type scale-down, en fermenteurs multizones. Les simulations numériques et les expériences de scale-down permettront d’évaluer la résistance des microorganismes aux gradients de concentrations en substrats subis dans les fermenteurs industriels
Mechanically-agitated reactors are widely used in aerobic fermentation, because they provide good mixing of reactants and high performance in terms of oxygen mass transfer. In the enzyme production process by filamentous fungi Trichoderma reesei, the mass transfer is hindered by the complex rheology of the fermentation broth. This process is a key step in the production of second-generation ethanol; however, because of the high fermentation volumes (∼ 100 m3) required for future bioethenol production units, the reactor scale-up is challenging. In fact, by increasing the size of the fermenter, large scale substrate gradients tend to appear.In this framework, the objective of this study is to develop a predictive tool based on Computational Fluid Dynamics (CFD) for the design and scale-up of aerated reactors. The numerical model here proposed, allows one to characterize such systems by coupling hydrodynamics, rheology, mass transfer, and a simplified metabolic model. To assess the fidelity of the model, several experimental analyses were carried out. Bubble size in shear-thinning liquids and in fermentation broth was measured thanks to a novel technique that was previously developed at IFPEN. This measuring techniques is based on phase- detective optical probes, and its use in stirred tank reactors and in viscous liquids was validated during this study. Bubble size measurements were supplemented with gas-liquid transfer coefficient (kLa) and gas holdup measurements. By combining these data, it was possible to develop a dimensional model for the liquid-side mass transfer coefficient (kL), that served to model the mass transfer mechanism in the CFD simulations.Moreover, the reactor hydrodynamics was characterized in terms of mixing time (via colorimetric method and image processing), and liquid velocity (with the Pavlov tube). These data were then used to quantify the accuracy of the simulations. The numerical model — based on the two-phase Eulerian model, and on Reynolds-averaged Navier-Stokes equations — was used to highlight the mixing degradation that accompanies the scale-up of the protein production process. Results from coupled simulations (distribution of substrate and oxygen concentrations) will be used to guide future design and technology optimization of fermenters, as well as to develop more representative scale-down models for microbial cultures. CFD simulations and scale-down data will assess the microorganisms’ resistance to exposure to substrate content variation inside industrial reactors

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Fundação de Amparo à Pesquisa do Estado de São Paulo (FAPESP)
Due to the high capacity of oxygen transfer and versatility, pneumatic reactors have been constantly used in bioprocesses. However, aiming to expand the use of these bioreactors in the industry, as well as increase the understanding of the complex phenomena that occur in these devices, this thesis aimed to evaluate the hydrodynamic, oxygen transfer and shear conditions in three models of pneumatic reactors (bubble column, concentric-tube airlift and split-cylinder airlift) in the scales of 5 and 10 L, using as liquid phase four Newtonian fluids and eight non-Newtonian fluids, and five specific air flow rate (air of 1 to 5 vvm). Related to the hydrodynamic were studied the global gas hold-up (g), the gas hold-ups in the riser (R) and in the downcomer (D), liquid circulation time (tC), superficial liquid velocity in the riser (ULR) and in the downcomer (ULD), and the percentage energy losses in the riser (%ER+%EFR), in the downcomer (%ED+%EFD), and in the bottom (%EB) of airlift reactors. The values of g, R, D, ULR and ULD showed increasing behaviour with increase of air and decreasing behaviour with the kinematic liquid viscosity (L) and the rheologic properties (K e n), and observed the opposite for tC. The higher values of g, R, D and tC were obtained for concentric-tube airlift reactor (ACC) and scale of 10 L. With exception of ULR of Newtonian fluids, the others liquid velocity tests resulted in higher values for split-cylinder airlift reactors (ASC) and scale of 10 L. This result was attributed to the greater driving force (R-D) to liquid circulation obtained in the ASC reactors and the higher energy losses in the riser and in the downcomer observed in the ACC reactors. In the bottom of the airlift reactors, the higher values of %EB were obtained to the ASC reactor. To evaluate the mass transfer were studied, the average bubble diameter (Db), the volumetric oxygen transfer coefficient (kLa) and the terms that compose the kLa, the convective mass transfer coefficient (kL) and the specific interfacial area of mass transfer (aL). With the increase of air, L, K and n, the air bubbles were predominantly coalescent in water, presenting distorted shape, and non-coalescent with spherical/elliptical shape in the other solutions. It was observed a similar behavior between the kLa and aL parameters, which were directly proportional to the air and inversely proportional to the L, K and n. In water, the aL values were lower than glycerol solutions due to the higher Db values observed in this liquid. For the kL, it was observed a decreasing behaviour with the increase of the air in the most solutions. The magnitude of kL values was due mainly the oxygen difusivity in the liquid, and the higher values were observed to the water, following by the non-Newtonian solutions. In general, the higher values of the mass transfer parameters were obtained in the ACC reactor and in the scale of 10 L. The proposed method to the estimate the average shear rate velocity based on Kolmogorov’s theory of isotropic turbulence showed results consistent with the literature relative to the behavior and magnitude of this variable, as well as the results obtained by the analysis of the morphological changes of Streptomyces clavuligerus in two models of airlift reactors and two aeration conditions. Were proposed correlations to predict all evaluated parameters. Were obtained in all cases a good fit with the experimental data, with deviations between the calculated and experimental values below 20%.
Devido à alta capacidade de transferência de oxigênio e versatilidade, reatores pneumáticos têm sido constantemente utilizados em bioprocessos. Entretanto, visando ampliar a utilização destes reatores na indústria, assim como aumentar a compreensão dos fenômenos complexos que ocorrem nestes dispositivos, na presente tese teve-se como objetivo avaliar as condições hidrodinâmicas, de transferência de oxigênio e de cisalhamento em três modelos de reatores pneumáticos (coluna de bolhas, airlift de cilindros concêntricos e airlift split-cylinder) nas escalas de 5 e 10 L, utilizando como fase líquida quatro fluidos newtonianos e oito fluidos nãonewtonianos e cinco vazões específicas de ar (ar de 1 a 5vvm). Em termos hidrodinâmicos foram estudadas as retenções gasosas global (g), no riser (R) e no downcomer (D), tempo de circulação do líquido (tC), velocidade superficial do líquido no riser (ULR) e no downcomer (ULD) e as perdas percentuais de energia no riser, no downcomer e na base (%EB) de reatores airlift. Os valores de g, R, D, ULR e ULD apresentaram comportamento crescente com o aumento de ar e decrescente com a viscosidade cinemática do líquido (L) e propriedades reológicas (K e n), sendo observado o oposto para tC. Os maiores valores de g, R, D e tC foram obtidos em reator airlift de cilindros concêntricos (ACC) e escala de 10 L. Com exceção de ULR de fluidos newtonianos, os demais testes de velocidade do líquido resultaram em maiores valores nos reatores airlift split-cylinder (ASC) e escala de 10 L. Tal resultado foi atribuído a maior força motriz (R-D) para circulação do líquido obtida em ASC e às maiores perdas de energia no riser e no downcomer observadas em reatores ACC. Na base dos reatores, os maiores valores de %EB foram obtidos para reator ASC. Para avaliação da transferência de massa foram estudados o diâmetro da bolha (Db), o coeficiente volumétrico de transferência de oxigênio (kLa) e os termos que o compõe, coeficiente convectivo de transferência de massa (kL) e área interfacial específica de transferência de massa (aL). Bolhas de ar, com o aumento de ar, L, K e n foram predominantemente coalescentes em água, apresentando formato distorcido e nãocoalescentes com formato esférico/elíptico nas demais soluções. Observou-se um comportamento análogo entre kLa e aL, com relação direta à ar e inversa à L, K e n. Em água, os valores de aL foram inferiores às soluções de glicerol em virtude do maior Db observado neste líquido. Para kL, observou-se um comportamento decrescente com o aumento de ar na maioria das soluções. A magnitude dos valores de kL obedeceu principalmente a difusividade do oxigênio no líquido, sendo os maiores valores observados para água, seguido das soluções não-newtonianas. De maneira geral, os maiores valores dos parâmetros de transferência de massa foram obtidos em reator ACC de 10 L. O método proposto para estimativa da taxa de cisalhamento com base na teoria de turbulência isotrópica de Kolmogorov apresentou resultados condizentes com a literatura em termos de comportamento e magnitude desta variável, assim como com os resultados obtidos pela análise das alterações morfológicas de Streptomyces clavuligerus em dois modelos de reatores airlift e duas condições de aeração. Para todos os parâmetros avaliados foram propostas correlações para sua predição, sendo obtidos em todos os casos bons ajustes aos dados experimentais com desvios inferiores à 20%. Palavras-chave: reatores pneumáticos, retenção gasosa, kLa, diâmetro da bolha, velocidade

L'objet de cette étude est de mieux formaliser et modéliser de façon générique le processus de structuration d'un produit par le procédé de foisonnement, en reliant les paramètres opératoires aux propriétés des mousses formées et de contribuer ainsi à un meilleur pilotage de l'opération. Une ligne de foisonnement par battage en continu a été instrumentée et l'évolution du diamètre des bulles en fonction des paramètres du produit et du procédé a été suivie pour des milieux modèles newtoniens et rhéofluidifiants. L'analyse dimensionnelle à l'échelle du procédé a permis d'aboutir à un modèle physique de l'opération, et donc d'avoir une compréhension des phénomènes en présence. Elle a aussi permis d'intégrer les paramètres du produit et du procédé et de simplifier la représentation des résultats expérimentaux. Enfin, la cohérence de ce modèle avec d'autres issus de la littérature et une première approche de validation avec un produit réel, semble justifier son caractère générique
The aim of this study is to better formalize and model in a generic way the structuring of a product by the foaming operation process, by linking the operating parameters to the foams properties and contribute to a better steering of the operation. A continuous whipping line was instrumented and the evolution of bubble diameter depending on both product and process parameters was characterized for Newtonian and shear-thinning model fluids. Dimensional analysis of the process has lead to a physical model of the operation, and therefore makes possible the understanding of the phenomena involved. It also helped to integrate the product and the process parameters and simplify the representation of experimental results. Finally, the consistency of this model with others from the literature and a first validation with a real product seems to justify his relevance

Acoustic cavitation plays an important role in a broad range of biomedical, chemical and oceanic engineering problems. For example, kidney stone can be crushed into the powder (being discharged naturally) by the acoustic cavitation generated by carefully controlled focused ultrasonic beams. Therefore, the prediction of generation of acoustic cavitation is essential to the aforementioned emerging non-invasive technique for kidney stone crushing. The objective of this PhD program is to study the generation of acoustic cavitation (e.g. through rectified mass diffusion across bubble interface) theoretically in the Newtonian fluids (e.g. water) or viscoelastic mediums (e.g. human soft tissue) under acoustic excitation of single or dual frequency. The compressibility and the viscosity of the liquid, heat and mass transfer across bubble-medium interface are all considered in this study. During this PhD program, the established works in the literature on the above topic have been re-examined. More physically general formulas of natural frequency and damping of gas bubble oscillations in Newtonian or viscoelastic mediums has been derived and further employed for solving the problem of bubble growth under acoustic field (i.e. rectified mass diffusion). For rectified mass diffusion of gas bubbles in Newtonian liquids, the predictions have been improved for high-frequency region of megahertz and above. Effects of medium viscoelasticity and dual-frequency acoustic excitation on rectified mass diffusion have also been studied. To facilitate the fast growth of bubble under acoustic field, dynamic-frequency and dual-frequency techniques have been proposed and demonstrated.

Les écoulements gaz-liquide constituent un axe de recherche très actif en microfluidique. Le rapport des débits entre les deux phases, la formation de bulles et les champs de vitesse des microcanaux ont été étudiés dans cette thèse, en utilisant une caméra numérique rapide et un microsystème de Particule Image Velocimetry (micro-PIV). En particulier, le diagramme des phases gaz-liquide ont été établi dans des microcanaux carrés ; la formation des bulles en fluides tant newtoniens que non newtoniens a été étudiée en détail dans plusieurs configurations géométriques telles que T-injonction et flow-focusing. Les mécanismes régissant la formation d'une bulle ont été modélisés pour chaque étape : expansion, amincissement et rupture. L'étape amincissement de la traînée d'une bulle est notamment contrôlée par une pression orthogonale qui dépend du débit du liquide. Dans le cadre de flow-focusing, le mécanisme de la rupture du film gazeux peut être décrit par une loi d'échelle reliant l'épaisseur minimale du film au temps restant juste avant la rupture avec un exposant 1/3. Le caractère non newtonien de fluides PAAm allonge la traînée d'une bulle par rapport aux fluides newtoniens. Enfin, l'étude de la coalescence entre bulles a été entreprise à l'échelle microscopique ainsi que le comportement complexe des trains de bulles dans des réseaux de microcannaux
Gas-liquid two-phase flow is an important research project in microfluidics. The gas-liquid two-phase flow, the bubble formation and moving behaviours in microchannels were investigated, by using a high speed digital camera and a micro Particle Image Velocimetry (micro-PIV). The gas-liquid two-phase flow in vertical rectangular microchannels was investigated and a flow pattern map was constructed; the bubble formation in both Newtonian and non-Newtonian fluids in cross-flowing microfluidic T-junctions and flow-focusing devices was investigated; the bubble formation process could be divided into expansion, collapse and pinch-off stages; the collapse speed of the gaseous thread in the second stage is controlled by the squeezing pressure, and is proportional to the liquid flow rates; while the minimum width of the neck of the gaseous thread in the third stage for bubble formation in flow-focusing devices could be scaled with the remaining time to the ultimate pinch-off as a power law relationship with an exponent of 1/3; the PAAm solutions prolong the gaseous thread in the tangential direction of the neck; bubble coalescence in a microchannel with an expansion section was studied; the bubble behavior in a microchannel with a loop was also investigated

Cette thèse est une contribution à la modélisation du comportement d'une suspension de bulles dans un fluide non newtonien du type fluide à seuil. Elle comprend trois parties. La première partie est une étude bibliographique recensant les travaux théoriques et expérimentaux pour des bulles cisaillées dans un matériau newtonien. La seconde partie est consacrée à l'étude expérimentale de cisaillement simple d'une bulle suspendue dans un fluide à seuil. La dernière partie présente une approche par changement d'échelle du comportement macroscopique d'une suspension de bulles dans un fluide à seuil. Pour le travail expérimental, nous avons développé un premier prototype de dispositif permettant de cisailler d'une bulle suspendue dans un fluide à seuil. Pour cela, une bulle d'air est injectée au sein d'un grand volume de Carbopol cisaillé loin de la bulle par un dispositif à bandes parallèles. Une première série d'essais a permis de montrer l'efficacité du dispositif et d'obtenir quelques résultats sur la déformabilité d'une bulle cisaillée par un fluide à seuil. Pour le travail théorique, d'abord nous avons proposé des estimations du comportement de la suspension dans le cas des schémas dilué, Mori-Tanaka, autocohérent et motifs morphologiques. Ces modèles nous ont permis de trouver que dans le régime élastique le module élastique macroscopique de la suspension dépend du nombre capillaire Caelast défini comme le rapport entre le module de cisaillement du fluide porteur et la pression capillaire de la bulle. Ensuite en utilisant une méthode d'homogénéisation sécante modifiée (Suquet 1997), nous avons estimé des caractéristiques non linéaires globales de la suspension. Le modèle prédit que le seuil d'écoulement de la suspension est égal au seuil d'écoulement du fluide porteur quelle que soit la taille des bulles. La validation de ces modèles micromécanique a été réalisée par comparaison aux résultats expérimentaux obtenus au laboratoire (Ducloué 2014).Mots clés : suspension de bulles, fluide à seuil, rhéologie, nombre capillaire, approche par changement d'échelle
This thesis contributes to characterizing the behavior of a suspension of bubbles dispersed in a non-Newtonian fluid (yield stress fluid type).It consists of three parts. The first part is a literature review identifying the theoretical and experimental works for bubbles sheared in a Newtonian material. The second part is dedicated to the experimental study of the simple shear of a bubble suspended in a yield stress fluid. The last part consists in developing an upscaling approach to study the macroscopic behavior of a suspension of bubbles in a yield stress fluid. For experimental work, we developped a first prototype of device for the study of the shearing of a bubble in a yield stress fluid. For that purpose, an air bubble is injected in a big volume of Carbopol sheared far from the bubble by a system in two parallel bands. A fist series of tests allowed to show the efficiency of the device and to obtain some results on the deformability of a sheared bubble in a yield stress fluid. For theoretical work, first we proposed estimates of the behavior of the suspension in the case of diluted scheme, Mori-Tanaka, autocoherent and morphological patterns. These models have allowed us to find that in the elastic regime the macroscopic elastic modulus of the suspension depends on the capillary number Caelast defined as the ratio of the shear modulus of the fluid suspended over the capillary pressure of the bubble. Then using a modified secant homogenization method (Suquet 1997), we estimated the overall nonlinear properties of the suspension. The model predicts that the overall yield stress of the suspension is that of the suspending fluid regardless of the size of bubbles. The validation of these micromechanical models was achieved thanks to the experimental results obtained in the laboratory (Ducloué 2014).Keywords: bubbles suspensions, yield stress fluid, rheology, capillary number, upscaling approach

Le but principal de cette étude était d'évaluer et de mieux comprendre l'impact de la vitesse superficielle de gaz et des propriétés de boues activées (BA), sur leur comportement rhéologique et le transfert de l'oxygène dans des bioréacteurs.Tout d'abord, la rhéologie des BA a été évaluée à l'aide d'un rhéomètre tubulaire, conçu et construit dans ce travail. Des mesures rhéologiques ont été effectuées avec des BA provenant de cinq stations d'épuration (STEP) et avec des concentrations en MES comprises entre 2.3 et 10.2 g L-1. Selon ces résultats, la rhéologie des BA est significativement déterminée par la concentration en matière en suspension (MES) mais d'autres caractéristiques liées à leur origine, tel que la taille, la cohésion et la densité du floc, peuvent aussi influencer la viscosité apparente des boues. Basé sur les rheogrames expérimentaux, le modèle rhéologique issu de cette étude est comparé à des modèles rhéologiques existants.Deuxièmement, le transfert d'oxygène a été évalué dans une colonne à bulles (Hc=4.4 m, Dc=0.29m) installée dans deux STEP: une installation classique et un bioréacteur à membrane. La colonne, alternativement équipée d'un diffuseur fines ou grosses bulles (FB, GB), a été alimentée en continu avec des BA extraites du réacteur d'aération, ou de la boucle de recirculation ou du réacteur membranaire. Pour des MES comprises entre 3.0 et 10.4 g L-1, le coefficient kLa a étéplus faible dans les BA que dans l'eau propre et encore réduit avec une augmentation des MES. Cette diminution est en partie attribuable à la réduction observée de la rétention de gaz (εG), associée à une augmentation de la viscosité apparente des boues, celle-ci entrainant une réduction de l'aire interfaciale spécifique (a) due à la coalescence de bulles et à la formation de bulles plus grosses. Aussi, la concentration des tensioactifs non ioniques, a montré un effetnégatif sur le coefficient kLa lors des tests d'oxygénation effectués en aération FB et faibles concentrations en MES. Cet impact n'a pas été observé dans des conditions d'aération GB, ce qui a été expliqué par le taux de renouvellement d’interface plus élevé généré par ces dernières. Enfin, le taux de cisaillement moyen exercé par l'essaim de bulles dans la colonne pendant les tests d’oxygénation a été théoriquement évalué compte tenu des conditions d’opération. Par lasuite, des corrélations empiriques ont été construites en utilisant des nombres adimensionnels et expriment le coefficient kLa en fonction de la vitesse superficielle de gaz et la viscosité apparente, tout en considérant sa dépendance du taux de cisaillement. Enfin, le facteur alpha est défini comme une loi de puissance décroissante en fonction de la viscosité apparente, pour des systèmes à faible chargé
The main purpose of this study was to evaluate and better understand the impact of superficial gas velocity and activated sludge properties,on activated sludge rheology and oxygen transfer in bioreactors. First of all, activated sludge rheology was evaluated using a tubular rheometer, designed and constructed in this work. Rheological measurements were performed with activated sludge from five different wastewater treatment plants and with MLSS concentrations between 2.3 and 10.2 g L-1. Results showed that although the sludge rheology is significantly defined by the MLSS concentration, other sludge characteristics related to the sludge orign, such as such as floc size, floc cohesiveness and floc density also influence the sludge apparent viscosity. Existing rheological models were evaluated on the set of obtained experimental flow curves. Besides, the oxygen transfer is evaluated in a bubble column (Hc=4.4, Dc=0.29 m) installed in two different wastewater treatment plants: a conventional activated sludge plant (CAS) and a membrane bioreactor (MBR). The column, alternatively equipped with a fine or a coarse bubble diffuser (FB, CB), was continuously fed with activated sludge extracted either from the aeration tank, the recirculation loop or the membrane reactor. With MLSS concentrations from 3.0 to 10.4 g L-1, the kkllaa coefficient was lower in activated sludge than in clean water and still reduced with an increase of the MLSS concentration. This reduction is partially attributed to the observed reduction of gas holdup (εεɢɢ), associated with an increase in the sludge apparent viscosity (µµαααααα), which leads to a reduction of the specific interfacial area (αα) due to bubble coalescence and the formation of larger bubbles. Besides, the concentration of non-ionic surfactants, exhibited a negative effect on the κκιιαα coefficient for the oxygenation tests performed under FB aeration conditions and low MLSS concentration. This impact was not observed under CB aeration conditions, which was explained by the higher renewal rates generated by coarse bubbles. Finally, the mean shear rate exerted by the bubble swarm in the column during the oxygen transfer tests was theoretically evaluated considering the operating conditions. Subsequently, empirical correlations were constructed using dimensionless numbers and express the oxygen transfer coefficient as a function of the superficial gas velocity and the apparent viscosity, considering its shear rate dependence. Finally, alpha factor is defined as a power law decreasing function of the apparent viscosity, for low loaded activated sludge systems

"The bubble rise characteristic is very important for the design of heat and masss transfer operations in chemical, biochemical, environmental, and food processing industries. The rate of heat and mass transfer is affected by the bubble size, pressure inside the gas phase, interaction between bubbles, rise velocity and rising trajectory. Research on bubble rise phenomena in non-Newtonian fluids is very limited and there is an increased demand for further research in this area since most of the industrial fluids are non-Newtonian in nature. This study investigated the bubble rise phenomena in water (Newtonian fluid) and various non-Newtonian stagnant fluids"--Abstract.

碩士
國立中正大學
化學工程研究所
90
Abstract This work is to study the bubble behavior and heat transfer in a non-Newtonian fluid of a bubble column. The flow fields around the single rising bubble and bubble coalescence are measured qualitatively and quantitatively by particle image analyzer (PIA). Also, the heat transfer coefficient distribution is measured by heat transfer probe. Four kinds of bubble shapes (teardrop, oblate-cusped, oblate and spherical cap) are discussed. The flow field around a bubble rising is steady and doesn’t change with time. For the bubble shape from teardrop to oblate, there is no complex vortex shedding in the wake, and instead of the complex phenomenon is the special phenomenon in non-Newtonian fluid, "negative wake". This phenomenon is caused by the shearthinning effect and viscoelasticity. The flow in the negative wake area is downward. The boundary of the negative wake shortens with the bubble volume increasing. Then, increase the bubble volume to the spherical cap, and the negative wake is disappeared, and the flow is upward to bubble as in Newtonian fluid. In the spherical cap bubble wake is a steady closed wake with two vortexes. It is because that the inertia force restrains the shearthinning effect and vicoelasticity. In bubble coalescence, the flow field is changed from two single bubble flow fields weld into one bubble flow field, and the process is stable. After getting the qualitative and quantitative analysis of the flow field as the two bubble coalescence, it classifies the reason that trailing bubble with different rising velocity; when the trailing bubble doesn’t get into the flow flied around leading bubble, the trail bubble with larger rising velocity is because of the fluid with some memory effect holding shearthinning effect. Then bubble get into the flow field around leading bubble is subject to the negative pressure gradient caused it accelerate. The heat transfer coefficient in the non-Newtonian fluid in bubble column is mostly dependent to the gas flow rate. The larger heat transfer rate is in the bubble cluster, because the bubble cluster carries the fluid flow upward and with larger rising velocity then the region with no bubble pass through. The larger liquid velocity causes the viscosity decreasing in favor of the surface renewal rate faster.

碩士
中原大學
機械工程研究所
97
The experiment performed the flow visualization by using nitrogen gas to drive the non-Newtonian fluids in a curved circular tube. A continuous long gas bubble was formed to expel the non-Newtonian fluids in the curved tube. Observation of the flow patterns in the curved region, the penetration behavior and leading edge contour of the long bubble were studied. The controlling variables of the experiments are the curving angle of the circular tube, the viscosity of the fluids and the volumetric flow rate of the injected gas. The images of the twin flow were taken and analyzed. The curving angles of the tubes are 90ﾟ, 135ﾟand 180ﾟ. The diameter and the curvature of the tube are 8.0 mm and 0.005 , respectively. The flow rates of the Nitrogen gas are 200, 600 and 1000 ml/min. The results of the experiments showed that the bubble width approaches constant value at the location six-diameter upstream from the bubble front. A difference variable is introduced at the six-diameter location to show the shifting deviation of the bubble in the curved tube. It is shown that, with the same fluid viscosity and the curving angle, the difference is higher when the gas flow rate is higher. Also, the difference increases proportionally when the Capillary number and the Weissenberg number increase.

碩士
中原大學
機械工程研究所
97
The study presents the visualization of the Non-Newtonian fluid flow driven by a continuous long Nitrogen gas bubble in a circular tube with a sudden contraction and a sudden expansion. The characteristics of the flow patterns and the penetration behaviors are recorded as, categorized and studied. The flow patterns is captured through a video capture device (DV). The controlling parameters of the experiments are the volumetric flow rate of Nitrogen, the viscosity of the expelled fluids and the sudden changed angle of the contraction and expansion portion in the circular tube. The fractional ratio is observed as the long gas bubble penetrates the fluid through the sudden contraction and the sudden expansion portion of the tube. The experiment results showed that when the volumetric flow rate of Nitrogen, the fluid viscosity or the angle of the sudden contraction and the sudden expansion protion of the circular tube increase, the velocity of the long bubble will also increase, causing a decreasing fractional ratio near the location of around the sudden contraction. The dominate parameters on the fractional ratio at the inlet are the volumetric flow rate of Nitrogen and the viscosity of the fluid. Also, the Capillary number and the Weissenberg number are inversely proportional to the fractional ratio.

碩士
中原大學
機械工程研究所
100
The flow behaviors of Non-Newtonian fluids driven by a long Nitrogen gas bubble in an inclined tube with a sudden contraction and a sudden expansion are investigated. Behaviors of Non-Newtonian fluids due to gas penetration, and relationships between some related parameters are recorded and studied. The bubble patterns are captured by a video capture device (DV). The controlling variables of experiments are the inclined angle, the volumetric flow rate of Nitrogen, the viscosity of experimental fluids and the sudden changed angles of the contraction and expansion portion in the circular tube. The experimental results showed that when the inclined angle decreases, as well as the volumetric flow rate of Nitrogen and the fluid viscosity increase, the velocity of the long bubble increases, which in turn, causing increases of the fractional coverage and the Capillary number. The angles of the sudden contraction and the sudden expansion of the circular tube have no apparent effects on the bubble penetration velocity. With a higher volumetric gas flow rate penetrates higher viscous fluids, the results indicated that the fractional coverage approaches 0.6 while the Capillary number increases. However, for lower viscous fluids, the fractional coverage obtained in the present experiments only reaches 0.43. An increase of the penetration gas velocity also causes increases of the Capillary number and the Weissenberg number. In addition, it showed that the relationship between both parameters is nearly linear.