Cette thèse est consacrée à l'étude de la dynamique et de la rhéologie des fluides complexes. Nous utilisons une méthode de simulation numérique à trois dimensions. Les systèmes que nous étudions ici sont des suspensions de micro-nageurs actifs, des suspensions de particules sphériques rigides en présence d'un champ externe auquel elles sont sensibles et de la dynamique de suspensions de particules sphériques et confinées en cisaillement. Les Micro-nageurs sont les objets microscopiques qui se propulsent dans un fluide et ils sont omniprésents dans la nature. Un exemple commun de micro-nageurs est la micro-algue textit{Chlamydomonas} . Un des buts principaux de cette thèse est de comprendre l'effet de la motilité de ces micro-organismes sur les propriétés macroscopiques globales de la suspension, telles que la viscosité effective pour expliquer les observations expérimentales. Nous avons élaboré différents modèles de suspensions de textit{Chlamydomonas} et effectué des simulations numériques utilisant la version 3D de la dynamique des particules fluides (FPD) (méthode expliquée dans cette thèse). Les résultats de nos simulations numériques ont été présentés et discutés à la lumière des observations expérimentales. Un des modèles proposés intègre tous les phénomènes observés expérimentalement et sont applicables à d'autres types de suspensions de micro-nageurs. Cette thèse consacre également un chapitre sur les effets du confinement sur la dynamique de cisaillement des suspensions diluées de particules sphériques. Nous avons constaté que dans la géométrie confinée, la vitesse angulaire des particules diminue par rapport à celle imposée par l'écoulement de cisaillement. La vitesse angulaire des particules diminue également lorsque la particule est proche d'une paroi unique et la vitesse de translation de la particule par rapport à la vitesse de la paroi diminue. Un autre objectif de cette thèse est d'étudier les suspensions à viscosité effective ajustable. Nous avons mené une étude numérique sur des suspensions de particules sphériques en présence d'un couple externe. Nous avons montré que le changement de vitesse angulaire des particules due à l'application d'un couple externe est suffisante pour modifier fortement la viscosité de la suspension. Basée sur des simulations numériques, une formule semi-empirique a été proposée pour la viscosité des suspensions de particules sphériques valables jusqu'à 40% de concentration. Nous avons également montré que la 2ème loi de Faxén peut être étendue par une expression empirique pour de grandes concentrations. / This work is dedicated to the study of dynamics and rheology of the complex fluids. We use three dimensional numerical simulations. The systems we study here are: suspensions of biological active micro-swimmers, suspensions of rigid spherical particles in presence of an external field and the dynamics of sheared confined spherical particles. Micro-swimmers are the microscopic objects that propel themselves through a fluid and they are ubiquitous in nature. A common example of micro-swimmers is the textit{Chlamydomonas} . One of the main goal of this thesis is to understand the effect of self-motility of these micro-organisms on the global macroscopic properties of the fluid, such as the effective viscosity to explain experimental observations. We elaborated different models for textit{Chlamydomonas} suspensions and conducted numerical simulations using the 3D version of the Fluid Particle Dynamics method (explained in this thesis). The results of our numerical simulations has been shown and discussed in light of the experimental observations. One of the proposed models incorporates all experimentally observed phenomena and is expendable for other types of micro-swimmer suspensions. This thesis is also dealing with the effects of confinement on the dynamics of sheared spherical particles. We found that in confined geometry, angular velocity of sheared particles decreases compared to the one imposed by the shear flow. The angular velocity of the particles decreases also when the particle are close to a single wall and the translational velocity of the particles changes so that the difference between velocity of the particle and the velocity of the wall decreases. Another objective of this work is to study suspensions with tunable effective viscosity. We conducted a numerical investigation of sheared spherical particle suspensions in presence of an external torque. We showed that the change of particle angular velocity with an external torque is sufficient to strongly change the effective viscosity of the suspension. Based on numerical simulations, a semi-empirical formula has been proposed for the effective viscosity of spherical particles suspensions valid up to 40% concentration. We also showed that a modified second Faxén law can be equivalently established for large concentrations.

Há uma demanda por competitividade entre as indústrias de aços, a fim de alcançar a excelência definida pelo termo clean steel. O processo de desgaseificação a vácuo (VD) ocorre durante o Refino Secundário de aços especiais. Sua principal função é remover gases indesejáveis, especialmente o hidrogênio. Entretanto, durante este processo, o fenômeno de flotação e a absorção de inclusões são reportados. O objetivo do presente trabalho foi estudar a viscosidade de escórias e a capacidade da estação de desgaseificação a vácuo do tipo tanque na limpeza de aços sob uma perspectiva industrial. Para realizar este objetivo, foram coletadas amostras de escória e aço antes e após a etapa de vácuo. Os resultados em limpeza de aço foram relacionados à energia de agitação durante o tratamento a vácuo (associada a um parâmetro cinético - βs) e ao efeito da viscosidade de escórias. É possível observar um decréscimo expressivo na população de inclusões entre as condições antes e após tratamento de desgaseificação a vácuo. A remoção de inclusões durante o vácuo atinge 64, 75 e 78% para as faixas de diâmetro de 2,5-5, 5-15 e ≥ 15 μm, respectivamente. Após o processo de desgaseificação, a composição das inclusões não-metálicas aproxima-se da composição química da escória. O processo de agitação na estação de desgaseificação a vácuo promove uma diminuição significativa na densidade de inclusões na faixa de diâmetro de 2,5-15 μm. Além disso, ao aumentar a intensidade do parâmetro cinético, a composição química de inclusões não-metálicas foi afetada e o teor de enxofre presente no aço líquido foi reduzido. Quanto às viscosidades efetiva das escórias, conclui-se que, para valores mais baixos (0,20 Pa.s) aumenta-se a capacidade da escória na remoção de inclusões, enquanto que valores mais altos (> 0,40 Pa.s) aparentaram ser prejudiciais à limpeza do aço. / There is a demand in competitiveness within the steel industry towards achieving excellence defined by clean steel term. The process of vacuum degassing (VD) occurs during the secondary refining of special steels. Its main function is to remove undesirable gases, primarily hydrogen. However, during this process, flotation phenomenon and inclusions absorption are reported. The aim of the present work was to study the slag viscosity and vacuum degassing (tank type) capacity in steel cleanliness from an industry perspective. To achieve this objective, slag and steel samples were taken before and after vacuum stage. The results in steel cleanliness were related to the stirring energy of the vacuum station (associated to a kinetic parameter – βs) and to the effect of slag viscosity. It is possible to observe an expressive decrease in the population of inclusions between the conditions before and after vacuum degassing treatment. The removal of inclusions during the vacuum stage reaches 64, 75 and 78% in the diameter ranges of 2,5-5, 5-15 and ≥ 15 μm, respectively. After the degassing process, the composition of non-metallic inclusions seemed to approach the slags’ chemical compositions. The stirring process in the vacuum degassing station promotes a significant decrease in the inclusion density with 2,5-15 μm diameter range. Also, by increasing the kinetic parameter intensity, the composition of non-metallic inclusions was affected. The sulfur content present in liquid steel was reduced. Regarding the effective viscosities of slags, it was concluded that lower values (0,20 Pa.s) increased slag capacity in inclusion removal, whereas higher values (> 0,40 Pa.s) was detrimental to steel cleanliness.

The purpose of this study was to investigate the velocity distribution through an annular bed packed randomly with equal sized spheres. Extensive research has been conducted on the velocity distribution inside packed beds packed with equal sized spheres, different sized spheres, deformed spheres, cylinders and Raschig-rings. A majority of these experimental and numerical studies focused on the cylindrical packed bed. These studies and numerical models are all confined to the velocity profile once the fluid flow is fully developed. The development of the velocity through the inlet region of the bed and the fluid flow redistribution in the outlet of the bed is thus neglected. The experimental investigation into the velocity distribution down stream of the annular packed bed of the HTTU indicated that the velocity profile was independent of the mass flow rate for a particle Reynolds number range of 439 £ Re £ 3453 . These velocity profiles did not represent the distribution of the axial velocity due to shortcomings associated with the single sensor hot wire anemometry system used to measure the velocity distribution. A numerical investigation, using the RANS CFD code STAR-CCM+®, into the velocity distribution downstream of an explicitly modelled bed of spheres indicated that the axial velocity distribution could be extracted from the experimental velocity profiles by using an adjustment factor of 0.801. This adjusted velocity profile was used in the verification of the implicit bed simulation model. The implicit bed simulation model was developed in STAR-CCM+®. The resistance of the spheres was modelled using the KTA (1981) pressure drop correlation and the structure of the bed was modelled using the porosity correlation proposed by Martin (1978), while the effective viscosity model of Giese et al. (1998), adjusted by a factor of 0.8, was used to model the velocity distribution in the near wall region. It was found that the structure in the inlet region of the bed, where two walls disturb the packing structure, can be modelled as the weighted average of the radial and axial porosity while the structure in the outlet regions can be modelled by letting the radial porosity increase linearly to unity. The basic shape of the velocity profile is established immediately when the fluid enters the bed. The amplitude of the velocity peaks however increase in magnitude until the velocity profile is fully developed at a distance approximately of five sphere diameters from the bed inlet. The profile remains constant throughout the bed until the outlet region of the bed is reached. In the outlet region a significant amount of fluid redistribution is observed. The amplitude of the velocity peaks is reduced and the position of the velocity peaks is shifted inwards towards the centre of the annular region. The fully developed velocity profile, predicted by the simulation model is in good agreement with profiles presented by amongst others Giese et al. (1998). The current model however also offers insight into the development of the profile through the inlet of the bed and the fluid redistribution, which occurs in the outlet region of the bed. / Thesis (M.Ing. (Mechanical Engineering))--North-West University, Potchefstroom Campus, 2010.

The purpose of this study was to investigate the velocity distribution through an annular bed packed randomly with equal sized spheres. Extensive research has been conducted on the velocity distribution inside packed beds packed with equal sized spheres, different sized spheres, deformed spheres, cylinders and Raschig-rings. A majority of these experimental and numerical studies focused on the cylindrical packed bed. These studies and numerical models are all confined to the velocity profile once the fluid flow is fully developed. The development of the velocity through the inlet region of the bed and the fluid flow redistribution in the outlet of the bed is thus neglected. The experimental investigation into the velocity distribution down stream of the annular packed bed of the HTTU indicated that the velocity profile was independent of the mass flow rate for a particle Reynolds number range of 439 £ Re £ 3453 . These velocity profiles did not represent the distribution of the axial velocity due to shortcomings associated with the single sensor hot wire anemometry system used to measure the velocity distribution. A numerical investigation, using the RANS CFD code STAR-CCM+®, into the velocity distribution downstream of an explicitly modelled bed of spheres indicated that the axial velocity distribution could be extracted from the experimental velocity profiles by using an adjustment factor of 0.801. This adjusted velocity profile was used in the verification of the implicit bed simulation model. The implicit bed simulation model was developed in STAR-CCM+®. The resistance of the spheres was modelled using the KTA (1981) pressure drop correlation and the structure of the bed was modelled using the porosity correlation proposed by Martin (1978), while the effective viscosity model of Giese et al. (1998), adjusted by a factor of 0.8, was used to model the velocity distribution in the near wall region. It was found that the structure in the inlet region of the bed, where two walls disturb the packing structure, can be modelled as the weighted average of the radial and axial porosity while the structure in the outlet regions can be modelled by letting the radial porosity increase linearly to unity. The basic shape of the velocity profile is established immediately when the fluid enters the bed. The amplitude of the velocity peaks however increase in magnitude until the velocity profile is fully developed at a distance approximately of five sphere diameters from the bed inlet. The profile remains constant throughout the bed until the outlet region of the bed is reached. In the outlet region a significant amount of fluid redistribution is observed. The amplitude of the velocity peaks is reduced and the position of the velocity peaks is shifted inwards towards the centre of the annular region. The fully developed velocity profile, predicted by the simulation model is in good agreement with profiles presented by amongst others Giese et al. (1998). The current model however also offers insight into the development of the profile through the inlet of the bed and the fluid redistribution, which occurs in the outlet region of the bed. / Thesis (M.Ing. (Mechanical Engineering))--North-West University, Potchefstroom Campus, 2010.

Há uma demanda por competitividade entre as indústrias de aços, a fim de alcançar a excelência definida pelo termo clean steel. O processo de desgaseificação a vácuo (VD) ocorre durante o Refino Secundário de aços especiais. Sua principal função é remover gases indesejáveis, especialmente o hidrogênio. Entretanto, durante este processo, o fenômeno de flotação e a absorção de inclusões são reportados. O objetivo do presente trabalho foi estudar a viscosidade de escórias e a capacidade da estação de desgaseificação a vácuo do tipo tanque na limpeza de aços sob uma perspectiva industrial. Para realizar este objetivo, foram coletadas amostras de escória e aço antes e após a etapa de vácuo. Os resultados em limpeza de aço foram relacionados à energia de agitação durante o tratamento a vácuo (associada a um parâmetro cinético - βs) e ao efeito da viscosidade de escórias. É possível observar um decréscimo expressivo na população de inclusões entre as condições antes e após tratamento de desgaseificação a vácuo. A remoção de inclusões durante o vácuo atinge 64, 75 e 78% para as faixas de diâmetro de 2,5-5, 5-15 e ≥ 15 μm, respectivamente. Após o processo de desgaseificação, a composição das inclusões não-metálicas aproxima-se da composição química da escória. O processo de agitação na estação de desgaseificação a vácuo promove uma diminuição significativa na densidade de inclusões na faixa de diâmetro de 2,5-15 μm. Além disso, ao aumentar a intensidade do parâmetro cinético, a composição química de inclusões não-metálicas foi afetada e o teor de enxofre presente no aço líquido foi reduzido. Quanto às viscosidades efetiva das escórias, conclui-se que, para valores mais baixos (0,20 Pa.s) aumenta-se a capacidade da escória na remoção de inclusões, enquanto que valores mais altos (> 0,40 Pa.s) aparentaram ser prejudiciais à limpeza do aço. / There is a demand in competitiveness within the steel industry towards achieving excellence defined by clean steel term. The process of vacuum degassing (VD) occurs during the secondary refining of special steels. Its main function is to remove undesirable gases, primarily hydrogen. However, during this process, flotation phenomenon and inclusions absorption are reported. The aim of the present work was to study the slag viscosity and vacuum degassing (tank type) capacity in steel cleanliness from an industry perspective. To achieve this objective, slag and steel samples were taken before and after vacuum stage. The results in steel cleanliness were related to the stirring energy of the vacuum station (associated to a kinetic parameter – βs) and to the effect of slag viscosity. It is possible to observe an expressive decrease in the population of inclusions between the conditions before and after vacuum degassing treatment. The removal of inclusions during the vacuum stage reaches 64, 75 and 78% in the diameter ranges of 2,5-5, 5-15 and ≥ 15 μm, respectively. After the degassing process, the composition of non-metallic inclusions seemed to approach the slags’ chemical compositions. The stirring process in the vacuum degassing station promotes a significant decrease in the inclusion density with 2,5-15 μm diameter range. Also, by increasing the kinetic parameter intensity, the composition of non-metallic inclusions was affected. The sulfur content present in liquid steel was reduced. Regarding the effective viscosities of slags, it was concluded that lower values (0,20 Pa.s) increased slag capacity in inclusion removal, whereas higher values (> 0,40 Pa.s) was detrimental to steel cleanliness.

Há uma demanda por competitividade entre as indústrias de aços, a fim de alcançar a excelência definida pelo termo clean steel. O processo de desgaseificação a vácuo (VD) ocorre durante o Refino Secundário de aços especiais. Sua principal função é remover gases indesejáveis, especialmente o hidrogênio. Entretanto, durante este processo, o fenômeno de flotação e a absorção de inclusões são reportados. O objetivo do presente trabalho foi estudar a viscosidade de escórias e a capacidade da estação de desgaseificação a vácuo do tipo tanque na limpeza de aços sob uma perspectiva industrial. Para realizar este objetivo, foram coletadas amostras de escória e aço antes e após a etapa de vácuo. Os resultados em limpeza de aço foram relacionados à energia de agitação durante o tratamento a vácuo (associada a um parâmetro cinético - βs) e ao efeito da viscosidade de escórias. É possível observar um decréscimo expressivo na população de inclusões entre as condições antes e após tratamento de desgaseificação a vácuo. A remoção de inclusões durante o vácuo atinge 64, 75 e 78% para as faixas de diâmetro de 2,5-5, 5-15 e ≥ 15 μm, respectivamente. Após o processo de desgaseificação, a composição das inclusões não-metálicas aproxima-se da composição química da escória. O processo de agitação na estação de desgaseificação a vácuo promove uma diminuição significativa na densidade de inclusões na faixa de diâmetro de 2,5-15 μm. Além disso, ao aumentar a intensidade do parâmetro cinético, a composição química de inclusões não-metálicas foi afetada e o teor de enxofre presente no aço líquido foi reduzido. Quanto às viscosidades efetiva das escórias, conclui-se que, para valores mais baixos (0,20 Pa.s) aumenta-se a capacidade da escória na remoção de inclusões, enquanto que valores mais altos (> 0,40 Pa.s) aparentaram ser prejudiciais à limpeza do aço. / There is a demand in competitiveness within the steel industry towards achieving excellence defined by clean steel term. The process of vacuum degassing (VD) occurs during the secondary refining of special steels. Its main function is to remove undesirable gases, primarily hydrogen. However, during this process, flotation phenomenon and inclusions absorption are reported. The aim of the present work was to study the slag viscosity and vacuum degassing (tank type) capacity in steel cleanliness from an industry perspective. To achieve this objective, slag and steel samples were taken before and after vacuum stage. The results in steel cleanliness were related to the stirring energy of the vacuum station (associated to a kinetic parameter – βs) and to the effect of slag viscosity. It is possible to observe an expressive decrease in the population of inclusions between the conditions before and after vacuum degassing treatment. The removal of inclusions during the vacuum stage reaches 64, 75 and 78% in the diameter ranges of 2,5-5, 5-15 and ≥ 15 μm, respectively. After the degassing process, the composition of non-metallic inclusions seemed to approach the slags’ chemical compositions. The stirring process in the vacuum degassing station promotes a significant decrease in the inclusion density with 2,5-15 μm diameter range. Also, by increasing the kinetic parameter intensity, the composition of non-metallic inclusions was affected. The sulfur content present in liquid steel was reduced. Regarding the effective viscosities of slags, it was concluded that lower values (0,20 Pa.s) increased slag capacity in inclusion removal, whereas higher values (> 0,40 Pa.s) was detrimental to steel cleanliness.

Dans ce travail, des écoulements liquide-liquide dispersés homogènes (c'est-à-dire sans gradient de concentration) ont été étudiés dans une conduite horizontale de 7.5m de long et de 50mm de diamètre interne. Les expériences ont été réalisées dans une large gamme de paramètres opératoires (vitesses de mélange comprises entre 0.28 et 1.2m/s et concentration volumique en phase dispersée, f, de 0.08 à 0.7). Le facteur de frottement de ces écoulements a été mesuré et modélisé en régime turbulent, intermédiaire et laminaire. Ces différents régimes ainsi que l’effet de la concentration en phase dispersée ont été identifiés à partir des mesures locales de vitesse par une technique de vélocimétrie par image de particules (PIV). Lorsque f=0.56, les dispersions se comportent comme des fluides newtoniens auxquels le concept de viscosité effective peut s’appliquer. Le modèle de viscosité de Krieger et Dougherty (1959) décrit l’ensemble des émulsions formées. Le facteur de frottement mesuré suit les lois de frottement classiques en régime laminaire et turbulent (Hagen-Poiseuille et Blasius respectivement) en fonction du nombre de Reynolds basé sur les propriétés de mélange des émulsions (densité et viscosité). Toutefois, la concentration en phase dispersée induit un retard à l’apparition de la turbulence. En milieu très concentré (f=0.7), la dispersion a un comportement rhéofluidifiant et suit la loi d’Ostwald avec un exposant, n=0.5. Tous ces écoulements ont été étudiés, en détail, par l’analyse locale des vitesses. / Homogeneous dispersed flows have been investigated in a horizontal pipe (7.5m long and 50mm internal diameter) in a wide range of flow parameters (mixture velocity from 0.28 to 1.2m/s and concentration, f, up to 0.7). In this work, the wall friction of this emulsion has been measured and modeled in turbulent, intermediate and laminar regime. The different flow regime and the effect of dispersed phase volume fraction have been determined from the velocity profiles measured by PIV measurements in a refractive index matched medium. When f=0.56, emulsion behaves as newtonian fluid. It was shown that the concept of effective viscosity is relevant to scale the wall friction of the emulsion flow. The effective viscosity follows the classical trend of low inertia suspension of hard spheres (Krieger & Dougherty 1959). The friction factor is described by the classical single phase laws in turbulent and laminar regime (Hagen-Poiseuille and Blasius respectively) as a function of Reynolds number based on mixture properties (density and viscosity). Compared to single phase flow, the transition to turbulence is delayed as dispersed phase fraction is increased. For higher dispersed phase fraction (f=0.7), emulsion behaves as a shear-thinning fluid. Emulsion follows the Ostwald law with an exponent equal to 0.5. All these homogeneous dispersed flow have been studied in details.

Ο στόχος της παρούσας εργασίας είναι η περαιτέρω κατανόηση και ποσοτική σύνδεση φαινομένων μεταφοράς που λαμβάνουν χώρα σε πορώδη μέσα με τα αντίστοιχα φαινόμενα στην κλίμακα λίγων πόρων. Η επέκταση των αποτελεσμάτων από την κλίμακα πόρου στην κλίμακα του πορώδους μέσου δεν είναι προφανής και για το λόγο αυτό η τοπολογία και μορφολογία της πορώδους δομής αντιμετωπίζονται εδώ με δίκτυα πόρων, με έμφαση στα φαινόμενα που λαμβάνουν χώρα στις διασταυρώσεις, αλλά και με ψηφιακές αναπαραστάσεις της δομής με βάση μικροφωτογραφίες δείγματος του υλικού. Συγκεκριμένα, στην εργασία αυτή εξετάζεται η διασπορά μορίων διαλυμένης ουσίας σε δίκτυα πόρων, παρουσιάζεται μία καινούργια τεχνική ανακατασκευής ανομοιογενών πορωδών υλικών και αναπτύσσεται μια μέθοδος προσομοίωσης της ροής αερίων δια μέσου ανακατασκευασμένων πορωδών υλικών στη μεταβατική περιοχή ροής όπου η μέση ελεύθερη διαδρομή των μορίων ενός αερίου είναι συγκρίσιμη με το μέγεθος των πόρων οπότε και παύει να ισχύει η συνήθης παραδοχή του συνεχούς. Η επίδραση της ανάμειξης μέσα σε πόρους ή στις διασταυρώσεις πόρων/ρωγμών στη διασπορά μορίων διαλυμένης ουσίας σε πορώδη μέσα ερευνήθηκε μέσα από την ανάπτυξη και χρήση διαφορετικών τεχνικών προσομοίωσης με έμφαση στις λεπτομέρειες της ροής και της μεταφοράς μάζας στην περιοχή της διασταύρωσης. Βρέθηκε ότι μία νέα μέθοδος τυχαίου περιπάτου αναπαράγει με καλή ακρίβεια το συντελεστή διασποράς σε χαμηλές και μεσαίες τιμές του Peclet, χάρη στο γεγονός ότι λαμβάνει υπ’ όψη την ανάντι της ροής κίνηση των σωματιδίων και τους διαφορετικούς χρόνους παραμονής μέσα σε κάθε κλάδο. Παράλληλα αναπτύχθηκε μία καινοτόμος μέθοδος ανακατασκευής πορωδών μέσων. Η τεχνική στηρίζεται στο διφασικό πρότυπο δικτύου Boltzmann, το οποίο περιγράφει την εξέλιξη συστημάτων υγρού-αερίου υπό την επίδραση της διεπιφανειακής τάσης. Ο μηχανισμός αυτός οδηγεί στη δημιουργία συσχετισμένων δομών, όπου τόσο η μορφολογία του πορώδους μέσου όσο και ο βαθμός συσχέτισής του καθορίζονται από τις λειτουργικές παραμέτρους του προτύπου. Η τεχνική εφαρμόστηκε επιτυχώς σε πραγματικό δείγμα εδάφους με αφετηρία την πληροφορία που δίνεται από μία μικροφωτογραφία μίας στατιστικά χαρακτηριστικής τομής του. Τέλος, μελετήθηκε η ροή αερίων σε πορώδη μέσα, σε πεπερασμένους αριθμούς Knudsen, όπου η μέση διάμετρος των πόρων είναι της ίδιας τάξης με τη μέση ελευθέρα διαδρομή των μορίων του αερίου. Η μελέτη έγινε με τη μεσοσκοπική μέθοδο DSMC. Ο έλεγχος της αξιοπιστίας της μεθόδου και της παρούσας υλοποίησής της έγινε μέσω της μελέτης της ισοθερμοκρασιακής ροής αερίου μεταξύ παραλλήλων πλακών. Παράλληλα υπολογίστηκε το δυναμικό ιξώδες αερίου σε συνθήκες υψηλής αραίωσης και παρουσιάστηκε η εξάρτησή του από τον αριθμό Knudsen. Βρέθηκε ότι τα αποτελέσματα προσεγγίζονται ικανοποιητικά από μία αναλυτική έκφραση τύπου Bosanquet που συσχετίζει το αποτελεσματικό ιξώδες με την τιμή του στο όριο του συνεχούς και με τον αριθμό Knudsen. Επιπρόσθετα μελετήθηκε για πρώτη φορά με τη μέθοδο DMSC η ροή αερίων σε υπολογιστικά ανακατασκευασμένες πορώδεις δομές. Επιβεβαιώθηκε το φαινόμενο του Klinkenberg και η γραμμική εξάρτηση του συντελεστή διαπερατότητας από την αντίστροφη πίεση. Τέλος χρησιμοποιήθηκε μια διαφορετική προσέγγιση στο πρόβλημα υπολογισμού της ροής στη μεταβατική περιοχή μέσω ανάπτυξης προτύπου δικτύου Boltzmann, κατάλληλα τροποποιημένου για ροές σε συνθήκες αραίωσης. Το πρότυπο δοκιμάστηκε τόσο στην περίπτωση ροής μεταξύ παραλλήλων πλακών όσο και σε ροή σε πορώδη μέσα όπου η συμφωνία με τη μέθοδο DSMC βρέθηκε πολύ ικανοποιητική. / The aim of the present study is the further understanding and quantification of transport phenomena in porous media and their connection with the phenomena in the scale of a few pores. The extension of the results from the pore-scale to the scale of the porous medium is not obvious and for this reason the representation of the porous medium is treated both with pore-networks and digital reconstruction. Specifically, in this study it is examined the dispersion of molecules of a solute in porous networks, a new reconstruction technique is presented for heterogeneous granular materials and also a methodology is developed for the study of gas flow in reconstructed porous media in the transient regime, where the mean free path of the gas molecules is comparable with the characteristic length of the pores and thus the continuum description is no longer valid. The effect of the mixing in the pores or the junctions of the pores on the dispersion of molecules of a solute in porous media is examined through various simulation techniques with emphasis on the details of the flow and mass transport in the area of the junction. It was found that a new random-walk technique is reproducing with good accuracy the dispersion coefficient for low and average values of the Peclet number, due to the fact that it takes into account the backwards, with respect to the main direction of the flow, movement of the molecules and the different residence time in each branch. Furthermore, a new reconstruction technique was developed for porous media. The technique is based on 2-phase lattice Boltzmann model, which describes the evolution of a gas-liquid system under the influence of the surface tension. This mechanism leads to the creation of correlated structures, where the morphology of the porous medium and the correlation factor are determined by the operating parameters of the model. The technique was applied successfully for the reconstruction of a real soil sample, starting from the information that is solely given from a microphotograph of a statistically adequate section of the material. Finally, the gas flow through porous media was examined at moderate Knudsen numbers, where the mean diameter of the pores is of the same order of magnitude with the mean free path of the gas molecules. The study was done mainly with the mesoscopic DSMC technique. The credibility of the technique was examined through the study of the isothermal gas flow through parallel plates. Additionally, the dynamic viscosity of a gas under rarefaction conditions was calculated and its dependence on the Knudsen number was shown. It was found that the results are approximated satisfactorily with an analytical Bosanquet-type equation that relates the effective viscosity with its value at the continuum limit and with the Knudsen number. Furthermore, it was studied for the first time with the DSMC method the gas flow through reconstructed porous media. The Klinkenberg effect was confirmed and the linear dependence of the permeability coefficient on the inverse pressure was shown. Finally an alternative approach was used for the calculation of gas flow though porous media in the transient regime through the development of a lattice Boltzmann model suitably modified for rarefied gas flows. The model was tested for the case of flow through parallel plates as well as for the case of flow through porous media and the agreement with the DSMC method was very satisfactory.