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<p>Measurements of film mass flow rate for annular, diabatic steam-water flow in tubes are presented. The measurements were carried out with four axial power distributions and at several axial positions at conditions typical for boiling water reactors, i.e. 7 MPa pressure and total mass flux in a range from 750 to 1750 kg/m2s. The results show that the influence of the axial power distribution on the dryout power corresponds to a consistent tendency in the film flow rate and that the film tends to zero when dryout is approached. Furthermore it is demonstrated that two selected phenomenological models of annular flow well predict the present data. A model for additional entrainment due to boiling is shown to degrade the predictions.</p>

<p>Focusing of strong shock waves in a gas-filled thin test section with various forms of the reflector boundary is investigated. The test section is mounted at the end of the horizontal co-axial shock tube. Two different methods to produce shock waves of various forms are implemented. In the first method the reflector boundary of the test section is exchangeable and four different reflectors are used: a circle, a smooth pentagon, a heptagon and an octagon. It is shown that the form of the converging shock wave is influenced both by the shape of the reflector boundary and by the nonlinear dynamic interaction between the shape of the shock and the propagation velocity of the shock front. Further, the reflected outgoing shock wave is affected by the shape of the reflector through the flow ahead of the shock front. In the second method cylindrical obstacles are placed in the test section at various positions and in various patterns, to create disturbances in the flow that will shape the shock wave. It is shown that it is possible to shape the shock wave in a desired way by means of obstacles. The influence of the supports of the inner body of the co-axial shock tube on the form of the shock is also investigated. A square shaped shock wave is observed close to the center of convergence for the circular and octagonal reflector boundaries but not in any other setups. This square-like shape is believed to be caused by the supports for the inner body. The production of light, as a result of shock convergence, has been preliminary investigated. Flashes of light have been observed during the focusing and reflection process.</p>

The amount and type of cohesive sediment found in gravel river beds can have important implications for the health of aquatic biota, surface/groundwater interactions and water quality. Due to landscape disturbances in the Elbow River watershed, increased sediment fluxes have negatively impacted fish habitat, water quality and water supply to the City of Calgary. However, little is known about the source of cohesive sediment and its interaction with gravel deposits in the Elbow River. This research was designed to: 1) quantify the transport properties (critical shear stress for erosion, deposition, porosity, settling velocity, density) of cohesive sediment and 2) evaluate the potential for coarse gravel to entrap cohesive sediment in the Elbow River. A 5m annular flume was used to conduct erosion and deposition experiments using plane and coarse bed conditions. The critical shear stress for deposition and erosion of the Elbow River cohesive sediments was 0.115Pa and 0.212Pa, respectively. The settling velocity of the cohesive sediment had an inverse relationship between floc size and settling velocity for larger flocs, due to a decrease in floc density with increased size. Cohesive sediment moved from the water column into the gravel bed via the coupling of surface and pore water flow. Once in the gravel bed, cohesive sediments were not mobilized from the bed because the shear produced by the flume was less than the critical shear to mobilize the gravel bed. Using a model developed by Krishnappan and Engel (2006), an entrapment coefficient of 0.2 was determined for the gravel bed. Entrapment coefficients were plotted against substrate size, porosity and hydraulic conductivity, demonstrating a relationship between entrapment coefficient and these variables. It was estimated that 864kg of cohesive sediment is stored in the upper 0.08m of a partially submerged point bar in the Elbow River. Accordingly, when flow conditions are sufficient to mobilize the gravel bed and disturb the amour layer, cohesive materials may be entrained and transported into the Glenmore Reservoir, where it will reduce reservoir capacity and may pose treatment challenges to the drinking water supply.

Short annular diffusers were essential components for turbomachines that have been used to expand the air entering the compressor, as interstage ducts between gas generators and power turbines, and on the exhaust gases exiting the turbine. The industrial community was interested and invested in improving diffuser design that was challenging owing to the unfavourable fluid flow effects. Efficient design of fluid flow devices was possible through the complementary use of experimental testing and computational fluid dynamics (CFD). A numerical shape optimization study was undertaken to determine preferential annular diffuser configurations. Experimental data were compared against CFD that simulated the steady-state Reynolds-averaged Navier-Stokes equations with two-equation turbulence models. This investigation reached equivalent conclusions with respect to the influences associated with diffuser geometry and swirl. Vorticity effects caused by square tabs, that were not as well understood, were investigated. The tabs were effective in reducing the central toroidal recirculation zone created by a swirling flow, but at a static pressure penalty for the area ratio, AR<2.73, diffusers tested. Results identified several shortcomings in the CFD that typically over-estimated pressure recovery and outlet velocity uniformity; however, properly qualitatively predicted wall pressure distributions and outlet velocity profiles. The use of CFD on modest grids, with preference given to the realizable k-epsilon turbulence model, for annular diffusers that have length to inlet height ratio of 12 and at least AR=2.73 with up to 20-degrees inlet swirl was encouraged as a design tool. / Thesis (Ph.D, Mechanical and Materials Engineering) -- Queen's University, 2014-05-29 09:03:16.591

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.

Dreissenid mussels alter particle transport dynamics in the near shore environment of the Great Lakes by intercepting, retaining and recycling suspended solids that might otherwise be exported to the offshore environment (Hecky et al., 2004). Particulate materials filtered from the water column by dreissenids are subsequently released as either feces or pseudofeces (Walz, 1978). This bio-transformation process alters the nature (grain size distribution, settling velocity and density) and transport properties (critical shear stress for erosion, erosion rates and bed stability) of particulate matter in surficial sediments. While knowledge of the transport characteristics of this material is required to refine particle transport dynamics and energy flow models in the Great Lakes, few studies have been specifically conducted to directly quantify these processes. An annular flume was used to determine the bed stability, rate of erosion and critical shear stress for erosion of dreissenid biodeposits. Materials studied in the flume consisted of 1) a combination of biodeposits and surface sediments collected from dreissenid beds and 2) biodeposits harvested in a weir box with dreissenids. The results show that erosion characteristics and sediment transport properties were strongly influenced by bed age; however particle sizes did not increase in the presence of mussels as originally speculated. Bed stability increased after 7 days, with a τcrit of 0.26 Pa compared to the 2 and 14 day consolidation periods (τcrit= 0.13 and 0.15 Pa respectively). In 2010, following a 2 day consolidation period, pure biodeposits harvested in the weir box had a critical shear stress for erosion of 0.052 Pa. The decrease in bed stability found in biodeposits from 2010 compared to the 2008 biodeposit mixture, may be a result of a more diffuse biofilm developing on the highly organic substrate. The mixture of biodeposits collected in 2008 were a combination organic and inorganic materials which may be creating a nutrient limited environment, where biofilm structure consists of more tightly organized biofilm cells and as a result enhance stability in the bed sediments. The decrease observed after 14 days is likely a result of the microbes depleting their resources and dying off. Due to the added roughness the mussels created in the flume, τcrit could not be measured and critical revolutions per minute (RPM) for erosion are reported for flume runs with mussels. During experiments conducted in 2009 with pure biodeposits and mussels the critical RPM was 5.83 while in 2010 in the presence of mussels a critical RPM was not observed. Settling experiments found biodeposits from both years (2008 and 2010) had decreased settling velocities when compared to different sediment types from lacustrine environments. I speculate that the added enrichment of the surficial sediments by mussel biodeposits is enhancing the process of biostabilization and increasing the bed stability and that the presence mussels themselves may additionally be enhancing bed stability by inhibiting flow from reaching the surface sediments/biodeposits.

Submitted by Kilvya Braga (kilvyabraga@hotmail.com) on 2018-04-26T15:19:43Z No. of bitstreams: 1 BRUNO FERREIRA SILVA -DISSERTAÇÃO (PPGEM) 2016.pdf: 3315035 bytes, checksum: 915092a23718ba159ff32b574a8fb04e (MD5) / Made available in DSpace on 2018-04-26T15:19:43Z (GMT). No. of bitstreams: 1 BRUNO FERREIRA SILVA -DISSERTAÇÃO (PPGEM) 2016.pdf: 3315035 bytes, checksum: 915092a23718ba159ff32b574a8fb04e (MD5) Previous issue date: 2016-02-29 / Capes / Na indústria de petróleo, o transporte de óleos pesados em oleodutos requer altas potências de bombeamento devido a sua alta viscosidade, sendo este um dos inconvenientes na produção de óleos dessa natureza; surge assim a necessidade de desenvolvimento de novas tecnologias que otimize tais processos. Uma técnica economicamente viável e que pode ser usada, é o core anular flow, onde uma camada de água é responsável pela lubrificação do óleo que escoa no centro do duto. Desse modo, o presente trabalho apresenta um estudo energético e hidrodinâmico envolvendo o transporte de óleos pesados e água em dutos de conexões curvadas, através de simulação numérica via software ANSYS CFX® Release 15.0. Foi utilizado um modelo matemático que considera o modelo de mistura para tratar o escoamento bifásico águaóleo pesado, tridimensional, transiente e isotérmico, assumindo regime laminar para fase óleo e turbulento para a fase água adotando o modelo de turbulência k . Uma análise energética envolvendo as bombas também foi realizada. Resultados de campos de pressão, velocidade e fração volumétrica para as duas fases são apresentados e analisados. Verifica-se que o uso da técnica core-flow proporciona uma redução de 95,4% na queda de pressão por fricção comparado ao escoamento monofásico de óleo pesado, e que o desligamento e repartida das bombas de óleo e água afetam a queda de pressão por fricção. / In the oil industry, the transport of heavy oils in pipelines requires high power pumping due to its high viscosity, which is one of the drawbacks in oils production of this nature, thus emerge a need to develop new technologies that optimize such processes. An economically viable technique that can be used is the core annular flow, where a water layer is responsible for oil lubrication flowing in the center of the duct. In this way, this work presents an energy and hydrodinamic study of the heavy oils transportation in curved connections by numerical simulation via software ANSYS CFX® Release 15.0. It used a mathematical model that considers the mixture model to treat heavy oil-water two-phase flow, three-dimensional, transient and isothermal, assuming laminar flow to oil phase and turbulent flow to water phase, using k-ε turbulence model. An energy analysis involving pumps was performed. Results of pressure, velocity and volumetric fraction fields for the two phases are show and analysed. It was verified that the use of core-flow technique has decreased in 95.4% friction pressure drop as compared to monophase heavy oil flow and that stop-and-go from the oil and water pumps affect pressure drop by friction

Orientador: Antonio Carlos Bannwart / Dissertação (mestrado) - Universidade Estadual de Campinas, Faculdade de Engenharia Mecânica e Instituto de Geociencias / Made available in DSpace on 2018-08-15T14:50:36Z (GMT). No. of bitstreams: 1 Granzotto_DesireeGrenier_M.pdf: 5773051 bytes, checksum: 11febefe7b30f0680e59ad8a34976576 (MD5) Previous issue date: 2008 / Resumo: As grandes reservas mundiais de óleo pesado e os elevados preços do barril de petróleo tornam essencial o desenvolvimento de tecnologias de elevação e transporte desses óleos. O óleo pesado, com suas características desfavoráveis de alta viscosidade (100 - 10000 cP) e de densidade (abaixo de 20° API), necessita de métodos específicos que viabilizem sua movimentação em dutos a altas vazões. Para isto, um dos métodos mais simples e que não requer utilização de calor ou diluentes é oferecido pelo escoamento anular óleo-água (core-flow). Entre as questões ainda não resolvidas sobre esse escoamento está o controle do escoamento bifásico, de modo a se obter uma operação segura com a razão água-óleo adequada. Neste trabalho é apresentada uma modelagem do escoamento anular de óleo viscoso e água em regimes permanente e transiente no interior de um duto horizontal. Das possíveis estratégias de controle, optou-se, por simplicidade, pelo controle da vazão de água a uma dada vazão de óleo (desejada para a linha), através da atuação na rotação da bomba d'água. A modelagem permanente da perda de carga em escoamento anular foi ajustada aos dados experimentais colhidos em uma linha de aço de 2,5 polegadas de diâmetro nominal e comprimento 30 m, para diversas combinações de vazões de óleo e água, devido a certa aderência do óleo na parede do duto. A modelagem transiente satisfaz o critério clássico de estabilidade de Ledinegg. Esses resultados possibilitaram projetar e testar um sistema de controle para a vazão de água em duas versões: proporcional-integral (PI) e fuzzy. As comparações permitiram concluir pelo melhor desempenho do controlador fuzzy, por suas características e robustez / Abstract: The significant heavy oil reserves worldwide and the presently high crude oil prices make it essential the development of technologies for heavy oil production and transportation. Heavy oils, with their inherent features of high viscosity (100-10,000 cP) and density (below 22°API) require specific techniques for pipe flow at high flow rates. For this purpose, one of the simplest methods, which does not require use of heat or diluents, is provided by oil-water annular flow (core-flow). Among the still unsolved issues regarding core-flow is the two-phase flow control, in order to obtain a safe operation of the line at the lowest possible water-oil ratio. In this work a model of the viscous oil-water annular flow in a horizontal pipe for both steady and unsteady regimes is presented. From the possible strategies, the water flow rate control for a given oil flow rate was selected for simplicity. Due to the observation of some oil adherence to the wall, the steady state flow model was adjusted to experimental data collected in a 2.5 inches, 30 meters long steel pipe at several combinations of oil and water flow rates. On the other hand the transient model is shown to satisfy the well-known Ledinegg stability criterion. These features made it possible to design and testing a control system for the water flow rate in two different versions: proportional-integral (PI) and fuzzy. Comparisons indicate that the fuzzy controller performs better due to its features and robustness / Mestrado / Explotação / Mestre em Ciências e Engenharia de Petróleo