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Multiphase flow in porous media are widespread in emerging subsurface application including geological carbon sequestration and underground hydrogen storage. Multiple fluid interactions introduce more complexity compared to single phase flow. On the gas-liquid interface, mass transfer and interfacial instability may arise. The study of multi-phase interaction behaviour allows the insights gained to be applied to underground storage and recovery applications. In this thesis, a microfluidics platform with high-speed imaging system was built to investigate gas-liquid flow in single microchannel as a simple model and interfacial instability in porous media with microchannel network: At the beginning, to simply the model, mass transfer of deformed bubble flow in the single rectangular and square microchannels was experimentally studied by using water as liquid phase and CO2 as gas phase. Depending on flow rates, flow patterns including slug flow, bubbly flow, and annular flow were observed in rectangular and square microchannels. Flow pattern map was proposed and compared with the maps in the literatures. By using digital image processing, the bubble volume especially that of deformed bubbles in rectangular and square microchannels was calculated based on 2D projection and 3D slicing, correspondingly. Scaling laws including important parameters of bubbles were derived to provide the guidance of microreactor design. Mass transfer coefficients were calculated based on bubble volume. The empirical correlations involving dimensionless numbers were fitted to precisely predict mass transfer coefficients. Further, to be universality, a semi-theoretical model considering length ratio of liquid and gas phases was developed to predict measured mass transfer coefficients in square microchannel precisely. Next, I began to switch our perspective from single microchannel to porous media with microchannel networks. In the first step, the gas-liquid two-phase displacement in porous medi

The bubble flow is used for different application in steel production and refining processes. It plays in indispensable role in the ladle refining process such as for homogenization and inclusion removal. Hence, it is important to understand the effect of the nozzle outlet geometry on the bubble formation. Three different nozzles with different outlet geometries were examined using a physical model. These geometries were: a) Circle, b) Square with round edges and c) Elliptical. All three nozzles had the same nozzle design and similar outlet cross-section areas. Therefore, the only tested parameter was the outlet geometry. The physical model is a water/air model, that consist of water tank ,the nozzles, gas gauge and a high speed camera. Each nozzle was tested under five different gas flow rates: starting from 10 L/min of air gas flow rate, until a 30 L/min of gas flow rate by incriminating with 5 L/min per experimental trial. Therefore, each nozzle was studied using a 5 experimental sets, so in total 15 experiments were made. For each set, 3000 photos were captured by the high speed camera. The photos were then analyzed using mainly the ImageJ software and the naked eye. After analyzing the photos for the experimental sets the following were found: a) The frequency of bubble formation was for the most part constant with an average of 11 bubbles per second. b) The elliptical nozzle produced for the most part the largest bubbles, while the circular produced the smallest ones. The square nozzle had similar bubble sizes comparable to the elliptical nozzle. c) The circular nozzle resulted in the bubbles with most stable surface, while the elliptical nozzle had the most unstable bubble boundary. The study had a drawback, which is the presence of a jetting flow which reduced the accuracy of the results. Thus, it is recommend that future work can solve this issue by finding at which gas flow rate pure bubbling flow stops for each nozzle geometry., Bubbelinjektion används för olika tillämpningar inom stålproduktion och raffineringsprocesser. Det spelar en oumbärlig roll i raffineringsprocesser som homogenisering och borttagning av inneslutningar. Därför är det viktigt att förstå effekten av utloppsgeometrin hos munstycket på bubbelbildningen. Tre olika munstycken med olika utloppsgeometrier undersöktes med hjälp av en fysisk modell. Dessa geometrier är: a) Cirkel, b) Fyrkantig med rundade kanter och c) Elliptisk. Alla tre munstyckena har samma munstycksdesign och liknande utloppstvärsnittsarea. Därför är den enda parametern som testas utloppsgeometrin. Den fysiska modellen bestod av en vattentank, munstyckena där var och en undersöks separat, en gasmätare, en höghastighetskamera och modellen använde vatten/luft. Varje munstycke testades under fem olika gasflöden: startande från 10 L/min luftgasflöde, tills 30 L/min gasflöde stegvis 5 L/min per experimentuppsättning. Därför har varje munstycke 5 experimentuppsättningar, så totalt 15 experiment togs. För varje uppsättning togs 3000 bilder med höghastighetskameran. Bilderna analyserades sedan med främst ImageJ-programvara och blotta ögat. Efter att ha analyserat bilderna från experimenten så visade resultaten följande: a) Frekvensen av bubbelbildning var mestadels konstant med ett genomsnitt på 11 bubblor per sekund. b) Det elliptiska munstycket producerade mestadels de största bubblorna, medan det cirkulära producerade de minsta bubblorna. Det fyrkantiga munstycket resulterade i en liknande bubbelstorlek som det elliptiska munstycket. c) Det cirkulära munstycket resulterade i bubblorna med den mest stabila ytan, medan det elliptiska munstycket hade den mest instabila bubbelgränsen. Studien hade en nackdel, vilket är närvaron av ett jetflöde som minskade noggrannheten i resultatet. Det rekommenderas att framtida arbete kan lösa detta problem genom att hitta vid vilken gasflödeshastighet rent bubblande flöde stoppar för varje munstycke

The bubble flow is used for different application in steel production and refining processes. It plays in indispensable role in the ladle refining process such as for homogenization and inclusion removal. Hence, it is important to understand the effect of the nozzle outlet geometry on the bubble formation. Three different nozzles with different outlet geometries were examined using a physical model. These geometries were: a) Circle, b) Square with round edges and c) Elliptical. All three nozzles had the same nozzle design and similar outlet cross-section areas. Therefore, the only tested parameter was the outlet geometry. The physical model is a water/air model, that consist of water tank ,the nozzles, gas gauge and a high speed camera. Each nozzle was tested under five different gas flow rates: starting from 10 L/min of air gas flow rate, until a 30 L/min of gas flow rate by incriminating with 5 L/min per experimental trial. Therefore, each nozzle was studied using a 5 experimental sets, so in total 15 experiments were made. For each set, 3000 photos were captured by the high speed camera. The photos were then analyzed using mainly the ImageJ software and the naked eye. After analyzing the photos for the experimental sets the following were found: a) The frequency of bubble formation was for the most part constant with an average of 11 bubbles per second. b) The elliptical nozzle produced for the most part the largest bubbles, while the circular produced the smallest ones. The square nozzle had similar bubble sizes comparable to the elliptical nozzle. c) The circular nozzle resulted in the bubbles with most stable surface, while the elliptical nozzle had the most unstable bubble boundary. The study had a drawback, which is the presence of a jetting flow which reduced the accuracy of the results. Thus, it is recommend that future work can solve this issue by finding at which gas flow rate pure bubbling flow stops for each nozzle geometry., Bubbelinjektion används för olika tillämpningar inom stålproduktion och raffineringsprocesser. Det spelar en oumbärlig roll i raffineringsprocesser som homogenisering och borttagning av inneslutningar. Därför är det viktigt att förstå effekten av utloppsgeometrin hos munstycket på bubbelbildningen. Tre olika munstycken med olika utloppsgeometrier undersöktes med hjälp av en fysisk modell. Dessa geometrier är: a) Cirkel, b) Fyrkantig med rundade kanter och c) Elliptisk. Alla tre munstyckena har samma munstycksdesign och liknande utloppstvärsnittsarea. Därför är den enda parametern som testas utloppsgeometrin. Den fysiska modellen bestod av en vattentank, munstyckena där var och en undersöks separat, en gasmätare, en höghastighetskamera och modellen använde vatten/luft. Varje munstycke testades under fem olika gasflöden: startande från 10 L/min luftgasflöde, tills 30 L/min gasflöde stegvis 5 L/min per experimentuppsättning. Därför har varje munstycke 5 experimentuppsättningar, så totalt 15 experiment togs. För varje uppsättning togs 3000 bilder med höghastighetskameran. Bilderna analyserades sedan med främst ImageJ-programvara och blotta ögat. Efter att ha analyserat bilderna från experimenten så visade resultaten följande: a) Frekvensen av bubbelbildning var mestadels konstant med ett genomsnitt på 11 bubblor per sekund. b) Det elliptiska munstycket producerade mestadels de största bubblorna, medan det cirkulära producerade de minsta bubblorna. Det fyrkantiga munstycket resulterade i en liknande bubbelstorlek som det elliptiska munstycket. c) Det cirkulära munstycket resulterade i bubblorna med den mest stabila ytan, medan det elliptiska munstycket hade den mest instabila bubbelgränsen. Studien hade en nackdel, vilket är närvaron av ett jetflöde som minskade noggrannheten i resultatet. Det rekommenderas att framtida arbete kan lösa detta problem genom att hitta vid vilken gasflödeshastighet rent bubblande flöde stoppar för varje munstycke

The breeding blanket is one of the fundamental components of a nuclear fusion reactor and is responsible for the fuel production, generating tritium through neutronic capture reaction between lithium and neutrons. Lithium is a liquid PbLi alloy and the helium formed as reaction by-product can coalesce into bubbles, generating a two-phase mixture with a high-density ratio (¿¿ ~ O5 ). These bubbles can accumulate and stagnate within the blanket channels with potentially harmful consequences. In this work, the interIsoFoam solver of OpenFOAM v2012 is used to simulate bubble motion for a two-phase mixture representative of the He-PbLi system to test its potential for future developments in the field of fusion. In a first phase, several traditional benchmarks were carried out, both 2D and 3D, and considering the two variants of the VOF method implemented in the solver, isoAdvector and plicRDF. Subsequently, He bubbles of different diameters rising in liquid PbLi (¿¿ = 1.2 × 105 ) were analysed to investigate different regimes. For a Eötvös number (Eo) greater than 10, it was possible to recreate the axisymmetric, skirted, oscillatory regimes and the peripheral and central breakup regimes. For Eo < 10, non-physical deformations of the interface are observed, probably generated by spurious velocities that have a greater impact on the solution for very small bubbles and rising velocities., Peer Reviewed, Postprint (published version)

This contribution is an overview of the latest advances in image processing made by the authors, as well as recent and potential applications, including magnetohydrodynamic systems. Contemporary research of two-phase liquid metal flow requires state of the art experimental methods to probe downscaled representative systems. Among these methods are dynamic neutron and X-ray radiography which have applications in studying bubble flow in liquid metal affected by applied magnetic field [1], bubble collective dynamics in Hele-Shaw liquid metal cells [2], particle flow in liquid metal channels [3] and mesoscale solidification of metals under applied magnetic field [4]. Pushing the boundaries, these measurements are inevitably performed under adverse conditions: low signal-to-noise ratio owing to high frame rates (relative to the source flux) required to capture the physics of interest, but also low image resolution, image artefacts, scattering, etc. Therefore, to extract meaningful information from experimental data and study the underlying processes, appropriate image processing methods and tools are required. Development of such tools is also motivated by very limited (for most researchers) access to high-end neutron and X-ray imaging setups and thus one must make the most of data acquired during limited beamtimes. Examples of applications of our solutions to experimental data from neutron and X-ray imaging are shown in Figures 1-4.

This contribution is an overview of the latest advances in image processing made by the authors, as well as recent and potential applications, including magnetohydrodynamic systems. Contemporary research of two-phase liquid metal flow requires state of the art experimental methods to probe downscaled representative systems. Among these methods are dynamic neutron and X-ray radiography which have applications in studying bubble flow in liquid metal affected by applied magnetic field [1], bubble collective dynamics in Hele-Shaw liquid metal cells [2], particle flow in liquid metal channels [3] and mesoscale solidification of metals under applied magnetic field [4]. Pushing the boundaries, these measurements are inevitably performed under adverse conditions: low signal-to-noise ratio owing to high frame rates (relative to the source flux) required to capture the physics of interest, but also low image resolution, image artefacts, scattering, etc. Therefore, to extract meaningful information from experimental data and study the underlying processes, appropriate image processing methods and tools are required. Development of such tools is also motivated by very limited (for most researchers) access to high-end neutron and X-ray imaging setups and thus one must make the most of data acquired during limited beamtimes. Examples of applications of our solutions to experimental data from neutron and X-ray imaging are shown in Figures 1-4.

The worlds energy demand is rising as a result of industrial activity and advances in countries around the world. Fossil fuel sources are used to meet this demand for much of the world [1]. The way in which energy is handled causes pollution e.g., CO2 emissions, inducing climate change, therefore a more sustainable industry is desired [2, 3]. Carbon Capture and Utilization (CCU) is a way to use CO2 from the atmosphere or which would end up in the atmosphere, limiting its influence on the climate. Sustainable fuels or chemicals can be produced from the captured CO2, reducing the use of fossil fuels and fossil feedstock [4, 5]. Formic Acid is a favourable product from CO2 electrolysis. Only 2 electrons are required for one molecule Formic Acid, which results in a high normalized price ($/electron) [6]. COVAL Energy works on scaling-up and commercialization of CO2 electrolysis to Formic Acid. Coval has already an operational reactor on lab scale with promising performance, a conversion efficiency up to 90%. Although the reaction kinetics are limited by a poor distribution of reactants on the electrode surface. Previous research by Jos van der Maas showed a highly uneven flow distribution in the cell reactor [7]. Gas bubbles are formed inside the reactor, which likely limit the reaction. Consequences of this poor distribution of reactants and these bubbles are a lower energy efficiency and higher electrical resistance. The main question of this thesis is: How can the current knowledge of electrolysers be applied to improve the Coval electrolyser design regarding flow distribution and mitigation of the impact of dissolved gas production? Experiments were performed to gain knowledge about the bubble behaviour in the Coval electrolyser. Computational Fluid Dynamics (CFD) was used to screen design ideas on liquid distribution. Promising designs were assessed in a flow and gas bubble visualisation experimental setup, in which also the bubble behaviour was investigate, Mechanical Engineering | Energy, Flow and Process Technology

An experimental study to assess the accuracy of wire-mesh sensors in dependence of bubble sizes and flow rates has been performed in a 50 mm x 50 mm transparent rectangular channel. The liquid superficial velocities were ranging from 0 m/s up to 0.62 m/s with the obtained bubble size ranging from 3 mm to 7 mm. A single wire-mesh sensor with 16 x 16 electrode wires was used with a temporal and spatial resolution of 10 kHz and 3.1 mm (lateral distance between two wires), respectively. Single bubbles with known bubble size, subsequently called reference bubble size, was injected into the test section via bubble injector approx. 25 cm upstream of the wire-mesh sensor. The bubble size measurement by using wire-mesh sensor cannot be obtained directly since it requires the information of bubble velocity which is not available only by installing a single sensor. Therefore, a stereoscopic observation was conducted to obtain the bubble velocity by tracking the successive frames as well as to study the intrusiveness of the sensor. This configuration gave an advantage that the registered bubble will be assigned with its real approach velocity and a better agreement is expected. As the result, a direct comparison of all individual bubbles with the reference bubble size showed an agreement within ±10%. However, a deceleration effect was found for low superficial and observed to disappear as the liquid superficial velocity increased then vanish at observed JL = 0.62 m/s.

An experimental study to assess the accuracy of wire-mesh sensor in dependence of bubble sizes and flow rates has been performed in a 50 mm x 50 mm transparent rectangular channel. The liquid superficial velocities were ranging from 0 m/s up to 0.62 m/s with the obtained bubble size ranging from 3 mm – 7 mm. A single wire-mesh sensor with 16x16 electrode wires was used with a temporal and spatial resolution of 10 kHz and 3.125 cm, respectively. A single bubble with known bubble size or termed as the reference bubble size was injected through the test section via bubble injector approx. 25 cm upstream of the wire-mesh sensor. The bubble size measurement by using wire-mesh sensor cannot be obtained directly since it requires the information of bubble velocity which is not available only by installing a single sensor. Therefore, a stereoscopic observation was conducted to obtain the bubble velocity by tracking the successive frames as well as to study the intrusiveness of the sensor. This configuration gave an advantage that the registered bubble will be assigned with its own velocity and a better agreement is expected. As the result, a direct comparison of all individual bubble with the reference bubble size showed an agreement within ±10%. However, the deceleration effect was found for low liquid superficial and observed to disappear as the liquid superficial velocity increased then vanish at observed J L =0.62 m/s.

An experimental study to assess the accuracy of wire-mesh sensor in dependence of bubble sizes and flow rates has been performed in a 50 mm x 50 mm transparent rectangular channel. The liquid superficial velocities were ranging from 0 m/s up to 0.62 m/s with the obtained bubble size ranging from 3 mm – 7 mm. A single wire-mesh sensor with 16x16 electrode wires was used with a temporal and spatial resolution of 10 kHz and 3.125 cm, respectively. A single bubble with known bubble size or termed as the reference bubble size was injected through the test section via bubble injector approx. 25 cm upstream of the wire-mesh sensor. The bubble size measurement by using wire-mesh sensor cannot be obtained directly since it requires the information of bubble velocity which is not available only by installing a single sensor. Therefore, a stereoscopic observation was conducted to obtain the bubble velocity by tracking the successive frames as well as to study the intrusiveness of the sensor. This configuration gave an advantage that the registered bubble will be assigned with its own velocity and a better agreement is expected. As the result, a direct comparison of all individual bubble with the reference bubble size showed an agreement within ±10%. However, the deceleration effect was found for low liquid superficial and observed to disappear as the liquid superficial velocity increased then vanish at observed J L =0.62 m/s.

Ein gegebener schneller Röntgentomograph mit zwei parallelen Messebenen dient zur örtlich aufgelösten Messung von Geschwindigkeiten. Seine Aufgabe soll ohne technischen Zusatzaufwand auf zeitlich aufgelöste Messungen ausgedehnt werden. Der Ebenenabstand ist dafür aber zu groß. Deshalb wird zusätzlich eine indirekte Messebene definiert, indem diejenige Strahlung ausgenutzt wird, die sich im Tomographen zwischen den regulären Ebenen ausbreitet. Die neue Messebene hat zu einer der regulären Ebenen einen genügend kleinen Abstand. Wie damit gemessen werden kann, verdeutlicht ein praktisches Beispiel. A given fast X-ray tomograph with two parallel measuring planes is used for spatially resolved measurements of flow velocities by design. Now it is to be extended to time-resolved measurements avoiding any additional technical effort. But the spacing between the planes is too big. Thus, an additional indirect measuring plane is defined utilizing radiation which propagates between the regular planes during the tomographic scan. This indirect plane is close enough to one of the regular planes. A practical example illustrates the mode of measurement using the new method.

In this study we investigate the flow structure in a liquid metal cylinder while a bubble driven recirculation flow is superposed with a rotating magnetic field (RMF). The flow structure and the bubble detection were measured by means of the ultrasound Doppler velocimetry (UDV) and ultrasound transit-time technique (UTTT). The measurements revealed the potential of the RMF to control both the amplitude of the meridional flow and the bubble distribution and to provide an effective mixing in the whole fluid volume. Various periodic flow patterns were observed in a certain parameter range with respect to variations of the magnetic field strength and the gas flow rate.

In this study we investigate the flow structure in a liquid metal cylinder while a bubble driven recirculation flow is superposed with a rotating magnetic field (RMF). The flow structure and the bubble detection were measured by means of the ultrasound Doppler velocimetry (UDV) and ultrasound transit-time technique (UTTT). The measurements revealed the potential of the RMF to control both the amplitude of the meridional flow and the bubble distribution and to provide an effective mixing in the whole fluid volume. Various periodic flow patterns were observed in a certain parameter range with respect to variations of the magnetic field strength and the gas flow rate.

In this study we investigate the flow structure in a liquid metal cylinder while a bubble driven recirculation flow is superposed with a rotating magnetic field (RMF). The measurements revealed the potential of the RMF to control both the amplitude of the meridional flow and the bubble distribution and to provide an effective mixing in the whole fluid volume. Various periodic flow patterns were observed in a certain parameter range with respect to variations of the magnetic field strength and the gas flow rate.

In this study we investigate the flow structure in a liquid metal cylinder while a bubble driven recirculation flow is superposed with a rotating magnetic field (RMF). The measurements revealed the potential of the RMF to control both the amplitude of the meridional flow and the bubble distribution and to provide an effective mixing in the whole fluid volume. Various periodic flow patterns were observed in a certain parameter range with respect to variations of the magnetic field strength and the gas flow rate.

In this study we investigate the flow structure in a liquid metal cylinder while a bubble driven recirculation flow is superposed with a rotating magnetic field (RMF). The flow structure and the bubble detection were measured by means of the ultrasound Doppler velocimetry (UDV) and ultrasound transit-time technique (UTTT). The measurements revealed the potential of the RMF to control both the amplitude of the meridional flow and the bubble distribution and to provide an effective mixing in the whole fluid volume. Various periodic flow patterns were observed in a certain parameter range with respect to variations of the magnetic field strength and the gas flow rate.

In this study we investigate the flow structure in a liquid metal cylinder while a bubble driven recirculation flow is superposed with a rotating magnetic field (RMF). The measurements revealed the potential of the RMF to control both the amplitude of the meridional flow and the bubble distribution and to provide an effective mixing in the whole fluid volume. Various periodic flow patterns were observed in a certain parameter range with respect to variations of the magnetic field strength and the gas flow rate.

In this study we investigate the flow structure in a liquid metal cylinder while a bubble driven recirculation flow is superposed with a rotating magnetic field (RMF). The flow structure and the bubble detection were measured by means of the ultrasound Doppler velocimetry (UDV) and ultrasound transit-time technique (UTTT). The measurements revealed the potential of the RMF to control both the amplitude of the meridional flow and the bubble distribution and to provide an effective mixing in the whole fluid volume. Various periodic flow patterns were observed in a certain parameter range with respect to variations of the magnetic field strength and the gas flow rate.

Bubble condensation plays an important role e.g. in sub-cooled boiling or steam injection into pools. Since the condensation rate is proportional to the interfacial area density, bubble size distributions have to be considered in an adequate modelling of the condensation process. To develop and validate closure models for CFD codes new experimental data are required. The effect of bubble sizes is clearly shown in experimental investigations done at the TOPFLOW facility of FZD. Steam bubbles are injected into a sub-cooled upward pipe flow via orifices in the pipe wall located at different distances from measuring plane. 1 mm and 4 mm injection orifices are used to vary the initial bubble size distribution. The variation of the distance between the location of the gas injection and the measuring plane allows investigating the evolution of the flow along the pipe. Measurements are done using wire-mesh sensors and thermocouples. Condensation is clearly faster in case of the injection via the smaller orifices, i.e. in case of smaller bubble sizes. Data on averaged void fraction, radial gas volume fraction profiles, profiles of the gas velocity and bubble size distributions in dependency of the L/D ratio are presented in the paper.

Bubble condensation plays an important role e.g. in sub-cooled boiling or steam injection into pools. Since the condensation rate is proportional to the interfacial area density, bubble size distributions have to be considered in an adequate modelling of the condensation process. To develop and validate closure models for CFD codes new experimental data are required. The effect of bubble sizes is clearly shown in experimental investigations done at the TOPFLOW facility of FZD. Steam bubbles are injected into a sub-cooled upward pipe flow via orifices in the pipe wall located at different distances from measuring plane. 1 mm and 4 mm injection orifices are used to vary the initial bubble size distribution. The variation of the distance between the location of the gas injection and the measuring plane allows investigating the evolution of the flow along the pipe. Measurements are done using wire-mesh sensors and thermocouples. Condensation is clearly faster in case of the injection via the smaller orifices, i.e. in case of smaller bubble sizes. Data on averaged void fraction, radial gas volume fraction profiles, profiles of the gas velocity and bubble size distributions in dependency of the L/D ratio are presented in the paper.

Bubble condensation plays an important role e.g. in sub-cooled boiling or steam injection into pools. Since the condensation rate is proportional to the interfacial area density, bubble size distributions have to be considered in an adequate modelling of the condensation process. To develop and validate closure models for CFD codes new experimental data are required. The effect of bubble sizes is clearly shown in experimental investigations done at the TOPFLOW facility of FZD. Steam bubbles are injected into a sub-cooled upward pipe flow via orifices in the pipe wall located at different distances from measuring plane. 1 mm and 4 mm injection orifices are used to vary the initial bubble size distribution. The variation of the distance between the location of the gas injection and the measuring plane allows investigating the evolution of the flow along the pipe. Measurements are done using wire-mesh sensors and thermocouples. Condensation is clearly faster in case of the injection via the smaller orifices, i.e. in case of smaller bubble sizes. Data on averaged void fraction, radial gas volume fraction profiles, profiles of the gas velocity and bubble size distributions in dependency of the L/D ratio are presented in the paper.

Bubble condensation plays an important role e.g. in sub-cooled boiling or steam injection into pools. Since the condensation rate is proportional to the interfacial area density, bubble size distributions have to be considered in an adequate modelling of the condensation process. To develop and validate closure models for CFD codes new experimental data are required. The effect of bubble sizes is clearly shown in experimental investigations done at the TOPFLOW facility of FZD. Steam bubbles are injected into a sub-cooled upward pipe flow via orifices in the pipe wall located at different distances from measuring plane. 1 mm and 4 mm injection orifices are used to vary the initial bubble size distribution. The variation of the distance between the location of the gas injection and the measuring plane allows investigating the evolution of the flow along the pipe. Measurements are done using wire-mesh sensors and thermocouples. Condensation is clearly faster in case of the injection via the smaller orifices, i.e. in case of smaller bubble sizes. Data on averaged void fraction, radial gas volume fraction profiles, profiles of the gas velocity and bubble size distributions in dependency of the L/D ratio are presented in the paper.

Measurements of the cross sectional distribution of gas fraction and bubble size distributions were conducted in a vertical pipe with an inner diameter of 51.2 mm and a length of about 3 m for air/water bubbly and slug flow. The use of a wire-mesh sensor allows a high resolution of the gas fraction data in space as well as in time. From these data time averaged values for the two-dimensional gas fraction profiles decomposed according to a large number of bubble size classes were calculated. This allows to extract data for the radial gas fraction profiles for a given range of bubble sizes as well as data for local bubble size distributions. The structure of the flow is characterized by these data. The measurements were done for up to 10 different inlet lengths and for about 100 combinations of gas and liquid volume flow rates. The data are very useful for the development and validation of meso-scale models for the forces acting on a bubble in a shear field of the liquid flow and models for bubble coalescence and break-up. Such models are necessary for the qualification of CFD codes for the simulation of bubbly flows.

A comparison between ultra-fast X-ray CT and a wire-mesh sensor is presented. The measurements were carried out in a vertical pipe of 42 mm inner diameter, which was supplied with an air-water mixture. Both gas and liquid superficial velocities were varied. The X-ray CT delivered 263 frames per second, while the wire-mesh sensor was operated at a frequency four times higher. Two different gas injectors were used: 4 orifices of 5 mm diameter for creating large bubbles and gas plugs and a sintered plate with a pore size of 100 µm for generating a bubbly flow. It was found that the wire-mesh sensor has a significantly higher resolution than the X-ray CT. Small bubbles, which are clearly shown by the wire-mesh sensor, cannot be found in the CT images, because they cross the measuring plane before a complete scan can be performed. This causes artifacts in the reconstructed images, instead. Furthermore, there are large deviations between the quantitative information contained in the reconstructed tomographic 2D distributions and the gas fractions measured by the sensor, while the agreement is very good, when the gas fraction is obtained by a direct evaluation of the X-ray attenuation along the available through-transmission chords of the tomography setup. This shows that there are still potentials for an improvement of the image reconstruction method. Concerning the wire-mesh sensor it was found, that the gas fraction inside large bubbles is slightly underestimated. Furthermore, a significant distortion of large Taylor bubbles by the sensor was found for small liquid velocities up to 0.24 m/s. This effect vanished with growing superficial water velocity.

A two-phase flow in a rectangular bubble column of 100×20 mm cross-section and 1.5 mm height was studied using a high-speed video system. Series of images were taken at different elevations at a frequency of 500 Hz. The images were processed using a bubble recognition algorithm. In such a way, an individual bubble in the gas swarm could be tracked. The time-averaged velocity profiles and the turbulent diffusion coefficients were derived as a function of the superficial gas velocity. The lateral displacement of bubbles travelling over a certain vertical distance was transformed into a probability density distribution in order to measure the turbulent diffusion coefficient of the gaseous phase. The shape of the distributions obtained was found to fit well to the Gaussian standard distribution. The dispersion coefficients were observed to grow proportionally to the square root of the vertical distance. The diffusion coefficients were calculated from the proportionality factor and were compared with some correlations published in the literature. The experiments were performed for superficial gas velocities ranging from 1 to 6 mm/s. The bubbles were generated either by a porous sparger or a set of capillaries placed at the bottom of the column. The measurements were taken at different heights between 1 and 1.2 m where the bubble cloud was occupying the entire cross-section.

On the basis of detailed experimental data obtained for stationary bubbly flow in vertical pipes with an inner diameter of 51.2 mm and 194.1 mm, analytical investigations on scaling effects were made. Because of the interaction between the phases the scaling behavior is very complex in case of two phase flow. Similarity can only be achieved regarding selected parameters. Thus the modeling of scaling effects has to be based on local models for the phase interaction. A simplified model, introduced earlier, is used for the validation of such models by consideration of scaling effects. Because of the strong influence of the bubble size distribution on the flow, the model considers a number of bubble classes. Models for the non-drag forces acting on bubbles were validated for the small pipe and afterwards used for the prediction of radial gas volume profiles in the large pipe. The comparison with measured profiles shows that there is a generality of these models. Even more complex is the situation regarding the development of the flow along the pipe. Here bubble coalescence and break-up are important. There is still a need for an improvement of these models.

On the basis of detailed experimental data obtained for stationary bubbly flow in vertical pipes with an inner diameter of 51.2 mm and 194.1 mm, analytical investigations on scaling effects were made. Because of the interaction between the phases the scaling behavior is very complex in case of two phase flow. Similarity can only be achieved regarding selected parameters. Thus the modeling of scaling effects has to be based on local models for the phase interaction. A simplified model, introduced earlier, is used for the validation of such models by consideration of scaling effects. Because of the strong influence of the bubble size distribution on the flow, the model considers a number of bubble classes. Models for the non-drag forces acting on bubbles were validated for the small pipe and afterwards used for the prediction of radial gas volume profiles in the large pipe. The comparison with measured profiles shows that there is a generality of these models. Even more complex is the situation regarding the development of the flow along the pipe. Here bubble coalescence and break-up are important. There is still a need for an improvement of these models.

On the basis of detailed experimental data obtained for stationary bubbly flow in vertical pipes with an inner diameter of 51.2 mm and 194.1 mm, analytical investigations on scaling effects were made. Because of the interaction between the phases the scaling behavior is very complex in case of two phase flow. Similarity can only be achieved regarding selected parameters. Thus the modeling of scaling effects has to be based on local models for the phase interaction. A simplified model, introduced earlier, is used for the validation of such models by consideration of scaling effects. Because of the strong influence of the bubble size distribution on the flow, the model considers a number of bubble classes. Models for the non-drag forces acting on bubbles were validated for the small pipe and afterwards used for the prediction of radial gas volume profiles in the large pipe. The comparison with measured profiles shows that there is a generality of these models. Even more complex is the situation regarding the development of the flow along the pipe. Here bubble coalescence and break-up are important. There is still a need for an improvement of these models.

On the basis of detailed experimental data obtained for stationary bubbly flow in vertical pipes with an inner diameter of 51.2 mm and 194.1 mm, analytical investigations on scaling effects were made. Because of the interaction between the phases the scaling behavior is very complex in case of two phase flow. Similarity can only be achieved regarding selected parameters. Thus the modeling of scaling effects has to be based on local models for the phase interaction. A simplified model, introduced earlier, is used for the validation of such models by consideration of scaling effects. Because of the strong influence of the bubble size distribution on the flow, the model considers a number of bubble classes. Models for the non-drag forces acting on bubbles were validated for the small pipe and afterwards used for the prediction of radial gas volume profiles in the large pipe. The comparison with measured profiles shows that there is a generality of these models. Even more complex is the situation regarding the development of the flow along the pipe. Here bubble coalescence and break-up are important. There is still a need for an improvement of these models.

To qualify CFD codes for two-phase flows, they have to be equipped with constitutive models standing for the interaction between the gaseous and the liquid phases. In case of bubble flow this particularly concerns the forces acting on the bubbles and bubble coalescence and break-up. Information on the local structure of the flow is also required by 1D thermal-hydraulic codes. Gas-liquid flow in vertical pipes is a very good object for studying the corresponding phenomena. Here, the bubbles move under clear boundary conditions, resulting in a shear field of nearly constant structure where the bubbles rise for a comparatively long time. The evolution of the flow within the pipe depends on a very complex interaction between bubble forces and bubble coalescence and break-up. E.g. the Lift-force, which strongly influences the radial distribution of the bubbles, changes its sign depending on the bubble diameter. Basing on extensive experimental data with a high resolution in space and time the applicability and the limits for the simulation of bubble flow with current CFX-codes are demonstrated, using the simulation of vertical pipe flow with CFX-4 as an example. Using a simplified model, parametric studies can be conducted. They give an indication for necessary improvements of the codes. Finally a possible way for the improvement of the CFD-codes is shown.

The new TOPFLOW facility of the Forschungszentrum Rossendorf allows investigations of two-phase flow phenomena in vertical pipes with an inner diameter up to 194 mm (DN200) and a length up to 8.5 m. The maximum water mass flow of 50 kg/s equals to a superficial velocity of 1.7 m/s in such a pipe, while the maximum air flow rate of 900 m3/h corresponds to a superficial velocity of 8 m/s. For the measurements presented here, a wire-mesh sensor with 64*64 measuring points was installed. It corresponds to a lateral resolution of 3 mm. The senor delivers instantaneous void fraction distributions over the entire cross section with a time resolution of 2500 frames per second, which can be used for fast flow visualisation as well as to obtain averaged void fraction profiles and bubble size distributions. Earlier, similar experiments were carried out at a 51.2 mm pipe. In this case, sensors with 16x16 and 24x24 points were applied. A comparison of the data obtained for the two diameters allows to identify the effects of scaling on void fraction profiles, bubbles size distributions and the flow patterns. In the small pipe, the increase of the air flow rate leads to a transition from bubbly to slug flow. In the bubble size distributions a second peak corresponding to the class of large Taylor bubbles respectively gas plugs was found in the slug flow region. In the large pipe at identical superficial velocities a similar behaviour was found, though the large bubble fraction has a significantly bigger mean diameter, the peak is less high but wider. This reflects the fact that large bubbles move more freely than in the small pipe. The transition from a mono-modal to a bimodal bubble size distribution starts in both pipes, if bubbles with an equivalent diameter larger 1/3 of the pipe diameter occur. Due to the less pronounced confining action of the pipe walls, the bubbles show much more deformations. Their shape can be complicated and far from an ideal Taylor bubble. The small bu

The new TOPFLOW facility of the Forschungszentrum Rossendorf allows investigations of two-phase flow phenomena in vertical pipes with an inner diameter up to 194 mm (DN200) and a length up to 8.5 m. The maximum water mass flow of 50 kg/s equals to a superficial velocity of 1.7 m/s in such a pipe, while the maximum air flow rate of 900 m3/h corresponds to a superficial velocity of 8 m/s. For the measurements presented here, a wire-mesh sensor with 64*64 measuring points was installed. It corresponds to a lateral resolution of 3 mm. The senor delivers instantaneous void fraction distributions over the entire cross section with a time resolution of 2500 frames per second, which can be used for fast flow visualisation as well as to obtain averaged void fraction profiles and bubble size distributions. Earlier, similar experiments were carried out at a 51.2 mm pipe. In this case, sensors with 16x16 and 24x24 points were applied. A comparison of the data obtained for the two diameters allows to identify the effects of scaling on void fraction profiles, bubbles size distributions and the flow patterns. In the small pipe, the increase of the air flow rate leads to a transition from bubbly to slug flow. In the bubble size distributions a second peak corresponding to the class of large Taylor bubbles respectively gas plugs was found in the slug flow region. In the large pipe at identical superficial velocities a similar behaviour was found, though the large bubble fraction has a significantly bigger mean diameter, the peak is less high but wider. This reflects the fact that large bubbles move more freely than in the small pipe. The transition from a mono-modal to a bimodal bubble size distribution starts in both pipes, if bubbles with an equivalent diameter larger 1/3 of the pipe diameter occur. Due to the less pronounced confining action of the pipe walls, the bubbles show much more deformations. Their shape can be complicated and far from an ideal Taylor bubble. The small bu

To qualify CFD codes for two-phase flows, they have to be equipped with constitutive models standing for the interaction between the gaseous and the liquid phases. In case of bubble flow this particularly concerns the forces acting on the bubbles and bubble coalescence and break-up. Information on the local structure of the flow is also required by 1D thermal-hydraulic codes. Gas-liquid flow in vertical pipes is a very good object for studying the corresponding phenomena. Here, the bubbles move under clear boundary conditions, resulting in a shear field of nearly constant structure where the bubbles rise for a comparatively long time. The evolution of the flow within the pipe depends on a very complex interaction between bubble forces and bubble coalescence and break-up. E.g. the Lift-force, which strongly influences the radial distribution of the bubbles, changes its sign depending on the bubble diameter. Basing on extensive experimental data with a high resolution in space and time the applicability and the limits for the simulation of bubble flow with current CFX-codes are demonstrated, using the simulation of vertical pipe flow with CFX-4 as an example. Using a simplified model, parametric studies can be conducted. They give an indication for necessary improvements of the codes. Finally a possible way for the improvement of the CFD-codes is shown.

To qualify CFD codes for two-phase flows, they have to be equipped with constitutive models standing for the interaction between the gaseous and the liquid phases. In case of bubble flow this particularly concerns the forces acting on the bubbles and bubble coalescence and break-up. Information on the local structure of the flow is also required by 1D thermal-hydraulic codes. Gas-liquid flow in vertical pipes is a very good object for studying the corresponding phenomena. Here, the bubbles move under clear boundary conditions, resulting in a shear field of nearly constant structure where the bubbles rise for a comparatively long time. The evolution of the flow within the pipe depends on a very complex interaction between bubble forces and bubble coalescence and break-up. E.g. the Lift-force, which strongly influences the radial distribution of the bubbles, changes its sign depending on the bubble diameter. Basing on extensive experimental data with a high resolution in space and time the applicability and the limits for the simulation of bubble flow with current CFX-codes are demonstrated, using the simulation of vertical pipe flow with CFX-4 as an example. Using a simplified model, parametric studies can be conducted. They give an indication for necessary improvements of the codes. Finally a possible way for the improvement of the CFD-codes is shown.

To qualify CFD codes for two-phase flows, they have to be equipped with constitutive laws describing the interaction between the gaseous and the liquid phases. In the case of bubble flow this particularly concerns the forces acting on the bubbles and bubble coalescence and break-up. To obtain detailed experimental data, an electrode wire-mesh sensor was used, which enables the measurement of the phase distribution with a very high resolution in space and in time. Air-water flow at ambient conditions in a vertical pipe (51.2 mm inner diameter) is investigated to have well defined boundary conditions. Local bubble size distributions are calculated from the data. The measurements were done in different distances from the gas injection device. As a result the development of bubble size distributions as well as the development of the radial gas fraction profiles can be studied. It was found, that the bubble size distribution as well as local effects determine the transition from bubble flow to slug flow. The data are used for the development of a model, which predicts the development of the bubble size distribution and the transition from bubble flow to slug flow in case of stationary flow in a vertical pipe.

The present paper describes the concept of a fast scanning X-ray tomograph, the hardware development, and measurement results of gas-liquid two-phase flow in a vertical pipe. The device uses 18 pulsed X-ray sources activated in a successive order. In this way, a complete set of 18 independent projections of the object is obtained within 38 ms, i.e. the measuring rate is about 250 frames per second. Finally, to evaluate the measurement capability of the fast X-ray CT, a wire-mesh sensor was installed in the flow loop and both systems were operated for the same two-phase flow simultaneously. Comparison of the time series of the cross section averaged void fraction from both systems showed sufficient agreement for slug flow at large void fractions, while the fast CT underestimated the void fraction of bubbly flow especially in low void fraction range. For the wire-mesh sensor, coerced deformation of slug bubble interface was found. Further hardware improvement is in progress to achieve better resolution with the fast X-ray CT scanner.

CFD codes are more and more used for practical applications as the design and optimization of technical facilities, e.g. in process industry or in nuclear power plants. For most cases this limited to single phase flows. To qualify CFD codes for two-phase flows, they have to be equipped with constitutive laws describing the interaction between the gaseous and the liquid phases. In the case of bubble flow this particularly concerns the forces acting on the bubbles and bubble coalescence and break-up. To obtain detailed experimental data, an electrode wire-mesh sensor was used, which enables the measurement of the phase distribution with high reso-lution in space and in time. Air-water flow at ambient conditions in a vertical pipe (51.2 mm inner diameter) is investigated to have well defined boundary condi-tions. Local bubble size distributions are calculated from the data. The measure-ments were done in different distances from the gas injection device. As a result the development of bubble size distributions and the development of the radial gas fraction profiles can be studied. It was found, that the bubble size distribution as well as local effects determine the transition from bubble flow to slug flow. The data are used for the development of a model, which predicts the development of the bubble size distribution and the transition from bubble flow to slug flow in case of stationary flow in a vertical pipe.

Air-water flow at ambient conditions in a vertical pipe with an inner diameter of 51.2mm is investigated. An electrode wire-mesh sensor enables the measurement of the phase distribution with a very high resolution in space and in time. Local bubble size distributions are calculated from the data. The measurements were done in different distances from the gas injection device. As a result the development of bubble size distributions as well as the development of the radial gas fraction profiles can be studied. It was found, that the bubble size distribution as well as local effects determine the transition from bubble flow to slug flow. The data are used for the development of a model, which predicts the development of the bubble size distribution and the transition from bubble flow to slug flow in case of stationary flow in a vertical pipe.

To qualify CFD codes for two-phase flows, they have to be equipped with constitutive models standing for the interaction between the gaseous and the liquid phases. In case of bubble flow this particularly concerns the forces acting on the bubbles and bubble coalescence and break-up. Information on the local structure of the flow is also required by 1D thermal-hydraulic codes. Gas-liquid flow in vertical pipes is a very good object for studying the corresponding phenomena. Here, the bubbles move under clear boundary conditions, resulting in a shear field of nearly constant structure where the bubbles rise for a comparatively long time. The evolution of the flow within the pipe depends on a very complex interaction between bubble forces and bubble coalescence and break-up. E.g. the Lift-force, which strongly influences the radial distribution of the bubbles, changes its sign depending on the bubble diameter. Basing on extensive experimental data with a high resolution in space and time the applicability and the limits for the simulation of bubble flow with current CFX-codes are demonstrated, using the simulation of vertical pipe flow with CFX-4 as an example. Using a simplified model, parametric studies can be conducted. They give an indication for necessary improvements of the codes. Finally a possible way for the improvement of the CFD-codes is shown.

To qualify CFD codes for two-phase flows, they have to be equipped with constitutive laws describing the interaction between the gaseous and the liquid phases. In the case of bubble flow this particularly concerns the forces acting on the bubbles and bubble coalescence and break-up. To obtain detailed experimental data, an electrode wire-mesh sensor was used, which enables the measurement of the phase distribution with a very high resolution in space and in time. Air-water flow at ambient conditions in a vertical pipe (51.2 mm inner diameter) is investigated to have well defined boundary conditions. Local bubble size distributions are calculated from the data. The measurements were done in different distances from the gas injection device. As a result the development of bubble size distributions as well as the development of the radial gas fraction profiles can be studied. It was found, that the bubble size distribution as well as local effects determine the transition from bubble flow to slug flow. The data are used for the development of a model, which predicts the development of the bubble size distribution and the transition from bubble flow to slug flow in case of stationary flow in a vertical pipe.

To qualify CFD codes for two-phase flows, they have to be equipped with constitutive models standing for the interaction between the gaseous and the liquid phases. In case of bubble flow this particularly concerns the forces acting on the bubbles and bubble coalescence and break-up. Information on the local structure of the flow is also required by 1D thermal-hydraulic codes. Gas-liquid flow in vertical pipes is a very good object for studying the corresponding phenomena. Here, the bubbles move under clear boundary conditions, resulting in a shear field of nearly constant structure where the bubbles rise for a comparatively long time. The evolution of the flow within the pipe depends on a very complex interaction between bubble forces and bubble coalescence and break-up. E.g. the Lift-force, which strongly influences the radial distribution of the bubbles, changes its sign depending on the bubble diameter. Basing on extensive experimental data with a high resolution in space and time the applicability and the limits for the simulation of bubble flow with current CFX-codes are demonstrated, using the simulation of vertical pipe flow with CFX-4 as an example. Using a simplified model, parametric studies can be conducted. They give an indication for necessary improvements of the codes. Finally a possible way for the improvement of the CFD-codes is shown.

The new TOPFLOW facility of the Forschungszentrum Rossendorf allows investigations of two-phase flow phenomena in vertical pipes with an inner diameter up to 194 mm (DN200) and a length up to 8.5 m. The maximum water mass flow of 50 kg/s equals to a superficial velocity of 1.7 m/s in such a pipe, while the maximum air flow rate of 900 m3/h corresponds to a superficial velocity of 8 m/s. For the measurements presented here, a wire-mesh sensor with 64*64 measuring points was installed. It corresponds to a lateral resolution of 3 mm. The senor delivers instantaneous void fraction distributions over the entire cross section with a time resolution of 2500 frames per second, which can be used for fast flow visualisation as well as to obtain averaged void fraction profiles and bubble size distributions. Earlier, similar experiments were carried out at a 51.2 mm pipe. In this case, sensors with 16x16 and 24x24 points were applied. A comparison of the data obtained for the two diameters allows to identify the effects of scaling on void fraction profiles, bubbles size distributions and the flow patterns. In the small pipe, the increase of the air flow rate leads to a transition from bubbly to slug flow. In the bubble size distributions a second peak corresponding to the class of large Taylor bubbles respectively gas plugs was found in the slug flow region. In the large pipe at identical superficial velocities a similar behaviour was found, though the large bubble fraction has a significantly bigger mean diameter, the peak is less high but wider. This reflects the fact that large bubbles move more freely than in the small pipe. The transition from a mono-modal to a bimodal bubble size distribution starts in both pipes, if bubbles with an equivalent diameter larger 1/3 of the pipe diameter occur. Due to the less pronounced confining action of the pipe walls, the bubbles show much more deformations. Their shape can be complicated and far from an ideal Taylor bubble. The small bu