Relevant bibliographies by topics / Interfacial area

Academic literature on the topic 'Interfacial area'

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Published: 4 June 2021
Last updated: 7 February 2022

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Journal articles on the topic "Interfacial area"

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Ishii, Mamoru. "INTERFACIAL AREA MODELLING." Multiphase Science and Technology 3, no. 1-4 (1987): 31–61. http://dx.doi.org/10.1615/multscientechn.v3.i1-4.20.

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Millies, Marco, and Dieter Mewes. "Interfacial area density in bubbly flow." Chemical Engineering and Processing: Process Intensification 38, no. 4-6 (September 1999): 307–19. http://dx.doi.org/10.1016/s0255-2701(99)00022-7.

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Kataoka, Isao, and Akimi Serizawa. "Interfacial area concentration in bubbly flow." Nuclear Engineering and Design 120, no. 2-3 (June 1990): 163–80. http://dx.doi.org/10.1016/0029-5493(90)90370-d.

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Yarbro, Stephen L., and Richard L. Long. "Using a New Interfacial Area Transport Equation to Predict Interfacial Area in Co-current Jet Mixers." Canadian Journal of Chemical Engineering 80, no. 4 (May 19, 2008): 1–10. http://dx.doi.org/10.1002/cjce.5450800416.

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Tamhankar, Y., B. King, J. Whiteley, K. McCarley, T. Cai, M. Resetarits, and C. Aichele. "Interfacial area measurements and surface area quantification for spray absorption." Separation and Purification Technology 156 (December 2015): 311–20. http://dx.doi.org/10.1016/j.seppur.2015.10.017.

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Godinez-Brizuela, Omar E., Nikolaos K. Karadimitriou, Vahid Joekar-Niasar, Craig A. Shore, and Mart Oostrom. "Role of corner interfacial area in uniqueness of capillary pressure-saturation- interfacial area relation under transient conditions." Advances in Water Resources 107 (September 2017): 10–21. http://dx.doi.org/10.1016/j.advwatres.2017.06.007.

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Li, Muzi, Yuanzheng Zhai, and Li Wan. "Measurement of NAPL–water interfacial areas and mass transfer rates in two-dimensional flow cell." Water Science and Technology 74, no. 9 (August 19, 2016): 2145–51. http://dx.doi.org/10.2166/wst.2016.397.

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The nonaqueous-phase liquid (NAPL)–water interfacial area and the mass transfer rate across the NAPL and water interface are often key factors in in situ groundwater pollution treatment. In this study, the NAPL–water interfacial area and residual NAPL saturation were measured using interfacial and partitioning tracer tests in a two-dimensional flow cell. The results were compared with previous column and field experiment results. In addition, the mass transfer rates at various NAPL–water interfacial areas were investigated. Fe2+-activated persulfate was used for in situ chemical oxidation remediation to remove NAPL gradually. The results showed that the reduction of NAPL–water interfacial areas as well as NAPL saturation by chemical oxidation caused a linear decrease in the interphase mass transfer rates (R2 = 0.97), revealing the relationship between mass transfer rates and interfacial areas in a two-dimensional system. The NAPL oxidation rates decreased with the reduction of interfacial areas, owing to the control of NAPL mass transfer into the aqueous phase.
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Machnicki, Catherine E., Fanfan Fu, Lin Jing, Po-Yen Chen, and Ian Y. Wong. "Mechanochemical engineering of 2D materials for multiscale biointerfaces." Journal of Materials Chemistry B 7, no. 41 (2019): 6293–309. http://dx.doi.org/10.1039/c9tb01006h.

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Atomically thin nanomaterials that are wrinkled or crumpled represent a unique paradigm for interfacing with biological systems due to their mechanical flexibility, exceptional interfacial area, and ease of chemical functionalization.
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Ishii, M., S. S. Paranjape, S. Kim, and X. Sun. "Interfacial structures and interfacial area transport in downward two-phase bubbly flow." International Journal of Multiphase Flow 30, no. 7-8 (July 2004): 779–801. http://dx.doi.org/10.1016/j.ijmultiphaseflow.2004.04.009.

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Bartel, Michael D., Mamoru Ishii, Takuyki Masukawa, Ye Mi, and Rong Situ. "Interfacial area measurements in subcooled flow boiling." Nuclear Engineering and Design 210, no. 1-3 (December 2001): 135–55. http://dx.doi.org/10.1016/s0029-5493(01)00415-0.

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Dissertations / Theses on the topic "Interfacial area"

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Spooner, Stephen. "Quantifying the transient interfacial area during slag-metal reactions." Thesis, University of Warwick, 2017. http://wrap.warwick.ac.uk/93620/.

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The steel industry is facing significant competition on a global scale due to the drive for light-weighting and cheaper more sustainable construction. Not aided by oversupply in geographic sectors of the industry, there is significant competition within the slowly shrinking sector. The recent growth in developing countries through installation of modern plant technology has led to the reduction in unique selling points for mature steelmaking locations. As such, to compete with the equalling product capability and innate cheaper production costs within developing areas the industries in Europe and North America require significant improvements in productivity and agile resource management. To date the basic oxygen furnace has been somewhat treated as a black box within industry, where only control parameters are monitored, not the fundamental mechanisms within the converter. Studies over the past 30 years have shown the basic oxygen furnace is unable to attain the thermodynamic minimum phosphorus content within the output liquid steel. Coupled with the need to drive down resource cost, with a potential for high content phosphorus ores the internal dynamic system of the basic oxygen furnace requires more rigorous understanding. With the aid of in-situ sampling of a pilot scale basic oxygen furnace, and laboratory studies of individual metal droplets suspended in a slag medium (known to be a key driving environment for impurity removal) the present project aims to provide insight into the transient interfacial area between slag and liquid metal through basic oxygen steelmaking processing. Initially the macroscopic dynamics including the amount of metal suspended in the gas/slag/metal emulsion, the period of time it is suspended for, and the speed at which it moves, is investigated. It was found that these parameters vary greatly through the blow, with a normal peak in residence times near the beginning of the blow and a dramatic increase in metal circulation rates at the end of the blow, when foaming is reduced or collapsed. Further to this, a method of interrogating the size of metal droplets within the slag layer using X-ray computed tomography is introduced. The study then progresses into the microscopic environments that individual droplets are subjected to during steel processing. Initially the cause of spontaneous emulsification in basic oxygen furnace type slags is investigated through high temperature-confocal scanning laser microscopy/X-ray computed tomography led experimentation, with the addition of null experiments conducted to rationalize the experimental technique. It was found that the flux of oxygen across the interface was the cause and thus the confirmation of material transfer across the interface being the driving force. Furthermore the physical pathway of emulsification is interrogated and quantified, with in-situ observation of spontaneous emulsification in the high temperature-confocal scanning laser microscope enabled through use of optically transparent slags. The life cycle of perturbation growth, necking and budding is observed and quantified through high-resolution X-ray computed tomography. In addition a phase-field model is developed to interrogate slag/metal systems in 2D and 3D variations, giving rise to the ability to track the cause of emulsification and to predict its occurrence. Finally the project progresses with the in-situ investigation of spontaneous emulsification as a function of initial metal composition. The behaviour of droplet spontaneous emulsification is seen to reduce in severity and subsequently to decline into a non-emulsifying regime below a critical level. Free energy calculations coupled with a measure of the global interfacial tension increase give quantifiable reasoning as to the behaviour seen.
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El, Ouni Asma. "Measuring Air-Water Interfacial Area in Unsaturated Porous Media Using the Interfacial Partitioning Tracer Test Method." Thesis, The University of Arizona, 2013. http://hdl.handle.net/10150/297008.

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Interfacial partitioning tracer tests (IPTT) are one method available for measuring air-water interfacial area (A(ia)).This study used the standard approach comprising tracer injection under steady unsaturated-flow conditions with a uniform water-saturation distribution within the column. Sodium dodecylbezene sulfonate (SDBS) and pentafluorobenzoic acid (PFBA) were used as the partitioning and nonreactive tracers, respectively. Three types of porous media were used for the study: a sandy soil, a well-sorted sand, and glass beads. Initial water saturations, S(w), were approximately 80%, 80%, and 26 % for the soil, sand, and glass beads, respectively. Water saturation was monitored gravimetrically during the experiments. The maximum interfacial areas (A(ia)/(1-S(w))) calculated from the results of the experiments are compared among the three porous media used in this work, and compared to previous air-water interfacial area studies.
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Wang, Xia. "Simulations of Two-phase Flows Using Interfacial Area Transport Equation." The Ohio State University, 2010. http://rave.ohiolink.edu/etdc/view?acc_num=osu1282066341.

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Rajapakse, Achula, and s9508428@student rmit edu au. "Drop size distribution and interfacial area in reactive liquid-liquid dispersion." RMIT University. Civil Environmental and Chemical Engineering, 2007. http://adt.lib.rmit.edu.au/adt/public/adt-VIT20080717.163619.

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Emulsion explosives have become the preferred choice as blasting agents for numerous industries including mining, agriculture, and construction. One of the most important components in such an emulsion is an emulsifier, which controls the emulsification properties of the explosive. The present study involves the production of one such emulsifier, which is produced by reacting two immiscible liquids, PIBSA (polyisobutylene succinic anhydride) and MEA (monoethanolamine). The study examines the effect of design variable such as the impeller speed, impeller type and the dispersed phase volume fraction on interfacial area. Experiments were carried out in a 0.15 m diameter fully baffled stirred tank using a 6-bladed Rushton turbine impeller and a marine propeller. Drop size was determined using a microscope with a video camera and image processing system. The transient concentration of PIBSA was determined using FTIR analysis and used to estimate the volume fraction of the dispersed phase (ƒÖ). The effective interfacial area was calculated using the Sauter mean drop diameter, d32 and ƒÖ. Impeller speeds ranging from 150 to 600 rpm and dispersed phase volume fractions, ƒÖ ranging from 0.01 to 0.028 were examined in the experimental study. It was found that that the evolution of Sauter mean drop diameter, d32 has four different trends depending on ƒÖ and impeller speed. At high impeller speeds and high ƒÖ, d32 values decrease initially and reach constant values after a long period of time. This trend is consistent with the findings in previous investigations. Under certain operating conditions, d32 values increase initially with stirring time to reach a maximum value and then decrease to reach a steady state value. The presence of these trends has been attributed to the effect of changing physical properties of the system as a result of chemical reaction. Results indicate that, in general, Sauter mean drop diameter d32 decreases with an increase in agitation intensity. However a decrease in the dispersed phase volume fraction is found to increase d32. These trends are found to be the same for both impeller types studied. Comparing the drop size results produced by the two impellers, it appears that low-power number propeller produces s ignificantly smaller drops than the Rushton turbine. It was found that the concentrations of reactants decrease with time for all impeller speeds thereby leading to a decrease in interfacial area with the progress of the reaction. Interfacial area values obtained at higher impeller speeds are found to be lower in spite of lower d32 values at these speeds. Also, these values decrease with time and become zero in a shorter duration indicating the rapid depletion of MEA. The interfacial area values obtained with the propeller at a given impeller speed are lower as compared to those for Rushton turbine. They also decrease and become zero in a shorter duration as compared to those for Rushton turbine suggesting propeller¡¦s performance is better in enhancing the reaction rate.
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Peng, Sheng. "Characterizing air-water interfacial area in variably saturated sandy porous media." Diss., The University of Arizona, 2004. http://hdl.handle.net/10150/280732.

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Air-water interface plays an important role in the transport of many contaminants in the vadose zone. It is also a limiting factor for many processes involve mass or energy transfer between air and water phases in vadose zone. In this research, the gas-phase partitioning tracer method was used to measure air-water interfacial area for eight porous media. The experimental results were used to investigate the influencing factors of the magnitude of air-water interfacial area and the relationship between the air-water interfacial area and water saturation, and capillary pressure. The porous media comprised a series of sands with narrow particle-size ranges, a sand with a wider particle-size distribution, a sandy soil, and a loamy sandy soil. The measurement range was extended to very low water contents in an attempt to determine upper limits for air-water interfacial areas. The measured values were compared to the normalized surface areas of the porous media. The results of the experiments showed that the magnitude of the air-water interfacial areas increased with decreasing water saturation, and approached that of the normalized surface areas. Generally, air-water interfacial areas were larger for media with larger specific surface areas. The change in air-water interfacial area with changing water saturation was less near saturated water contents and greater at smaller values. In addition, the change was greater for the poorly-sorted media than the well-sorted media. An empirical model was developed to describe the observed relationship between air-water interfacial area and water saturation. The coefficients of the model were found to correlate to the porous-medium uniformity coefficient. With this model and associated correlations, only bulk density, specific surface area, and uniformity coefficient are needed to estimate air-water interfacial area for a given water saturation. The model was shown to provide a reasonable description of a literature data set. Potential relationships between air-water interfacial area and capillary pressure under higher water-content conditions are investigated for unsaturated sandy porous media. A conceptual relationship between air-water interfacial area and capillary pressure is hypothesized, and is tested using air-water interfacial area data obtained from gas-phase tracer tests and saturation-pressure data obtained from water-drainage experiments. The results show that the magnitude of the air-water interfacial area increases with increasing capillary pressure, which corresponds to decreasing water content. (Abstract shortened by UMI.)
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Hollis, Peter Graham. "The overall oxygen transfer coefficient and interfacial area in hydrocarbon-based bioprocesses." Thesis, Stellenbosch : Stellenbosch University, 2015. http://hdl.handle.net/10019.1/96868.

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Thesis (MEng)--Stellenbosch University, 2015.
ENGLISH ABSTRACT: Bioconversion of hydrocarbons to value-added intermediates and products has significant industrial potential using both prokaryotic and eukaryotic organisms. In particular, alkanes can be converted to an expansive range of commercially important products using aerobic bioprocesses under mild process conditions. Coupled with the relative abundance of alkanes derived from gas to liquid (GTL) technologies, such as those employed by SASOL, South Africa, the commercial potential for bioconverison of alkanes is large. However, unlike carbohydrate substrates, alkane feedstocks are devoid of oxygen in their molecular structure. This means that the entire oxygen demand needs to be met by oxygen transfer. Furthermore, a decline in oxygen transfer in aqueous-hydrocarbon dispersions with increasing alkane concentration has been observed to result from depression of the overall volumetric oxygen transfer coefficient (KLa). Therefore, understanding KLa and the fundamental parameters underpinning its behaviour is critical to ensuring the bioprocess is kinetically, rather than transport, limited in terms of both operation and scale-up. Previous studies have examined KLa in aerated-alkane-aqueous systems. In light of the importance of oxygen transfer in bioprocesses, this study expands on the KLa understanding in 3-phase studies by including a fourth solid phase, thus more closely representing a hydrocarbonbased bioprocess. The project aimed to determine the impact of agitation, alkane concentration and solid loading on the Sauter mean bubble diameter (DSM), gas hold-up and specific interfacial area (a) and correlate these parameters to KLa. This ultimately determined which parameter was dominant over a range of process conditions. Furthermore, concurrent measurement of the KLa and interfacial area meant the behaviour of the liquid side oxygen transfer coefficient (KL) could be defined, providing further insight into how changes in the process conditions impact on KLa. Experiments were conducted in a 5 litre stirred tank bioreactor containing n-C14-20 straight chain alkane, sparged with air at 0.8 vvm. In line with process conditions typical of a hydrocarbonbased bioprocess, KLa and a were measured for agitation rates from 450 to 1000 RPM, alkane concentrations from 2 to 20% v/v and yeast solids from 1 to 10 g/l. KLa was measured using the gassing out procedure using a dissolved oxygen (DO) probe which measured the response of the system to a step change in the sparge gas oxygen pressure. The probe response lag ( P), equal to the time taken for the probe to reach 63.2% of the saturation DO concentration, was determined for every set of process conditions. The inverse of P, KP was taken into account when calculating KLa from the DO probe response. The area was calculated from DSM and gas hold-up. DSM was quantified using high speed photography and image analysis was performed in Matlab® using bespoke routines. Elimination of optical distortion and the development of an adequate light source was key to acquiring clear images. Both KLa and interfacial area were found to be affected by changes in agitation, alkane concentration and yeast loading. An increase in agitation increased the KLa over the entire range of alkane concentration and yeast loading. Similarly, an increase in agitation resulted in an increase in interfacial area, underpinned by a decrease in the DSM. It is therefore likely that the interfacial area plays a dominant role in defining KLa when considering an increase in agitation. Increases in alkane concentration resulted in a peak in KLa between 2.5 and 5% alkane concentration while further increases in alkane concentration depressed KLa. This peak was not observed in interfacial area, where an increase in alkane concentration resulted only in a decrease in interfacial area, thus indicating a positive influence of KL on KLa at low alkane concentrations. Further increases in alkane concentration beyond those creating the peak KLa resulted in KLa depression, suggesting that the increasing viscosity imparted by the alkane decreases both KL and interfacial area. Increased yeast loading had opposing effects at low and high agitation rates. At low agitation rates, increased loadings were observed to increase KLa, while increased loadings at high agitation rates caused a decrease in KLa. This behaviour was also evident in interfacial area, suggesting that in this regime KLa was defined by interfacial area behaviour. Increased yeast loading was observed to depress the KLa for all alkane concentrations when examined at a constant midpoint agitation rate. This trend was not evident in interfacial area, which increased with increasing yeast loading at the same agitation rate. The positive influence of yeast on interfacial area was likely caused by adhesion of the yeast particles to the bubble surface, lowering the DSM by preventing coalescence. The disagreement between the KLa and interfacial area results suggested that yeast loading impacted negatively on KL, which had an over-riding negative impact on KLa. The use of reliable methods for the determination of both interfacial area and KLa were demonstrated for application in model hydrocarbon-based bioprocesses. The combined results offer a unique insight into how changes in the process conditions impact independently on KL and interfacial area, which when combined ultimately defined the KLa behaviour. Quantification of the relative magnitude of the impact each parameter had on KLa contributed toward a fundamental understanding of oxygen transfer in model hydrocarbon-based bioprocesses.
AFRIKAANSE OPSOMMING: Biologiese omsetting van koolwaterstowwe na produkte met finansiële waarde het beduidende industriële potensiaal met behulp van beide prokariotiese en eukariotiese organismes. In die besonder, kan alkane omgeskakel word na ’n uitgebreide reeks van kommersieel belangrike produkte met behulp van aerobiese bioprosesse onder ligte proses voorwaardes. Tesame met die relatiewe oorvloed van alkane afgelei van GTL tegnologie, soos dié van Sasol, Suid-Afrika, die kommersiële potensiaal vir bioconverison van alkane is groot. Maar, in teenstelling koolhidrate substrate, alkaan voerstowwe is beroof van suurstof in hul molekulêre struktuur. Dit beteken dat die hele suurstof vereiste moet nagekom word deur suurstof oordrag. Verder het ’n afname in suurstof oordrag in waterige-koolwaterstof dispersies met toenemende alkaan konsentrasie waargeneem te lei van depressie van die algehele volumetriese suurstofoordragkoëffisiënt (KLa). Daarom verstaan KLa en die fundamentele parameters onderliggend sy gedrag is van kritieke belang om te verseker dat die bioprocess is kineties, eerder as vervoer, beperk in terme van beide werking en skaal-up van bioprosesse. Vorige studies het KLa in deurlug-alkaan-waterige stelsels ondersoek. In die lig van die belangrikheid van suurstof oordrag in bioprosesse hierdie studie brei uit op die KLa begrip in driefase studies deur die insluiting van ’n vierde soliede fase, dus meer nou wat ’n koolwaterstofgebaseerde bioprocess. Die doel van die projek is om die impak van vermengingstempo, alkaan konsentrasie en soliede inhout op die Sauter gemiddelde borrel deursnee (DSM), gas-vasvanging en spesifieke gas-vloistof oppervlakarea (a) te kwantifiseer en korreleer met KLa gedrag. Dit sou defineer die dominante parameter oor ’n verskeidenheid van proses voorwaardes. Verder, gelyktydige meting van die KLa en oppervlakarea kan die gedrag van die vloeistof-kant suurstofoordragkoëffisiënt (KL) gedefinieer. Dit sal verskaf verdere insig in hoe die veranderinge in die proses voorwaardes impak op KLa. Eksperimente was uitgevoer in ’n 5 liter belugte geroerde tenk bioreaktor bevat n - C14-20 reguitketting alkane, met lug met lug deurgeborrel by 0.8 VVM. In lyn met die proses voorwaardes tipies van ’n koolwaterstof-gebaseerde bioprocess, KLa en a was gemeet vir vermengignstempos van 450-1000 RPM, alkaan konsentrasies van 2-20 % v/v en gis vastestowwe van 1 tot 10 g / l. KLa is gemeet deur die vergassinguit prosedure met behulp van ’n suurstofmeter wat die reaksie van die stelsel na ’n stap verandering in die voer gas suurstof druk gemeet het. Die suurstofmeter reaksie vertraging ( P), gelyk aan die tyd wat dit neem vir die suurstofmeter 63.2 % van die versadiging DO konsentrasie te bereik, is bepaal vir elke procesopset. Die inverse van P, KP is in ag geneem by die berekening van KLa uit die suurstofmeter reaksie. Die gas-vloistof oppervlak is bereken vanaf DSM en gas hold-up. DSM is gekwantifiseer met behulp van hoë spoed fotografie en beeld analise is uitgevoer in Matlab ® roetines. Uitskakeling van optiese vervorming en die ontwikkeling van ’n voldoende ligbron was die sleutel tot die verkryging van helder beelde. Beide KLa en grens oppervlakarea gevind geraak word deur veranderinge in vermengignstempo, alkaan konsentrasie en gis laai. ’N toename in geroer het die KLa verbeter oor die hele reeks van alkaan konsentrasie en gis laai. Net so, ’n toename in geroer het gelei tot ’n toename in grens oppervlak, ondersteun deur ’n afname in die DSM. Dit is dus waarskynlik dat die grens oppervlak speel ’n dominante rol in die definisie van KLa by die oorweging van ’n toename in roering. Stygings in alkaan konsentrasie gelei tot ’n hoogtepunt in KLa tussen 2.5 en 5 % alkaan konsentrasie terwyl verdere verhogings in alkaan konsentrasie druk die KLa af. Die piek was nie in oppervlakarea duidelik, waar ’n toename in alkaan konsentrasie gelei net tot ’n afname in oppervlakarea, dus dui op ’n positiewe invloed van KL op KLa teen lae alkaan konsentrasies waargeneem. Verdere stygings in alkaan konsentrasie verder as die skep van die piek KLa gelei tot KLa depressie, wat daarop dui dat die toenemende viskositeit meegedeel deur die alkaan verminder beide KL en grens oppervlak. Verhoogde gis laai het opponerende effekte teen ’n lae en hoë vermengingstempo. By lae vermengingstempo, ’n verhoging in gis laai waargeneem KLa te verhoog, terwyl ’n verhoging in gis laai op ’n hoë vermengingstempo veroorsaak ’n afname in KLa . Hierdie gedrag was ook duidelik in grens oppervlak, wat daarop dui dat daar in hierdie regime KLa gedefinieer deur grens oppervlak gedrag. Verhoogde gis laai waargeneem die KLa te onderdruk vir alle alkaan konsentrasies wanneer ondersoek teen ’n konstante middelpunt vermengingstempo. Hierdie tendens was nie duidelik in tussenvlak gebied, wat verhoog met toenemende gis laai op dieselfde geroer koers. Die positiewe invloed van gis op grens oppervlak is waarskynlik veroorsaak deur adhesie van die gis deeltjies aan die borrel oppervlak, die verlaging van die DSM deur die voorkoming van die saamsmelting van gasborrels. Die meningsverskil tussen die KLa en grens oppervlakarea resultate voorgestel dat gis laai negatiewe uitwerking op KL, met ’n dominante negatiewe impak op KLa. Die gebruik van ’n betroubare metodes vir die bepaling van beide oppervlakarea en KLa gedemonstreer vir toepassing in model koolwaterstof-gebaseerde bioprosesse. Die gekombineerde resultate bied ’n unieke insig in hoe die veranderinge in die proses voorwaardes impak onafhanklik op KL en oppervlakarea, wat wanneer gekombineer gedefinieer die KLa gedrag. Kwantifisering van die relatiewe grootte van die impak elke parameter het op KLa bygedra tot ’n fundamentele begrip van suurstof oordrag in model koolwaterstof-gebaseerde bioprosesse.
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Morel, Christophe. "Modélisation multidimensionnelle des écoulements diphasiques gaz - liquide : application à la simulation des écoulements à bulles ascendants en conduite verticale." Châtenay-Malabry, Ecole centrale de Paris, 1997. http://www.theses.fr/1997ECAP0543.

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Cette étude comporte en premier lieu une réflexion générale sur la modélisation multidimensionnelle des écoulements diphasiques gaz - liquide. Une nouvelle notion de carte de configuration locale de l'écoulement est proposée. L’effort de modélisation est porté plus particulièrement sur les écoulements dispersés à bulles. La fermeture des termes de diffusion turbulente et de transferts interfaciaux est explicitée dans le cadre d'un modèle à deux fluides. Le modèle K- a été retenu pour la turbulence de la phase liquide. Les équations originales de ce modèle étant particulièrement complexes, une analyse des ordres de grandeurs a été effectuée afin de ne retenir que les termes les plus importants. Par ailleurs, les transferts interfaciaux sont proportionnels à l'aire interfaciale volumique qui est inconnue. Une équation de transport pour cette quantité a été établie à l'aide de deux méthodes différentes. La première méthode, originale, est indépendante du régime d'écoulement considéré. La seconde méthode, basée sur un formalisme statistique, est restreinte à l'étude d'écoulements dispersés. Des relations de fermeture sont également proposées pour les termes dus à la coalescence des bulles et à la compressibilité et la dilatabilité du gaz qui apparaissent dans l'équation d'aire interfaciale volumique. Les différents modèles proposes ont été implantés dans le module tridimensionnel du code CATHARE. De nombreux tests de sensibilité aux constantes intervenants dans ces modèles ont été effectués. Les résultats des simulations ont été comparés aux résultats expérimentaux disponibles dans la littérature et discutés.
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Lyu, Ying, Mark L. Brusseau, Ouni Asma El, Juliana B. Araujo, and Xiaosi Su. "The Gas-Absorption/Chemical-Reaction Method for Measuring Air-Water Interfacial Area in Natural Porous Media." AMER GEOPHYSICAL UNION, 2017. http://hdl.handle.net/10150/626480.

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The gas-absorption/chemical-reaction (GACR) method used in chemical engineering to quantify gas-liquid interfacial area in reactor systems is adapted for the first time to measure the effective air-water interfacial area of natural porous media. Experiments were conducted with the GACR method, and two standard methods (X-ray microtomographic imaging and interfacial partitioning tracer tests) for comparison, using model glass beads and a natural sand. The results of a series of experiments conducted under identical conditions demonstrated that the GACR method exhibited excellent repeatability for measurement of interfacial area (A(ia)). Coefficients of variation for A(ia) were 3.5% for the glass beads and 11% for the sand. Extrapolated maximum interfacial areas (A(m)) obtained with the GACR method were statistically identical to independent measures of the specific solid surface areas of the media. For example, the A(m) for the glass beads is 29 (1) cm(-1), compared to 32 (3), 30 (2), and 31 (2) cm(-1) determined from geometric calculation, N2/BET measurement, and microtomographic measurement, respectively. This indicates that the method produced accurate measures of interfacial area. Interfacial areas determined with the GACR method were similar to those obtained with the standard methods. For example, A(ia)s of 47 and 44 cm(-1) were measured with the GACR and XMT methods, respectively, for the sand at a water saturation of 0.57. The results of the study indicate that the GACR method is a viable alternative for measuring air-water interfacial areas. The method is relatively quick, inexpensive, and requires no specialized instrumentation compared to the standard methods.
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Barigou, Mostafa. "Bubble size, gas holdup and interfacial area distributions in mechanically agitated gas-liquid reactors." Thesis, University of Bath, 1987. https://ethos.bl.uk/OrderDetails.do?uin=uk.bl.ethos.376338.

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Prasser, Horst-Michael, Tobias Sühnel, Christophe Vallée, and Thomas Höhne. "Experimental investigation and CFD simulation of slug flow in horizontal channels." Forschungszentrum Dresden, 2010. http://nbn-resolving.de/urn:nbn:de:bsz:d120-qucosa-28061.

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For the investigation of stratified two-phase flow, two horizontal channels with rectangular cross-section were built at Forschungszentrum Dresden-Rossendorf (FZD). The channels allow the investigation of air/water co-current flows, especially the slug behaviour, at atmospheric pressure and room temperature. The test-sections are made of acrylic glass, so that optical techniques, like high-speed video observation or particle image velocimetry (PIV), can be applied for measurements. The rectangular cross-section was chosen to provide better observation possibilities. Moreover, dynamic pressure measurements were performed and synchronised with the high-speed camera system. CFD post-test simulations of stratified flows were performed using the code ANSYS CFX. The Euler-Euler two fluid model with the free surface option was applied on grids of minimum 4∙105 control volumes. The turbulence was modelled separately for each phase using the k-ω based shear stress transport (SST) turbulence model. The results compare well in terms of slug formation, velocity, and breaking. The qualitative agreement between calculation and experiment is encouraging and shows that CFD can be a useful tool in studying horizontal two-phase flow. Furthermore, CFD pre-test calculations were done to show the possibility of slug flow generation in a real geometry and at relevant parameters for nuclear reactor safety. The simulation was performed on a flat model representing the hot-leg of the German Konvoi-reactor, with water and saturated steam at 50 bar and 263.9°C. The results of the CFD-calculation show wave generation in the horizontal part of the hot-leg which grow to slugs in the region of the bend.
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Books on the topic "Interfacial area"

1

Nix, Ernest E. Modeling and simulation of a Fiber Distributed Data Inferface Local Area Network (FDDILAN) using OPNET® for interfacing through the Common Data Link (CDL). Monterey, Calif: Naval Postgraduate School, 1994.

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Dejesus, Julio M. *. Measurement of interfacial area and void fraction by two-phase flow in a vertical tube. 1989.

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Alan K.F.* Chan. Experimental study of interfacial area and other flow parameters in developing slug flow in a vertical tube. 1989.

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Allen, Michael P., and Dominic J. Tildesley. Inhomogeneous fluids. Oxford University Press, 2017. http://dx.doi.org/10.1093/oso/9780198803195.003.0014.

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In this chapter, the special techniques needed to simulate and calculate properties for inhomogeneous systems are presented. The estimation of surface properties, such as the interfacial tension, may be accomplished by a variety of methods, including the calculation of the stress tensor profiles, the change in the potential energy on scaling the surface area at constant volume, the observation of equilibrium capillary wave fluctuations, or direct free energy measurement by cleaving. The structure within the interface is also of interest, and ways of quantifying this are described. Practical issues such as system size, preparation of a two-phase system, and equilibration time, are discussed. Special application areas, such as liquid drops, fluid membranes, and liquid crystals, are described.
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1955-, Katz Randy H., and United States. National Aeronautics and Space Administration., eds. Interfacing a high performance disk array file server to a gigabit LAN. [Washington, DC: National Aeronautics and Space Administration, 1993.

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1955-, Katz Randy H., and United States. National Aeronautics and Space Administration., eds. Interfacing a high performance disk array file server to a gigabit LAN. [Washington, DC: National Aeronautics and Space Administration, 1993.

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Cates, M. Complex fluids: the physics of emulsions. Oxford University Press, 2017. http://dx.doi.org/10.1093/oso/9780198789352.003.0010.

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These lectures start with the mean field theory for a symmetric binary fluid mixture, addressing interfacial tension, the stress tensor, and the equations of motion (Model H). We then consider the phase separation kinetics of such a mixture: coalescence, Ostwald ripening, its prevention by trapped species, coarsening of bicontinuous states, and the role of shear flow. The third topic addressed is the stabilization of emulsions by using surfactants to reduce or even eliminate the interfacial tension between phases; the physics of bending energy, which becomes relevant in the latter case, is then presented briefly. The final topic is the creation of long-lived metastable emulsions by adsorption of colloidal particles or nanoparticles at the fluid–fluid interface; alongside spherical droplets, these methods can be used to create a range of unconventional structures with potentially interesting properties that are only now being explored.
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Bocquet, Lydéric, David Quéré, Thomas A. Witten, and Leticia F. Cugliandolo, eds. Soft Interfaces. Oxford University Press, 2017. http://dx.doi.org/10.1093/oso/9780198789352.001.0001.

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Many of the distinctive and useful phenomena of soft matter come from its interaction with interfaces. Examples are the peeling of a strip of adhesive tape or the coating of a surface or the curling of a fibre via capillary forces or the electrically driven ow along a microchannel, or the collapse of a porous sponge. These interfacial phenomena are distinct from the intrinsic behaviour of a soft material like a gel or a microemulsion. Yet many forms of interfacial phenomena can be understood via common principles valid for many forms of soft matter. Our goal in organizing this school was to give students a grasp of these common principles and their many ramifications and possibilities. The school comprised over fifty 90-minute lectures over four weeks in July 2013. Four four-lecture courses by Howard Stone, Michael Cates, David Nelson, and L. Mahadevan served as an anchor for the program. A number of shorter courses and seminars rounded out the school.This volume presents lecture notes prepared by the speakers and submitted for publication after the school. The lectures are grouped under two main themes: Hydrodynamics and interfaces, and Soft matter.
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Furst, Eric M., and Todd M. Squires. Microrheology applications. Oxford University Press, 2018. http://dx.doi.org/10.1093/oso/9780199655205.003.0010.

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The wide number of microrheology methods and techniques serve as new tools for measuring the rheology of soft materials. Several emerging applications of microrheology are presented, including the rheology of hydrogelators, gelation kinetics, and degradation (gel breaking). Viscosity measurements, in particular of protein solutions, is also discussed. These problems generally take advantage of the small volume requirements of microrheology as well as its sensitivity. The chapter begins with a discussion of mechanical and microrheology operating regimes to aid the reader in planning experiments. It concludes with a discussion of emerging trends and future areas of microrheology, including interfacial rheology.
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Thomsen, Bodil Marie Stavning, ed. Affects, Interfaces, Events. Imbricate! Press, 2021. http://dx.doi.org/10.22387/imbaie.

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This book engages with how affective encounters are shaped and conditioned by interfacial events. Together, the chapters explore the implications of this on a micro-perceptual and macro-relational level through an experimental middling of approaches and examples. While broadly departing from a Spinozist and Deleuzian theoretical foundation, the book weaves together a compelling number of conceptual and empirical trajectories. Always attuned to the implications, modulations and tonalities arising in the readings through art, journalism, bodies, an/archives, data and design, Affects, Interfaces, Events allows for a truly transdisciplinary resonance driven by theory, technology and practice.
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Book chapters on the topic "Interfacial area"

1

Drew, Donald A., and Stephen L. Passman. "Interfacial Area." In Theory of Multicomponent Fluids, 199–220. New York, NY: Springer New York, 1999. http://dx.doi.org/10.1007/0-387-22637-0_18.

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Ishii, Mamoru, and Takashi Hibiki. "Interfacial Area Transport." In Thermo-Fluid Dynamics of Two-Phase Flow, 217–42. New York, NY: Springer New York, 2010. http://dx.doi.org/10.1007/978-1-4419-7985-8_10.

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Ishii, Mamoru, and Takashi Hibiki. "Interfacial Area Transport." In Thermo-Fluid Dynamics of Two-Phase Flow, 217–42. Boston, MA: Springer US, 2006. http://dx.doi.org/10.1007/978-0-387-29187-1_10.

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Rao, P. S. C., Heonki Kim, and Michael D. Annable. "3.3.6 Air-Water Interfacial Area." In SSSA Book Series, 783–96. Madison, WI, USA: Soil Science Society of America, 2018. http://dx.doi.org/10.2136/sssabookser5.4.c29.

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Ishii, Mamoru, and Takashi Hibiki. "Constitutive Modeling of Interfacial Area Transport." In Thermo-Fluid Dynamics of Two-Phase Flow, 243–313. New York, NY: Springer New York, 2010. http://dx.doi.org/10.1007/978-1-4419-7985-8_11.

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Ishii, Mamoru, and Takashi Hibiki. "Constitutive Modeling of Interfacial Area Transport." In Thermo-Fluid Dynamics of Two-Phase Flow, 243–99. Boston, MA: Springer US, 2006. http://dx.doi.org/10.1007/978-0-387-29187-1_11.

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Kaviany, Massoud. "Solid-Fluid Systems with Large Specific Interfacial Area." In Mechanical Engineering Series, 349–415. New York, NY: Springer New York, 2001. http://dx.doi.org/10.1007/978-1-4757-3488-1_5.

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Cox, Rick, Dario Gomez, Daniel A. Buttry, Peter Bonnesen, and Kenneth N. Raymond. "High Surface Area Silica Particles as a New Vehicle for Ligand Immobilization on the Quartz Crystal Microbalance." In Interfacial Design and Chemical Sensing, 71–77. Washington, DC: American Chemical Society, 1994. http://dx.doi.org/10.1021/bk-1994-0561.ch007.

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Ishii, Mamoru, and Takashi Hibiki. "One-Dimensional Interfacial Area Transport Equation in Subcooled Boiling Flow." In Thermo-Fluid Dynamics of Two-Phase Flow, 475–81. New York, NY: Springer New York, 2010. http://dx.doi.org/10.1007/978-1-4419-7985-8_17.

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Matsui, Goichi, Yutaka Yamashita, and Toshio Kumazawa. "Effect of Interfacial Area on Flow Characteristics in Bubble Flow." In NATO ASI Series, 87–95. Boston, MA: Springer US, 1988. http://dx.doi.org/10.1007/978-1-4613-0707-5_6.

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Conference papers on the topic "Interfacial area"

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Fukamachi, Norihiro, Tatsuya Hazuku, Tomoji Takamasa, Takashi Hibiki, and Mamoru Ishii. "Interfacial Area Transport of Bubbly Flow Under Microgravity Environment." In ASME/JSME 2003 4th Joint Fluids Summer Engineering Conference. ASMEDC, 2003. http://dx.doi.org/10.1115/fedsm2003-45160.

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In relation to the development of the interfacial area transport equation, axial developments of one-dimensional void fraction, bubble number density, interfacial area concentration, and Sauter mean diameter of adiabatic nitrogen-water bubbly flows in a 9 mm-diameter pipe were measured by using an image-processing method under microgravity environment. The flow measurements were performed at four axial locations (axial distance from the inlet normalized by the pipe diameter = 7, 30, 45 and 60) under various flow conditions of superficial gas velocity (0.0083 m/s ∼ 0.022 m/s) and superficial liquid velocity (0.073 m/s ∼ 0.22 m/s). The interfacial area transport mechanism under microgravity environment was discussed in detail based on the obtained data and the visual observation. These data can be used for the development of reliable constitutive relations which reflect the true transfer mechanisms in two-phase flow under microgravity environment.
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Hazuku, Tatsuya, Tomoji Takamasa, Takashi Hibiki, and Mamoru Ishii. "Interfacial Area Transport of Vertical Upward Annular Two-Phase Flow." In ASME 2005 Summer Heat Transfer Conference collocated with the ASME 2005 Pacific Rim Technical Conference and Exhibition on Integration and Packaging of MEMS, NEMS, and Electronic Systems. ASMEDC, 2005. http://dx.doi.org/10.1115/ht2005-72489.

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Accurate prediction of the interfacial area concentration is essential to successful development of the interfacial transfer terms in the two-fluid model. The interfacial area concentration in annular flow and annular mist flow is especially relevant to the transition process to the liquid film dryout, which might lead to fatal problem in the safety and efficient operation of boiling heat transfer system. However, very few experimental and theoretical studies focusing on the interfacial area concentration in annular flow region have been conducted. From this point of view, accurate measurements of annular flow parameters such as local liquid film thickness, one-dimensional interfacial area concentration of liquid film, and local interfacial area concentration profile of liquid film were performed by a laser focus displacement meter at 21 axial locations in vertical upward annular two-phase flow using a 3-m-long and 11-mm-diameter pipe. The axial distances from the inlet (z) normalized by the pipe diameter (D) varied over z/D = 50 to 250. Data were collected for preset gas and liquid flow conditions and for Reynolds numbers ranging from Reg = 31,800 to 98,300 for the gas phase and Ref = 1,050 to 9,430 for the liquid phase. Axial development of the one-dimensional interfacial area concentration and the local interfacial area concentration profile of liquid film were examined with the data obtained in the experiment. Total interfacial area concentration including liquid film and droplets was also discussed with help of the existing drift-flux model, entrainment correlation, and droplet size correlation.
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Crandall, Dustin, Goodarz Ahmadi, and Duane Smith. "Measurement of Interfacial Area Production and Permeability Within Porous Media." In ASME 2010 8th International Conference on Nanochannels, Microchannels, and Minichannels collocated with 3rd Joint US-European Fluids Engineering Summer Meeting. ASMEDC, 2010. http://dx.doi.org/10.1115/fedsm-icnmm2010-30214.

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An understanding of the pore-level interactions that affect multi-phase flow in porous media is important in many subsurface engineering applications, including enhanced oil recovery, remediation of dense non-aqueous liquid contaminated sites, and geologic CO2 sequestration. Standard models of two-phase flow in porous media have been shown to have several shortcomings, which might partially be overcome using a recently developed model based on thermodynamic principles that includes interfacial area as an additional parameter. A few static experimental studies have been previously performed, which allowed the determination of static parameters of the model, but no information exists concerning the interfacial area dynamic parameters. A new experimental porous flow cell that was constructed using stereolithography for two-phase gas-liquid flow studies was used in conjunction with an in-house analysis code to provide information on dynamic evolution of both fluid phases and gas-liquid interfaces. In this paper, we give a brief introduction to the new generalized model of two-phase flow model and describe how the stereolithography flow cell experimental setup was used to obtain the dynamic parameters for the interfacial area numerical model. In particular, the methods used to determine the interfacial area permeability and production terms are shown.
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Banuti, Daniel, Sebastian Karl, and Klaus Hannemann. "Interfacial Area Modeling for Eulerian Spray Simulations in Liquid Rocket Engines." In 44th AIAA/ASME/SAE/ASEE Joint Propulsion Conference & Exhibit. Reston, Virigina: American Institute of Aeronautics and Astronautics, 2008. http://dx.doi.org/10.2514/6.2008-5231.

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Wenger, George M., Richard J. Coyle, Patrick P. Solan, John K. Dorey, Courtney V. Dodd, Anthony Primavera, and Robert Erich. "Case Studies of Brittle Interfacial Failures in Area Array Solder Interconnects." In ISTFA 2000. ASM International, 2000. http://dx.doi.org/10.31399/asm.cp.istfa2000p0355.

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Abstract A common pad finish on area array (BGA or CSP) packages and printed wiring board (PWB) substrates is Ni/Au, using either electrolytic or electroless deposition processes. Although both Ni/Au processes provide flat, solderable surface finishes, there are an increasing number of applications of the electroless nickel/immersion gold (ENi/IAu) surface finish in response to requirements for increased density and electrical performance. This increasing usage continues despite mounting evidence that Ni/Au causes or contributes to catastrophic, brittle, interfacial solder joint fractures. These brittle, interfacial fractures occur early in service or can be generated under a variety of laboratory testing conditions including thermal cycling (premature failures), isothermal aging (high temperature storage), and mechanical testing. There are major initiatives by electronics industry consortia as well as research by individual companies to eliminate these fracture phenomena. Despite these efforts, interfacial fractures associated with Ni/Au surface finishes continue to be reported and specific failure mechanisms and root cause of these failures remains under investigation. Failure analysis techniques and methodologies are crucial to advancing the understanding of these phenomena. In this study, the scope of the fracture problem is illustrated using three failure analysis case studies of brittle interfacial fractures in area array solder interconnects. Two distinct failure modes are associated with Ni/Au surface finishes. In both modes, the fracture surfaces appear to be relatively flat with little evidence of plastic deformation. Detailed metallography, scanning electron microscopy (SEM), energy dispersive x-ray analysis (EDX), and an understanding of the metallurgy of the soldering reaction are required to avoid misinterpreting the failure modes.
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Liu, Hang, Liang-ming Pan, Wen-xiong Zhou, Quanyao Ren, Haojie Huang, and Bin Yu. "INTERFACIAL AREA TRANSPORT SYSTEM FOR BUBBLY FLOW IN VERTICAL ROD BUNDLES." In International Heat Transfer Conference 16. Connecticut: Begellhouse, 2018. http://dx.doi.org/10.1615/ihtc16.mpf.023971.

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Gladkikh, Mikhail, Vivek Jain, Steven Bryant, and Mukul Sharma. "Experimental and Theoretical Basis for a Wettability-Interfacial Area-Relative Permeability Relationship." In SPE Annual Technical Conference and Exhibition. Society of Petroleum Engineers, 2003. http://dx.doi.org/10.2118/84544-ms.

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Rioua, X., J. Fabrea, and C. Colin. "Closure Laws for the Transport Equation of Interfacial Area in Dispersed Flow." In ASME 2002 Joint U.S.-European Fluids Engineering Division Conference. ASMEDC, 2002. http://dx.doi.org/10.1115/fedsm2002-31386.

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Derivation of a transport equation for the interfacial area concentration. In two-phase flows, the interfacial area is a key parameter since it mainly controls the momentum heat and mass transfers between the phases. An equation of transport of interfacial area may be very useful, especially for the two-fluid models. Such an equation should be able to predict the transition between the flow regimes. With this aim in view, we shall focus our attention on pipe flow. Besides in a first step, our study will be limited to dispersed flows. Different models are used to predict the evolution of bubble sizes. Some models use a population balance that provides a detailed description of the bubble size distributions, but they require as many equations as diameter ranges (Coulaloglou & Tavlarides1). Some others use only one equation for the transport of the mean interfacial area (Hibiki & Ishii2). In that case the bubble size distribution is treated as it would be monodispersed, its mean diameter being equal to the Sauter diameter. An intermediate approach was proposed by Kamp et al.3, in which polydispersed size distributions can be taken into account. It is the starting point of the present study in which: • The choice of an interfacial velocity is discussed. • The sink and source terms due to bubble coalescence, break-up or phase change are established. The model of Kamp et al. consists of transport equations of the various moments of the density probability function P(d) of the bubble diameter. In many experimental situations, P(d) is well predicted by a log-normal law (with two characteristic parameters d00 the central diameter of the distribution and a width parameter): The different moments of order ? of P(d) may be calculated: Sγ=n∫P(d)dγd(d)(1) where n is the bubble number density, S1/n, the mean diameter and S2/?, the interfacial area. A transport equation can be written for each moment: ∂Sγ∂t+∇·(uGSγ)=φγ(2) The lhs of (2) is an advection term by the gas velocity uG and the rhs is a source or sink term due to bubble coalescence, break-up or mass transfer. Since the bubble size distribution is characterised by the two parameters d00 and σˆ, only two transport equations (for S1 and S2) have to be solved to calculate the space-time evolution of the bubble size distribution. These two equations are still too cumbersome for a two-fluid model. Under some hypotheses (σˆ ∼ constant), they are lead to a single equation for the interfacial area. In its dimensionless form the interfacial area ai+ (ai+ = π S2 D, where D is the pipe diameter) reads: d/dt+(ai+)=f(RG,Re,We,ai+)(3) where RG is the gas fraction, Re is the Reynolds number of the mixture, We the Weber number of the mixture and t+ a dimensionless time.
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Wang, Xia, and Xiaodong Sun. "Hyperbolicity of One-Dimensional Two-Fluid Model With Interfacial Area Transport Equations." In ASME 2009 Fluids Engineering Division Summer Meeting. ASMEDC, 2009. http://dx.doi.org/10.1115/fedsm2009-78388.

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Two-fluid model with an empirical flow regime concept is widely used for two-phase flow analyses but suffers from its static and often non-hyperbolic nature. Recently, an interfacial area transport equation (IATE) has been proposed within the framework of the two-fluid model to dynamically describe the interfacial structure evolution and model the interfacial area concentration with the ultimate goal of modeling flow regime transition dynamically. Studies showed that the two-fluid model with the IATE (termed “two-fluid-IATE model” hereafter) could provide a more accurate prediction of the phase distributions and therefore improve the predictive capability of the two-fluid model. The inclusion of the IATE in the two-fluid model, however, brings about a subject of concern, namely, the well-posedness of the model. The objective of the present study is to investigate the issue of the hyperbolicity of a one-dimensional two-fluid-IATE model by employing momentum flux parameters, which take into account the coupling of the void fraction (volumetric fraction of the dispersed phase) and radial velocity distributions over the cross section of a flow passage. A characteristic analysis of the partial differential equations of the one-dimensional two-fluid model and two-group IATEs for an adiabatic flow was performed to identify a necessary condition for the system to achieve hyperbolicty. A case study was performed for an adiabatic liquid-liquid slug flow and the analysis showed that the hyperbolicty of the two-fluid-IATE model was guaranteed if appropriate correlations of the momentum flux parameters were applied in the two-fluid-IATE model.
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Niessner, Jennifer, S. Majid Hassanizadeh, and Dustin Crandall. "Modeling Two-Phase Flow in Porous Media Including Fluid-Fluid Interfacial Area." In ASME 2008 International Mechanical Engineering Congress and Exposition. ASMEDC, 2008. http://dx.doi.org/10.1115/imece2008-66098.

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We present a new numerical model for macro-scale two-phase flow in porous media which is based on a physically consistent theory of multi-phase flow. The standard approach for modeling the flow of two fluid phases in a porous medium consists of a continuity equation for each phase, an extended form of Darcy’s law as well as constitutive relationships for relative permeability and capillary pressure. This approach is known to have a number of important shortcomings and, in particular, it does not account for the presence and role of fluid–fluid interfaces. An alternative is to use an extended model which is founded on thermodynamic principles and is physically consistent. In addition to the standard equations, the model uses a balance equation for specific interfacial area. The constitutive relationship for capillary pressure involves not only saturation, but also specific interfacial area. We show how parameters can be obtained for the alternative model using experimental data from a new kind of flow cell and present results of a numerical modeling study.
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Reports on the topic "Interfacial area"

1

Tan, M. J., and M. Ishii. Interfacial area measurement methods. Office of Scientific and Technical Information (OSTI), February 1989. http://dx.doi.org/10.2172/6144035.

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Ishii, M. [Interfacial area and interfacial transfer in two-phase flow]. Office of Scientific and Technical Information (OSTI), September 1993. http://dx.doi.org/10.2172/10180933.

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Kojasoy, G. Interfacial area and interfacial transfer in two-phase flow systems. Office of Scientific and Technical Information (OSTI), August 1992. http://dx.doi.org/10.2172/6956765.

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Ishii, Mamoru, T. Hibiki, S. T. Revankar, S. Kim, and J. M. Le Corre. Interfacial area and interfacial transfer in two-phase systems. DOE final report. Office of Scientific and Technical Information (OSTI), July 2002. http://dx.doi.org/10.2172/809191.

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Zhang, Z. F., and Raziuddin Khaleel. The Interfacial-Area-Based Relative Permeability Function. Office of Scientific and Technical Information (OSTI), September 2009. http://dx.doi.org/10.2172/992385.

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Yarbro, Stephen Lee. Modeling interfacial area transport in multi-fluid systems. Office of Scientific and Technical Information (OSTI), November 1996. http://dx.doi.org/10.2172/426963.

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Guo, T., J. Park, and G. Kojasoy. Interfacial Area and Interfacial Transfer in Two-Phase Flow Systems (Volume I. Chapters 1-5). Office of Scientific and Technical Information (OSTI), March 2003. http://dx.doi.org/10.2172/901869.

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Guo, T., J. Park, and G. Kojasoy. Interfacial Area and Interfacial Transfer in Two-Phase Flow Systems (Volume II. Chapters 6-10). Office of Scientific and Technical Information (OSTI), March 2003. http://dx.doi.org/10.2172/901870.

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Guo, T., J. Park, and G. Kojasoy. Interfacial Area and Interfacial Transfer in Two-Phase Flow Systems (Volume III. Chapters 11-14). Office of Scientific and Technical Information (OSTI), March 2003. http://dx.doi.org/10.2172/901872.

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Guo, T., J. Park, and G. Kojasoy. Interfacial Area and Interfacial Transfer in Two-Phase Flow Systems (Volume IV. Chapters 15-19). Office of Scientific and Technical Information (OSTI), March 2003. http://dx.doi.org/10.2172/901873.

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