Academic literature on the topic 'Bubble column reactor'

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Journal articles on the topic "Bubble column reactor"

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Ning, Chen, and Fang Bing Wang. "Numerical Simulation of Hydrodynamics in Slurry Bubble Column Reactor." Applied Mechanics and Materials 303-306 (February 2013): 2679–82. http://dx.doi.org/10.4028/www.scientific.net/amm.303-306.2679.

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Gas dispersion and solid suspension in industrial size slurry bubble column reactors for producing sodium dichromate are simulated numerically by using of computational fluid dynamics (CFD). The Eulerian multi-fluid model and standard k-ε turbulence model are used to describe the flow behavior in bubble columns. The simulated results show that gas is easy to flow toward the centre of the bubble column and in relatively high local gas holdup there. Installing gas-re-distributors in the bubble column is favorable for gas dispersion. Solid suspension in the bubble columns under the operating condition we investigated is relatively uniform.
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Arunkumar, S., V. Harshavardhan Reddy, T. M. Sreevathsav, and M. Venkatesan. "Hydrodynamic Study of Bubbles in a Bubble Column Reactor Part II – Numerical Study." Applied Mechanics and Materials 813-814 (November 2015): 1023–27. http://dx.doi.org/10.4028/www.scientific.net/amm.813-814.1023.

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The present work deals with the use of CFD analysis and the validation of the experimental work carried out on the artificial splitting of an air bubble in a bubble column reactor. In Part I of this work, artificial splitting of bubble in a bubble column rector is experimentally studied by using a high speed camera. Image processing technique was used to identify bubble size and bubble velocity. In present work CFD simulations are carried out using ANSYS FLUENT software using Volume of Fluids (VOF) method. VOF is based on a surface tracking technique applied to a fixed Eulerian space. The phase fraction in physical quantities that can be used to distinguish the distribution of gas hold up in a bubble Column reactor. The numerical study of splitting of bubble into two bubbles of nearly equal size is considered. In the bubble column reactor, the liquid phase is stationary and gas flow rate in it is varied. The superficial gas flow rates are 10 lph, 15 lph, 20 lph and 25 lph. The characteristics of bubble after splitting which include its shape, size and velocity for various gas flow rates mentioned above are studied numerically and are compared with experimental results. These hydrodynamic characteristics play a pivotal role in the reactions occurring between the liquid and gas phases in the bubble column reactor.
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Hammond, Keren Naa Merley, Kofi Aduhene Bosumbru, Kelvin Aduse-Poku, and Kwame Sarkodie. "Flow regime dynamics in a bubble column reactor." Journal of the Ghana Institution of Engineering (JGhIE) 24, no. 3 (2024): 9–20. https://doi.org/10.56049/jghie.v24i3.215.

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This study investigates fluid dynamics within bubble column reactors. Using an air-water system, flow regimes were generated and assessed using predictive models such as homogenous, Armand, and drift flux models. This study highlights the complexities of two-phase fluid flow, particularly focusing on the dynamic behaviours of fluids and bubbles within the column reactor. The experimental setup consisted of a transparent test section, utilizing advanced image processing techniques to accurately determine gas holdups and their relationship with superficial velocities. The results show that the Homogenous model effectively predicts the bubble flow regime but encounters limitations in the slug flow regime due to intricate phase interactions and transitional conditions. However, the Armand model and drift flux model showed accuracy in the slug and transitional flow regimes and improved at higher superficial liquid velocities. The study underscores the necessity of integrating several empirical models to enhance predictive capabilities in bubble columns. Thus, addressing experimental uncertainties in flow dynamics would be more optimal when other advanced models are integrated in the prediction of multiphase flow regimes.
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Hadavand, Laleh, and Ali Fadavi. "Effect of Vibrating Sparger on Mass Transfer, Gas Holdup, and Bubble Size in a Bubble Column Reactor." International Journal of Chemical Reactor Engineering 11, no. 1 (2013): 47–56. http://dx.doi.org/10.1515/ijcre-2012-0094.

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Abstract Bubble size has a key role in gas holdup and mass transfer in bubble column reactors. In order to have small and uniform bubbles, a new structure was designed; the reactor operates in two modes, with vibrating sparger and conventional bubble column in which sparger is fixed. In vibrating mode, the sparger vibrates gently during gas entering. The vibrating sparger performs like a paddle, resulting in a forced recirculation of gas–liquid inside the reactor; moreover, the bubble detachment is accelerated. The superficial gas velocity was between 0.003 and 0.013 ms− 1, and the vibration frequency was changed between 0 and 10.3 Hz. The bubble size was measured at three various positions of the reactor height by photographic method and using MATLAB 7.0.1 software. The mass transfer coefficient was determined by means of the dynamic gassing-out method. The results show that the bubbles were bigger in vibrating mode than those working without vibration. The bubble size decreases with increase in height from sparger. Gas holdup increased with increase in superficial gas velocity and vibration frequency. The effect of vibration increased the gas holdup with an average of 70% for all superficial gas velocities. Volumetric mass transfer coefficient was almost stable as vibration frequency increased.
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Kováts, P., and K. Zähringer. "Statistical Analysis of Bubble Parameters from a Model Bubble Column with and without Counter-Current Flow." Fluids 9, no. 6 (2024): 126. http://dx.doi.org/10.3390/fluids9060126.

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Bubble columns are widely used in numerous industrial processes because of their advantages in operation, design, and maintenance compared to other multiphase reactor types. In contrast to their simple design, the generated flow conditions inside a bubble column reactor are quite complex, especially in continuous mode with counter-current liquid flow. For the design and optimization of such reactors, precise numerical simulations and modelling are needed. These simulations and models have to be validated with experimental data. For this reason, experiments were carried out in a laboratory-scale bubble column using shadow imaging and particle image velocimetry (PIV) techniques with and without counter-current liquid flow. In the experiments, two types of gases—relatively poorly soluble air and well-soluble CO2—were used and the bubbles were generated with three different capillary diameters. With changing gas and liquid flow rates, overall, 108 different flow conditions were investigated. In addition to the liquid flow fields captured by PIV, shadow imaging data were also statistically evaluated in the measurement volume and bubble parameters such as bubble diameter, velocity, aspect ratio, bubble motion direction, and inclination. The bubble slip velocity was calculated from the measured liquid and bubble velocities. The analysis of these parameters shows that the counter-current liquid flow has a noticeable influence on the bubble parameters, especially on the bubble velocity and motion direction. In the case of CO2 bubbles, remarkable bubble shrinkage was observed with counter-current liquid flow due to the enhanced mass transfer. The results obtained for bubble aspect ratio are compared to known correlations from the literature. The comprehensive and extensive bubble data obtained in this study will now be used as a source for the development of correlations needed in the validation of numerical simulations and models. The data are available from the authors on request.
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Naveen, S., T. Sriram, S. Prithvi Raj, and M. Venkatesan. "Hydrodynamic Study of Bubbles in a Bubble Column Reactor Part I – Image Processing." Applied Mechanics and Materials 813-814 (November 2015): 1018–22. http://dx.doi.org/10.4028/www.scientific.net/amm.813-814.1018.

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The study of bubble column reactors has its significance in applications such as multiphase reactors, aerators and in industrial waste-water treatment. Extensive works has been done in studying the hydrodynamics of a single gas bubble flowing through stationary liquid phase. The natural breakup of bubble during its motion has been studied in the past. In the Part I of the present work, hydrodynamics of an air bubble after its artificial splitting using a stainless steel mesh is experimentally studied using image processing and high speed photography. The significance of bubble splitting is that it increases the surface area of contact between stationery and moving fluid which in turn increases the rate of reaction desired during the process. The motion of the bubble is captured during its release and after splitting using High-Speed Camera. The velocity, area and diameter of the bubble before and after splitting are calculated by applying Image processing technique on the high speed photograph. The splitting of the bubble is found to vary with the superficial gaseous velocity. The splitting of bubbles into two bubbles of nearly equal size is considered and its hydrodynamic characteristics are studied.
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Popa, Simona, Andra Tamas, Vasile Simulescu, Dorin Jurcau, Sorina Boran, and Giannin Mosoarca. "A Novel Approach of Bioesters Synthesis through Different Technologies by Highlighting the Lowest Energetic Consumption One." Polymers 13, no. 23 (2021): 4190. http://dx.doi.org/10.3390/polym13234190.

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Fatty acids esters have a wide application as bioplasticizers and biolubricants in different industries, obtained mainly in classic batch reactors, through an equilibrium complex reaction, that involves high temperatures, long reaction times, vigorously stirring, and much energy consumption. To overcome these shortcomings, we synthesized a series of fatty acid esters (soybean oil fatty acids being the acid components with various hydroxyl compounds) through novel low energy consumption technologies using a bubble column reactor, a microwave field reactor and for comparison meaning, a classic batch reactor. The obtained bioesters physicochemical properties were similar to one another, a good concordance among their rheological properties was obtained, but the energetic consumption is lower when using the bubble column or the microwave reactors instead of the classical batch reactor.
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Alattar, Saja A., Khalid A. Sukkar, and May A. Alsaffar. "The role of TiO2 NPs catalyst and packing material in removal of phenol from wastewater using an ozonized bubble column reactor." Acta Innovations, no. 46 (November 4, 2022): 93–105. http://dx.doi.org/10.32933/actainnovations.46.7.

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Phenol is present as a highly toxic pollutant in wastewater, and it has a dangerous impact on the environment. In the present research, the phenol removal from wastewater has been achieved using four treatment methods in a bubble column reactor (treatment by ozone only, using packed bubble column reactor with ozone, utilizing ozone with TiO2 NPs catalyst in the reactor without packing, and employing ozone with TiO2 NPs in the presence of packing). The effects of phenol concentration, ozone dosage, TiO2 NPs additions, and contact time on the phenol removal efficiency were determined. It was found that at a contact time of 30 min, the phenol removal was 60.4, 74.9, 86.0, and 100% for the first, second, third, and fourth methods, respectively. The results indicated that the phenol degradation method using catalytic ozonation in a packed bubble column with TiO2 NPs is the best treatment method. This study demonstrated the advantages of using packing materials in a bubble column reactor to enhance the mass transfer process in an ozonation reaction and then increase the phenol removal efficiency. Also, the presence of TiO2 NPs as a catalyst improves the ozonation process via the production of hydroxyl routs. Additionally, the reaction kinetics of ozonation reaction manifested that the first order model is more applicable for the reaction. Eventually, the packed bubble column reactor in the presence of TiO2 NPs catalyst provided a highperformance removal of phenol with a high economic feasibility.
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Mohagheghian, Shahrouz, Afshin J. Ghajar, and Brian R. Elbing. "Effect of Vertical Vibration on the Mixing Time of a Passive Scalar in a Sparged Bubble Column Reactor." Fluids 5, no. 1 (2020): 6. http://dx.doi.org/10.3390/fluids5010006.

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The present study used a sparged bubble column to study the mixing of a passive scalar under bubble-induced diffusion. The effect of gas superficial velocity (up to 69 mm/s) and external vertical vibrations (amplitudes up to 10 mm, frequency <23 Hz) on the mixing time scale were investigated. The bubble-induced mixing was characterized by tracking the distribution of a passive scalar within a sparged swarm of bubbles. Void fraction and bubble size distribution were also measured at each test condition. Without vibrations (static), the bubble column operated in the homogenous regime and the mixing time scale was insensitive to void fraction, which is consistent with the literature. In addition, the temporal evolution of the static column mixing was well approximated as an error function. With vertical vibrations at lower amplitudes tested, the bubble-induced mixing was restrained due to the suppression of the liquid velocity agitations in the bubble swarm wake, which decelerates mixing. Conversely, at higher amplitudes tested, vibration enhanced the bubble-induced mixing; this is attributed to bubble clustering and aggregation that produced void fraction gradients, which, in turn, induced a mean flow and accelerated the mixing. The vibration frequency for the range studied in the present work did not produce a significant effect on the mixing time. Analysis of the temporal evolution of the concentration of the passive scalar at a fixed point within the column revealed significant fluctuations with vibration. A dimensionally reasoned correlation is presented that scales the non-dimensional mixing time with the transient buoyancy number.
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Yavorskyy, Alexander, Oksana Shvydkiv, Carolin Limburg, Kieran Nolan, Yan M. C. Delauré, and Michael Oelgemöller. "Photooxygenations in a bubble column reactor." Green Chemistry 14, no. 4 (2012): 888. http://dx.doi.org/10.1039/c2gc16439f.

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Dissertations / Theses on the topic "Bubble column reactor"

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Cox, Shane Joseph Chemical Sciences &amp Engineering Faculty of Engineering UNSW. "Design and analysis of a photocatalytic bubble column reactor." Awarded by:University of New South Wales, 2007. http://handle.unsw.edu.au/1959.4/37818.

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The current work has developed a CFD model to characterise a pseudo-annular photocatalytic bubble column reactor. The model development was divided into three stages. Firstly, hydrodynamic assessment of the multiphase fluid flow in the vessel, which incorporated residence time distribution analysis both numerically and experimentally for validation purposes. Secondly, the radiation distribution of the UV source was completed. The final stage incorporated the kinetics for the degradation the model pollutant, sodium oxalate. The hydrodynamics were modelled using an Eulerian-Eulerian approach to the multiphase system with the standard k- turbulence model. This research established that there was significant deviation in the fluid behaviour in the pseudo-annular reactor when compared with traditional cylindrical columns due to the nature of the internal structure. The residence time distribution study showed almost completely mixed flow in the liquid phase, whereas the gas phase more closely represented plug flow behaviour. Whilst there was significant dependence on the superficial gas flow rate the mixing behaviour demonstrated negligible dependence on the liquid superficial velocity or the liquid flow direction, either co- or counter- current with respect to the gas phase. The light distribution was modelled using a conservative variant of the Discrete Ordinate method. The model examined the contribution to the incident radiation within the reactor of both the gas bubbles and titanium dioxide particles. This work has established the importance of the gas phase in evaluating the light distribution and showed that it should be included when examining the light distribution in a gas-liquid-solid three-phase system. An optimal catalyst loading for the vessel was established to be 1g/L. Integration of the kinetics of sodium oxalate degradation was the final step is developing the complete CFD model. Species transport equations were employed to describe the distribution of pollutant concentration within the vessel. Using a response surface methodology it was shown that the reaction rate exhibited a greater dependency on the lamp power that the lamp length, however, the converse was true with the quantum efficiency. This work highlights the complexity of completely modelling a photocatalytic system and has demonstrated the applicability of CFD for this purpose.
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Goraki, Fard Mojtaba. "CFD Modeling of Multiphase Turbulent Flows in a Bubble Column Reactor." Doctoral thesis, Universitat Rovira i Virgili, 2020. http://hdl.handle.net/10803/670965.

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Aquest treball presenta l'estudi numèric de fluxos turbulents bifàssics en un reactor de columna de bombolles en 3D utilitzant diferents models a diferents escales. En primer lloc se centra en la hidrodinàmica, las transicions del règim de flux i la transferència de massa utilitzant el model de barreja Euler-Euler k-ε per amplis rangs de velocitats superficials de gas. S'ha posat èmfasi en avaluar el rendiment d'aquest model i l'anàlisi de les transicions del règim de flux i el comportament del flux transitori dins del reactor de columna de bombolles. Es presenta la quantificació de les forces interfacials en diferents parts del reactor. Es comparen diferents models de l'estimació del coeficient global de transferència de massa, como són el model de penetració per lliscament i el model de cel·les de remolí, amb les dades experimentals per analitzar la transferència de massa. Els resultats revelen alguns dels trets característics dels règims de flux homogenis i heterogenis en la circulació de líquids, la retenció de gas, les fluctuacions turbulentes i la transferència de massa gas-líquid. Per als règims de flux transitori i turbulent s'han utilitzat les simulacions de grans remolins d'Euler-Euler per obtenir una resolució fiable de l'escala.<br>Este trabajo presenta el estudio numérico de flujos turbulentos bifásicos en un reactor de columna de burbujas en 3D utilizando diferentes modelos a diferentes escalas. En primer lugar se centra en la hidrodinámica, las transiciones del régimen de flujo y la transferencia de masa utilizando el modelo de mezcla Euler-Euler k-ε para amplios rangos de velocidades superficiales de gas. Se ha puesto énfasis se ha puesto en evaluar el rendimiento de este modelo y el análisis de las transiciones del régimen de flujo y el comportamiento del flujo transitorio dentro del reactor de columna de burbujas. Se presenta la cuantificación de las fuerzas interfaciales en diferentes partes del reactor. Se comparan diferentes modelos de la estimación del coeficiente global de transferencia de masa, como son el modelo de penetración por deslizamiento y el modelo de celdas de remolino, con los datos experimentales para analizar la transferencia de masa. Los resultados revelan algunos de los rasgos característicos de los regímenes de flujo homogéneos y heterogéneos en la circulación de líquidos, la retención de gas, las fluctuaciones turbulentas y la transferencia de masa gas-líquido.<br>This work presents numerical study turbulent two-phase flows in a 3D bubble column reactor using different models at different scales. The focus is first set on the hydrodynamics, flow regime transitions and mass transfer using the Euler-Euler mixture k-ε model at wide ranges of superficial gas velocities. The emphasis is to assess the performance of this model and the analysis of the flow regime transitions and the transient flow behavior inside the bubble column reactor. The quantification of the interfacial forces at different parts of the reactor are presented. Different models of the overall mass transfer coefficient estimation, namely the slip penetration model and the eddy cell model, are compared against the experimental data to analyze the mass transfer. The results reveal some of the characteristic features of homogeneous and heterogeneous flow regimes on the liquid circulation, gas holdup, turbulent fluctuations and gas-liquid mass transfer. For transient and turbulent flow regimes, Euler-Euler large eddy simulations were used for a reliable scale resolution. The flow is more dynamic, and more details of the instantaneous local flow structure have been obtained including large-scale structures and vortices developed in the bubble plume edge.
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Cloete, Jannean Christelle. "Oxygen transfer in a model hydrocarbon bioprocess in a bubble column reactor." Thesis, Stellenbosch : Stellenbosch University, 2015. http://hdl.handle.net/10019.1/96981.

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Thesis (MEng)--Stellenbosch University, 2015.<br>ENGLISH ABSTRACT: The expansion of the global fuels industry has caused an increase in the quantity of hydrocarbons produced as a by-product of refinery gas-to-liquid processes. Conversion of hydrocarbons to higher value products is possible using bioprocesses, which are sustainable and environmentally benign. Due to the deficiency of oxygen in the alkane molecule, the supply of sufficient oxygen through aeration is a major obstacle for the optimization of hydrocarbon bioprocesses. While the oxygen solubility is increased in the presence of hydrocarbons, under certain process conditions, the enhanced solubility is outweighed by an increase in viscosity, causing a depression in overall volumetric oxygen transfer coefficient (KLa). The rate at which oxygen is transferred is defined in terms of a concentration driving force (oxygen solubility) and the overall volumetric oxygen transfer coefficient (KLa). The KLa term comprises an oxygen transfer coefficient (KL) and the gas-liquid interfacial area (a), which are dependent on the uid properties and system hydrodynamics. This behaviour is not well understood for hydrocarbon bioprocesses and in a bubble column reactor (BCR). To provide an understanding of oxygen transfer behaviour, a model hydrocarbon bioprocess was developed using a BCR with a porous sparger. To evaluate the interfacial area, the Sauter mean bubble diameter (D32) was measured using an image analysis algorithm and gas holdup (ϵG) was measured by the change in liquid height in the column. Together the D32 and ϵG were used in the calculation of interfacial area in the column. The KLa was evaluated with incorporation of the probe response lag, allowing more accurate representation of the KLa behaviour. The probe response lag was measured at all experimental conditions to ensure accuracy and reliability of data. The model hydrocarbon bioprocess employed C14-20 alkane-aqueous dispersions (2.5 - 20 vol% hydrocarbon) with suspended solids (0.5 - 6 g/l) at discrete super ficial gas velocity (uG) (1 - 3 cm/s). For systems with inert solids (corn our, dp = 13.36 m), the interfacial area and KLa were measured and the behaviour of KLa was described by separation of the in uences of interfacial area and oxygen transfer coefficient (KL). To further the understanding of oxygen transfer behaviour, non-viable yeast cells (dp = 5.059 m) were used as the dispersed solid phase and interfacial area behaviour was determined. This interfacial area behaviour was compared with the behaviour of systems with inert solids to understand the differences with change in solids type. In systems using inert solids, a linear relationship was found between G and uG. An empirical correlation fo rthe prediction of this behaviour showed an accuracy of 83.34% across the experimental range. The interfacial area showed a similar relationship with uG and the empirical correlation provided an accuracy of 78.8% for prediction across the experimental range. In inert solids dispersions, the KLa increased with uG as the result of an increase in interfacial area as well as increases in KL. An increase in solids loading indicated an initial increase in KLa, due to the in uence of liquid-film penetration on KL, followed by a decrease in KL at solids loading greater than 2.5 g/l, due to diffusion blocking effects. In systems with yeast dispersions, the presence of surfactant molecules in the media inhibited coalescence up to a yeast loading of about 3.5 g/l, and resulted in a decrease in D32. Above this yeast loading, the fine yeast particles increased the apparent viscosity of the dispersion sufficiently to overcome the in uence of surfactant and increase the D32. The behaviour of G in yeast dispersions was similar to that found with inert solids and demonstrated a linear increase with uG. However, in yeast dispersions, the interaction between alkane concentration and yeast loading caused a slight increase in dispersion viscosity and therefore G. An empirical correlation to predict G behaviour with increased uG was developed with an accuracy of 72.55% for the experimental range considered. Comparison of yeast and inert solids dispersions indicated a 37.5% lower G in yeast dispersions compared to inert solids as a result of the apparent viscosity introduced by finer solid particles. This G and D32 data resulted in a linear increase in interfacial area with uG with no significant in uence of alkane concentration and yeast loading. This interfacial area was on average 6.7% lower than interfacial area found in inert solid dispersions as a likely consequence of the apparent viscosity with finer particles. This study provides a fundamental understanding of the parameters which underpin oxygen transfer in a model hydrocarbon bioprocess BCR under discrete hydrodynamic conditions. This fundamental understanding provides a basis for further investigation of hydrocarbon bioprocesses and the prediction of KLa behaviour in these systems.<br>AFRIKAANSE OPSOMMING: Die uitbreiding van die internasionale brandstofbedryf het 'n toename veroorsaak in die hoeveelheid koolwaterstowwe geproduseer as 'n deur-produk van raffinadery gas-tot-vloeistof prosesse. Omskakeling van koolwaterstowwe na hoër waarde produkte is moontlik met behulp van bioprosesse, wat volhoubaar en omgewingsvriendelik is. As gevolg van die tekort aan suurstof in die alkaan molekule, is die verskaffing van voldoende suurstof deur deurlugting 'n groot uitdaging vir die optimalisering van koolwaterstof bioprosesse. Terwyl die suurstof oplosbaarheid verhoog in die teenwoordigheid van koolwaterstowwe, onder sekere proses voorwaardes is die verhoogde oplosbaarheid oortref deur 'n toename in viskositeit, wat 'n depressive veroorsaak in die algehele volumetriese suurstofoordragkoëffisiënt (KLa). Die suurstof oordrag tempo word gedefinieer in terme van 'n konsentrasie dryfkrag (suurstof oplosbaarheid) en KLa. Die KLa term behels 'n suurstofoordragkoëffisiënt (KL) en die gas-vloeistof oppervlakarea (a), wat afhanklik is van die vloeistof eienskappe en stelsel hidrodinamika. Hierdie gedrag is nie goed verstaan vir koolwaterstof bioprosesse nie, asook in kolom reaktors (BCR). Om 'n begrip van suurstof oordrag gedrag te voorsien, is 'n model koolwaterstof bioproses ontwikkel met 'n BCR met 'n poreuse besproeier. Om die oppervlakarea te evalueer, is die gemiddelde Sauter deursnit (D32) gemeet deur 'n foto-analise algoritme en gas vasvanging ( G) is gemeet deur die verandering in vloeibare hoogte in die kolom. Saam is die D32 en G gebruik in die berekening van die oppervlakarea in die kolom. Die KLa is geëvalueer met insluiting van die meter se reaksie sloering, om n meer akkurate voorstelling van die KLa gedrag te bereken. Die meter reaksie sloering was gemeet op alle eksperimentele toestande om die akkuraatheid en betroubaarheid van data te verseker. Die model koolwaterstof bioproses gebruik n-C14-20 alkaan-water dispersies (2.5 - 20 vol% koolwaterstof) solide partikels (0.5 - 6 g/l) op diskrete oppervlakkige gas snelhede (1 - 3 cm/s). Vir stelsels met inerte solides (koring meel, dp = 13.36 m), is die oppervlakarea en KLa gemeet en die gedrag van KLa beskryf deur skeiding van die invloede van oppervlakarea en KL. Om die begrip van suurstof oordrag se gedrag te bevorder, is nie-lewensvatbare gisselle (dp = 5.059 m) gebruik as die verspreide solide fase en oppervlakarea is bepaal. Hierdie oppervlakarea gedrag is vergelyk met die van stelsels met inerte solides om die verskille met verandering in solide tipes te verstaan. In stelsels met inerte solides, is 'n line^ere verwantskap gevind tussen G en uG. 'n Empiriese korrelasie vir die voorspelling van hierdie gedrag is opgestel met 'n akkuraatheid van 83.34% in die eksperimentele reeks. Die oppervlakarea het 'n soortgelyke verhouding met uG en die empiriese korrelasie verskaf 'n akkuraatheid van 78,8% vir die voorspelling van oppervlakarea oor die eksperimentele reeks. In inerte solide dispersies, het die KLa toegeneem met uG as die gevolg van 'n toename in grens oppervlak asook stygings in KL. 'n Toename in solides belading het n aanvanklike styging in KLa aangedui, as gevolg van die invloed van die vloeistof-film penetrasie op KL, gevolg deur 'n afname in KL op vastestowwe ladings groter as 2.5 g/l, te danke aan diffusie blokkeer effekte. In stelsels met gis dispersies, het die teenwoordigheid van benattings molekules in die media samesmelting geïnhibeer tot 'n gis lading van ongeveer 3.5 g/l, en het gelei tot 'n afname in D32. Bo hierdie gis lading, het die fyn gis partikels die skynbare viskositeit van die verspreiding verhoog genoegsaam om die invloed van benattings molekules te oorkom en die D32 te verhoog. Die gedrag van G in gis dispersies was soortgelyk aan die van inerte solides en dui op 'n lineêre toename met uG. Maar in gis dispersies, het die interaksie tussen alkaan konsentrasie en gis lading 'n effense toename veroorsaak in die verstrooiing viskositeit en dus in G. 'n Empiriese korrelasie is ontwikkel om G gedrag te voorspel en het 'n akkuraatheid van 72,55% vir die eksperimentele verskeidenheid beskou. Vergelyking van gis en inerte patrikel dispersies wys 'n 37.5% laer G in gis dispersies in vergelyking met inerte vaste stowwe as 'n gevolg van die skynbare viskositeit bekendgestel deur fyner vastestowwe partikels. Hierdie G en D32 data het gelei tot 'n linere toename in grens oppervlak met uG met geen beduidende invloed van alkaan konsentrasie en gis lading nie. Die oppervlakarea was gemiddeld 6.7% laer as oppervlakarea gevind in inerte partikel dispersies as 'n waarskynlike gevolg van die skynbare viskositeit met fyner partikels. Hierdie studie bied 'n fundamentele begrip van die veranderlikes wat die suurstof oordrag definieer in 'n model koolwaterstof bioproses BCR onder diskrete hidrodinamiese voorwaardes. Hierdie fundamentele begrip bied n basis vir verdere ondersoek van koolwaterstof bioprosesse en en die voorspelling van KLa gedrag in hierdie stelsels.
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Studley, Allison F. "Numerical Modeling of Air-Water Flows in Bubble Columns and Airlift Reactors." Thesis, Virginia Tech, 2010. http://hdl.handle.net/10919/36380.

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Bubble columns and airlift reactors were modeled numerically to better understand the hydrodynamics and analyze the mixing characteristics for each configuration. An Eulerian-Eulerian approach was used to model air as the dispersed phase within a continuous phase of water using the commercial software FLUENT. The Schiller-Naumann drag model was employed along with virtual mass and the standard k-e turbulence model. The equations were discretized using the QUICK scheme and solved with the SIMPLE coupling algorithm. The flow regimes of a bubble column were investigated by varying the column diameter and the inlet gas velocity using two-dimensional simulations. The typical characteristics of a homogeneous, slug, and heterogeneous flow were shown by examining gas holdup. The flow field predicted using two-dimensional simulations of the airlift reactor showed a regular oscillation of the gas flow due to recirculation from the downcomer and connectors, whereas the bubble column oscillations were random and resulted in gas flow through the center of the column. The profiles of gas holdup, gas velocity, and liquid velocity showed that the airlift reactor flow was asymmetric and the bubble column flow was symmetric about the vertical axis of the column. The average gas holdup in a 10.2 cm diameter bubble column was calculated and the results for the two-dimensional simulation of varying inlet gas velocities were similar to published experimental results. The average gas holdup in the airlift reactor for the three-dimensional simulations compared well with the experiments, and the two-dimensional simulations underpredicted the average gas holdup.<br>Master of Science
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Lefebvre, Jonathan [Verfasser]. "Three-phase CO2 methanation Methanation reaction kinetics and transient behavior of a slurry bubble column reactor / Jonathan Lefebvre." München : Verlag Dr. Hut, 2019. http://d-nb.info/1181515408/34.

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Lefebvre, Jonathan [Verfasser]. "Three-phase CO$_2}$ methanation: methanation reaction kinetics and transient behavior of a slurry bubble column reactor / Jonathan Lefebvre." Karlsruhe : KIT-Bibliothek, 2019. http://d-nb.info/1187343382/34.

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7

Adetunji, Olubode Caleb. "Hybridization of electrical resistance tomography to population balance model for accurate bubble column reactor hydrodynamic parameter predictions." Doctoral thesis, University of Cape Town, 2016. http://hdl.handle.net/11427/22979.

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A novel approach of obtaining bubble size and spatial distribution is developed by hybridising techniques of Electrical Resistance Tomography and the Gas Disengagement Technique using a Population Balance as a framework. As a result, detailed hydrodynamic predictions suitable for Bubble Column Reactor [BER] optimisation results with minimal computing effort. Electrical Resistance Tomography [ERT] is a technique for creating 3D images of objects occurring in space. The images are obtained through current stimulations through a body surface electrodes and measurements of resulting voltage signals due to interior spatial conductivity field distribution. The use of ERT imaging method for hydrodynamic parameter predictions in a BCR has a benefit of yielding high temporal resolution but low spatial resolution. The low spatial resolution in electrical imaging accounts for underestimated or overestimated hydrodynamic parameter predictions similar to results obtained from the use of alternative techniques. The population balance model [PBM] is a mathematical framework with which the spatial transport of properties of bubble population can be described. The PBM also allows for the description of the time-variant bubble population properties by a division of bubble population into size classes. Moreover, the PBM allows for the inclusion of models of bubble coalescence and breakage phenomena, which affect the distribution of bubble population properties during bubble swarming. The included source terms enable accurate modelling of the bubble evolution either in a steady or unsteady state fluid flow regime. The objective of the present study is to develop an ERT interpretation technique yielding a high accuracy reconstruction of bubble population distribution through coupling ERT measurements to a PBM. It is hypothesized that a higher accuracy interpretation of ERT measurements will result from coupling ERT measurements to a PBM. The ERT technique has the capacity to image the steady and time-dependent gas void fractions in column sections as bubbles swarm and during dynamic gas disengagement [DGD]. This ERT potential is explored in hybridizing ERT and a PBM in the present work.
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Qazaq, Amjad Saleh Hussein Chemical Sciences &amp Engineering Faculty of Engineering UNSW. "Application of photocatalysis to the treatment of complex industrial aqueous effluent in a pilot-scale bubble column reactor." Awarded by:University of New South Wales. Chemical Sciences & Engineering, 2009. http://handle.unsw.edu.au/1959.4/44774.

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In this study, the photocatalytic mineralization of the industrial dump-site leachate was evaluated using an internally-irradiated 18-Litre pilot-scale aerated annular bubble column photoreactor. The study includes evaluating the effect of catalyst loading, leachate initial concentration, initial solution pH, light intensity and oxygen partial pressure. The reaction runs were performed over a 48-hours period at room temperature and atmospheric pressure. Titanium catalyst loading was optimized to be 3 gL-1 where the reaction rate constant 20x10-6 mol L-1 min-1.Beyond this dosage, the effect of light scattering by the catalyst particles were noticed on dropping the degradation rate. Moreover, at high catalyst loading, particles aggregates reduce the interfacial area between the reaction solution and the photocatalyst resulting in significant reduction in the number of active sites on the catalyst surface. It is also noticed that when the initial leachate concentration is high, the number of the active sites are decreased because of their competitive adsorption on the TiO2 particles; while on the other hand, during the light intensity illumination period, the OH radicals formed on the catalyst surface are remaining constant as evidenced by constant hydroxyl production rate. Thus, the reactive O2 attacking the contaminants molecules decrease and simultaneously the overall photodegradation efficiency also decrease dramatically. The plot of the apparent reaction rate constant versus the initial leachate concentration exhibits almost a quadratic behaviour which has an optimum value at concentration of 50 mM. Finally, it was found that the degradation rate constant increased with O2 partial pressure until a maximum was obtained around 50% O2/N2 of gas feed composition. The drop in the rate beyond 50% can be explained by the fact that the dissolved oxygen molecular oxygen is strongly electrophilic and thus increasing the dissolved oxygen content probably reduced electron-hole recombination rate and hence the system was able to maintain favourable charge balance necessary for the photocatalytic-redox process. Moreover, in the presence of excess O2, the photocatalyst surface may become highly hydroxylated to the point of inhibiting the adsorption of organic species causing decrease in the degradation rate. Effect of upflow co-current and counter current continuous operation mode were performed in the 18-litre bubble column photoreactor for the photooxidation degradation tratment of the dump-site landfill leachate. The best situation is liquid flow rate at 800 mL min-1 and total gas flow rate at 5 Lmin-1 for the counter current operation, while for the up-flow co-current operation, the best situation is liquid flow rate at 600 mL min-1 and total gas flow rate at 5 Lmin-1
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Sarah, Oddy. "Effect of Phase-Contacting Patters and Operating Conditions on Gas Hydrate Formation." Thesis, Université d'Ottawa / University of Ottawa, 2014. http://hdl.handle.net/10393/31414.

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Research into hydrate production technologies has increased in the past years. While many technologies have been presented, there is no consensus on which reactor design is best for each potential application. A direct experimental comparison of hydrate production technologies has been carried out in between a variety of reactor configurations at similar driving force conditions. Three main reactor types were used: a stirred tank, a fixed bed and a bubble column and compared different phase contacting patterns for the stirred tank and bubble column. In the initial phase of hydrate formation in a stirred tank, formation was mass and heat transfer limited at the lower stirring speed, and heat transfer limited at the higher stirring speed. After more than 10% of the water had been converted to hydrate, formation was mass transfer limited regardless of the other conditions. Neither the use of a gas inducing impeller, nor a 10 wt% particle slurry significantly affected hydrate formation rates; however, the particle slurry did lower the induction time. Due to the poor scale-up of impeller power consumption in a stirred tank, a semi-batch fixed bed was studied since it does not require any power input for mixing. The significantly slower rates of formation observed in the semi-batch fixed bed, as well as the lost reactor capacity to particles, mean that this type of system would require a much larger reactor. Faster volume and power normalized rates of hydrate formation were observed in the bubble column than in a stirred tank at similar mass transfer driving force conditions. Higher conversions of water to hydrate were observed in the bubble column because mixing was accomplished by bubbling gas from the bottom rather than by an impeller. The highest conversions of water and gas were achieved during a later stage of accelerated hydrate formation, indicating an optimal hydrate fraction for continuously operated bubble column reactors. The second stage of hydrate formation occurred more frequently at higher gas flowratess. Therefore, the increased water conversion and single-pass gas conversion justify the increased energy input required by the higher gas flowrate. Balancing the rates of mass transfer and heat removal was also critical for optimal bubble column as insufficient mass transfer would result in a lower rate of formation and insufficient heat transfer would cause previously formed hydrates to dissociate. The addition of 10wt% glass beads to the reactor promoted hydrate formation; however, it did not do so sufficiently to make up for the loss in reactor capacity or the increased energy requirement.
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Xiao-Xiong, Lu. "A study of the characteristics of a novel cocurrent downflow bubble column contactor for use as a three-phase reactor." Thesis, University of Birmingham, 1988. http://ethos.bl.uk/OrderDetails.do?uin=uk.bl.ethos.589427.

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A cocurrent downflow contactor (CDC) has been constructed in and potential as a reactions. Prior to studying the CDC as a reactor its performance order reactor to investigate its for use with behaviour gas-liquid-solid was investigated with respect to its hydrodynamic behaviour with liquids of varying viscosity and surface tension. Liquid systems employed were water based, containing various concentrations of sodium alginate, glycerol, and I-propanol. Parameters such as minimum inlet liquid velocity, column liquid velocity, pressure drop, bubble size, gas holdup, and gas liquid interfacial area were determined. Empirical relationships were derived enabling minimum inlet velocity, maximum column velocity, pressure drop and gas holdup to be calculated. It was observed that gas holdup values in the range of 0.5-0.6 could be obtained and these are much greater than those attainable with conventional stirred or bubble column systems. The gaS-liquid mass transfer characteristics of the CDC were studied by the absorption of oxygen into water and a dimensional analysis of data allowed the overall mass transfer coefficient to be determined and correlated with experimental data. The hydrogenation of itaconic acid (CSHS04) using a 5% and 10%w/w Pd/Charcoal catalyst was studied at 15-50oC and 1 bar absolute in a stirred reactor and at 200C and 1-3 bars absolute in the CDC reactor using the following solvents: water, methanol, 2-propanol and aqueous glycerol. It was found that gas-liquid mass transfer rate control could be eliminated, due to the efficient agitation and high gasliquid interfacial areas generated. The rate controlling steps were found to be those of liquid-solid mass transfer and surface reaction, both steps being almost equally important in the CDC reactor. In the case of the stirred reactor, the liquid-solid mass transfer contribution depended upon the solvent and ranged from 5% (methanol) to 40% (water). Finally it was observed that on a laboratory scale the stirred and CDC reactor can give similar performances. However, in industrial or pilot plant scale, the CDC could retain its efficiency, giving high values of overall mass transfer coefficients and overcome the inefficient mixing of large scale stirred reactors.
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Books on the topic "Bubble column reactor"

1

Robert Gerardus Jacobus Maria Van der Lans. Hydrodynamics of a bubble column loop reactor. Zoetermeer, 1985.

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Wadley, R. J. Studies of a bubble column reactor system for finechemicalsproduction. UMIST, 1994.

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Lu, Xiao-Xiong. A study of the characteristics of a novel cocurrent downflow bubble column contactor for use as athree-phase reactor. University of Birmingham, 1988.

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Sulidis, Andrew Thomas. Application of the occurrent downflow bubble column contactor (CDC) for use as a photocatalytic reactor and associated mass transfer studies. University of Birmingham, 1995.

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Deckwer, Wolf-Dieter. Bubble column reactors. Wiley, 1992.

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Majumder, Subrata Kumar. Hydrodynamics and Mass Transfer in Downflow Slurry Bubble Columns. Apple Academic Press, Incorporated, 2019.

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Majumder, Subrata Kumar. Hydrodynamics and Mass Transfer in Downflow Slurry Bubble Columns. Apple Academic Press, Incorporated, 2019.

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Majumder, Subrata Kumar. Hydrodynamics and Mass Transfer in Downflow Slurry Bubble Columns. Taylor & Francis Group, 2021.

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Hydrodynamics and Mass Transfer in Downflow Slurry Bubble Columns. Taylor & Francis Group, 2018.

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Book chapters on the topic "Bubble column reactor"

1

Jakobsen, Hugo A. "Bubble Column Reactors." In Chemical Reactor Modeling. Springer International Publishing, 2014. http://dx.doi.org/10.1007/978-3-319-05092-8_8.

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Gamwo, Isaac K., Dimitri Gidaspow, and Jonghwun Jung. "Slurry Bubble Column Reactor Optimization." In ACS Symposium Series. American Chemical Society, 2007. http://dx.doi.org/10.1021/bk-2007-0959.ch017.

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Duduković, M. P., and N. Devanathan. "Bubble Column Reactors: Some Recent Developments." In Chemical Reactor Technology for Environmentally Safe Reactors and Products. Springer Netherlands, 1992. http://dx.doi.org/10.1007/978-94-011-2747-9_14.

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Deckwer, Wolf-Dieter. "Design and Simulation of Bubble Column Reactors." In Chemical Reactor Design and Technology. Springer Netherlands, 1986. http://dx.doi.org/10.1007/978-94-009-4400-8_12.

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Baum, Sören, Jakob J. Mueller, Lutz Hilterhaus, Marrit Eckstein, Oliver Thum, and Andreas Liese. "The Bubble Column Reactor: A Novel Reactor Type for Cosmetic Esters." In Applied Biocatalysis: From Fundamental Science to Industrial Applications. Wiley-VCH Verlag GmbH & Co. KGaA, 2016. http://dx.doi.org/10.1002/9783527677122.ch15.

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Palit, Sukanchan. "Advanced Oxidation Processes, Nanofiltration, and Application of Bubble Column Reactor." In Nanomaterials for Environmental Protection. John Wiley & Sons, Inc, 2014. http://dx.doi.org/10.1002/9781118845530.ch13.

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Mohd Yusof, Muhammad Nur Amirulhaq, and Nurul Fitriah Nasir. "Effects of Reaction Temperature and Inlet Velocity of a Bubble Column Reactor on the Bubble Size for Biodiesel Production." In Lecture Notes in Mechanical Engineering. Springer Nature Singapore, 2022. http://dx.doi.org/10.1007/978-981-19-3179-6_54.

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Madhania, Suci, Lailatul Alawiyah, Azriel Iqbal Hamayaputra, Kusdianto, and Sugeng Winardi. "Scale-Up of Bubble Column Reactor for Carbon Mineralization with Precipitated CaCO3 Product." In Lecture Notes in Mechanical Engineering. Springer Nature Singapore, 2025. https://doi.org/10.1007/978-981-97-7898-0_23.

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Godo, S., K. Junghans, A. Lapin, and A. Lübbert. "Dynamics of the Flow in Bubble Column Reactors." In Bubbly Flows. Springer Berlin Heidelberg, 2004. http://dx.doi.org/10.1007/978-3-642-18540-3_6.

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Febrada, Mayongga Heriz, Wanda Oktavia Maharani, Kusdianto, et al. "Carbon Capture and Utilization Technology to Upgrading Biogas Using Bubble Column Reactor: Effect of Concentration of Ca(OH)2 Solution on CO2 Removal." In Lecture Notes in Electrical Engineering. Springer Nature Singapore, 2025. https://doi.org/10.1007/978-981-97-8197-3_17.

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Conference papers on the topic "Bubble column reactor"

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Marais, Willem-Louis. "MEA Triazine Contactor Optimization to Increase Efficiency and Reduce Fouling Potential." In CONFERENCE 2024. AMPP, 2024. https://doi.org/10.5006/c2024-20391.

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Abstract Liquid absorbents have been utilized for decades to remove impurities from produced natural gas. Throughout the last 15 years, monoethanolamine (MEA) triazine has become an industry-recognized name for the removal of sour gas (H2S). MEA triazine has one of the lowest cost profiles in terms of cost per mass of H2S removed and has obtained a commodity status. It is widely used in the oil and gas industry, both on production (upstream, midstream) and processing (downstream). MEA Triazine is typically applied via direct injection into flowlines or applied in contactor vessels (“scrubbers”, “towers”, “bubble columns”). The application type depends on numerous factors but in general, the application via contactor vessel is preferred due to its increased efficiency. However, due to the many different contactor configurations available, a wide range of efficiencies are achieved, ranging from 50 – 70%. MEA Triazine systems are also known to foul with acid-insoluble polymeric solids. This occurs when the MEA Triazine and its reaction products are not managed properly, or the system is not designed for the specific conditions. The spent material, commonly referred to as dithiazine, can form solids (amorphous dithiazine) in the contactor packing, post contactor separator, or in downstream pipelines if carry-over occurs. This paper aims to provide the reader guidance on how to optimize MEA Triazine contactor vessels to achieve maximum efficiency and to reduce or eliminate fouling. Optimization principles discussed will include contactor configurations, contactor modifications, and MEA Triazine properties and its effect on system performance. Increasing system efficiency and eliminating solids formation in these systems will have a direct impact on the user’s operating expense (OPEX). This is due to better scavenger utilization and a reduction in maintenance and downtime due to solids formation. A reduction in scope three emissions will also be achieved.
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Chai, I. C. H., Y. H. Chan, K. Nikulainen, J. Laukka, and M. A. Ishak. "Methane Pyrolysis to Produce Hydrogen and Carbon Solids Using Thermocatalytic Pathway." In APOGCE 2024. SPE, 2024. http://dx.doi.org/10.2118/221204-ms.

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Thermo-catalytic decomposition (TCD) of natural gas is a suitable technology to provide clean hydrogen (H2). This TCD process directly splits hydrocarbons, mainly methane (CH4), into H2 and carbon as illustrated in Equation 1. [Equation 1]CH4(g)→C(s)+2H2(g)ΔH∘=74 kJ/mol In TCD process, H2 is produced as a gas while carbon is generated in solid form. Though the reaction can occur with heat energy alone, the use of a catalyst significantly reduces the required reaction temperature, making the process less energy-intensive. Various reactor designs are used for TCD to pyrolyze CH4, including fluidized/packed bed reactor, moving bed reactor, bubble column reactor (using molten metal or salt), and plug flow reactor. This paper elucidates ROTOBOOST's bubble column reactor, which utilizes a specific molten metal alloy as TCD catalyst. Although methane pyrolysis demonstration has started since the 1950s, the development and understanding of liquid catalyst in bubble column has gained more momentum since the 2000s. This stems from the benefit of lowering the reaction temperature to below 1000°C, making the process less energy-intensive, mitigating coking issues and subsequent deactivation of solid catalysts, and allowing better control and tuning of solid carbon quality Von Wald et al. (2020) reported that methane pyrolysis using the bubble column technology with liquid metal catalyst is a suitable process for reducing CO2 emissions in the short term. In TCD process with bubble column reactor, pre-treated natural gas or methane is continuously fed to the bottom of the reactor, allowing it to travel upward through the molten catalytic alloy, which is heated to the reaction temperature. The catalytic alloy, with high heat capacity, provides a homogenous heat supply directly to each hydrocarbon gas molecule. As the bubbles burst at the upper interface of the liquid media, H2 and carbon are released. Since the density of carbon is much lower than that of the molten media, the produced carbon rises with the bubbles, floating at top of the liquid surface, and finally deposits at the surface of the liquid column. Therefore, the produced carbon does not affect the reaction zone on the inside/surface of the bubbles as they rise through the molten media, ensuring the bubble surface is a continuously renewed catalyst. The main advantage of liquid bubble column reactors is the continuous carbon removal from the liquid media due to density differences, preventing reactor blockage or contamination from carbon accumulation.
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Strasser, W., and A. Wonders. "Commercial scale slurry bubble column reactor optimization." In ADVANCES IN FLUID MECHANICS 2008. WIT Press, 2008. http://dx.doi.org/10.2495/afm080271.

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Studley, Allison, and Francine Battaglia. "CFD Analyses of the Mixing Characteristics in Bubble Columns and Airlift Reactors." In ASME 2011 International Mechanical Engineering Congress and Exposition. ASMEDC, 2011. http://dx.doi.org/10.1115/imece2011-63221.

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The mixing characteristics in bubble columns and airlift reactors are analyzed using computational fluid dynamics. In the simulations, an Eulerian-Eulerian approach was used to model air as the dispersed phase within a continuous phase of water using the commercial software FLUENT. The Schiller-Naumann drag model was employed along with virtual mass and the standard k–ε turbulence model. An effective bubble diameter was specified for each case studied and depended on the inlet gas velocity specified. The predicted flow field in the airlift geometry showed a regular oscillation of the gas flow due to flow recirculating from the downcomer and connectors, whereas the bubble column oscillations were random and resulted in flow moving through the center of the column. The profiles of gas holdup, gas velocity, and liquid velocity versus column width showed that the airlift reactor flow is asymmetric and the profile shape varied along the height of the column. The bubble column flow became independent of height after 20 cm above the inlet because there was less mixing than the airlift reactor. It was shown that the airlift reactor increased the mixing of the gas-liquid flow due to the addition of the downcomer. The airlift reactor showed less gas holdup in the riser than the bubble column but its velocity and gas holdup never became independent of column diameter like in the bubble column. The gas and liquid flow field showed increased mixing with increasing inlet velocity.
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Ravinuthala, Sharad Chand, and Ismail B. Celik. "Numerical Modelling of Bubble Columns for High Temperature Glass Melting Applications." In ASME 2014 4th Joint US-European Fluids Engineering Division Summer Meeting collocated with the ASME 2014 12th International Conference on Nanochannels, Microchannels, and Minichannels. American Society of Mechanical Engineers, 2014. http://dx.doi.org/10.1115/fedsm2014-22054.

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Bottom heating approach for glass melting offers potential benefits of higher efficiency and lower emissions compared to the conventional surface fired melters with burners above the bath surface. Recent advances in the enabling technologies such as burners, controls, heat recovery and refractive materials have led to successful demonstration of bottom heating Submerged Combustion Melting (SCM) of glass. In the proposed reactor, combustion products of natural gas oxy combustion are bubbled through the three phase re-circulating tank reactor. The turbulence generated by the rising bubble column would result in rapid heating and mixing of the charge resulting in fast melting and homogeneous composition of the product. Detailed understanding of such two-phase gas liquid flows is imperative for developing efficient multi-phase reactors through precise control of mixing and reaction kinetics. The bubble column, without any phase change and heating, is a good apparatus for an elementary experimental study and numerical modeling of such flows. In this study, the hydrodynamics of the bubble column are investigated using two different numerical approaches i) Using ANSYS FLUENT with an Eulerian-Eulerian approach to model the bubble and continuous phases and ii) Using a Navier-Stokes solver with the Eulerian-Lagrangian method with the Particle-in-Ball approach. The results thus obtained are discussed in detail in comparison with the experimental data available. Experiments have been conducted to gain a deeper understanding of the behaviour of the bubbles in very viscous media.
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Ibrahim, Nur Afizah, Amir Khalid, Izzuddin Zaman, Azwan Sapit, and Bukhari Manshoor. "Flow visualization of bubble structure in bubble column reactor for fluid mixing." In 7TH INTERNATIONAL CONFERENCE ON MECHANICAL AND MANUFACTURING ENGINEERING: Proceedings of the 7th International Conference on Mechanical and Manufacturing Engineering, Sustainable Energy Towards Global Synergy. Author(s), 2017. http://dx.doi.org/10.1063/1.4981165.

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Mortuza, S. M., Anil Kommareddy, Stephen P. Gent, and Gary A. Anderson. "Computational and Experimental Investigation of Bubble Circulation Patterns Within a Column Photobioreactor." In ASME 2011 5th International Conference on Energy Sustainability. ASMEDC, 2011. http://dx.doi.org/10.1115/es2011-54205.

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This research project investigates bubble and liquid circulation patterns in a vertical column photobioreactor (PBR) both experimentally as well as computationally using Computational Fluid Dynamics (CFD). Dispersed gas–liquid flow in the rectangular bubble column PBR are modeled using Eulerian–Lagrangian approach. A low Reynolds number k–ε CFD model is used to describe the flow pattern near the wall. Bubble size distribution measurements are carried out using a high-speed digital camera. A flat surface bubble column PBR is used to achieve sufficient light penetration into the system. Carbon dioxide, which is necessary for photosynthetic microalgae growth, is added to the sparged air. The results are validated with experimental data and from current literature. Design parameters, bubble flow pattern and internal hydrodynamics of a bubble column reactor were studied and the numerical simulations presented for the hydrodynamics in a bubble column PBR account for bubble phenomena that have not been sufficiently accounted for in previous research. Bubble size and shape affect the hydrodynamics as does bubble interaction with other bubbles (multiple bubbles in a flow versus single bubbles and wall effects on bubble(s) which are not symmetrical or bubbles not centered on the reactor cross-section). Understanding the bubble movement patterns will aid in predicting other design parameters like mass transfer (bubble to liquid and liquid to bubble), heat transfer (within the PBR and between the PBR and environment surrounding the PBR), and interaction forces inside the PBR.
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Mudde, Robert F. "Gravity Driven Bubbly Flows: The Role of Vortical Structures." In ASME/JSME 2003 4th Joint Fluids Summer Engineering Conference. ASMEDC, 2003. http://dx.doi.org/10.1115/fedsm2003-45672.

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Gravity driven bubbles are found in many industrial applications. Two typical reactors are the bubble column, in which the liquid is stagnant and the air lift reactor in which the liquid circulates, under the action of gravity, through the reactor. These reactors are attractive for a number of reasons: they have no moving parts and are thus low in maintenance; the size can be enormous (diameters of several meters, heights of tens of meters) allowing large volume flows to be processed; good mixing and heat transfer characteristics, etc. Our knowledge about the structure of the flow induced is rather limited. This makes design, fine tuning of operation and scale up still difficult. The two-phase flow in a bubble reactor is complicated. In the bubble columns, the liquid exhibits a large-scale circulation in a time averaged sense, with upward flow in the center and downward flow in the wall region. The first reliable data on this large-scale circulation date back to the work of Hills (174). In 1984, Franz et al. reported on the motion of what was later called vortical structures, eddy like structures (with sizes on the order of the column diameter) that move through the bubbly mixture. These vortical structures have been research more extensive during the last ten year by e.g. Fan and coworkers, Dudukovic and coworkers and Mudde &amp; Van den Akker. The structures are found for a wide range of gas fractions, ranging from a few percent to well above 20%. The vortical structures seem to be a universal feature of the gravity driven bubble flows as they were also found in air lift reactors. For this reactor it has been reported that the liquid flow behaves more or less like the superposition of a net liquid flow and the complicated flow features found in the bubble column. The similarities will be high lighted. The vortical structures have important consequences for e.g. the (pseudo-)turbulence and the mixing in the bubbly flow. In 2-dimensional equipment they appear very regular and a separation between the low frequency fluctuations and the high frequency ‘turbulence’ is easily made. However, in 3-dimensional columns the situation is more complicated. LDA data show that the vortical structures are still responsible for a the occurrence of low frequency oscillations (on the order of 0.1Hz), but they are no longer appearing regularly and a separation of frequencies is no longer possible. Finally, the newest experiment seem to show that the vortical structures can be suppressed up to gas fraction of (at least) 10%. These new experiments suggest that the gravity driven bubbly flow is not inherently unstable, but rather sensitive to the conditions at the gas inlet.
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Iyer, Kritika, S. Shridharani, S. Arunkumar, and M. Venkatesan. "Application of image processing for a bubble column reactor." In 2013 IEEE International Conference on Computational Intelligence and Computing Research (ICCIC). IEEE, 2013. http://dx.doi.org/10.1109/iccic.2013.6724169.

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McGuffie, Sean M., Mike A. Porter, and Dennis H. Martens. "Experimental and CFD Evaluation of a Bubble Column Reactor." In ASME 2010 Pressure Vessels and Piping Division/K-PVP Conference. ASMEDC, 2010. http://dx.doi.org/10.1115/pvp2010-25823.

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During the scale-up design of a slurry bubble column reactor from a pilot demonstration facility to a production reactor, the design team used computational fluid dynamics (CFD) as a tool to quantify design variables, such as gas holdup and liquid velocities/structural pressures within the reactor. At the time of the analysis, all available physics models for modeling the multi-phase flow had significant limitations that would require “tuning” of the CFD input parameters to ensure confidence in the results. The authors initially conducted a literature search to find data that could be used to calibrate the model. While a wide variety of literature is available, none provided the exact data required for model calibration. For this reason, the authors constructed a test column and performed experiments to derive data for tuning the CFD models. Statistical analysis of the experimental data provided distributions on the input parameters of interest. CFD studies were then used to tune the CFD input parameters to match the experimental data. A correlation was developed, tested and verified. This correlation was then used to provide confidence in the results of the design analysis performed on the scaled up reactor.
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Reports on the topic "Bubble column reactor"

1

Dimitri Gidaspow. Hydrodynamic models for slurry bubble column reactor. Office of Scientific and Technical Information (OSTI), 1997. http://dx.doi.org/10.2172/750383.

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Shollenberger, K. A., J. R. Torczynski, N. B. Jackson, and T. J. O`Hern. Experimental characterization of slurry bubble-column reactor hydrodynamics. Office of Scientific and Technical Information (OSTI), 1997. http://dx.doi.org/10.2172/292851.

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Bernard A. Toseland, Ph D. ENGINEERING DEVELOPMENT OF SLURRY BUBBLE COLUMN REACTOR (SBCR)TECHNOLOGY. Office of Scientific and Technical Information (OSTI), 2000. http://dx.doi.org/10.2172/783047.

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Bernard A. Toseland, Ph D. ENGINEERING DEVELOPMENT OF SLURRY BUBBLE COLUMN REACTOR (SBCR) TECHNOLOGY. Office of Scientific and Technical Information (OSTI), 2000. http://dx.doi.org/10.2172/783049.

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Toseland, B. A. Engineering Development of Slurry Bubble Column Reactor (SBCR) Technology. Office of Scientific and Technical Information (OSTI), 1998. http://dx.doi.org/10.2172/1304.

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Bernard A Toseland, Ph D. ENGINEERING DEVELOPMENT OF SLURRY BUBBLE COLUMN REACTOR (SBCR) TECHNOLOGY. Office of Scientific and Technical Information (OSTI), 2000. http://dx.doi.org/10.2172/793999.

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Bernard A Toseland, Ph D. ENGINEERING DEVELOPMENT OF SLURRY BUBBLE COLUMN REACTOR (SBCR) TECHNOLOGY. Office of Scientific and Technical Information (OSTI), 2002. http://dx.doi.org/10.2172/794000.

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Bernard A Toseland, Ph D. ENGINEERING DEVELOPMENT OF SLURRY BUBBLE COLUMN REACTOR (SBCR) TECHNOLOGY. Office of Scientific and Technical Information (OSTI), 2002. http://dx.doi.org/10.2172/794001.

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Bernard A Toseland, Ph D. ENGINEERING DEVELOPMENT OF SLURRY BUBBLE COLUMN REACTOR (SBCR) TECHNOLOGY. Office of Scientific and Technical Information (OSTI), 1999. http://dx.doi.org/10.2172/794298.

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Toseland, Bernard A. ENGINEERING DEVELOPMENT OF SLURRY BUBBLE COLUMN REACTOR (SBCR) TECHNOLOGY. Office of Scientific and Technical Information (OSTI), 1998. http://dx.doi.org/10.2172/803205.

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