Effect of corrugation angle and F‐factor on dry pressure drop caused by friction
Adding the effect of corrugation angle in correlations improves dry pressure drop predictions
Owens et al. [23]
REU (intermediate scale)
Optimization of computational resources to simulate more effectively at the REU scale. Use of X‐ray computer tomography to generate geometries
Number of REU considerably increased to include half an element of Mellapak N250Y
Haroun et al. [24]
REU (intermediate scale)
Gas–liquid interface tracking in four REU geometries. Their approach constitutes a step forward toward integrating the corrugation and REU scales
Not only is the REU scale valid for representing the dry pressure drop per unit length but also the interface area versus liquid flow rate
Lautenschleger et al. [25]
REU (intermediate scale)
Single‐phase (gas) flow characteristics of novel packing PD‐10
Optimization of packing geometry to reduce pressure drop without jeopardizing mass transfer
Sebastia‐Saez et al. [26]
REU (intermediate scale)
Characteristics of multiphase gas–liquid flow on a limited set of REUs
Dependence between liquid flow rate and both gas–liquid interface area and liquid hold‐up successfully represented in a set of four REUs
Li et al. [27]
REU (intermediate scale)
Transition between corrugation and REU scale
Wet pressure drop and liquid hold‐up complemented with data obtained at the corrugation scale
Isoz and Haidl [21]
REU (intermediate scale)
Parametric study on the effect of slope of packing channels among others on the dry pressure drop. The authors used the imaging software Blender to obtain accurate representations of the column inner intricacies
Largest set of REUs along with that presented by Fernandes et al. [19, 20]
Yang et al. [28]
REU (intermediate scale)
Multiphase VOF gas–liquid flow within three piled REUs of Mellapak 250 Y. The work focuses on the effect of liquid flow patterns on the formation of dead zones
Portion of dead zones increased at high values of the Weber No. Wetted area highly affected by liquid flow rate but not by gas flow rate. The latter affects film stability and droplet formation
Asendrych et al. [29]
Full scale
Operating parameters including profiles of velocity of both phases, pressure liquid hold‐up, and species concentration by using the Euler–Euler multiphase method + mass source terms for chemical reactions
The model was validated in terms of CO2 capture efficiency by comparison to own experimental data
Niegodajew and Asendrych [30]
Full scale
Parametric 2‐D study of the entire column using the full‐scale porous medium approach
There is a mild effect of the carbon dioxide concentration at inlet conditions on the capture efficiency, which highlights the suitability of amine scrubbing on diverse scenarios (change of fuel, etc.)
Kim et al. [31]
Full scale
Effect of four modification factors in the Ergun equation related to the liquid hold‐up and the liquid load in order to determine the pressure drop
Good match between simulation and experimental results in terms of carbon dioxide conversion, wet pressure drop, and hold‐up using the new factors in the Ergun equation
Gu et al. [32]
Corrugation scale (small scale)
2‐D study of the effect of corrugation geometry on the hydrodynamics of liquid films
Research on surfactants and treatment of packing surface are crucial to obtain desired film flow patterns
Valluri et al. [33]
Corrugation scale (small scale)
2‐D multiphase study of gravity‐driven liquid films flowing down a corrugated textured solid surface (Mellapak) at low Reynolds numbers
The ratio between gas–liquid interface and specific packing area diminishes with increased surface roughness
Ataki and Bart [34]
Corrugation scale (small scale)
Morphology of rivulets in Rombopak 4M
Simulations used to develop or modify the degree of wetting, liquid hold‐up, and effective area
Haroun et al. [35]
Corrugation scale (small scale)
2‐D direct multiphase simulation of the formation of liquid recirculation areas in packing corrugation and its effect on mass transfer
Recirculation areas substantially affect the liquid hold‐up (liquid dead zones). Mass transfer not affected by the formation of recirculation areas
Iso et al. [36]
Corrugation scale (small scale)
Study of the effect of packing texture patterns on the gas–liquid interface area
To place ridges perpendicularly to the flow direction results in enhanced gas–liquid interface area
Sebastia‐Saez et al. [37]
Corrugation scale (small scale)
Study of the hydrodynamics of rivulet instabilities (braiding)
Braiding caused by interplay between surface tension and inertia and results in reduced interface area. Packing texture must be designed to hamper the effect of surface tension
2.3 Eulerian, Eulerian–Lagrangian, and Discrete Element Methods for the Simulation of Calcium Looping, Mineral Carbonation, and Adsorption in Other Solid Particulate Materials
Alongside amine scrubbing, calcium looping (CaL) has also proved a promising technology to be implemented commercially [38]. A CaL facility consists of two reactors: the carbonator and the calciner. In the carbonator, CO2 is chemically trapped in CaO particles to form limestone (CaCO3); the regeneration of the sorbent and subsequent release of CO2 takes place in the calciner. CFD offers the possibility of studying the interaction between a particulate solid phase and a gaseous phase in a fluidized bed by means of the Eulerian multiphase method. Phase tracking using the Eulerian method is (similarly to the VOF method) accomplished by solving the volume fraction field. The difference between the VOF and the Eulerian method is that a single set of conservation equations is solved in the VOF method for all of the phases involved, whereas in the Eulerian method, a different set of conservation equations is solved for each phase in the system, thus enabling the description of granular flows. The Eulerian method has been widely used in the literature to model the flow within fluidized beds, while the VOF method has traditionally been reserved to tracking free interface problems such as the
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