Hydrodynamics of the gas phase in stirred gas—liquid contactors

Analysis of the Fluid Dynamic Behavior of the Liquid and Gas Phases in Reactors Stirred with Multiple Hydrofoil Impellers

“…The RTD of the latter devices was evaluated by means of single tracer pulses into the funnel and convoluted with the model equations (see section 3.2). Besides, the experimental response curve is affected by tracer mass transfer between the gas and the liquidessentially in the part after the peak. , Although tracers less soluble than methane would have reduced this effect, , the simple procedure available to account for this artifact 18,19 was used throughout the whole investigation (see section 3.2).…”

Analysis of the Fluid Dynamic Behavior of the Liquid and Gas Phases in Reactors Stirred with Multiple Hydrofoil Impellers

“…The RTD of the latter devices was evaluated by means of single tracer pulses into the funnel and convoluted with the model equations (see section 3.2). Besides, the experimental response curve is affected by tracer mass transfer between the gas and the liquidessentially in the part after the peak. , Although tracers less soluble than methane would have reduced this effect, , the simple procedure available to account for this artifact 18,19 was used throughout the whole investigation (see section 3.2).…”

Analysis of the Gas Behavior in Sparged Reactors Stirred with Multiple Rushton Turbines: Tentative Model Validation and Scale-up

“…The RTD of these devices was evaluated by means of single tracer pulses into the funnel. Besides, the experimental response curve is affected by tracer mass transfer between the gas and the liquidsessentially in the part after the peak (Rovero et al, 1987;Nocentini et al, 1988a). Although tracers less soluble than methane would have reduced this effect (Joseph and Shah, 1986;Linek et al, 1996), they were not used since the whole instrumentation was already mounted and checked and a procedure was available to account for this artifact (Nocentini et al, 1988a).…”

“…Because of this complexity, zero-parameter models, namely, ideal mixing and plug flow are not suitable for describing the fluid dynamics of either phase, except under special circumstances and to a first approximation only (e.g., Nocentini, 1990). Only few studies are available of the gas behavior in single-impeller vessels (Hanhart et al, 1963;Gal-Or and Resnick, 1966;Popovic et al, 1983;Rovero et al, 1987;Theijert et al, 1992;Svihla et al,1995) or multiple-impeller configurations (Abrardi et al, 1988;Nocentini et al, 1988a;Svihla et al, 1995;Linek et al, 1996). In either case, the gas has been recognized to behave nonideally; for multipleimpellers, it has often been described with the simple axial dispersion model, exceptions being the studies of Svihla et al (1995) and Breman et al (1995).…”

Gas Flow Behavior in a Two‐Phase Reactor Stirred with Triple Turbines

“…The RTD of the latter devices was evaluated by means of single tracer pulses into the funnel and numerically convoluted with the model equations (see below). It is also worth mentioning that the experimental response curve (apparent RTD) is affected by tracer mass transfer between the gas and the liquid ± essentially in the part after the peak [10,13].…”

Analysis of the Fluid Dynamic Behavior of the Liquid and Gas Phases in Reactors Stirred with Multiple Hydrofoil Impellers

“…The RTD of the latter devices was evaluated by means of single tracer pulses into the funnel and convoluted with the model equations (see section 3.2). Besides, the experimental response curve is affected by tracer mass transfer between the gas and the liquidessentially in the part after the peak. , Although tracers less soluble than methane would have reduced this effect, , the simple procedure available to account for this artifact 18,19 was used throughout the whole investigation (see section 3.2).…”

Analysis of the Gas Behavior in Sparged Reactors Stirred with Multiple Rushton Turbines: Tentative Model Validation and Scale-up

“…The RTD of these devices was evaluated by means of single tracer pulses into the funnel. Besides, the experimental response curve is affected by tracer mass transfer between the gas and the liquidsessentially in the part after the peak (Rovero et al, 1987;Nocentini et al, 1988a). Although tracers less soluble than methane would have reduced this effect (Joseph and Shah, 1986;Linek et al, 1996), they were not used since the whole instrumentation was already mounted and checked and a procedure was available to account for this artifact (Nocentini et al, 1988a).…”

“…Because of this complexity, zero-parameter models, namely, ideal mixing and plug flow are not suitable for describing the fluid dynamics of either phase, except under special circumstances and to a first approximation only (e.g., Nocentini, 1990). Only few studies are available of the gas behavior in single-impeller vessels (Hanhart et al, 1963;Gal-Or and Resnick, 1966;Popovic et al, 1983;Rovero et al, 1987;Theijert et al, 1992;Svihla et al,1995) or multiple-impeller configurations (Abrardi et al, 1988;Nocentini et al, 1988a;Svihla et al, 1995;Linek et al, 1996). In either case, the gas has been recognized to behave nonideally; for multipleimpellers, it has often been described with the simple axial dispersion model, exceptions being the studies of Svihla et al (1995) and Breman et al (1995).…”

Gas Flow Behavior in a Two‐Phase Reactor Stirred with Triple Turbines

“…The RTD of the latter devices was evaluated by means of single tracer pulses into the funnel and numerically convoluted with the model equations (see below). It is also worth mentioning that the experimental response curve (apparent RTD) is affected by tracer mass transfer between the gas and the liquid ± essentially in the part after the peak [10,13].…”

Analysis of the Fluid Dynamic Behavior of the Liquid and Gas Phases in Reactors Stirred with Multiple Hydrofoil Impellers

“…The RTD of the latter devices was evaluated by means of single tracer pulses into the funnel and convoluted with the model equations (see section 3.2). Besides, the experimental response curve is affected by tracer mass transfer between the gas and the liquidessentially in the part after the peak. , Although tracers less soluble than methane would have reduced this effect, , the simple procedure available to account for this artifact 18,19 was used throughout the whole investigation (see section 3.2).…”

Analysis of the Gas Behavior in Sparged Reactors Stirred with Multiple Rushton Turbines: Tentative Model Validation and Scale-up

“…The RTD of these devices was evaluated by means of single tracer pulses into the funnel. Besides, the experimental response curve is affected by tracer mass transfer between the gas and the liquidsessentially in the part after the peak (Rovero et al, 1987;Nocentini et al, 1988a). Although tracers less soluble than methane would have reduced this effect (Joseph and Shah, 1986;Linek et al, 1996), they were not used since the whole instrumentation was already mounted and checked and a procedure was available to account for this artifact (Nocentini et al, 1988a).…”

“…Because of this complexity, zero-parameter models, namely, ideal mixing and plug flow are not suitable for describing the fluid dynamics of either phase, except under special circumstances and to a first approximation only (e.g., Nocentini, 1990). Only few studies are available of the gas behavior in single-impeller vessels (Hanhart et al, 1963;Gal-Or and Resnick, 1966;Popovic et al, 1983;Rovero et al, 1987;Theijert et al, 1992;Svihla et al,1995) or multiple-impeller configurations (Abrardi et al, 1988;Nocentini et al, 1988a;Svihla et al, 1995;Linek et al, 1996). In either case, the gas has been recognized to behave nonideally; for multipleimpellers, it has often been described with the simple axial dispersion model, exceptions being the studies of Svihla et al (1995) and Breman et al (1995).…”

Gas Flow Behavior in a Two‐Phase Reactor Stirred with Triple Turbines

“…The RTD of the latter devices was evaluated by means of single tracer pulses into the funnel and numerically convoluted with the model equations (see below). It is also worth mentioning that the experimental response curve (apparent RTD) is affected by tracer mass transfer between the gas and the liquid ± essentially in the part after the peak [10,13].…”