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Meanwhile, the exponents related to the power input and the superficial gas velocity depend on bubble break up and coalescence, and the dispersions generated.
The relative bubble break up performance of the two impellers are compared in terms of measured local rates of energy dissipation and turbulent kinetic energy in the impeller zone.
The results indicate that, though in the present study the spinning-disc impeller is found to be a less efficient device for bubble break up than a standard Rushton turbine, this could be rectified through a different selection of spinning-disc dimensions and operating conditions.
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At higher superficial gas velocities, the bubble breaks up to very small bubbles and bypasses the wire mesh unaffected.
Furthermore in case of a polydisperse air water or water steam bubbly flow the bubble size distribution, bubble break-up and coalescence processes as well as different gas velocities in dependency on the bubble diameter are taken into account in the newly developed inhomogeneous MUSIG model.
Bubble break-up depends on the critical deformation of the bubbles in the continuum phase.
New kernel functions for the rate of bubble break-up and coalescence are presented.
Bubble sizes, bubble coalescence and bubble break-up rates were determined by video image analysis.
The resulting bubble flow regime increased the bed and freeboard region gas holdups due to enhanced bubble break-up.
A new explanation for the results is presented, based on experimentally obtained evidence that gas density influences bubble break-up.
A bubble number density equation is implemented in order to account for the combined effect of bubble break-up and coalescence in the tank.
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