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Experimental data on intensity of liquid-phase mass transfer in a bubbling layer sectionalized by sieve plates are reported. Relationships of volume mass transfer coefficient with gas mixture velocity and sparge density and of overall hydraulic resistance with air velocity and sparge density are determined. The flow diagram of a high-boiling organic absorbent regeneration process, where mass and heat transfer processes are combined in a single regenerator, is scrutinized.Ventilation emissions can be cleaned from organic solvents by using a high-boiling organic absorbent (HBOA) [1], but the process is difficult to implement because of relatively low concentrations of the trapped components and low pressure of the vapor−air mixture. To solve this problem at the absorption stage, it is essential to have equipment having high mass transfer coefficients and low hydraulic resistance, and at the desorption (absorbent regeneration) stage, to also ensure high heat transfer coefficients.One way of accelerating gas−liquid mass transfer processes in an absorber is to expand in contact devices the areas with conditions of unstabilized motion of the flows characterized by increased turbulization (agitation) of the interacting phases, which leads to a marked increase in the local mass transfer coefficients. Such local acceleration of the mass transfer process generally occurs in the input and output sections of the contact devices (the so-called end effect of mass transfer device).Let us check the possibility of speeding up mass transfer in the liquid phase by using end effects for a bubbling (diffusion) layer where the phase contact surface (phase interface) is formed due to diffusion of the gas through the liquid layer on a perforated (sieve) plate [2] where occurs counterflow contact of the gas with the liquid film running across the contact surface. Experiments were performed to study the intensity of liquid-phase mass transfer in the diffusion (bubbling) layer sectionalized by sieve (perforated) plates as a function of gas mixture velocity w g (in terms of full cross section of the absorption column) and sparge (flooding) density L. The gas mixture velocity varied within 0.4-1.45 m/sec and the sparge density, within 104-343 m 3 /(m 2 ⋅h). From the obtained data, plotted in Fig. 1, it follows that under the studied hydrodynamic conditions the volume mass transfer coefficient β lv varies within 0.25-0.555/sec. Comparison of the obtained β lv values with the data in [3] on the intensity of liquid-phase mass transfer in usual bubbling (diffusion) layers, where under comparable hydrodynamic conditions β lv = 0.05-0.14/sec, shows that in a bubbling layer sectionalized by sieve plates, much higher (4-5 times) mass transfer intensity is attainable, i.e., the test contact device helps obtain high β lv values in a wide range of gas velocity w g and sparge density L variation.The hydraulic resistance ∆p of the sectionalized bubbling layer was studied on a water−air system as a function of air velocity w g (in terms of full cross sect...

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