Improved Adsorptive-Catalytic Process for VOC Removal from Waste Gases

Mathematical Modeling of the Adsorption-Catalytic Process with Internal Heater in a Multisectional Arrangement

“…In the 2-sectional case, the catalyst domain was divided by a 3 cm thick mineral wool wall and the volume of each section was about 0.8 l. A more detailed description of the experimental setup and technique can be found in our preceding work. 7 The inlet toluene concentrations were 140 and 120 ppmv for 1-and 2-sectional reactors. The total gas flow rate for a singlesectional system was 50 l/min in the adsorption stage and 25 l/ min for the regeneration stage.…”

“…The chemistry of the processes was described by the simplified kinetic scheme 7 that includes the reversible VOC adsorption (eq 1), the transition of physically adsorbed VOCs ([A]) into the irreversibly adsorbed chemisorbed form ([P]) (eq 2), and the oxidation of the chemisorption intermediates into deep oxidation products (eq 3)…”

“…The disadvantages include parasitic heating of the inlet gas pipe when the reactor is heated from an external heater, partial desorption of VOCs during catalyst heating (in this case, the concentration of VOCs at the outlet can significantly exceed the inlet concentration), and the possibility of high-temperature gas (300−500 °C) being released into the exhaust gas duct. 7 One of the possibilities to reduce the energy consumption of the process is the location of the regeneration initiator directly inside the input part of the catalytic bed. According to theoretical estimates, this modification makes it possible to reduce the specific energy consumption by 2−3 orders of magnitude.…”