Characterization of Fluidized Bed Reactors With Gas Tracer Measurements

Abstract

In a steady state bench scale fluidized bed the decomposition reaction of NaHCO, was carried out. The residence times distributions, DRT, of carbon dioxide (the gaseous product) and non adsorbing argon (the reference tracer) were mass spectroscopically measured as a function of the bed temperature. By means of single-, two-and three-phase dispersion models as well as by a cell model, the DRT's were evaluated on line by a computer.The steady state transverse and longitudinal concentration profiles of these tracers upstream from the plane source were also measured and evaluated by a dispersion model as well as by a counter current back mixing model. Comparison of the steady state and nonsteady state dispersion coefficient measurements indicate that the longitudinal gas mixing is only partially due to backmixing. The experimentally determined wake fractions agree well with those published in the literature. Since the adsorption rate of CO, on the pore surface area of the particles in the dense phase is high no interphase transfer from the interstitial gas of the dense phase into the bubble phase takes place.The desorption of CO, and its return into the interstitial gas and than into the gas phase occurs only slowly and with an initial time lag. The on-line DRT can be used as a diagnostical technique for investigation of the reactor during its operation, if operation disturbances or breakdowns occur.

Fluidized bed hydrodynamic modeling of CO2 in syngas: Distorted RTD curves due to adsorption on FCC

“…Finally, to approximate reality more closely, the 3-phase model introduces powder physico-chemical properties-porosity, and mass transfer from the gas in the emulsion to the particle surface. First, the flux equation for each phase is 21 :…”

“…The index p represents the phases: emulsion (E), bubble (B), or solid (S). Additionally, the continuity equation for each phase is 21 :…”

“…To solve Equations 6 and 7 for three phases (E, B, and S), we suppose that the velocity and mixing coefficient of the solid phase is negligible (u S ¼ M S ≈ 0). 21 The models proposed in the literature for RTD analysis in fluidized bed reactors have limitations:…”