Limestone/dolomite sulfation in a vertical pneumatic transport reactor

Abstract

Ind. Eng. Chem. Process Des. Dev. 1984, 23, 538-545 x = mole fraction of methane in solution A a = solubility constant, eq 4 A@ = solubility constant, eq 4 y = activity coefficient AA = solubility constant, eq 4 4 = fugacity coefficient vij = moles of ith ionic species per mole of jth dissolved salt e = residual, eq 6 Registry No. Methane, 74-82-8. Literature CitedArnold, D. S.; Plank, C. A.; Erlckson, E. E.; Pike, F. P. Ind. Eng. Chem., Chem. Eng. Data Ser. 1958, 3, 253-256. Blount, C. W.; Price, L. C.; Wenger, L. M.; Tarullo, M. Proc. 4th U.S. Gulf Coast GeopressurebOeothermaI Energy Conference: Research and Development: Dorfman M. H.; w. L. Flsher, Ed.; Center for Energy Studles,The sulfation characteristics of "estone/dolomite sorbents in a vertlcal pneumatic transport reactor operated with or without the spent sorbent recycle are examined In this study. Experiments are performed in a 25.4-cm (10 in.) pilot scale reactor where limestone/ddomlte reacts with sulfur dioxide generated from coal combustion. A mathematical model i s employed to account for the SW dkxide conversian and the sorbent utilization in the vertlcal pneumatic transport reactor as a scrubber for flue gas desulfurization with limestone/dolomite sorbents. The comparison between the experimental data and model prediction is conducted.

Kinetic modeling of the reaction between hydrated lime and SO2at low temperature

“…At low temperatures and in the presence of water vapor, the primary reaction that has been traditionally proposed in an FGD process is as follows2: Numerous studies have been devoted to describing mathematically the kinetics of the reaction between Ca‐based sorbents and SO 2 at high temperatures and for large particles (100–3000 μm). The kinetic models proposed can be grouped as: (1) grain models,3–7 (2) pore models,8–11 (3) volume reaction models,12 and (4) deactivation models 13, 14…”