Turbulent Bed Contactor

The 1970 s also brought about increased use of three-phase systems in environmental applications. A three-phase fluidized bed system, known as the Turbulent Bed Contactor, was commercially used in the 1970 s to remove sulfur dioxide and particulates from flue gas generated by coal combustion processes. This wet scrubbing process experienced several... 

A Study of a Fluidized Turbulent Bed Contactor with Application to Cooling Towers... 

Performance and Design of a Turbulent Bed (Contactor (TBC)) Cooling Tower... 

See also heterogeneous gas-liquid separations, turbulent bed contactor (TCA, TVA) (Section... 

Turbulent bed contactor both gas absorption and removal of heavy, sticky participates. Related to Section 16.11.5.2. 

Turbulent bed contactor (see also Section 16.11.4.8, absorber) temperature <100°C OK for heavy, sticky particles allows high gas and liquid flow rates with high mass transfer efficiencies for gas absorption 1 to 2 pm 2.5 to 20 kW s/m. ... 

Turbulent bed contactor Liquid loadings 20 L/m s superficial gas velocity based on actual inlet gas flow rate 2 to 11 m /s m horizontal cross section mass loading liquid/gas = 4 to 8. Related topics include fluidized bed, drying (Section 16.11.5.5) heat transfer (Section... 

The general characteristics of gas-liquid contacting are described in Section 1.6.1. Other operations that use this type of contactor include gas desorption/stripping, Section 4.9 gas-liquid separations. Section 5.1 turbulent bed contactor (TCA, TVA) contactor. Section 5.2, distillation. Section 4.2, reactors. Sections 6.13-6.16 and 6.19 and direct contact heat exchange Sections 3.7-3.9. 

Continuous, Cocurrent, Counter-current, Cross flow (Not studied detail) in sufficient Miscellaneous (Wetted-wall column, venturi scrubber, turbulent bed contactor etc. 

The term three-phase fluidization requires some explanation, as it can be used to describe a variety of rather different operations. The three phases are gas, liquid and particulate solids, although other variations such as two immiscible liquids and particulate solids may exist in special applications. As in the case of a fixed-bed operation, both co-current and counter- current gas-liquid flow are permissible and, for each of these, both bubble flow, in which the liquid is the continuous phase and the gas dispersed, and trickle flow, in which the gas forms a continuous phase and the liquid is more or less dispersed, takes place. A well established device for countercurrent trickle flow, in which low-density solid spheres are fluidized by an upward current of gas and irrigated by a downward flow of liquid, is variously known as the turbulent bed, mobile bed and fluidized packing contactor, or the turbulent contact absorber when it is specifically used for gas absorption and/or dust removal. Still another variation is a three-phase spouted bed contactor. 

For example, when mass transfer limits the overall reaction rate, reaction occurs near the gas-liquid interface to make significant liquid volume unnecessary. To minimize the value of jS, bulk liquid volume is minimized, while interfacial area is maximized. As intense mixing and turbulence throughout a large liquid volume would be of limited benefit, the gas-liquid contactor of choice is a packed bed or a spray column as in the earlier TPA hydrogenation reactor example. 

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