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COUNTERCURRENT CONTINUOUS-CONTACT EQUIPMENT

Your objectives in studying this section are to be able to  [Pg.292]

Define the concepts number of mass-transfer units (NTU), and height of a mass-transfer unit (HTU). [Pg.292]

Estimate the required packed height for a continuous-contact absorber or stripper in terms of the number and height of mass-transfer units. [Pg.292]

The development of the design equation for a countercurrent packed tower absorber or stripper begins with a differential mass balance of component A in the gas phase, in a manner similar to that of Example 2.12. However, this time we do not restrict the analysis to dilute solutions or to constant molar velocity. If only component A is transferred (4 G = VA[ = 1.0), considering the fact that the gas-phase molar velocity will change along the column, and that F-type mass-transfer coefficients are required for concentrated solutions, the mass balance is [Pg.292]

Both V and y vary from one end of the tower to the other, but Vs does not. Therefore, [Pg.292]


Equipment in this category is usually arranged for multistage countercurrent contact of the insoluble hquids, without repeated complete separation of the hquids from each other between stages or their equivalent. Instead, the liquids remain in continuous contact throughout their passage through the equipment. [Pg.1473]

Since most continuous extraction methods use countercurrent contacts between two phases, one a light liquid and the other a heavier one, many of the fundamentals of countercurrent gas absorption and of rectification carry over into the study of liquid extraction. Thus questions about ideal stages, stage efficiency, minimum ratio between the two streams, and size of equipment have the same importance in extraction as in distillation. [Pg.632]

This is a special case of countercurrent gas-liquid contact in which the liquid enters the equipment at the adiabatic-saturation temperature of the entering gas. This can be achieved by continuously reintroducing the exit liquid to the contactor without removal or addition of heat, as shown in Figure 8.11. For this case, equation (8-25) becomes... [Pg.503]

Reactions between components of a gas and a liquid, the kinetics of which were discussed in Chapter 6, are carried out in a variet> of equipment, often having confusing names. The variety stems from a number of conditions that have to be fulfilled simultaneously efficient contact between gas and liquid—and eventually a solid catalyst, limitation of pressure drop, ease of removal of heat, low cost of construction and operation. Depending on whether the main mass transfer resistance is located in the gas or in the liquid, multiphase reactors or absorbers are operated either with a distributed gas phase and continuous liquid phase or vice versa. Whether co- or countercurrent flow of gas and liquid is used depends on the availability of driving forces for mass and heat transfer and reaction. [Pg.691]


See other pages where COUNTERCURRENT CONTINUOUS-CONTACT EQUIPMENT is mentioned: [Pg.292]    [Pg.293]    [Pg.295]    [Pg.297]    [Pg.299]    [Pg.292]    [Pg.293]    [Pg.295]    [Pg.297]    [Pg.299]    [Pg.20]    [Pg.1675]    [Pg.325]    [Pg.325]    [Pg.1496]    [Pg.1998]    [Pg.63]    [Pg.417]    [Pg.1986]    [Pg.1679]    [Pg.290]    [Pg.347]    [Pg.718]    [Pg.417]    [Pg.266]    [Pg.88]    [Pg.91]    [Pg.266]    [Pg.599]    [Pg.64]    [Pg.955]    [Pg.187]    [Pg.598]    [Pg.735]    [Pg.32]    [Pg.266]    [Pg.584]    [Pg.1735]    [Pg.1859]    [Pg.340]    [Pg.266]    [Pg.49]    [Pg.616]    [Pg.1729]    [Pg.1851]    [Pg.271]    [Pg.736]    [Pg.599]    [Pg.1178]   


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Contact Equipment

Continuous contacting

Countercurrent

Countercurrent contact

Countercurrent contacting

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