Tray absorbers

Nonisothermal Gas Absorption. The computation of nonisothermal gas absorption processes is difficult because of all the interactions involved as described for packed columns. A computer is normally required for the enormous number of plate calculations necessary to estabUsh the correct concentration and temperature profiles through the tower. Suitable algorithms have been developed (46,105) and nonisothermal gas absorption in plate columns has been studied experimentally and the measured profiles compared to the calculated results (47,106). Figure 27 shows a typical Hquid temperature profile observed in an adiabatic bubble plate absorber (107). The close agreement between the calculated and observed profiles was obtained without adjusting parameters. The plate efficiencies required for the calculations were measured independendy on a single exact copy of the bubble cap plates installed in the five-tray absorber. [Pg.42]

A general, approximate, short-cut design procedure for adiabatic bubble tray absorbers has not been developed, although work has been done in the field of nonisothermal and multicomponent hydrocarbon absorbers. An analytical expression which will predict the recovery of each component provided the stripping factor, ie, the group is known for each component on each tray of the column has been developed (102). This requires knowledge... [Pg.42]

In a trayed absorber the amine falls from one tray to the one below in the same manner as the liquid in a condensate stabilizer (Chapter 6, Figure 6-4). It flows across the tray and over a weir before flowing into the next downcomer. The gas bubbles up through the liquid and creates a froth that must be separated from the gas before it reaches the underside of the next tray. For preliminary design, a tray spacing of 24 in. and a minimum diameter capable of separating 150 to 200 micron droplets (using the equations developed in Volume 1 for gas capacity of a vertical separator) can be assumed. The size of packed towers must be obtained from manufacturer s published literature. [Pg.185]

Distillation column, tray absorber Diameter, height, internal pressure, material of construction, tray type, number of trays, condenser, reboiler (see item 3)... [Pg.608]

AV reciprocating tachycardia, 5 108 Axial dispersion coefficient, 10 762 Axial dispersion/mixing, 10 762-763 in adsorption columns, 2 604 in bubble tray absorbers, 2 88-89 chromatographic adsorption, 2 610 in packed column absorbers, 2 61-65 Axial dissolved oxygen profiles, 25 707-708 Axial filtration, 22 385-386 Axial-flow angular-momentum flowmeter, 22 672-673... [Pg.81]

Bubbles, in fluidized beds, 11 805-806 Bubble size control, 11 805 in fluidized beds, 11 819, 821 Bubble size distribution, 12 14 in foams, 12 11 Bubble tear-offs, 20 229 Bubble tray absorbers, 1 27, 29 design, 1 83-86 Bubble-tube reactor, 25 194 Bubble tube viscometer, 21 739 Bubble two-phase theory of fluidization, 11 805-806... [Pg.121]

Krausening, in beer making, 3 584 Krebs cycle, 6 632-633 Kremser-Brown method, of bubble tray absorber design, 1 85 Kreysiginone, 2 91... [Pg.506]

Nonisothermal gas absorption in bubble tray absorbers, 1 86-87 in packed column absorbers,... [Pg.632]

Pebax, commercial block copolymer, 7 648t Pebble mills, 25 64 Pebble quicklime, 15 28 Peclet numbers (Pe), 2 63 10 763 22 746 25 686t, 687t 25 279. See also Mass transfer Peclet number (PeMT) axial dispersion in bubble tray absorbers, 2 89... [Pg.678]

Tray Efficiencies in Tray Absorbers ana Strippers Computations of the theoretical trays N assume that the liquid on each tray is completely mixed and that the vapor leaving the tray is in equilibrium with the liquid. In practice, complete equilibrium cannot exist since interphase mass transfer requires a finite driving force. This leads to the definition of an overall tray efficiency... [Pg.15]

A hydrocarbon feed gas is to be treated in an existing four-theoretical-tray absorber to remove butane and heavier components. The recovery specification for the key component, butane, is 75 percent. The composition of the exit gas from the absorber and the required liquid-to-gas ratio are to be estimated. The feed-gas composition and the equilibrium K values for each component at the temperature of the (solute-free) lean oil are presented in the following table ... [Pg.19]

Correlations for Estimating fob Purchased Costs for Internals (e.g., Distillation Trays, Absorber Packings, Solvent Extraction Columns, and Others. Referenced to Mid-1968 Dollars with (M S = 273.1). Correlated Using Information from Guthrie [71]... [Pg.730]

Estimate the number of real trays required for a sieve-tray absorber or stripper by graphical stepwise construction on an xy diagram, incorporating in the analysis the Murphree tray efficiency. [Pg.284]

Example 5.2 Sieve-Tray Absorber for Recovery of Benzene Vapors... [Pg.288]

Combine material and energy balances with equilibrium considerations to determine the number of equilibrium stages required by a tray absorber or stripper when heat effects are important. [Pg.301]

Consider a tray absorber with a constant Murphree efficiency Emge = 0.75 and an average absorption factor A = 1.5. [Pg.308]

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