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45639
Separations
Descrição
Mapa Mental sobre Separations, criado por nikitamachacek em 14-04-2013.
Mapa Mental por
nikitamachacek
, atualizado more than 1 year ago
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nikitamachacek
mais de 11 anos atrás
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Resumo de Recurso
Separations
different separations
by phase creation
by phase addition
by solid agent
by force field or gradient
energy addition
distillation
mass addition
liquid-liquid extraction
phase rule
feed line
slope
-q/(1-q)
also equal to -L/V
bubble point
q is infinite (vertical line)
all feed descends (sat)
dew point
q is zero (horizontal line)
all feed ascends (sat)
partiallty vaporized (when sat)
feed liquid descends
feed vapour ascends
single phase
subcooled liquid
all of feed descends
superheated vapour
all of feed ascends
Raoult's Law
Antoine's Equation
McCabe-Thiele
assumptions
constant molar overflow
molar flow rates do not change from stage to stage in each of two sections
pressure uniform throughout column
heat loss is negligible
components have equal and constant molar enthalpies of vap
operating lines
rectifying
slope
R/(R+1)
R is reflux ratio = L/D (reflux/distillate)
reflux ratio: R/Rmin
stripping
slope
(Vb+1)/Vb
Vb boilup ratio= V(bar)/B (boilup/bottoms)
both operating lines intersect at same point with q-line
equilibrium stages can be drawn after
minimum stages Nmin
R goes to infinite
both operating lines coincide with 45 line
'shut in' - no feed, distillate or bottoms
increasing relative volatility reduces staging
minimum reflux
pinch point
infinite stages
feed line touches equilibrium line
optimal reflux ratio
mulitple of Rmin
dictated by economic considerations
simple basis for design of binary distillation proces
two different cases
two feeds
two q lines and intermediate operating line
feed plus side stream
side stream treated as feed but negative flow
steam injection
sat steam injected at bottom
instead of reboiler
(xb, 0) becomes a point on lower operating line
Efficiency
the steam leaving a stage in a plate distillation is not in complete thermodynamic equilibrium
the actual no of plates needed is greater than theoretical stages
accounted for by overall efficiency factor
overall column efficiency
N/E0
partial reboiler treated as full theoretical stage
so the no of theoretical stages required in column is one less than determined in McCabe-Thiele construction
O'Connell Method
correlation between overall column efficiency average viscosity and relative volatility
Columns
Rectifying Column with Reflux
feed at bottom - superheated vapour
reboils some descending liquid
Stripping Column with Reboiler
feed at top - subcooled liquid
creates an internal reflux of raising vapour
these two columns may be operated independently
both one operating line on the McCabe-Thiele diagram
non-ideal systems
including with azeotropes
if assumption is not adequate
material and energy balances carried out for each stage
eg pressure drop in column and constant molar overflow
Condenser Type
total condenser
low pressure
many trays
partial condensation
if vapour top product is desired
avoids requirement of chilled condenser water
condenser and reboiler duty
energy balance for entire column
used to estimate operating costs
Batch Distillation
differential distillation
Rayleigh equation
S - amount of liquid residue in the still
preferred for smaller quantities, multi-use plant and periodic demand
McCabe-Thiele
additional assumption of negligible hold up
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