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Separation Processes 1 Resit > Topic 5: Absorption and Stripping in Plate Columns > Flashcards

Topic 5: Absorption and Stripping in Plate Columns Flashcards

1
Q

how does distillation differ to absorption and stripping processes

A

distillation is a process of separation by phase creation whereas, absorption and stripping operations are processes of separation by phase addition

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2
Q

why are stripping and absorption processes used

A

stripping and absorption processes are normally used to recover components that are present in low concentrations

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3
Q

what is absorption

A

absorption is the removal of a volatile solute from a gas stream by means of contact with a liquid solvent

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4
Q

what is stripping

A

stripping is the removal of a volatile solute from a liquid stream by means of contact with a stripping gas

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5
Q

what are some simplified assumptions for stripping and absorption processes

A

there are 3 components

  • liquid component (carrier liquid or solvent)
  • gas component (carrier or stripping gas)
  • single volatile solute

only the volatile solute can transfer between phases

isothermal and isobaric throughout

no vaporization of solvent

no dissolution of carrier gas

constant molar overflow

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6
Q

what is L’ in stripping and absorption processes

A

L’ is the liquid molar flowrate of the solute- free solvent

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7
Q

what is V’ in stripping and absorption processes

A

V’ is the molar flowrate of solute-free carrier gas

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8
Q

how can we assume constant molar overflow in stripping and absorption processes

A

we can assume constaqnt molar overflow if L’ and V’ are constants throughout the column.

this will happen is we assume no vaporization and no dissolution of the carrier gas

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9
Q

define variable X

A

X is the mole ratio of solute to solvent in the liquid phase, X=x/1-x where x is the mole fraction in the liquid phase

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10
Q

define the variable Y

A

Y is the mole ratio of solute to carrier gas in the gas phase, Y=y/1-y where y is the mole fraction in the gas phase

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11
Q

explain the absorber diagram

A

liquid flows in from the top (L’, x0) and flows out the bottom (L’, xN)
gas flows in from the bottom (V’, yN+1) and exits from the top (V’, y1)
the stages are labelled from the top (stage 1) to the bottom (stage N)

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12
Q

what is observed about X and Y in dilture solutions

A

in dilute solutions, X is approx. = x , and Y is approx. = y

when x and y are4 much much smaller than 1, meaning that they are dilute

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13
Q

what do we need to design absorption/ stripping equipment by the equilibrium stage method

A

Y(X) OR X(Y)

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14
Q

what is the general equilibrium ratio relation expressed in?

A

for a single solute the general equilibrium relation is expressed in terms of the k factor and mole fractionm of the solute; k=y/x

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15
Q

what is the inverse relation between mole fractions and mole ratios?

A

y=Y/1+Y

and

x=X/1+X

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16
Q

using inverse relations between mole fractions and mole ratios, express Y(X) and its inverse X(Y) in terms of K

A

Y=KX/1+X(1-K)

X=Y/K(1+Y)-Y

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17
Q

what is the new equilibrium factor in terms of mole ratios?

A

K’=Y/X

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18
Q

if we do not have necessary Y(X) OR X(Y) data to construct the equilibrium curve, what do we do

A

we would calculate the equilibrium curve through other methods

we would need to calculate it from a thermodynamic model for the k factor

appropriate thermodynamic models for dilute systems are;
K=Y1-P1*/P modified raoult’s law non-ideal dilute volatile liquid solute
K=H1/P dilute gaseous state

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19
Q

for dilute solutions, what is the relationship between K’ and K

A

for dilute solutions
X=x and Y=y approx.

therefore
K’= K approx.

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20
Q

what are the basis for the mccabe thiele graphical analysis for absorption/stripping

A

countercurrent flow of gas and liquid
carrier liquid/ solvent molar flowrate is L’
carrier/ stripping gas molar flow rate is V’
transfer of solute only between plates
hence L’ and V’ are constant throughout the cascade and we have constant molar overflow
mole ratios X and Y are the composition variables
linear operating lines follow mccabe thiele graphical analysis

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21
Q

discuss the operating line for the absorber

A
  • top and bottom gas stream and inlet solvent compositions are specified as design variables
  • to determine the operating line for the process, a solute balance is carried out down to an arbitrary stage n

V’. Yn+1 +L’.X0 = V’.Y1 +L’,Xn

-thus thus the equation of the operating line is
Y=[Y1-(L’/V’)X0] +(L’/V’)X

this equation relates the compositions of the passing streams such as Yn+1 and Xn

the slope is L’/V’ c.f. L/V

as the process is absorption, the operating line lies above the equilibrium urve

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22
Q

where does the operating line lie with respect to the equilibrium curve for an absorber

A

as the process is absorption, the operating line lies above the equilibrium curve

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23
Q

what is the equation of the operating line

A

Y=[Y1-(L’/V’)X0] +(L’/V’)X

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24
Q

what is the slope of the operating line for absorption

A

L’/V’

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25
Q

how is the operating line equation for an absorber obtained

A

to determine the operating line for the process, a solute balance is carried out down to an arbitrary stage n

V’. Yn+1 +L’.X0 = V’.Y1 +L’,Xn

26
Q

what are the given values when doing a design problemm and what do you have to solve for

A

gas flow V’, inlet gas composition YN+1, desired outlet gas composition Y1, inlet liquid composition X0

use these to solve for minimum solvent flow rate L’

27
Q

how do you find the minimum liquid flow rate for absorption?

A

there is a minimum liquid flow rate corresponding to a pinch point at the bottom of the column

28
Q

how does the pinch point occur?

A

the pinch point occurs when L’ is reuced to the point which the operating line intersects the equilibrium curve at Y=YN+1

29
Q

can the pinch point be found graphically

A

yes

30
Q

what is a typical liquid flowrate?

A

L’ (1.1 to 2) xL’ min

31
Q

what is the equation for minimum solvent flow rate for a dilute system

A

Y=K’X
Y=Y1+(L’/V’)(X-X0)

hence L’min can be found by equating X from the operating line and equilibrium line equations as Y=YN+1 leading to

L’min=V’(YN+1-Y1)[(YN+1/K’)-X0]^-1

if X0 =0 this becomes
‘min=V’K’(1-Y1/YN+1)

32
Q

what are the specified design variables in a stripper

A

top and bottom liquid stream and inlet gas compositions

X1, XN+1, Y0, YN

33
Q

what is the operating line for a stripper and how is it obtained?

A

V’Y0 +L’. XN+1= V’.YN +L’ X1

Y=[Y0-(L’/V’)X1]+(L’/V’)X

34
Q

what does the operating line for a stripper relate

A

compositions of passing streams like Y1 and Xn+1

35
Q

where does the operating line for a stripper lie in respect to the equilibrium curve

A

as the process is stripping the operating line lies below the equilibrium curve

36
Q

what are the given values in the design problem of a stripper and what do they solve

A

given values;
liquid flow L’, inlet gas composition Y0, inlet liquid composition XN+1, desired outlet liquid composition X1

solving for minimum gas flowrate V’

37
Q

what does the minimum gas flow rate correspond to?

A

the minimum gas flowrate corresponds to a pinch point at the top of the column

38
Q

when does a pinch point occur in stripping

A

the pinch point occurs when V’ is reduced to the point at which the operating line intersects the equilibrium curve

39
Q

can the pinch point be found graphically for strippingyw

A

yes, the pinch point is at the top of the graph where X=XN+1

40
Q

what is a typical actual gas flow rate

A

a typical actual gas flow rate is (2.2 to 2) x V’min

41
Q

what is the minimum gas flow rate for a dilute system?

A

Y=K’X
Y=Y0+(L’/V’)(X-X1)

hence V’min can be found analytically by equating Y from the operating lineand the equilibrium equations atX=XN+1 leading to:

V’min=l’(XN+1-X1)[K’XN+1-Y0}^-1

if Y0=0 this becomes:
V’min =(L’/K’)[1-X1/XN+1]

42
Q

when do analytical solutions exist

A

if in X,Y coordinates the equilibrium relationship is linear
and
if the solvent or stripping gas entering the process is solute free then an analytical solution exists

this requiresK’ to be constant over the operating range of X and in sufficiently dilute systems this is the case

43
Q

how dilute do dilute systems need to be be/

A

how dilute is ‘dilute’ entirely depends upon the system

the key criterion is the linearity of the equilibrium relationship

44
Q

what is the analytical solution called

A

the analytical solution is called the kremser method

45
Q

what is the absorption coefficient

A

A=L’/K’V’

46
Q

what is the stripping coefficient

A

S=K’V’/L’

47
Q

what is the fraction of solute absorbed or stripped f?

A

f=1-Y1/YN+1 absorber

f=1-X1/XN+1 stripper

48
Q

what is the analytical solution for f given N and theta (theta = A or S)

A

f=theta(N+1)-theta/ theta (N+1) -1

49
Q

what is the inverse relation for N given f and theta?

A

N=ln[(theta-f)/(1-f)]/ln(theta) -1

50
Q

what does the inverse relation tell you about theta and f

A

because ln(theta -f0….

theta must be equal to or greater than f
because ln(0) DNE
51
Q

what is the limit of feasibility?

A

thetamin=f is the limit of feasibility

N tends to infinity as theta tends to f

52
Q

what may cause a pinch point to occur/

A

if A or S is less than 1 then a pinch point may occur

53
Q

what causes the limit of feasibility

A

if A and S are at the minimum possible values (Amin and Smin) we ahve the limit if feasibility where N tends to infinity
smaller values of A or S lead to an infeasible process

54
Q

when is the operating line parallel to the equilibrium line?

A

if A or S is greater than 1 the operating line is parallel to the equilibrium line

55
Q

when does the operating line slope away from the equilibrium curve?

A

if A or S is greater than 1 then the operating line slopes away from the equilibrium curve

56
Q

what trend is noticed ona graph of number of theoretical tages N against the fraction not absorbed/stripped

A

for any A or S greater than 1, the fraction not absorbed or stripped decreases monotically with increasing N

57
Q

how is the overall efficiency estimated for stripping/ absorption

A

empirical correlations of overall efficiency are available based on the liquid viscosity and other properties

a method of correlation was first developed by O’Connell Eo
the number of trays required in the column is N/Eo where N is the numbr of equilibrium stages

58
Q

can murphree efficiency factors be used

A

as in distillation, , murphree vapour efficiency factors can be specified for each stage of a plate absorber or stripper

59
Q

what is the differrence between the linear operating lines for stippers and absorbers

A

for an absorber, the operating line is above the equilibrium curve
for a stripper, the operating line is below the equilibrium curve

60
Q

what two ways can the minimum flow rates of solvent or stripping gas be obtained

A

minimum flow rates of solvent or stripping gas obtained graphically or (for constatn K’) analytically

61
Q

when are analytical solutions available?

A

analytical solution are available for dilute systems where the solvent/ stripping gas is solute free

Separation Processes 1 Resit (7 decks)

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