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Design insights for reactive distillation
Arthur W. WesterbergDept. of Chemical Engineering and
Institute for Complex Engineered SystemsCarnegie Mellon University
Pittsburgh, PA 15213
Acknowledgements: NSF and Eastman Chemicals
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Collaborators• Steinar Hauan (was here, joined CMU Aug. 1999)• Jae Woo Lee (my Ph.D. student - finished May, 2000)
• Kristian Lien• Amy Ciric (Univ. of Cincinnati)
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Outline• Design in transport space• Four reactive distillation examples
+ diluted ternary: MTBE+ quaternary (using projection): methyl acetate+ binary: McCabe-Thiele+ binary: bypassing an azeotrope
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Transport space rather than unit operation space
ProposalUse transport processes as the building blocks for synthesis rather than existing unit operations
Transport spaceBalances for• material ==> composition• energy ==> molar enthalpy• momentum ==> molar momentum??
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Useful geometry in “transport space”
Straight linesGiven a set of balances of the form
If
Then we see
au bv cw+=
uii∑ vi
i∑ wi
i∑= =
a b c+=
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And
i.e., points satisfying these balances are on a straight line in this vector space
Augmenting this spaceAdding another dimension that satisfies
leads to straight lines in this augmented space
u bb c+------------ v⋅ c
b c+------------ w⋅+ α v⋅ 1 α–( ) w⋅+= =
aunew bvnew cwnew+=
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Consider the top of a columnComposition space
Augmented with molar enthalpy
Thus balances in a composition space and in an augmented molar enthalpy + composition space both give rise to points on straight lines. (Is there a way to include momentum?)
D
LnVn+1
QC
Vn 1+ yn 1+⋅ Ln xn⋅ D xD⋅+=
Vn 1+ Hn 1+⋅ Ln hn⋅ D hD
QC
D-------+
⋅+=
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Difference points - the geometry of balances• Vn+1 is the mixing of two positive flows, Ln and D• The lever rule indicates relative amounts
D (~pure A)
LnVn+1
B
C
LnVn+1
mat’l balance
Vn+1 = Ln + D
DA
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Reaction as a “flow” and “composition”
A + B <--> C <==> -1 A -1 B + 1 C = 0; ν’ =[-1, -1, 1]• Flow: Every time reaction “turns over” (ξ mol/s), we lose one
mol/s of materialflow = (-1 + (-1) + 1) ξ = −1 ξ (mol/s) = νT ξ
• Composition: We lose one mol/s of A, one mol/s of B and gain one mol/s of C
composition =
Note: composition sums to one but lies outside composition trian-gle
1–1–
1
νT( )⁄
1
11–
=
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The reaction difference pointD
LnVn+1
Vn+1 = Ln + D - νΤξ = Ln + D + ξ
∆ = D + ξ
Ln
Vn+1mat’l
D
νΤξ = −ξ
A + B <--> C
balance
111–varies with ξ
∆
δr
ξ
D
Ln
D + ξ
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Steering tray compositions in column
Ln
D
Vn
Vn+1
LnVn+1
Vn
n
n+1Vn+1
Note: altered material balance can maketemperature changes reverse in column
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Ex 1: MeOH + IBUT <==> MTBE
MeOHExcess IBUT
MTBE
IBUT
Why did industry settle on this design?
catalyst on ionexchange resin
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Reaction difference point (MeOH + IBUT <==> MTBE)
MeOH (128.8)
MTBE (136.8)
AZ (121.7)
IBUT (62.0)
AZ (60.1)
δr111–
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Two distillation regions
MeOH (128.8)
MTBE (136.8)
AZ (121.7)
IBUT (62.0)
AZ (60.1)
I
II
residue curve
B D
F
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Liquid and vapor (rxn) equilibrium curves
MeOH
MTBE IBUT
I
II
vapor equil
liquid equilresidue curve
curve
curve
x y*(x)
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Reactive diff pt and lever rule ==> little reaction in bottom
MeOH
MTBE IBUT
δr
infeasible
negative
positiveξ
B
Ln = Vn+1 + ∆∆ = B + ξ
B
Ln between Vn+1and ∆
Want ξ positive==> ∆ positive
Cannot be muchreaction in
bottom
In bottom
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Nonreactive bottom section required
MeOH (128.8)
MTBE (136.8)
AZ (121.7)
IBUT (62.0)
AZ (60.1)
Lowest trays+ nonreactive+ in region II
to recover pure MTBE
II
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Major reaction possible and needed in top section
MeOH
MTBE IBUT (62.0)
AZ (60.1)
δr
∆
D
ξ
(excess IBUT)Vn+1 = Ln + ∆
∆ = D + ξ
D
with no rxn
with rxn
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A “split” lever rule yn+1Vn+1 =xnLn + xDD + (νR-νP)2ξ
==> x∆∆ = xDD + (νR-νP)2ξ
BA
C
νR2ξ
νP2ξ
xDD
νP
νR
xD
D
2ξ
∆
xnLnyn+1Vn+1
δr
νT = -1-1+2 = 0
A+C <==> 2B
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Ex 2: Methyl acetate, MeOH + AC = MA + W
MA
W
AC
MeOH
2 moles produce 2 moles so reaction point at infinity
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Four components - use following projection• Set acetic acid concentration to a low value (say 5%) and fix it• Map to acetic acid free basis• All equations transform nicely• On acetic acid free basis
+ MeOH = MA + W+ reaction difference point moves to finite location
Question: Why does the amount of reaction that can occur in the column decrease with large reflux ratios? This is counterintuitive.
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Geometry
1.00.80.60.40.20.0
1.0
0.8
0.6
0.4
0.2
TMd~
Bx~
Dx~
nx~
1n+y~Ftx~
MAM
W
* *1
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2 *
n1n yy ~~ =+
ξn
Ln
D
Vn+1
~
~
Vn+1~
Ln~ + ξn = + D
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Maximum in conversion vs. reflux ratio
0
20
40
60
80
100
1 2 3 4 5 6 7 8
Molar reflux ratio
Ove
rall
con
vers
ion
(%
)
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Ex. 3: McCabe-Thiele: H-->L - Rxn in top
yP1
xP1
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3
4
5
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xD xB
Operating lines
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zF
D?
x 3D −
D?
x 2D −
Top
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Reaction in bottom - makes separation harder
yP1
xP1
123
xD xB
Operating lines
Pinch point
zF
B?
x 1sB
+−B?
x sB −
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Ex. 4: Breaking an azeotrope
0.2 0.4 0.6 0.8 1.0
0.2
0.4
0.6
0.8
1.0
zF
xB
xD
yA
xA
2 1
3
4
5
6
7
δ2
δ3
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Conclusions• Reactive distillation is rich with geometry• Simple projections allow one to visualize behavior for four com-
ponent system• We have even been able to see geometrically some general results
about where to place reaction• This stuff can be taught