1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 Acrylonitrile [S] Water [SN] Acetonitrile [SN] LLVE Heteroazeotrope [UN]E + B Vapour line A + B xD xO YTope xE 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0
Entrainer TB (°C) Process Rejection Acetic acid 118 1.87 BED 1, 3 Allyl alcohol 97 1.23 BED 1, 2, 3 Aliphatic Alcohols 96 - 118 1.50 BED 3
Water 100 398 HBED - n-Butyl acetate 126 .5 0.11 BED 3 Furfural 161. 4 0.42 BED 1, 2, 3 Pyridine 115.2 0.52 BED 1, 2, 3 Nitrobenzene 210.6 0.05 BED 1, 2, 3 4-methyl-2-pentanone 116.7 0.18 BED 2, 3
Methyl cyclohexane 101 0.02 HBED 2, 3
Chloroform (A)
61.1°C
+
Methanol (B)
64.5°C
+
Water (E)
100°C
REGSOLexpert : Entrainer Selection Tool for Waste Solvent
Recovery by Batch Distillation Processes
RODRIGUEZ DONIS Ivonne, GERBAUD Vincent, BAUDOUIN Olivier, JOULIA Xavier
ivonne.rdguez@infomed.sld.cu; Vincent.Gerbaud@ensiacet.fr
Objective
:
General procedure to systematize the search of several alternatives enabling the separation of non-ideal binary mixtures such as
pressure-swing distillation, azeotropic and extractive distillation.
Objective:
General procedure to systematize the search of several alternatives enabling the separation of non-ideal binary mixtures such as
pressure-swing distillation, azeotropic and extractive distillation.
REGSOLexpert
A wizard computer tool including 224 feasibility rules, and 326 batch azeotropic and extractive distillation processes.
Systematic checking for each entrainer candidate for determining its feasibility to be used in rectifying or stripping batch column.
A list of potential homogeneous and heterogeneous entrainers
E
in an optimal time for separating
A
and
B
as any industrial mixture.
Strategy for solvent recovery by distillation
3 – Column configuration
REGSOLexpert software algorithm
Extractive Distillation (HEBD)
Extractive Distillation (HEBD)
excellent agreement
20 mol/hr 150 W N= 45 yTOPF
ED
Extractive SectionA
+
B
20 moles 25°C(1 toxic, 2 pollution, 3 cost) A
A
B
B
1 - Selecting Entrainer
with RegSolExpert®
-0.9914 0.9690 Water Chloroform Methanol purity recovery 98.0% 89.6% -0.9988 0.9906 0.9957 91.6% 95.1% -0.9914 0.9690 Water Chloroform Methanol purity recovery 98.0% 89.6% -0.9988 0.9906 0.9957 91.6% 95.1% - A
A
B
B
= 0.19
1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 xDDecanter Tie Line AB=1 xP
Top Destination Region:XTOP Methanol (B) 64.5°C [S] Water (E) 100.0°C [SN] azeoAE 56.3°C [S] azeoAB53.3°C [S] Chloroform (A) 61.1°C [ SN ] azeoABE 53.1 °C [UN] LLVE LLE (25°C) Vapour Line
2 - Residue Curve Map
USE:
Extraction of bioactive substances from biological sources
TMIN Azeotrope: T = 53.5 °C, XA
= 0.65
4 – Simulation vs Experiments
: heat up 12 min : R FE = 0 120 min : R FE = 20 100 min : R = 1.4 (-D) FE = 20 60 min R = 10 (-D) FE = 20 20 min : E-B separation FE = 0 R = 1.5 250 min 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 1 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0 Methanol (B) [S] azeoAE [S] azeoAB[S] xS2Water (E) [SN] Chloroform (A)
[SN] R = 1.4 xS2exp x’S3Exp x x’s2 xs3 xs4 x’s3 XD=XII R xS2Exp azeoABE[UN] YTOP Column x profile xtop Initial charge xS1 R = 10 S4Exp
Industrial Applications
Brabant Industry case:
Cyclopentanone
(130.6°C) –
Propylene Glycol Monomethyl ether
(146°C)
Heterogeneous Azeotropic Distillation (HABD)
Heterogeneous Azeotropic Distillation (HABD)
Acetonitrile (A)
81°C
+
Water (B)
100°C
+
Heterogeneous (E)
USE:
Liquid chromatography separation in pharmaceutical Industry
TMIN Azeotrope: T = 77 °C, XA
= 0.67
1 - Selecting Heterogeneous Entrainer
with RegSolExpert®
Initial List: 55 candidates from several chemical families (DIPPR database)
Heterogeneous
E
:
Acrylonitrile
and
Chloroform
form unstable heteroazeotrope with H
20
2 - Residue Curve Map
and
3 – Column configuration
Chloroform [S] Acetonitrile [SN] Heteroazeotrope [UN] Water [SN] A + B E + B LLVE Vapour line xE xD YTope xO
D, xD
T = 25°C V = 70 mL 12.2 mol, xO N.= 50 150 W4 – Simulation vs Experiments
0.92 0.93 0.94 0.95 0.96 0.97 0.98 0.99 1 1.01 0 0.1 0.20.30.4 0.50.60.7 0.80.9 1 Total Press ure (atm )xA 0 20 40 60 80 100 120 140 T (° C )
2– (x
A(azeot), T
azeot) vs P
A
+
B
x
A=0.996 T=93.1°C X (mass) A 130.5 0.6 B 146 0.3287 isopropanol 82.3 0.0353 Water 100 0.02 volatil impurity n-methyl pyrrolidone 204.3 0.016 heavyimpurity TB (°C) Components A [sn] B [sn] isopropanol [s] Water [sn] Homogeneous [UN] [S] Heterogeneous [S] Heterogeneous [S] volatil impurity
A,
x
AD 10 mol, xAmass=0.6 N.= 50 1500 WP= 0.3 atm
0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1 0.000.200.400.600.801.001.201.401.601.802.00 0.98 0.981 0.982 0.983 0.984 0.985 0.986 0.987 0.988 0.989 0.99 0.991 0.992 0.993 0.994 0.995 0.996 0.997 0.998 0.9993- Column Configuration
4- Simulation
ProSim Batch
1- Mixture analysis
XADdistillate XASstill XAD(average) =0.9951 Recovery yield (A)= 92.5% XAS Time (h) xAmolarChloroform Acrylonitrile (* experimental values)
Aqueous Phase xRecovery=97.8%Water=0.9996 xRecovery=92.6%Water=0.947 *x*Recovery=89 %Water=0.946
Entrainer Phase xE=0.9990 Recovery=81% xE=0.712 Recovery=72% *xE=0.6916 *Recovery=69%
Final Still xacetonitrile= 0.9945
Recovery= 99.2 % xacetonitrile= 0.992 Recovery= 95.6% *xacetonitrile= 0.995 *Recovery= 91.8% B A b c a d e f f e d AB<1.5 c f e
Pressure Swing Distillation
Pressure Swing Distillation
Mixture AB: Determination AB azeotrope or AB ideal a heterogeneous
b
homogeneous
AB<1.5Pressure swing distillation c
xazeot constant, Tboiling<30°C
1- Chose entrainer candidates Ei for d e f
Computation azeotropes: AEi, BEi, ABEi
2- Residue curve map of ABEi
Topological stability: A, B, Ei, AB, AEi, BEi, ABEi
3- Feasibility rule cheking
Not match
match
4 - Batch distillation sequences 5- Simulation + Economic evaluation
CONCLUSIONS
Heterogeneous entrainers have a more privileged position than homogeneous. Higher number of ternary diagram match with feasible rules
Pressure swing distillation is a privileged option. It doesn’t involve additional entrainer. Simple performance in one or two batch distillation column operating at different pressures.
Heterogeneous entrainers in HABD: little amount of entrainer, separatrix can be crossed by the still path, simplest batch distillation sequence, more flexible reflux policy (entrainer-rich phase or both decanted phases)
Heterogeneous entrainers in HEBD: Complex ternary residue curves are feasibles, withdrawal of saddle binary heterazeotrope at the column top by feeding E at the top of the column , more flexible reflux policy as HABD Water seems a promising candidate for treatment organic wastes by HEBD and HABD. cheap, non toxic, non pollutant