(2) : :, α. α (3)., (3). α α (4) (4). (3). (1) (2) Antoine. (5) (6) 80, α =181.08kPa, =47.38kPa.. Figure 1.

Continuous Distillation Column Design Jungho Cho Department of chemical engineering, Dongyang university 1. ( ).... 2. McCabe-Thiele Method K-value. (1) : :, K-value.

(2) : :, α. α (3)., (3). α α (4) (4). (3). (1) (2) Antoine. (5) (6) 80, α =181.08kPa, =47.38kPa.. Figure 1.

1.0 Vapor Mole Fraction of Methanol 0.8 0.6 0.4 0.2 0.0 0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0 Liquid Mole Fraction of Methanol Figure 1 : (7). (7) : f :, f 5., Figure 2., ( ), (), (- ), (), ( )

.. Figure 2. Feed Feed plate Figure 2 : Cold liquid feed... f < 0".. Table 1.. Figure 3. Feed Feed plate Figure 3 : Saturated liquid feed.., f = 0". Table 1..

. -. Figure 4 Feed Feed plate Figure 4 : Vapor-liquid two phase feed. f 0 1.. (Table 1 ). Figure 5. Feed Feed plate Figure 5 : Saturated vapor feed. f = 1.. Figure 6.. f > 1. f = 2.

Feed Feed plate Figure 6 : Superheated vapor feed Table 1 : (a) (b) (c) (d) (e) Fraction Vaporized, ( f ) -1.0 0.0 0.5 1.0 2.0 Slope f - 1- f 2-1 0 0.5 Concentration, Mole fraction of Methanol Liquid x B Vapor y D 0.6995 0.8989 0.5000 0.7925 0.9545 0.0455 0.2075 0.5000 0.1011 0.3006 Feed condition Sub-cooled liquid Saturated liquid Two-phase Saturated vapor Superheated vapor 95mole%, 95mole%..,. Figure 7. Figure 7 (0.3385, 0.6615)..

1.0 Vapor Mole Fraction of Methanol 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0.0 0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0 Liquid Mole Fraction of Methanol Figure 7 : - (f = 0.5 ). (Rectifying section). Figure 8. V L plate n D x D V n+1 y n+1 L n x n Vn +1 = Ln + D Figure 8 :. Figure 8 (8) (8)

MaCable-Thiele... (?) (9). (9) Figure 8 (10). (10) (Reflux ratio). (11) (10) (11) (9). (12) : : Figure 7 Figure 9. Figure 9 (0.95, 0.95). y (0, 0.3385).. 1.8065..

1.0 Vapor Mole Fraction of Methanol 0.9 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0.0 0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0 Liquid Mole Fraction of Methanol Figure 9 : -, (f = 0.5 ) (Stripping section) Figure 10. Lm x m V y m+1 m+ 1 plate m B x B L = V + B Figure 10 :. Figure 10 (13)

(13) MaCable-Thiele... (?) (9). (14) Figure 10 (15). (15) (15) (14) (16). (16) (16) (0.4 0.6). Figure 11. Figure 11.. x. 7...... 1. Figure 12 4.5.

1.0 0.9 Vapor Mole Fraction of Methanol 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0.0 0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0 Liquid Mole Fraction of Methanol Figure 11 : 1.0 0.9 Vapor Mole Fraction of Methanol 0.8 0.7 0.6 0.5 0.4 0.3 0.2 0.1 0.0 0.0 0.1 0.2 0.3 0.4 0.5 0.6 0.7 0.8 0.9 1.0 Liquid Mole Fraction of Methanol Figure 12 :

3. PRO/II with PROVISION (Chemical Process Simulator). McCabe-Thiele. PRO/II. ASPEN PLUS. McCabe-Thiele -. Figure 13 Figure 15. Vapor Mole Fraction METHANOL 1.0 0.8 0.6 0.4 0.2 0.0 0.0 0.2 0.4 0.6 0.8 1.0 Liquid Mole Fraction METHANOL Figure 13 : - () Figure 13 ()..

. Figure 14 SRK -. Vapor Mole Fraction METHANOL 1.0 0.8 0.6 0.4 0.2 0.0 0.0 0.2 0.4 0.6 0.8 1.0 Liquid Mole Fraction METHANOL Figure 14 : - (SRK ) SRK..

Vapor Mole Fraction METHANOL 1.0 0.8 0.6 0.4 0.2 0.0 0.0 0.2 0.4 0.6 0.8 1.0 Liquid Mole Fraction METHANOL Figure 15 : - (NRTL ) NRTL - Figure 15. NRTL. NRTL -..,. 1.2bar 50mole%. Flash. PRO/II Flash Keyword. PRO/II Keyword Input Listing TITLE PROJECT=CLASS, PROBLEM=STEP1, USER=JHCHO, DATE=06/19/01 PRINT INPUT=ALL, FRACTION=M, PERCENT=M DIMENSION METRIC, TEMP=C, PRES=BAR SEQUENCE PROCESS COMPONENT DATA LIBID 1,METHANOL/2,WATER THERMODYNAMIC DATA METHOD SYSTEM=NRTL STREAM DATA PROPERTY STREAM=1, TEMPERATURE=25, PRESSURE=1.2, PHASE=M, & RATE(M)=100, COMPOSITION(M)=1,50/2,50 UNIT OPERATIONS FLASH UID=F01 FEED 1 PRODUCT M=2 TPSPEC SPEC STREAM=2, VFRAC, VALUE=0.5 END PRO/II Keyword Output Summary FLASH ID F01

NAME FEEDS 1 PRODUCTS MIXED 2 VAPOR LIQUID TEMPERATURE, C 81.973 PRESSURE, BAR 1.200 PRESSURE DROP, BAR 0.000 MOLE FRAC VAPOR 0.50000 MOLE FRAC LIQUID 0.50000 DUTY, M*KCAL/HR 0.54611 FLASH TYPE SPEC-P PRO/II 50% 81.973. SHORTCUT. PRO/II Keyword Input Listing TITLE PROB=STEP2,PROJ=CLASS,USER=Dr_JHCHO DIME METRIC,PRES=BAR,TEMP=C PRINT INPUT=ALL,RATE=M,PERC=M COMP DATA LIBID 1,METHANOL/2,WATER THERMO DATA METHODS SYSTEM=NRTL STREAM DATA PROP STRM=1,TEMP=81.973,PRES=1.2,RATE=100,COMP=1,50/2,50 UNIT OPERATIONS DATA SHORCUT UID=S01 FEED 1 PROD STREAM=2,PRES=1.05,RATE=50 PROD STREAM=3,PRES=1.30 COND TYPE=TFIX,TEMP=45 EVAL MODEL=CONV,KEYL=1,KEYH=2 SPEC STREAM=2,COMP=2,PERC,VALUE=5 SPEC STREAM=3,COMP=1,PERC,VALUE=5 END PRO/II Keyword Output Summary ------------- TOTAL STREAM RATES ------------- MOLES WEIGHT LIQUID VOL NORM VAPOR NUM STREAM + PHASE KG-MOL/HR KG/HR M3/HR M3/HR SECTION TRAYS -------------- ---------- ---------- ---------- ---------- ------- ----- 2 L 50.00 1566.92 1.96 1120.67 1 3.85 3 L 50.00 935.93 0.96 1120.73 TOTALS 100.00 2502.85 2.92 2241.40 3.85

PRO/II 3.85. 4.85. 4.5. NRTL.. Figure 16.... ( 1) ( 2). 100x10 3 Total Costs = (1) + (2) Annual Costs, $ 80x10 3 60x10 3 40x10 3 20x10 3 Annual Operating Costs (2) Initial Capital Costs (1) 0 1.0 1.2 1.4 1.6 1.8 2.0 Reflux Ratio Figure 16 : Utility.. SHORTCUT. - SHORTCUT Table 2 Figure 17. Table 2 : SHORTCUT (PRO/II )

16 14 Number of Stages 12 10 8 6 4 2 Utility Consumptions 0 0 1 2 3 4 Reflux Ratio Figure 17 : - Utility Figure 16 ( ) 1.2. - Figure 17 1.15 8. 8 7 1. 8 95mole% 95mole% Rigorous R/R min Number of Condenser Total Utility Reflux Ratio Reboiler Duty Tray Duty Costs 1.00 0.940 - - - 1.05 14.96 0.777-7.923x10-1 3.338x10-1 1.1261 1.10 11.36 0.814-8.088x10-1 3.503x10-1 1.1591 1.50 8.10 1.109-9.407x10-1 4.822x10-1 1.4229 2.00 6.73 1.479-1.106x10 0 6.471x10-1 1.7531 2.50 6.14 1.849-1.271x10 0 8.120x10-1 2.0830 5.00 4.95 3.698-2.095x10 0 1.637x10 0 3.7320 3.85 - - - Simulation. 8 PRO/II Rigorous Simulation Keyword Input.

PRO/II Keyword Input Listing TITLE PROJECT=CLASS, PROBLEM=STEP2, USER=Dr_JHCHO, DATE=06/25/01 PRINT INPUT=ALL, RATE=M, PERCENT=M DIMENSION METRIC, TEMP=C, PRES=BAR SEQUENCE PROCESS COMPONENT DATA LIBID 1,METHANOL/2,WATER THERMODYNAMIC DATA METHOD SYSTEM=NRTL STREAM DATA PROPERTY STREAM=1, TEMPERATURE=81.973, PRESSURE=1.2, PHASE=M, & RATE(M)=100, COMPOSITION(M)=1,50/2,50 UNIT OPERATIONS COLUMN UID=T01 PARAMETER TRAY=8,IO=100 DAMPING=0.4 FEED 1,4 PRODUCT OVHD(M)=2,50, BTMS(M)=3, SUPERSEDE=ON CONDENSER TYPE=TFIX, PRESSURE=1.05, TEMPERATURE=45 DUTY 1,1/2,8 PSPEC PTOP=1.2, DPCOLUMN=0.1 PRINT PROPTABLE=PART ESTIMATE MODEL=CONVENTIONAL SPEC STREAM=2,PCT, COMP=2,WET, VALUE=5 SPEC STREAM=3,PCT, COMP=1,WET, VALUE=5 VARY DUTY=1,2 END PRO/II Keyword Output Summary COLUMN SUMMARY ---------- NET FLOW RATES ----------- HEATER TRAY TEMP PRESSURE LIQUID VAPOR FEED PRODUCT DUTIES DEG C BAR KG-MOL/HR M*KCAL/HR ------ ------- -------- -------- -------- --------- --------- ------------ 1C 45.0 1.05 114.4 50.0L -1.4704 2 70.8 1.20 119.8 164.4 3 73.0 1.22 117.2 169.8 4 76.8 1.23 165.5 167.2 100.0M 5 78.0 1.25 164.3 115.5 6 80.9 1.27 161.1 114.3 7 88.2 1.28 156.1 111.1 8R 99.5 1.30 106.1 50.0L 1.0119 STREAM ID 1 2 3 NAME PHASE MIXED LIQUID LIQUID FLUID MOLAR PERCENTS 1 METHANOL 50.0000 95.0000 5.0000 2 WATER 50.0000 5.0000 95.0000

TOTAL RATE, KG-MOL/HR 100.0000 50.0001 49.9999 4. ASPEN PLUS PRO/II ASPEN PLUS -. PRO/II 1.2bar 50mole%. PRO/II Keyword Graphic. Figure 17 Figure 23. Figure 17 Flash drum Stream number. Step1.bkp. Figure 17 : Flowsheet of Two-phase Flash

Figure 18 : Setup Specification Figure 18 Setup specification'.. Component specification' Next button. Figure 19 : Component Specification Figure 19 Component specification'.. Property specification' NRTL.

Figure 20. Figure 20 : Property Specification Figure 21 : Stream Specification,,. Figure 21., Requied Input Incomplete"..,. Next button.

Figure 22 : Block Specification Figure 22 1.2bar Vapor fraction 0.5.. ASPEN PLUS. 1.2bar 50mole%(0.5fraction) 82.074 PRO/II 81.973. Figure 23 : Flash Calculation Simulation Results

. PRO/II Shortcut' ASPEN PLUS DSTWU'. Figure 24 : Flowsheet of DSTWU for the separation of methanol-water

Figure 25 : Block specification fot DSTWU Figure 25 PRO/II Shortcut 1.05bar 1.30bar, 0.95 0.05. Reflux ratio -1.05. Inpt Changed' Step1.bkp.. Figure 26 : DSTWU Modeling Results Figure 26 PRO/II Shortcut. ASPEN PLUS 4.45 PRO/II 3.85.

ASPEN PLUS PRO/II. PRO/II Sub-cooled type ASPEN PLUS Bubble type.. ASPEN PLUS Table 2 Table 3. Table 3 : DSTWU Case Study Results using ASPEN PLUS Table 3 Figure 27. R/R min Number of Condenser Total Utility Reflux Ratio Reboiler Duty Tray Duty Costs 1.00 0.798 - - - 1.05 25.00 0.837-0.7797 0.3442 1.1239 1.10 15.33 0.877-0.7976 0.3621 1.1597 1.50 8.64 1.196-0.9357 0.5001 1.4358 2.00 7.29 1.595-1.1069 0.6713 1.7782 2.50 6.39 1.949-1.2785 0.8429 2.1214 5.00 5.47 3.988-2.1334 1.6978 3.8312 4.45 - - - Figure 27 : - Utility (ASPEN PLUS)

Figure 27 Figure 17 Number of Stages 16 14 12 10 8 6 4 2 0 0 1 2 3 4 Reflux Ratio Utility Consumptions 1.15 8. Rigorous Modeling. PRO/II COLUMN ASPEN PLUS RADFRAC. Figure 28 Figure??. Model library Radfrac Stream Figure 28. Block option Figure 29 Figure 37.

Figure 28 : Flowsheet of RADFRAC for the separation of methanol and water Figure 29 : Block specification (1) : Configuration Figure 29 PRO/II 8 Total condenser Top Distillate Rate 50Kmol/hr 2.3..

Figure 30 : Block specification (2) : Streams Figure 31 : Block specification (3) : Pressure Profile Figure 31. Bubble condenser. Condenser. Figure 32.

Figure 32 : Block specification (4) : Condenser Temperature Specification. 95mole% 95mole%. Figure 33 Figure??. Figure 33 : Block specification (5) : Design specification (1)

Figure 34 : Block specification (6) : Design specification (2) Figure 35 : Block specification (7) : Design specification (3) Heavy Key Component 0.05.

Figure 36 : Block specification (8) : Variable (1) Light Key Component 0.05 Distillate Rate. Figure 37 Figure 39. Figure 37 : RADFRAC Modeling Results (1)

Figure 38 : RADFRAC Modeling Results (2) Figure 39 : RADFRAC Modeling Results (3) 5. - McCabe-Thiele PRO/II ASPEN PLUS..

PRO/II ASPEN PLUS.