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3 TITLE 'Dew Pressure Calculation for the Condenser Pressure' IN-UNITS ENG DEF-STREAMS CONVEN ALL DESCRIPTION " General Simulation with English Units : F, psi, lb/hr, lbmol/hr, Btu/hr, cuft/hr. Property Method: None Flow basis for input: Mole Stream report composition: Mole flow " DATABANKS PURE10 / AQUEOUS / SOLIDS / INORGANIC / & NOASPENPCD PROP-SOURCES PURE10 / AQUEOUS / SOLIDS / INORGANIC COMPONENTS C2 C2H6 / C3 C3H8 / NC4 C4H10-1 FLOWSHEET BLOCK DEW IN=1 OUT=2 3 PROPERTIES RK-SOAVE STREAM 1 SUBSTREAM MIXED TEMP=130. VFRAC=0. MOLE-FLOW=1. MOLE-FRAC C / C / NC BLOCK DEW FLASH2 PARAM TEMP=130. VFRAC=1. TITLE PROJECT=DISTILLATION, PROBLEM=DEWP, USER=JHCHO, DATE=08/28/00 PRINT INPUT=ALL SEQUENCE PROCESS COMPONENT DATA LIBID 1,C2/2,C3/3,NC4 THERMODYNAMIC DATA METHOD SYSTEM=SRK STREAM DATA PROPERTY STREAM=1, TEMPERATURE=100, PRESSURE=300, PHASE=M, & RATE(M)=100, COMPOSITION(M)=1,13.27/2,84.51/3,2.22 UNIT OPERATIONS FLASH UID=F01 FEED 1 PROD V=1V, L=1L DEW TEMP=130 END

4 Mole Fraction Property Model Methanol in Bottoms Ideal/Raoult's Law 800 ppm RK-Soave 10 ppm NRTL (with BIP's) 152 ppm

5 Vapor Mole Fraction METHANOL Liquid Mole Fraction METHANOL Vapor Mole Fraction METHANOL Liquid Mole Fraction METHANOL

6 Vapor Mole Fraction METHANOL Liquid Mole Fraction METHANOL

7 φ φ φ φ φ φ φ γ

8 φ γ γ γ γ γ

9 γ γ Unstable A = 0.0 A = 0.5 A = 1.0 A = 2.0 A = 3.0 Pressure (kpa) x 1, y 1

11 90 80 Pressure (kpa) Sub-cooled Liquid positive negative 40 ideal Super-heated Vapor x 1, y 1

13 φ

16 Component Methyl Chloride T c (K) P c (atm) 65.9 R T (K) 322

18 ω α

19 α ω ω α α ω ω

20 Equation u w Zc van der Waals Redlich-Kwong SRK Peng-Robinson

21 α α ω ω

22 Alpha Value for Hydrogen Reduced Temperature of Hydrogen

23 Pressure, MPa Mole Fraction of Carbon Dioxide α Soave (1972) α Peng-Robinson (1980) α Soave (1979) α Boston-Mathias (1980) α α Twu (1988) Twu-Bluck-Cunningham (1990)

25 Porperty Method Equation of State Mixing Rule PRMHV2 Peng-Robinson Huron Vidal PRWS Peng-Robinson Wong Sandler PSRK Peng-Robinson Holderbaum Gmehling RK-ASPEN Redlich-Kwong-Soave Mathias RKSMHV2 Redlich-Kwong-Soave Huron Vidal RKSWS Redlich-Kwong-Soave Wong Sandler SR-POLAR Redlich-Kwong-Soave Schwartzentruber Renon

26 2 0. Activity of Component M le o F car n iot o mo Cf nenop 1t

27 Activity Coefficient of each components γ mo C id u iq L sop n ioti x, γ γ

28 Mixing pure A and B gases Vaporization of liquid A and B into gases Condensation of gaseous mixture into liquid solution Pure A Pure B Directly mixing process Liquid solution A + B

29 γ γ α α β β β α α β α β

30 Obtained from Obtained from regression vdw EOS System α β α β Acetaldehyde-water Acetone-methanol Acetone-water

31 Λ γ Λ Λ Λ

36 τ τ α τ α α γ τ τ τ α

37 α Mole Percent of Ethanol 0 01 M 02 le o 03 ep 04 necr 05 ot eneznebf Mole Percent of Ethanol M 02 le o 03 ep 04 necr 05 ot eneznebf

38 Φ θ Φ θ τ τ Φ θ γ γ γ γ Φ θ θ Φ Φ γ θ τ θ τ θ τ

41 γ

42 Temperature ( o C ) Mole Fraction of Water Temperature ( o C ) Mole Fraction of Water

44 4 Liquid Phase Activity Coefficients Mole Fraction of Acetic Acid 2.0 Vapor -phase Fugacity Coefficients Vapor Composition of Acetic Acid

45 20 Pressure 40 bar P-xy of ETHANE PROPYLEN Mole fraction ETHANE

(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).