Fondamenti delle operazioni unitarie dell'industria chimica - Diagrammi e tabelle 2015

Transcription

1 a. Water (A) Glycerol (B) System P ¼ 11.3 kpa Data of Chen and Thompson, J. Chem. Eng. Data, 15, 471 (197) Temperature, C y A x A a A,B b. Methanol (A) Water (B) System P ¼ 11.3 kpa Data of J.G. Dunlop, M.S. thesis, Brooklyn Polytechnic Institute (1948) Temperature, C y A x A a A,B c. Para-xylene (A) Meta-xylene (B) System P ¼ 11.3 kpa Data of Kato, Sato, and Hirata, J. Chem. Eng. Jpn., 4, 35 (197) Temperature, C y A x A a A,B

2 a. Methanol (A) Water (B) System T ¼ 5 C Data of McGlashan and Williamson, J. Chem. Eng. Data, 21, 196 (1976) Pressure, psia y A x A a A,B b. Methanol (A) Water (B) System T ¼ 15 C Data of Griswold and Wong, Chem. Eng. Prog. Symp. Ser., 48(3), 18 (1952) Pressure, psia y A x A a A,B c. Methanol (A) Water (B) System T ¼ 25 C Data of Griswold and Wong, Chem. Eng. Prog. Symp. Ser., 48(3), 18 (1952) Pressure, psia y A x A a A,B

3 Temperature, C 1 9 Saturated vapor 8 7 Saturated liquid Mole fraction of methanol in liquid, x, or vapor, y (a) Mole fraction of methanol in vapor. 1 Mole fraction of methanol in liquid (b) 2 System pressure, psia Mole fraction of methanol in liquid (c) Vapor liquid equilibrium conditions for the methanol water system: (a) T y x diagram for 1 atm pressure; (b) y x diagram for 1 atm pressure; (c) P x diagram for 15 C. 1 Mole fraction of component in vapor, y α 1,2 = y A ¼ a A;B x A 1 þ x A ða A;B 1Þ 275 H Mole fraction of component 1 in liquid, x 25 G Vapor Temperature, F D E B F Saturated vapor C Temperature, C 175 Saturated liquid 79.4 Liquid A Mole fraction n-hexane, x or y

4 Pressure, torr Total pressure Partial pressure of isopropyl ether P 1 Partial pressure of alcohol P 2 isopropyl Mole fraction isopropyl ether in liquid phase, x Pressure, kpa Mole fraction isopropyl ether in vapor phase, y Equilibrium line Reference line, y 1 = x 1 Mole fraction isopropyl ether in liquid phase, x 1 (a) (b) Temperature, C Vapor Dew-point line Vapor + liquid Bubble-point line Liquid Minimum-boiling-point azeotrope, isopropyl ether isopropyl alcohol system: (a) partial and total pressures at 7 C; (b) vapor liquid equilibria at 11 kpa; (c) phase diagram at 11 kpa. [Adapted from O.A. Hougen, K.M. Watson, and R.A. Ragatz, Chemical Process Principles. Part II, 2nd ed., John Wiley & Sons, New York (1959).] 5 Mole fraction isopropyl ether (c) 1 atm Pressure, torr Total pressure Partial pressure u e Partial press r of acetone p 1 of chloro f rm p 2 Mole fraction acetone in liquid phase, x 1 o Pressure, kpa Mole fraction acetone in vapor phase, y Equilibrium line Reference line, y 1 = x 1 Mole fraction acetone in liquid phase, x 1 y ethyl alcohol 45 line Equilibrium x ethyl alcohol Equilibrium curve for n-hexane/ethanol. (a) (b) Temperature, C Vapor Dew-point line Bubble-point line Vapor + liquid Liquid Mole fraction acetone (c) Maximum-boiling-point azeotrope, acetone chloroform system: (a) partial and total pressures at 6 C; (b) vapor liquid equilibria at 11 kpa; (c) phase diagram at 11 kpa pressure. [Adapted from O.A. Hougen, K.M. Watson, and R.A. Ragatz, Chemical Process Principles. Part II, 2nd ed., John Wiley & Sons, New York (1959).] 4

5 5

6 S.9 Phase envelope Wt fraction S Tie line Extract x C =.3 x C = x C =.1 x C = A 1 Wt fraction C.3 x C =.5 x C = M.1 x C = x C =.9 C.1 x C =.7 x C = Plait point A F A Raffinate 6

7 Ethylene Glycol (B) Mass fraction ethylene glycol.7 Plait Point P Miscibility boundary.3 Mass fraction water.5 R.3 Extract Tie line Raffinate.7 M.1 E.9 Furfural (C) D Mass fraction furfural (a) G Water (A) Mass fraction glycol R Raffinate P Mass fraction furfural (b) M Extract E Mass fraction glycol in extract P E R Mass fraction glycol in raffinate (c) 45 Line Liquid liquid equilibrium, ethylene glycol furfural water, 25 C, 11 kpa: (a) equilateral-triangular diagram; (b) right-triangular diagram; (c) equilibrium solute diagram in mass fractions; (continues ) 7

8 Glycol/furfural in extract E Glycol/water in raffinate (d) R P Mutual Equilibrium (Tie-Line) Data for the Furfural Ethylene Glycol Water System at 25 C and 11 kpa Glycol in Water Layer, wt% Glycol in Furfural Layer, wt% Furfural/(glycol + water) M R P Tie lines Glycol/(glycol + water) (d) equilibrium solute diagram in mass ratios; (e) Janecke diagram. (e) E Equilibrium Miscibility Data in Weight Percent for the Furfural Ethylene Glycol Water System at 25 C and 11 kpa Furfural Ethylene Glycol Water

9 9

10 6 4 2 NH Values of, mole fraction per atmosphere H Cl 2 SO 2 H 2 S CO 2 Cl 2 Br 2 H 2 S C 2 H 4 4 CH 4 C 2 H 6 2 CO 1 5 O 2 H 2 N Temperature, C Henry s law constant for solubility of gases in water [Adapted from O.A. Hougen, K.M. Watson, and R.A. Ragatz, Chemical Process Principles. Part I, 2nd ed., John Wiley & Sons, New York (1954).] 1

11 x B, Mass solute/mass of liquid F Overflow Tie line V M U S x A, Mass of solid/mass of liquid Underflow (a) x B, Mass solute/mass of liquid F Overflow Underflow Tie line V M U S x A, Mass of solid/mass of liquid (b) Figure 4.2 Underflow overflow conditions for ideal leaching: (a) constant-solution underflow; (b) variable-solution underflow. Solid feed, F Insoluble A Solute B Liquid solvent, S C MIXER-SETTLER Overflow, V Liquid B, C Liquid B, C Underflow, U Solid A 11

12 1 Experimental data of Yarborough N 2 S R K correlation Temperature 25 F C 1 1 CO 2 C 2 H 2 S K-value C 3 nc 5.1 Toluene nc 7 nc , Pressure, psia 12

13 .9 y = 1 x Mole fraction propane in gas, y Equilibrium S, g solid Gas in F = (A + P) = 2 mmol z F = P/ (A + P) =.5 x* =.365 y* = 35 S, g solid x* = P/(P + A) W = P + A =1 mmol Stage Gas out G = (A + P) = 1 mmol y* = P/ (P + A) Mole fraction propane in adsorbate, x (a) 2.3 mmole adsorbate/g adsorbent 2. x* x 1.7 x 1.6 y y y* y y Mole fraction propane in adsorbate, y, x (b) Figure 4.29 Adsorption equilibrium at 25 C and 11 kpa of propane and propylene on silica gel. [Adapted from W.K. Lewis, E.R. Gilliland, B. Chertow, and W. H. Hoffman, J. Am. Chem. Soc, 72, 1153 (195).] 13

14 14

15 15

16 16

17 17

18 18

19 19

20 2

21 21

22 Pressure, bar Solid Liquid Supercritical Triple point Gas Critical point fluid region Temperature, K Concentration of solute in gas phase, g/l K Pressure, MPa Effect of pressure on solubility of picb in supercritical ethylene. 22

23 C 2 H 5 OH H 2 O CO 2 Figure Liquid fluid equilibria for CO 2 C 2 H 5 OH H 2 Oat K and MPa. Critical Critical Critical Temperature, Pressure, Density, Solvent K MPa kg/m 3 Methane Ethylene Carbon dioxide Ethane Propylene Propane Ammonia Water