Separation Process Principles on COCO/ChemSep 化学プロセスシミュレータ

Separation Process Principles on COCO/ChemSep

based on Henley, Seader, Roper: Separation Process Principles, Third edition, Wiley (2011).

(p. 160) EXAMPLE 4.1 Phase Conditions of a Process Stream. (4成分系フラッシュ蒸留)

---Calculate that pressure using the following composition, activity coefficients, and vapor pressures:

(p. 162) EXAMPLE 4.4 Distillation column operating pressure. (プロピレン／ブテン系フラッシュ蒸留)

Propylene is separated from 1-butane by distillation into a vapor distillate containing 90mol% propylene. Calculate the column pressure if the partial condenser exit temperature is 100F----

(p. 163) EXAMPLE 4.5 Adiabatic Flash of the Feed to a Distillation Column. (メタン／ベンゼン系フラッシュ蒸留)

-- Calculate the percent molar vaporization of the feed and compositions of the vapor and liquid if the pressure is decreased adiabatically from 485 to 165 psia ---

(p. 164) EXAMPLE 4.6 Single-Stage Extraction of Acetic Acid. (メチルイソブチルケトンによる酢酸の抽出)

Methyl isobutyl ketone (C) is used as a solvent to remove acetic acid (B) from -- water (A)---estimate the kg/h of solvent for a single equilibrium stage.

(p. 167) EXAMPLE 4.7 Single-Equilibrium Stage Extraction Using Diagrams. (フルフラールによるエチレングリコールの抽出)

Determine extract and raffinate compositions when a 45wt% glycol (B)-55wt% water (A) solution is contacted with twice its weight of pure furfural solvent (C) at 25°C and 101 kPa.

(p. 171) EXAMPLE 4.8 Liquid-Liquid Equilibrium for a Four-Component Mixture. (水／アセトン／イソプロパノール／酢酸エチル系液液平衡)

Estimate the amounts of the phases in kg/h and the equilibrium phase compositions ---

(p. 177) EXAMPLE 4.13 Absorption of CO2 with Water. (水による二酸化炭素の吸収・放散)

The CO2 is vented at the top of the mountain --- calculate the amount of water --

(p. 178) EXAMPLE 4.14 Equilibrium Diagram for Air-NH3-H2O at 20C and 1 atm. (アンモニア／空気／水系の平衡)

-- If 10 mol of gas of Y=0.3 are contacted with 10 mol of solution of X=0.1, what are the compositions of the resulting phases? ----

(p. 200) EXAMPLE 5.2 Extraction with Different Cascade Arrangements. (ジオキサンのベンゼンによる抽出)

-- A feed of a 25% solution of p-dioxane in water is to be separated with benzene. ---

(p. 203) EXAMPLE 5.3 Absorption of Hydrocarbons by Oil. (炭化水素ガスの吸収)

-- the heavier components in a superheated hydrocarbon gas are to be removed by absorption with a high-molecular -weight oil.

(p. 223) Chapter 6, Industrial Example ( Acetone vapor absorption by water). (アセトン蒸気の水による吸収)

--30-trey absorber is to recover the acetone by contacting the gas with a suitable absorbent, water. --

(p. 234) EXAMPLE 6.1 Recovery of Alcohol. (エタノール蒸気の水による吸収)

A CO2-rich vapor with a small amount of ethyl alcohol is evolved. The alcohol is recovered by absorption with water in a sieve-tray tower. --

-- the stripping by air of volatile organic compounds (VOCs) from wastewater. ---

Performance data, given below for a trayed absorber --, were reported. -- Based on the these data, back-calculate the overall stage efficiency--

(p. 255) EXAMPLE 6.10 Absorption of SO2 in a Packed Column. (SO2の水による吸収)

Air containing 1.6% by volume SO2 is scrubbed with pure water in a packed column -----

(p. 256) EXAMPLE 6.11 Absorption of Ethylene Oxide. (酸化エチレンの水による吸収)

A gaseous reactor effluent of 2 mol% ethylene oxide in a inert gas is scrubbed with water at 30°C and 20 atm. -----

(p. 261) EXAMPLE 6.13 Flooding, Pressure Drop, and Diameter. (アンモニアの水による吸収)

Forty lb mol/h of air containing 5 mol% NH3 enters a packed column at 20°C and 1 atm, where 90% of the ammonia is scrubbed by a countercurrent flow of 3000 lb/h of water. -----

(p. 270) EXAMPLE 6.16 NTU for a Packed Column with Concentrated Solute. (アンモニアの水による吸収)

To remove 95% of the ammonia from an air stream containing 40% ammonia by volume, 488 lbmol/h of absorbent per 100 lbmol/h of entering gas are used -----

(p. 281) Chapter 7, Industrial Example: Distillation of a binary mixture of benzene and toluene. (ベンゼン／トルエン系蒸留)

(p. 291) EXAMPLE 7.1 Distillation of a Mixture of Benzene and Toluene. (ベンゼン／トルエン系蒸留)

Four hundred and forty lbmol/h (204 kmol/h) of a mixture of 60 mol% benzene (LK) and 40 mol% toluene (HK) is to be separated into a liquid distillate and a liquid bottoms product of 95 mol% and 5 mol% benzene, respectively. ------

(p. 295) EXAMPLE 7.3 McCabe-Thiele Methd for a Column with Only a Feed Plate. (ヘキサン／オクタン系蒸留)

Solve Example 7.2: (a) graphically, assuming that the feed is introduced on plate 1----

(p. 299) EXAMPLE 7.4 McCabe-Thiele Method for a Very Sharp Separation. (ベンゼン／トルエン系蒸留)

Repeat part (c) of Example 7.1 for benzene distillate and bottoms purities of 99.9 and 0.1 mol%, respectively. ------

(p. 324) Chapter 8, Industrial Example. (酢酸の酢酸エチルによる抽出)

A feed of 30,260 lb/h of 22 wt% acetic acid in water is sent to a single-section extraction column operating at ambient conditions, where it is contacted with 71,100 lb/h of ethyl-acetate solvent. ------

(p. 342) EXAMPLE 8.1 Equilibrium Stages for Extraction. (アセトンの水による抽出)

Acetone is to be extracted from a 30 wt% acetone (A) and 70 wt% ethyl acetate (C) feed at 30°C, using pure water (S) as the solvent ------

(p. 382) EXERCISE 8.11. Extraction of acetone by trichloroethane. (アセトンのトリクロロエタンによる抽出)

One thousand kg/h of a 45 wt% acetone-in-water solution is to be extracted at 25°C in a continuous, countercurrent system with pure 1,1,2-trichloroethane to obtain a raffinate containing 10 wt% acetone.----

(p. 382) EXERCISE 8.13. Extraction of isopropanol with water. (イソプロピルアルコールの抽出)

A distillate of 45 wt% isopropyl alcohol, 50 wt% diisopropylether, and 5 wt % water is obtained from an isopropyl alcohol finishing unit. The ether is to be recovered by liquid-liquid extraction with water, the solvent, entering the top and the feed entering the bottom, ------

(p. 392) EXAMPLE 9.1 - 9.7. Debutanizer. (C4-C9炭化水素の蒸留　脱ブタン塔)

The multicomponent hydrocarbon feed in Figure 9.2 is typical of the feed to the recovery section of an alkylation plant in a petroleum refinary. ---

Sulfur dioxide and butadienes (B3 and B2) are to be stripped with nitrogen from the liquid stream given in Figure 9.15 ---

(p. 406) EXERCISE 9.1 Type of condenser and operating pressure. (プロピオン酸の蒸留)

A mixture of propionic and n-butyric acids is to be separated by distillation into a distillate containing 95 mol % propionic acid and a bottoms of 98 mol% n-butyric acid. --

(p. 406) EXERCISE 9.2 Type of condenser and operating pressure. (C1-C5炭化水素の蒸留　2塔プロセス)

Two distillation columns are used to produce the produce the products indicated in Figure 9.19. Establish the type of condenser and an operating pressure --

(p. 406) EXERCISE 9.4 Stages for a deethanizer. (C1-C5炭化水素蒸留　脱エタン塔)

For the deethnizer in Figure 9.21, use the Fenske equation to determine Nmin ---

(p. 406) EXERCISE 9.5 Fenske equation for a column with a vapor sidestream. (ベンゼン／トルエン系蒸留)

For the complex distillation in Figure 9.22, use the Fenske equation to determine Nmin ---

(p. 407) EXERCISE 9.6 Comparison of Fenske equation with McCabe-Thiele method. (アセトン／水系蒸留)

A 25 mol% mixture of acetone (A) in water (W) is to be separated by distillation at 130 kPa into a distillate containing 95 mol% acetone and a bottoms of 2 mol% acetone ---Calculate Mmin by the Fenske equation. --

(p. 407) EXERCISE 9.7 Distribution of nonkeys and minimum stages. (C3-C8炭化水素の蒸留)

For the distillation in Figure 9.23, calculate Nmin and the distribution of the nonkey components by the Fenske equation --

(p. 407) EXERCISE 9.8 Type of condenser, operating pressure, nonkey distribution, and Nmin. (C1-C4炭化水素の蒸留)

For the distillation in Figure 9.24, calculate Nmin and the distribution of the nonkey components. --

(p. 407) EXERCISE 9.9 Type of condenser, operating pressure, nonkey distribution, and Nmin. (C2-C6炭化水素の蒸留)

For the distillation in Figure 9.24, calculate Nmin and the distribution of the nonkey components. --

(p. 408) EXERCISE 9.16 FUG method for HC distillation. (C2-C7炭化水素の蒸留)

The hydrocarbon feed to a distillation column is a bubble point liquid at 300 psia with mole fractions: C2=0.08, C3=0.15, nC4=0.2, nC5=0.27, nC6=0.2,,, and nC7=0.10.--

(p. 408) EXERCISE 9.17 FUG method for HC distillation. (C3-C5炭化水素の蒸留)

The following feed mixture is to be separated by ordinary distillation at 120 psia to obtain 92.5 mol% of the nC4 in the liquid distillate and 82.0 mol% of the iC5 in the bottoms.

(p. 408) EXERCISE 9.18 FUG method for a chlorination effluent. (塩素化生成物の蒸留)

Consider the separation by distillation of a chlorination effluent to recover C2H5Cl. ----

(p. 408) EXERCISE 9.22 Effect of N and operating pressure on absorption. (炭化水素ガスの吸収)

Determine, by the Kremser method, the achievable separation for the absorber in Figure 9.26 -------

(p. 408) EXERCISE 9.23 Effect of N on absorption of a paraffin mixture. (炭化水素ガスの吸収)

One thousand kmol/h of rich gas at 70°F with 25% C1, 15% C2, 25% C3, 20% nC4, and 15% nC5 by mols is to be absorbed by 500 kmol/h of nC10 at 90°F in an absorber at 4 atm. -------

(p. 409) EXERCISE 9.26 Extraction of a HC mixture by DEG. (グリコールによるC6-C7炭化水素の抽出)

One hundred kmiol/h of an equimolar mixture of benzene (B), toluene (T), n-hexane (C6), n-heptane (C7) is to be extracted at 150 by 300 kmol/h of diethylene glycol (DEG) on a countercurrent, liquid-liquid extractor having five equilibrium stages. -----

(p. 417) EXAMPLE 10.1 First Iteration of the BP Method. (C3-C5炭化水素の蒸留)

Calculate stage temperatures, interstage vapor and liquid flow rates and compositions, reboiler duty, and condenser duty by the BP method for the column specifications given in Figure 10.8.

Calculate stage temperatures and interstage vapor and liquid flow rates and compositions by SR method for the absorber specifications in Figure 5.11.

The separation of benzene (B) from n-heptane --- liquid-liquid extraction with a mixture of dimethylformamide (DMF) and water can be used. ---

(p. 446) EXERCISE 10.37. Absorption of a hydrocarbon gas. (炭化水素ガスの吸収)

Calculate product rates and compositions, stage temperatures, and interstage vapor and liquid flow rates and compositions for an absorber having four equilibrium stages with the specifications in Figure 10.37. Assume the oil is nC10.

(p. 467) EXAMPLE 11.5 Pressure-Swing Distillation. (圧力スイング蒸留　エタノール／ベンゼン系)

Ninety mol/s of a mixture of 2/3 by mols ethanol and 1/3 benzene -- is to be separated--- Apply the sequence shown in Figure 11.23b with the first column operating ar 30 kPa ---The distillate is sent to the second column, which as a top tray pressure of 106 kPa---

(p. 475) Chapter 11.6 HETEROGENEOUS AZEOTROPIC DISTILLATION. (エタノール／水系共沸蒸留（ベンゼン溶剤）)

Ethanol-water-benzene heterogeneous azeotropic distillation with two columns and a decanter.

Use REATEFRAC to predict column profiles for a 3.5-fr-diameter, 20-bubble-cap tray absorber operating at the conditions in Table 12.4.

A feed of 44,090 lb/h of an aqueous solution containing 8 wt% colloids is to be concentrated to 45 wt% colloids in a triple-effect-evaporator system using forward feed.---