Isopropyl ether data

Two studies have been performed by Littler on the oxidation of cyclohexanol by Hg(II), the second leading to more detailed and reliable data. The reaction is first-order in both oxidant and substrate but the rate is independent of acidity. E is 24.8 kcal.mole AS is 1 eu, Ath/Acd is 3.0 and ko ol HzO 1-30-At 50 °C di-isopropyl ether is attacked at about one-half the rate of isopropanol, which implies that hydride ion abstraction is occurring in both cases. This is supported in the case of cyclohexanol by the isotope effects. 

Example 10.3 A feed with a flowrate of 1000 kg-h 1 contains 30% acetic acid by mass in aqueous solution. The acetic acid (AA) is to be extracted with isopropyl ether to produce a raffinate with 2% by mass on a solvent-free basis. Equilibrium data are given in Table 10.11,8. 

A batch process produces 5 t of aqueous waste containing 25% wt acetic acid. The acetic acid is to be recovered by extraction with isopropyl ether. Equilibrium data are given in Table 10.1. 

Class 4 solvents, for which no adequate data were found, include di-isopropyl ether, methyltetrahydrofuran and isooctane. 

Fig. 8. Dependence of C-solvent strength ( on coverage of adsorbent surface 0. Mixtures A/C of nonpolar solvent A and polar localizing solvent C , isopropanol/hexane/silica , acetone/hexane/silica , ethyl ether/hexane/silica/ V, ethyl ether/pentane/silica O, isopropyl ether/pentane/alumina. Data taken from Snyder and Glujch (14) and Hara et al. (25). Curves through data are best fit to Eqs. (12) and (40).

A 1000 kg/hr stream of a solution containing 30 wt% acetic acid and 70 wt% water is to be fed to a countercurrent extraction process. The solvent is 99% isopropyl ether and 1% acetic acid, and has an inlet flowrate of 2500 kg/hr. The exiting raflflnate stream should contain 10 wt% acetic acid. The equilibrium data are the same as given in Table 5.1 for the cross-flow Example 5.1. Find the number of equilibrium-limited stages required. 

LLE Data for Acetic Acid (A), Water(W), and Isopropyl Ether (E)... 

FIGURE 10.2 Liquid-liquid data for the system water, acetic acid, and isopropyl ether. Since mixture M falls inside the mumal soluhihty curve, it separates into extract and raffinate phases with compositions E and R, respectively. The equUihrium data are at 25°C and 1 atm. 

FIGURE 10.5 Liquid-liquid data at 25°C for the system water, acetic acid, and isopropyl ether. Mixing liquids with compositions and Eg resnlts in mix point M. Specification of yields E, since the same line also intersects M. The eqnihhrinm data are at 25 °C and 1 atm. 

A solution of acetic acid (C) in water (A) is to be extracted using isopropyl ether (C) as the solvent. The feed is 1000 kg/h of a solution containing 35 wt% acid and 65 wt% water. The solvent used is essentially pure isopropyl ether. The exiting raffinate stream should contain 2 wt% acetic acid. Operation is at 293 K and 1 atm. Determine (a) the minimum amount of solvent which can be used and (b) the number of theoretical stages if the solvent rate used is 60% above the minimum. Table 7.2 gives the equilibrium data. 

Table 7.2 Water-Isopropyl Ether-Acetic Acid Equilibrium Data at 293 K and 1 atma ...

Estimate the diameter and height of an RDC column to extract acetic acid from water using isopropyl ether for the conditions and data of Problem 7.21. For the desired degree of separation, 15 equilibrium stages are required. 

For the minimum-boiling isopropyl ether-isopropyl alcohol mixture in Fig. 3.5 a, the maximum total pressure is greater than the vapor pressure of either component. Thus, in distillation, the azeotropic mixture would be the overhead product. The y-x diagram in Fig. 3.5b shows that at the azeotropic mixture the liquid and vapor have the same composition. Figure 3.5c is an isobaric diagram at 101 kPa, where the azeotrope, at 78 mole % ether, boils Bt 66°C. In Fig. 3.5a, which displays isothermal (70°C) data, the azeotrope, at 123 kPa, is 72 mole % ether. 

Isopropyl ether (E) is used to separate acetic acid (A) from water (W). The liquid-liquid equilibrium data at 25°C and 1 atm (101.3 kPa) are given below. 

The literature data and our own experience indicate that drying with a molecular sieve can be employed with good results for the following solvents acetone, acetonitrile, benzene, butane, butyl acetate, carbon tetrachloride, dichloroethane, cyclohexane, diethyl ether, dimethylformamide, dimethyl sulphoxide, ethanol, heptane, isopropanol, di-isopropyl ether, pyridine, toluene and xylene. 

Table 13-5. Equilibrium data for water-acetic acid-isopropyl ether at 20°C and 1 atm...

D14. The equilibrium data for the system water-acetic acid-isopropyl ether are given in Table 13-S. We have a feed that is 30 wt % acetic acid and 70 wt % water. The feed is to be treated with pure isopropyl ether. A batch extraction done in a mixed tank will process 15 kg of feed. 

D27. We have a total feed of 100 kg h to a countercurrent extraction column. The feed is 40 wt % acetic acid and 60 wt % water. We plan to extract the acetic acid with isopropyl ether. Equilibrium data are in Table 13-5. The entering isopropyl ether is pure and has a flow rate of 111.2 kg h. We desire a raffinate that is 20 wt % acetic acid. 

This Appendix gives the location of the large amount of data scattered throughout the textbook, abietic acid-heptane-methylcellosolve+10% water Distribution coefficient. Table 13-3 acetic acid Adsorption isotherm on activated carbon, Table 18-2 and Problem 18.D7 acetic acid-benzene-water Distribution coefficients. Table 13-3 acetic acid-l-butanol-water Distribution coefficient. Table 13-3 acetic acid-3-heptanol-water Distribution coefficient. Problems 13.D5 and 13.D6 acetic acid-isopropyl ether-water Equilibrium data. Table 13-5 acetonaphthalene Adsorption isotherm on silica gel. Table 18-2... 

The data of Elgin and Browning (25) for the extraction of acetic acid between isopropyl ether and water are shown in Fig. 10.31. For approximately equal rates of flow of both phases, either phase may be dispersed with no very great effect on the HTU, but the HTU s are invariably lower, or rate of extraction greater, at increased rates of the ether. Extraction... 

Calculate the activity coefficients for the system isopropyl ether-isopropyl acetate from the data of Miller and Bliss [Ind, Eng, Chem, 32, 123 (19 ))]. Determine the best values of the constants of the van Laar, Margules, and Scatchard-Hamer equations for these data, and compare the ability of these equations to describe this system. 

Table 1 reports the retention data relative to several substituted monocychc phenols examined on silica gel 60 in benzene and di-isopropyl ether. 

Equilibrium data on rectangular coordinates. Since triangular diagrams have some disadvantages because of the special coordinates, a more useful method of plotting the three component data is to use rectangular coordinates. This is shown in Fig. 12.5-3 for the system acetic acid (i4)-water (B)-isopropyl ether solvent (C). Data are from the Appendix A.3 for this system. The solvent pair B and C are partially miscible. The concentration of the component C is plotted on the vertical axis and that of A on the horizontal axis. The concentration of component B is obtained by difference from Eqs. (12.5-2) or (12.5-3). 

EXAMPLE 12.7-1. Material Balance for Countercurrent Stage Process Pure solvent isopropyl ether at the rate of, = 600 kg/h is being used to extract an aqueous solution of Lq = 200 kg/h containing 30 wt % acetic acid (/4) by countercurrent multistage extraction. The desired exit acetic acid concentration in the aqueous phase is 4%. Calculate the compositions and amounts of the ether extract and the aqueous raffinate L. Use equilibrium data from Appendix A.3. 

Resa, J. M. Echeharria, S. Betolaza, M. A. Ruiz, A. Moradillo, B. Isobaric vapor-hquid equilibria of 3-pentanone with acetone and isopropyl ether at 101.3 kPa J. Chem. Eng. Data 1996,41, 63-65... 

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