Diisopropyl ether data

Fuangfoo, S., Kersting, M., and Viswanath, D.S. Isothermal vapor-liquid equilibria for methyl-2,2-dimethylethyl ether + 2-methylpropan-2-ol, diethyl ether -t ethyl-2,2-dimethylethyl ether. 2-methyl-2-buteue+ (2-methylbutan-2-ol), and diisopropyl ether -t octane, J. Chem. Eng. Data, 44(3) 405-410, 1999. 

Garriga, R., Andres, A.C., Perez, P., and Gracia, M. Vapor pressnres at several temperatnres and excess functions at 298.15 K of bntanone with di-n propyl ether or diisopropyl ether, J. Chem. Eng. Data, 44(2) 296-302, 1999. 

Table 1.2 Amounts of water associated with various components of a reaction mixture containing Celite-immobilized enzyme in diisopropyl ether at aw = 0.7. Data from [18].

The product from Step 1 (3.2mmol) was dissolved in 50ml CH2CI2 and treated with 1,T-carbonyldiimidazole (3.6 mmol) and aniline (4.4 mmol), stirred 18 hours, concentrated, and purified by chromatography on silica gel using diisopropyl ether/diethyl ether. Thereafter, the product was dissolved in 10 ml hot propan-2-ol and the solution acidified with ethereal HCl. The material crystallized upon trituration with ether and 0.897 g product isolated as dihydrochloride quarter hydrate, mp = 250-255 °C (dec.). Elemental analysis data supplied. 

D8. We have a feed of 15,000 kg/h of diisopropyl ether (C0 H 4 0) that contains 0.004 wt frac water. We want a diisopropyl ether product that contains 0.0004 wt frac water. Feed is a saturated liquid. Use the system shown in Figure 8-4. operating at 101.3 kPa. Use L/D = 1.5 (L/D) -Determine (L/D), L7D, optimum feed stage, and total number of stages required. Assume that CMO is valid. The following data for the diisopropyl ether— water azeotrope are given Trans. MChE, 36, 593,1940) y = 0.959, Separator Top layer x = 0.994 bottom layer x = 0.012 at 101.3 kPa and 62.2°C. All conpositions are weight fractions of diisopropyl ether. 

After condensation in a total condenser and separation of the two liquid layers, the water layer is withdrawn as product and the diisopropyl ether layer is returned as reflux. We operate at an external reflux ratio that is 2.0 times the minimum external reflux ratio. Operation is at 1.0 atm. Find the minimum external reflux ratio, the actual L/D, the distillate flow rate and mole frac water, the bottoms flow rate and mole frac water, and the number of equilibrium stages required (number the top stage as number 1). Use an expanded McCabe-Thiele diagram to determine the number of stages. Data for the azeotropic conposition fProblem 8.D81 can be used to find the mole fracs of water in the two layers in the separator and the relative volatility of water with respect to ether at low water concentrations. The weight fractions have to be converted to mole fracs first. 

Chamorro, C. R. Martin, M. C. Villamanan, M. A. S ovia, J. J. Characterization tmd modelling of a gasoUne containing 1,1-dimethylethyl methyl ether (MTBE), diisopropyl ether (DIPE) or 1,1-dimethylpropyl methyl ether (TAME) as fuel oxygeneite based on new isothermtd binary vapour-liquid data Fluid Phase Equilib. 2004,220, 1()5-112... 

Wichterle, I. Isothermal vapor-liquid equhibria in the ternary system propan-2-ol -I- diisopropyl ether -I- 2,2,4-trimethylpentane and the three binary subsytems at 330 K and 340 KELDATA Int. Electron. J. Phys.-Chem. Data 1999,5, 179-189... 

Gonzalez Benito, G. Carton Lopez, A. Vapor-liquid equilibrium data for the binary systems fornied by diisopropyl ether with ethanol, n-propanol and ethyl, isopropyl and propyl acetates Rev. Roum. Chim. 1992,37,973-978... 

Uncertainties (T(xj) = 0.0010 C7(I)/K = 0.1 ciyO - 0.0010 Resa J. M. Gonzalez C. Betolaza, M. A. Ruiz, A. Behaviour of butyl ether as entrainer for the extractive distillation of the azeotropic mixture propanone + diisopropyl ether. Isobaric VLE data of the azeotropic components with an entrainer Fluid Phase Equilib. 1999,156, 89-99... 

Pineiro, A. Olvera, A. Garda-Maja, G. Costas, M. Excess molar enthalpies of tetrahydrofuran or diisopropyl ether + 1-alkanols at 298.15 K, using a newly designed flow mixing cell for an isothermal microcalorimeter 7. Chem. Eng. Data 2001,46, 1274-1279... 

Monton, J. B. De la Torre, J. Burguet, M. C. Munoz, R. Loras, S. Isobaric vapor-liquid equilibrium in the systems 2,3-dimethylpentane + methyl 1,1-dimethylethyl ether + diisopropyl ether and + methyl 1,1-dimethylpropyl ether. J. Chem. Eng. Data 1999, 44, 1158-1162. 

Class 4 solvents, for which no adequate data are available, include diisopropyl ether, methyl tetrahydrofman, and isooctane. 

Kuroda and co-workers [34] fractionated ethylene-1-butene copolymers by successively extracting it with diisopropyl ether at 20 "C (Fraction 1), w-hexane at 20 "C [Fraction 2), n-hexane at its boiling point (Fraction 3), and cyclohexane at its boiling point (Fraction 4). The residual polymer (cyclohexane insolubles) is designated Fraction 5. The whole (unfractionated) polymer is called W. The C-NMR triad distribution data reported by Kuroda and co-workers are summarised in Table 7.2. 

An investigation of lithium diisopropyl amide (LDA) by solid state NMR led to the observation of dramatic differences between the spectra of the solid polymer and the complex crystallized from THF. Li as well as "C and "N MAS spectra showed large sideband patterns in the former case and only a few sidebands in the latter. For both materials X-ray data are available and establish a helix structure for the polymeric material, which is insoluble in hydrocarbon or ethereal solvents, and a dimer structure of the THF complex (25, 26, Scheme 4). The obvious difference between both structures, apart from the solvent coordination in the THF complex, is the magnitude of the structural N-Li-N angle, which is close to 180° in the first case and close to 90° in the second (176° and 107°, respectively). Thus, a large difference for the electric field gradient around the Li cation is expected for the different bonding situations. 

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