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polyStyrene
Published in Allan F. M. Barton, and Solubility Parameters, 2018
Apart from these results, most of the information on polystyrene–ester systems is scattered in the chemical literature, Green5 determined polymer-liquid interaction parameters from viscosity measurements at 25°C on solutions of polystyrene (Mw = 300,000) (0.51 for n-propyl acetate). Doty,143 as part of an investigation of styrene–divinylbenzene gels, reported graphically polymer-liquid interaction parameters for polystyrene on the assumption of a base value of 0.44 for toluene, yielding 0.48 for ethyl laurate. Schick, Doty, and Zimm93 measured osmotic pressures of solutions of polystyrene (Mn ~540,000) over the concentration range 0.5 to 11%, and Orwoll102 subsequently reported the results in terms of extrapolated χ0 values for ethyl acetate of 0.49 at both 27 and 49°C. Sakurada, Nakajima, and Aoki176 studied the equilibrium composition of gels obtained by swelling cross-linked poly(vinyl acetate) in a linear low polymeric polystyrene (degree of polymerization 24 and 35) solution in ethyl acetate at 30°C, reporting χ = 0.47, compared with 0.45 at 25°C found by Boyer and Spencer.18
Practical Laboratory Data
Published in W. M. Haynes, David R. Lide, Thomas J. Bruno, CRC Handbook of Chemistry and Physics, 2016
W. M. Haynes, David R. Lide, Thomas J. Bruno
Solvent Acetic acid* Acetone Acetonitrile* Aniline* Benzene 1-Butanol Butylamine* Carbon disulfide* Chlorobenzene* Cyclohexane Decane 1-Decanol* Dichloromethane Diethyl ether N,N-Dimethylaniline* Ethanol Ethyl acetate* Ethylbenzene Ethyl formate* Ethyl propanoate* Heptane Hexane 1-Hexanol* Isopropylbenzene* Methanol Methyl acetate* N-Methylaniline* Methylcyclohexane Methyl formate* Methyl propanoate* Nitromethane* Nonane Octane Pentanoic acid* 1-Propanol* 2-Propanol Propyl acetate* Propylbenzene* Propyl formate* Tetrachloromethane* Toluene Trichloromethane* 2,2,4-Trimethylpentane o-Xylene m-Xylene p-Xylene
Innovative industrial technology starts with iodine
Published in Tatsuo Kaiho, Iodine Made Simple, 2017
Acetic acid is an important industrial material with an annual production of 6.5 megatons. Polyvinyl acetate, a typical adhesive agent, is produced by the polymerization of vinyl acetate monomer, which is synthesized from polyvinyl acetate and ethylene. In addition, ethyl acetate which is used as a solvent for paint and printing ink, and ester acetates such as butyl acetate and propyl acetate, are produced from acetic acid and various types of alcohol.
Reactive extraction of protocatechuic acid by di-n-octylamine and optimisation with Box–Behnken design
Published in Indian Chemical Engineer, 2023
İsmayil İsayev, Özge Demir, Aslı Gök, Şah İsmail Kırbaşlar
This study aimed to examine the reactive extraction of PCA by DOA in different kinds of solvents. An alcohol (linalool), an ester (propyl acetate) and a ketone (isobutyl methyl ketone) solvents were used with DOA in this study. Box–Behnken design of response surface methodology (RSM) was used to optimise the reactive extraction parameters, namely, initial PCA concentration, DOA amount and temperature. Besides, thermodynamic parameters of the process have been revealed by a temperature study. PCA has been recovered from its aqueous solutions by an amine called tri-n-octly amine [3,5,7,36], organophosphorus extractants, namely, tri-n-butyl phosphate [4,37] and di-(2-ethylhexyl)phosphoric acid (D2EHPA) [3,6,7]. Linalool and isobutyl methyl ketone have not been tested yet as solvents in the PCA reactive extraction studies. Within this study, PCA reactive extraction by DOA with linalool, isobutyl methyl ketone and propyl acetate has been examined for the first time. Therefore, this study is very important and presents useful information for its further industrial application.
Glove permeation of chemicals: The state of the art of current practice—Part 2. Research emphases on high boiling point compounds and simulating the donned glove environment
Published in Journal of Occupational and Environmental Hygiene, 2020
The glove permeation of mixtures has been modeled by other methods. The heat of mixing, related to solubility theory of regular solutions (Que Hee 1996), was able to reconcile swelling and ASTM F739 permeation parameters with BT at 0.1 µg/cm2/min at room temperature empirically for 73% of the cases of butyl, nitrile, and neoprene rubber glove membranes challenged by acetone, chloroform, p-dioxane, dimethyl sulfoxide, heptane, hexane, diisopropyl ether, 2-propanol, tetrachloromethane, tetrahydrofuran, and toluene singly and in binary and ternary mixtures (Perron et al. 2002). For mixtures that did not degrade the gloves, those with large and exothermic heats of mixing permeated less than expected based on single solvent permeation, initial swelling rate, and on its mole fraction, while those with large and endothermic heats of mixing permeated more. A solvent with high affinity for the membrane carried singly non-permeating components through with it when the high affinity solvent was the dominant component. Challenge solvent molecule size and polarity, fluorocarbon glove thickness, and swelling behavior were investigated as the basis of a predictive breakthrough time model that showed BTs for homologous series were exponentially related to molar volume (Geerissen et al. 2008a), and also for binary mixtures of t-butyl acetate/toluene, acetone/n-hexane, and t-butyl acetate/n-propyl acetate for bromobutyl rubber where an inverse mixing rule was predictive (Geerissen et al. 2008b).
Energy saving in acetic acid process using an azeotropic distillation column with a side stripper
Published in Chemical Engineering Communications, 2018
The designs of the conventional and the proposed processes are shown in Table 2. In both processes, the extractor conditions are similar, except that the small amount of recycled stream to the extractor in the conventional system is eliminated in the modified process. The feed amounts listed in Table 2 contrast the conventional process and the proposed process. Figure 5 demonstrates the column composition profiles in the conventional process. The extractor profiles, azeotropic distillation column, and two dehydration columns are included. The profiles of the modified process are shown in Figure 6, where the extractor profiles, azeotropic column, and side-stripper are included. Table 3 summarizes the stream flow rates of four components at the extractor. The solvent in the proposed process is 9% larger than the conventional process. This is primarily due to the elevated amount of i-propyl acetate required to raise the recovery of acetic acid in the extract. It aids the separation of acetic acid at the azeotropic distillation.