Equilibrium Solubility Determination and Correlation of Monobenzone in Fifteen Monosolvents at a Series of Temperatures

Self Cite

Section: Resultsmentioning

confidence: 99%

Solubility Measurement and Thermodynamic Model Correlation of Baclofen in 12 Pure Organic Solvents

Luo

Huang

et al. 2022

Self Cite

“…In the present work, the experimental solubilities of rhein in methanol, ethanol, n -propanol, isopropyl alcohol, 1-butanol, isobutyl alcohol, 1,4-dioxane, 2-butanone, cyclohexanone, acetone, acetonitrile, and DMF at various temperatures from 283.2 K to 323.2 K were fitted by the modified Apelblat model and λh model with a nonlinear regression method to describe the solid–liquid equilibrium. The relationship between solubility data ( x ) in mole fraction and the absolute temperature ( T ) was presented in the modified Apelblat equation. − A , B , and C are equation parameters. …”

Section: Resultsmentioning

confidence: 99%

Determination and Model Correlation of Rhein in 12 Pure Solvents from 283.15 K to 323.15 K

Xie²,

Shi³

2022

In this work, the mole fraction solubility of rhein in 12 pure solvents including methanol, ethanol, n-propanol, isopropyl alcohol, 1-butanol, isobutyl alcohol, 1,4-dioxane, 2-butanone, cyclohexanone, acetone, acetonitrile, and N,N-dimethylformamide (DMF) at the temperature range from 283.15 K to 323.15 K was studied. The largest mole fraction solubility is observed in 1,4-dioxane (1.450 × 10 −3 ) at 323.15 K, followed by in DMF (6.964 × 10 −4 ), cyclohexanone (4.026 × 10 −4 ), acetone (2.432 × 10 −4 ), 2-butanone (2.009 × 10 −4 ), 1-butanol (5.646 × 10 −5 ), isopropyl alcohol (5.082 × 10 −5 ), n-propanol (4.552 × 10 −5 ), isobutyl alcohol (3.375 × 10 −5 ), ethanol (3.798 × 10 −5 ), methanol (3.083 × 10 −5 ), and acetonitrile (1.655 × 10 −5 ). The solubility first increases and then decreases with the increase of carbon chain length in alcohols. Through the analysis of 1,4-dioxane and DMF properties, the solute molecules should belong to weakly polar compounds, which is also reflected in the alcohols. However, for ketone solvents, the solubility decreases with the decrease of dipolarity/ polarizability. This may be caused by the joint action of the solvent cavity term effect and hydrogen bonds. The largest relative average deviation (RAD) from the data is no more than 5%, which suggests that the calculated solubility data using the modified Apelblat model and λh model agreed very well with the experimental ones for each solvent. Compared with the values reported by Cheng and co-workers, there is an increase of 87.61-fold of solubility between 1,4-dioxane and acetonitrile at 323.15 K. Hence, the solubility data achieved in the present work could be very useful for the purification and crystallization of rhein.

“…In this work, the solubility result of ternary systems for 2,3-NMBA and 4,3-NMBA in methanol and acetone at all researched temperature was correlated by NRTL model. When the system reaches equilibrium, the relationship between the activity coefficient of solute and solubility is shown in eq . − R represents the gas constant. γ i is the activity coefficient, and x i is the mole solubility. …”

Section: Resultsmentioning

confidence: 99%

Construction and Application of a Ternary Solid–Liquid Phase Diagram of 3-Methyl-4-nitrobenzoic Acid and 3-Methyl-2-nitrobenzoic Acid in Methanol and Acetone

Ren

Zhang

2020

A ternary system solid–liquid equilibrium phase diagram is very useful to design industrial separation and purification operation. The ternary phase equilibrium for 3-methyl-4-nitrobenzoic acid (4,3-NMBA) and 3-methyl-2-nitrobenzoic acid (2,3-NMBA) in methanol and acetone at 298.15, 308.15, and 318.15 K was studied under atmospheric pressure in this work. In each ternary phase diagram, the saturated liquids divided the phase diagram into four regions, including three crystallization regions (pure 4,3-NMBA, 2,3-NMBA, and a mixture of 4,3-NMBA and 2,3-NMBA) and an unsaturated region. The crystallization region of 4,3-NMBA was larger than that of 2,3-NMBA in methanol and acetone at all evaluated temperatures. Moreover, the NRTL model was used to correlate the phase equilibrium data, and the interaction parameters of solute–solute were obtained. These parameters are of great importance to control the separation and purification process of 4,3-NMBA and 2,3-NMBA. To demonstrate the implementation of diagram application in industrial separation and purification, ternary equilibrium phase was analyzed and discussed.