Densities, Viscosities and Excess Properties for Dimethyl Sulfoxide with Diethylene Glycol and Methyldiethanolamine at Different Temperatures

Abstract

Densities and viscosities of the binary systems dimethylsulfoxide with diethylene glycol and methyldiethanolamine were measured at temperatures ranging from 293.15 to 313.15 K, at atmospheric pressure and over the entire composition range. The experimental density data was correlated as a function of composition using Belda’s and Herraez’s equations, and as a function of temperature and composition using the models of Emmerling et al. and Gonzalez-Olmos-Iglesias. The viscosity results were fitted to the Grunberg-Nissan, Heric-Brewer, Wilson, Noda, and Ishida and Eyring-NRTL equations. The values of viscosity deviation ($\Delta \eta$), excess molar volume (V^E), partial molar volumes ($\overline{V_1}$ and $\overline{V_2}$) and apparent molar volume ($V_{\phi ,1}$ and $V_{\phi ,2}$) were determined. The excess functions of the binary systems were fitted to the polynomial equations. The values of thermodynamic functions of activation of viscous flow were calculated and discussed.

1. Introduction

The removal of acidic gases or liquids such as carbon dioxide (CO₂), sulfur dioxide (SO₂), hydrogen sulfide (H₂S), carbonyl sulfide (COS) and carbon disulfide (CS₂) from natural settings, refineries, synthesis gas streams and petrochemicals are of increasing importance as environmental protection becomes more and more serious [1]. It is a significant operation in gas processing to eliminate acid compounds by means of various processes, among which is gas absorption by chemical solutions such as alkanolamines (monoethanolamine, diethanolamine, diisopropanolamine, or methyldiethanolamine) [2]. The importance of basic physicochemical properties for the density and viscosity data is an indispensable requirement over a broad range of temperatures for the absorption and desorption processes of SO₂ [3].

Dimethyl sulfoxide (DMSO) was used intensively in SO₂ absorption because of its low volatility and good affinity with SO₂ [4,5]. The physicochemical properties of solutions of glycols are useful, since such solutions are used in several processes in the pharmaceutical, petroleum, cosmetic, oil and food industries [6]. Binary solution of DMSO with glycols may attract attention due to the possible intermolecular interplay of S=O group in DMSO with –OH group in glycol [7].

In this work, the densities and viscosities of binary systems of dimethyl sulfoxide (DMSO) + diethylene glycol (DEG) or methyldiethanolamine (MDEA) were measured at temperatures between 293.15 and 313.15 K, over the entire composition range and at atmospheric pressure. Investigations into the literature have shown that these systems have been examined but not in the same conditions. Tsierkezos et al. [6] reported the values of densities for diethylene glycol with dimethylsulfoxide at 298.15 K and Naidu et al. [8] investigated the densities and viscosities of diethylene glycol with dimethyl sulfoxide at 308.15 K. Wang et al. [1] studied densities of binary mixtures of dimethyl sulfoxide with methyldiethanolamine at atmospheric pressure with temperatures ranging from 293.15 to 363.15 K. Wang et al. [9] studied the densities and viscosities of diethylene glycol + dimethyl sulfoxide solutions in the temperature range 298.15–313.15 K.

The present work was mainly focused on investigating density and viscosity data of binary solutions of DEG + DMSO and MDEA + DMSO at T = 293.15, 298.15, 303.15, 308.15, and 313.15 K for the whole composition range. From our experimental data, excess molar volumes and viscosity deviations were calculated and correlated with the polynomial equations. The thermodynamic functions of activation of viscous flow have been estimated from the experimental values. Five equations were tested to correlate viscosity of the binary mixtures.

2. Materials and Methods

2.1. Materials

The chemical DMSO (mass ≥99.5%, CAS 67-68-5, water content ≤0.05%) was obtained from Merck, DEG (mass ≥99%, CAS 111-46-6, water content ≤1%) was supplied by Chemical Company and MDEA (mass ≥99%, CAS 105-59-9, water content ≤1%) was purchased from Chemical Company. In order to reduce the influence of water on the experiment, the chemicals DEG and MDEA were dried over molecular sieves (Fluka type 4 Å), and their effective component content was determined by means of gas chromatography. All specification of chemical samples is listed in

Table 1. Specification of chemical samples.

Chemical Name	Chemical Formula	Source	Mass Fraction Purity	Isolation Method
DMSO DEG MDEA	C2H6OS C4H10O3 C5H13NO2	Merck Chemical Company Chemical Company	99.5% ≥99.3% ≥99.3%	None Desiccation a and Degasification b Desiccation a and Degasification b

^a Molecular sieve type 4Å. ^b Ultrasound.

. The measurements were made at atmospheric pressure, p = 0.1 MPa, which was measured in our laboratory by a mercury barometer with an uncertainty of ±0.002 MPa.

2.2. Measurements and Method Analysis

The binary solutions were prepared by weighing using an analytical balance (Adventurer Pro AV 264CM model) at atmospheric pressure and ambient temperature with a precision of ±10⁻⁴ g. The uncertainty for the mixtures’mole fraction was less than 0.0006.

Densities of pure liquids and their mixtures were determined with an Anton Paar digital vibrating U-tube densimeter (model DMA 500). The temperature was determined with an integrated Pt100 platinum thermometer together with a Peltier element. The stated repeatability for density and temperature measurements by the manufacturer was 0.0002 g·cm⁻³ and 0.1 K respectively. The densimeter was calibrated with bidistilled and degassed water before and after each of the density measurements. The combined expanded uncertainty of the densities is estimated within 0.0015 g·cm⁻³ with a 0.95 level of confidence for the present work. Expanded uncertainty of the excess volume is estimated to be 0.04 cm³·mol⁻¹ (0.95 confidence level).

Viscosities of the pure compounds and of the binary solutions were determined with an Ubbelohde kinematic, viscosity measuring unit ViscoClock (Schott-Gerate GmbH) that was kept in a vertical position in a thermostatic bath (U-10 Freital). The temperature was controlled with a precision of ±0.05 K.

The kinematic viscosity was calculated using the equation:

$$\nu =At-\left(B/t\right)$$

(1)

where ν is the kinematic viscosity and t is the flow time, A and B are characteristic constants of the viscometer. The constants A and B were determined by taking doubly distilled water and benzene (Merck, mole fraction purity ≥0.995) as the calibrating liquids. The accuracy of time measurement is ±0.01 s. The dynamic viscosity was determined using the equation:

$$\eta =\nu \rho$$

(2)

where ρ is the density of the liquid.

Each value of the viscosity was the average of five measurements (the measurements refer to the uncertainty values within ±0.02 s). The combined relative expanded uncertainty of the dynamic viscosity was estimated to be 5%. Expanded uncertainties in the deviation viscosity was estimated to be 0.06 mPa·s (0.95 of confidence).

3. Results

3.1. Density and Viscosity

The experimental densities and viscosities for pure DMSO, DEG and MDEA in the temperature range from 293.15 to 313.15 K are found to be in good agreement with reported values in the literature and comparison of these values is reported in

Table 2. Experimental and literature values of density (ρ) and viscosity (η) of the pure components in the temperature range from 293.15 to 313.15 K.

Component	T/(K)	ρ/(g·cm−3)		η/(mPa·s)
		This Work	Lit. Value	This Work	Lit. Value
DMSO	293.15 298.15 303.15 308.15 313.15	1.1002 1.0952 1.0902 1.0853 1.0803	1.1002 [10] 1.10053 [11] 1.100865 [1] 1.0955 [12] 1.0954 [13] 1.09530 [6] 1.0946 [9] 1.0904 [12] 1.0900 [14] 1.0888 [9] 1.090812 [1] 1.0854 [12] 1.08573 [15] 1.0831 [9] 1.0807 [12] 1.08024 [16] 1.0785 [9] 1.080770 [1]	2.271 2.021 1.843 1.710 1.525	2.245 [17] 2.2255 [18] 2.00 [12] 2.025 [19] 1.40 [9] 1.84 [12] 1.843 [20] 1.21 [9] 1.69 [3] 1.6689 [21] 1.12 [9] 1.5351 [21] 1.52 [12] 1.00 [9]
DEG	293.15 298.15 303.15 308.15 313.15	1.1185 1.1148 1.1108 1.1064 1.1024	1.11705 [22] 1.116583 [23] 1.11303 [24] 1.11351 [25] 1.1128 [9] 1.11260 [1] 1.1098 [26] 1.10948 [27] 1.1093 [9] 1.1056 [26] 1.10629 [22] 1.1052 [9] 1.1023 [28] 1.102274 [23] 1.0998 [9]	33.270 26.865 21.280 17.291 14.117	- 27.15 [26] 27.5 [28] 17.00 [9] 21.7 [28] 21.754 [26] 12.4 [9] 17.26 [26] 16.9 [28] 10.4 [9] 14.2 [28] 8.19 [9]
MDEA	293.15 298.15 303.15 308.15 313.15	1.0409 1.0363 1.0326 1.0288 1.0250	1.0406 [29] 1.03966 [30] 1.0406 [1] 1.03556 [31] 1.037863 [32] 1.0331 [29] 1.03213 [30] 1.033017 [1] 1.02834 [31] 1.0303 [33] 1.0255 [29] 1.0250 [34] 1.025401 [1]	100.614 74.927 57.582 45.129 34.833	102.7 [31] 100.72 [29] 74.81 [35] 57.57 [36] 57.615 [30] 44.21 [37] 44.62 [29] 34.78 [36] 35.00 [37] 34.89 [29]

Standard uncertainties: u(p) = 0.002 MPa, Expanded uncertainties: Ur(η) = 5% and U(ρ) = 0.0015 g·cm⁻³(0.95 of confidence).

.

DMSO density values reported in the literature [1,6,9,10,11,12,13,14,15,16] differ from our experimental data with a maximum of 0.2% and viscosity values reported in the literature [3,12,17,18,19,20,21] differ with a maximum of 2.5%. For DEG, density values found in the literature [1,9,22,23,24,25,26,27,28] differ with a maximum of 0.2% and for MDEA [1,29,30,31,32,33,34] they differ by less than 0.07%. Viscosity values reported in the literature differ from our results by a maximum of 2.3% for DEG [26,28] and a maximum of 2.1% for MDEA [29,30,31,35,36,37]. Viscosity values of DMSO and DEG reported by Wang et al. [9] differ by more than 30% compared with our results. These differences can be attributed to the different purity of the reagents used.

The experimental densities and viscosities for the binary systems DEG (1) + DMSO (2) and MDEA (1) + DMSO (2) are listed in

Table 3. Density values ρ/(g·cm⁻³) as a functions of mole fraction in the temperature range from 293.15 to 313.15 K and at atmospheric pressure.

	T/(K)
x1	293.15	298.15	303.15	308.15	313.15
DEG (1) + DMSO (2)
0.1062 0.2007 0.3034 0.4110 0.5108 0.5972 0.6955 0.8096 0.8819	1.1038 1.1068 1.1095 1.1117 1.1133 1.1144 1.1155 1.1168 1.1174	1.0988 1.1019 1.1049 1.1072 1.1090 1.1102 1.1114 1.1128 1.1135	1.0939 1.0970 1.1000 1.1026 1.1045 1.1058 1.1071 1.1086 1.1094	1.0889 1.0921 1.0951 1.0978 1.0998 1.1012 1.1025 1.1041 1.1049	1.0840 1.0873 1.0904 1.0932 1.0953 1.0968 1.0982 1.0998 1.1007
MDEA (1) + DMSO (2)
0.1003 0.1967 0.2997 0.4006 0.5001 0.6020 0.6937 0.7983 0.8967	1.0899 1.0808 1.0725 1.0654 1.0595 1.0544 1.0504 1.0465 1.0436	1.0850 1.0762 1.0678 1.0607 1.0549 1.0498 1.0458 1.0419 1.0390	1.0803 1.0718 1.0635 1.0565 1.0509 1.0459 1.0419 1.0381 1.0353	1.0758 1.0675 1.0592 1.0525 1.0469 1.0419 1.0380 1.0342 1.0315	1.0712 1.0631 1.0550 1.0483 1.0428 1.0379 1.0341 1.0303 1.0277

Standard uncertainties: u(x₁) = 6 × 10⁻⁴, u(p) = 0.002 MPa, u(T) = 0.1 K; Expanded uncertainties: U(ρ) = 0.0015 g·cm⁻³ (0.95 of confidence).

and

Table 4. Viscosity values η/(mPa·s) as a functions of mole fraction in the temperature range from 293.15 to 313.15 K and at atmospheric pressure.

	T/(K)
x1	293.15	298.15	303.15	308.15	313.15
DEG (1) + DMSO (2)
0.1062 0.2007 0.3034 0.4110 0.5108 0.5972 0.6955 0.8096 0.8819	3.110 4.306 5.792 7.884 10.198 12.843 16.372 21.286 24.874	2.877 3.799 5.115 6.762 8.630 10.717 13.356 17.154 20.097	2.520 3.404 4.334 5.702 7.072 8.605 10.796 13.923 16.220	2.281 3.012 3.883 5.082 6.337 7.647 9.502 11.854 13.703	2.049 2.677 3.383 4.361 5.394 6.428 7.951 9.912 11.431
MDEA (1) + DMSO (2)
0.1003 0.1967 0.2997 0.4006 0.5001 0.6020 0.6937 0.7983 0.8967	5.745 7.771 10.987 15.147 21.152 29.452 40.462 54.870 71.350	4.859 6.572 9.100 12.513 16.806 23.184 30.372 40.971 53.015	4.170 5.595 7.542 10.120 13.775 18.668 24.585 32.239 40.925	3.680 4.837 6.364 8.490 11.189 15.024 19.888 25.861 32.869	3.173 4.084 5.508 7.188 9.673 12.455 15.955 20.465 25.494

Standard uncertainties: u(x₁) = 6 × 10⁻⁴, u(p) = 0.002 MPa, u(T) = 0.05 K; Expanded uncertainties: Ur(η) = 5%.

.

The density of binary system DEG (1) + DMSO (2) increases with the increase in DEG concentration, and for the system MDEA (1) + DMSO (2), density increases with the increase in DMSO concentration. Viscosity of binary system DEG (1) + DMSO (2) increases with the increase in DEG concentration, while for the system MDEA (1) + DMSO (2), it increases with the increase in MDEA concentration.

The densities of binary solutions were represented as a function on composition by the following Belda [38] (Equation (3)) and Herraez [39] (Equation (4)) equations, and with composition and temperature using the Emmerling et al. [40] (Equation (5)) and Gonzalez-Olmos Iglesias [41] (Equation (6)) equations:

$$\rho ={\rho }_2+\left({\rho }_1-{\rho }_2\right)x_1\left(\frac{1+m_1\left(1-x_1\right)}{1+m_2\left(1-x_1\right)}\right)$$

(3)

$$\rho ={\rho }_2+\left({\rho }_1-{\rho }_2\right)x_1^{A+B{x}_1+C{x}_1^2}$$

(4)

$$\rho =x_1{\rho }_1+x_2{\rho }_2+x_1{x}_2\left[\begin{array}{c}{P}_1+P_{2}T+P_3{T}^2+\left(P_4+P_{5}T+P_6{T}^2\right)\left(x_1-x_2\right)+\\ \left(P_7+P_{8}T+P_9{T}^2\right){\left(x_1-x_2\right)}^2\end{array}\right]$$

(5)

$$\rho ={\displaystyle \sum }_{i=0}^2{A}_i{x}^i$$

(6)

The temperature dependence of the densities (ρ_i) of each pure substance i involved in Equation (5) is expressed using the equation:

$${\rho }_i=A_i+B_{i}T+C_i{T}^2(i=1, 2)$$

(7)

$$A_i={\displaystyle \sum }_{j=0}^2{A}_{ij}{T}^i$$

(8)

The adjustable parameters of these equations (m₁, m₂, A, B, C, P₁–P₉, A_i, B_i, C_i and A_ij) were estimated using the experimental data and a nonlinear regression analysis employing the Levenberg-Marquardt algorithm [42].

Table A1. Parameters for the Belda and Herraez equations and standard deviations at temperature range from (293.15 to 313.15) K.

	Parameters and σ/(g·cm−3)	T/(K)
Model		293.15	298.15	303.15	308.15	313.15
DEG (1) + DMSO (2)
Belda	m1 m2 104.σ	0.0732 −0.5208 1.49	0.0781 −0.4861 1.94	0.0914 −0.4518 1.81	0.1248 −0.4087 1.97	0.0734 −0.4267 2.12
Herraez	A B C 105·σ	0.8147 −1.0314 0.7901 7.84	0.8549 −1.1068 0.8852 7.49	0.8652 −1.0394 0.8077 4.70	0.8883 −1.0627 0.8238 4.95	0.8994 −1.0737 0.8712 2.80
MDEA (1) + DMSO (2)
Belda	m1 m2 104·σ	0.3401 −0.2987 1.13	0.3454 −0.2827 1.24	0.3586 −0.2690 1.53	0.3935 −0.2366 1.77	0.4319 −0.2016 2.09
Herraez	A B C 104·σ	0.8238 −0.7358 0.3382 1.17	0.8289 −0.7382 0.3382 0.99	0.8346 −0.7492 0.3481 1.13	0.8448 −0.7638 0.3557 1.27	0.8576 −0.7930 0.3788 1.20

and

Table A2. Values of parameters in the range 293.15–313.15 K for the Emmerling et al. and Gonzales-Olmos-Iglesias models and standard deviations ¹.

DEG (1) + DMSO (2) A1 = 1.0860 A2 = 1.4180 P1 = −0.0368 P4 = −0.3664 P7 = 0.4773 A00 = 1.4584 A10 = −0.4239 A20 = 0.0383 MDEA (1) + DMSO (2) A1 = 1.6658 A2 = 1.4324 P1 = 0.1702 P4 = −0.2610 P7 = 0.3710 A00 = 1.4621 A10 = 0.3647 A20 = −0.1692

Emmerling et al. B1 = 9.7611 × 10−4 B2 = −0.0012 P2 = 3.6037 × 10−4 P5 = 0.0023 P8 = −0.0030 104·σ = 1.09 Gonzalez-Olmos-Iglesias A01 = −0.0014 A11 = 0.0028 A21= −3.6947 × 10−4 104·σ = 3.14 Emmerling et al. B1 = −0.0034 B2 = −0.0013 P2 = −0.0016 P5 = 0.0019 P8 = −0.0026 104·σ = 1.52 Gonzalez-Olmos-Iglesias A01 = −0.0015 A11 = −0.0035 A21 = 0.0016 104·σ = 3.87

C1 = −2.9500 × 10−6 C2 = 2.9207 × 10−7 P3 = −6.2313 × 10−7 P6 = −3.6487 × 10−6 P9 = 4.6316 × 10−6 A02 = 6.9155 × 10−7 A12 = −4.4132 × 10−6 A22 = 6.3730 × 10−7 C1 = 4.2989 × 10−6 C2 = 4.4600 × 10−7 P3 = 3.0708 × 10−6 P6 = −3.4634 × 10−6 P9 = 4.5659 × 10−6 A02 = 8.2965 × 10−7 A12 = 6.4086 × 10−6 A22 = −3.0582 × 10−6

¹ Units: A_i, P₁, P₄, P₇, A₀₀, A₁₀, A₂₀, σ:g·cm⁻³; B_i, P₂, P₅, P₈, A₀₁, A₁₁, A₂₁: g·cm⁻³ K⁻¹; C_i, P_3,P₆, P₉, A₀₂, A₁₂, A₂₂: g·cm⁻³·K⁻².

in the Appendix A show the fitting parameters along with the standard deviation calculated with the equation:

$$\sigma ={\left[\frac{{\displaystyle \sum }{\left(X_{exp}-X_{calc}\right)}^2}{m-n}\right]}^{1/2}$$

(9)

where X is the value of the analyzed property, m is the number of data points, and n is the number of estimated parameters. Data presented in Table A1 and Table A2 show that Herraez’s equation offers the best results for correlating the density with composition, while Emmerling et al.’s equations the best for correlating the density of the binary solutions with composition and temperature.

In this paper, the one-parameter Grunberg–Nissan [43] and two-parameter Heric–Brewer [44], Wilson [45], Noda and Ishida [46] and Eyring-NRTL [47] models were used to represent the dependence of viscosity on the concentration of components in binary systems.

Grunberg and Nissan [43] proposed an equation based on a parameter:

$$ln\eta =x_{1}ln{\eta }_1+x_{2}ln{\eta }_2+x_1{x}_{2}d$$

(10)

The Heric–Brewer [44] equation with two parameters is:

$$ln\eta =x_{1}ln{\eta }_1+x_{2}ln{\eta }_2+x_{1}ln{M}_1+x_{2}ln{M}_2-ln\left(x_1{M}_1+x_2{M}_2\right)+x_1{x}_2\left[{\alpha }_{12}+{\alpha }_{21}\left(x_1-x_2\right)\right]$$

(11)

By the application of the Wilson [45] equation, viscosity of the binary mixtures can be expressed as:

$$\ln \left(\eta V\right)=x_1\ln \left({\eta }_1{V}_1\right)+x_2\ln \left({\eta }_2{V}_2\right)+x_1\ln \left(x_1+x_2\frac{V_2}{V_1}\exp \left(-\frac{{\lambda }_{12}}{RT}\right)\right)+x_2\ln \left(x_2+x_1\frac{V_1}{V_2}\exp \left(-\frac{{\lambda }_{21}}{RT}\right)\right)$$

(12)

Noda and Ishida [46] proposed the following semi-empirical equation:

$$\ln \left(\eta V\right)=x_1\ln \left({\eta }_1{V}_1\right)+x_2\ln \left({\eta }_2{V}_2\right)+x_1{x}_2\left[\frac{w_{12}}{x_2+x_1\exp \left(\frac{-w_{12}}{RT}\right)}+\frac{w_{21}}{x_1+x_2\exp \left(\frac{-w_{21}}{RT}\right)}\right]$$

(13)

The Eyring-NRTL [47] correlative model is given by the relation:

$$\ln \left(\eta V\right)=x_1\ln \left({\eta }_1{V}_1\right)+x_2\ln \left({\eta }_2{V}_2\right)+x_1{x}_2\left[\frac{{\tau }_{21}\exp \left(-\alpha {\tau }_{21}\right)}{x_1+x_2\exp \left(-\alpha {\tau }_{21}\right)}+\frac{{\tau }_{12}\exp \left(-\alpha {\tau }_{12}\right)}{x_2+x_3\exp \left(-\alpha {\tau }_{12}\right)}\right]$$

(14)

In these equations η, and η₁, η₂ are the dynamic viscosities of the liquid mixtures and of the pure components 1 and 2, x₁, x₂ are the mole fractions, M₁, M₂ are the molecular masses, V is the molar volume of the mixtures, V₁ and V₂ are the respective molar volumes of the pure components, T is the temperature, R is the gas constant; d, α₁₂, α_21, λ₁₂, λ₂₁, w₁₂, w₂₁, τ₁₂ and τ₁₂ are interaction parameters (viscosity coefficients) and reflect the non-ideality of the systems. The Eyring-NRTL equation has three parameters, including α, which is a measure of non-ideality of the systems, considered here to be fixed at 0.20 [48].

The parameters were estimated using the experimental viscosity data and a non-linear regression analysis employing the Levenberg-Marquardt algorithm [42].

The ability of these models to correlate viscosity data was tested by calculating the average absolute deviation (ADD%), between the experimental and calculated values, using the equation:

$$ADD\%=\frac{100}{m}{\displaystyle \sum }_{i=1}^m{\left|\frac{{\eta }_{exp}-{\eta }_{cal}}{{\eta }_{exp}}\right|}_i$$

(15)

where n is the number of experimental data points.

The presented data in

Table A3. Values of parameters for the relations of Grunberg–Nissan, Heric–Brewer, Wilson, Noda–Ishida and Eyring–NRTL and average absolute deviation in the temperature range from 293.15 to 313.15 K.

Model	Parameters and ADD%	T/(K)
		293.15	298.15	303.15	308.15	313.15
DEG (1) + DMSO (2)
Grunberg- Nissan	d ADD%	0.528 1.03	0.533 1.91	0.426 2.00	0.520 0.84	0.531 0.96
Heric-Brewer	α12 α21 ADD%	0.575 −0.122 0.75	0.582 −0.357 0.41	0.475 −0.350 0.69	0.568 −0.130 1.45	0.579 −0.164 0.51
Wilson	λ12 λ21 ADD%	−481.19 −681.61 0.82	1985.47 −1986.45 0.86	1754.04 −1754.39 1.23	−287.47 −868.51 0.56	724.45 −1501.24 0.50
Noda and Ishida	w12 w21 ADD%	−30.23 30.42 1.02	−31.10 −31.28 1.90	−28.29 28.43 1.97	−30.77 30.96 0.85	−31.31 31.50 0.93
Eyring-NRTL a	τ12 τ12 ADD%	−0.455 1.172 0.80	−1.227 2.586 0.58	−1.380 2.753 0.66	−0.544 1.297 0.54	−0.780 1.681 0.50
MDEA (1) + DMSO (2)
Grunberg- Nissan	d ADD%	1.627 10.41	1.517 10.68	1.383 9.60	1.224 8.84	1.250 8.47
Heric-Brewer	α12 α21 ADD%	1.719 −1.889 5.82	1.610 −1.965 5.02	1.474 −1.762 4.82	1.316 −1.609 4.90	1.342 −1.574 3.68
Wilson	λ12 λ21 ADD%	3811.93 −3812.09 6.33	3720.99 −3727.36 6.68	3538.15 −3555.24 6.37	3393.73 −3399.01 6.50	3422.86 −3425.11 5.46
Noda and Ishida	w12 w21 ADD%	−53.26 53.84 10.43	−52.00 52.55 10.68	−50.55 51.04 9.62	−48.21 48.65 8.88	−48.71 49.17 8.49
Eyring-NRTL a	τ12 τ12 ADD%	0.014 14.593 2.18	−0.136 14.381 1.61	−0.049 15.552 1.74	−1.329 8.453 3.30	−1.362 7.5085 3.30

^a Eyring-NRTL as two-parameter model (α = 0.20).

show that, for the DEG + DMSO system, ADD% values of maximum 2% are obtained for the Grunberg–Nissan and Noda–Ishida equations, and for the MDEA + DMSO system, the ADD% values for the two equations are very high (10%). For the Heric–Brewer equation, ADD% values of maximum 1.5% are obtained for the DEG + DMSO system and of maximum 6.0% in the case of the system formed by MDEA and DMSO. Approximately the same values are obtained for the Wilson equation. The Eyring–NRTL equation presents the best results, with ADD% values of maximum 0.8% for the DEG + DMSO system and maximum 3.3% for the MDEA + DMSO system. The higher ADD% in the MDEA + DMSO system than in the DEG + DMSO system can be attributed to higher deviation of the system from ideality. The obtained ADD% values lower than 5% are regarded to be acceptable for engineering calculations [49].

3.2. Excess Properties

3.2.1. Excess Molar Volume

The excess molar volumes have been calculated from the experimental densities data using the following equation:

$$V^E=\frac{\left[x_1{M}_1+x_2{M}_2\right]}{\rho }-\left[\frac{x_1{M}_1}{{\rho }_1}+\frac{x_2{M}_2}{{\rho }_2}\right]$$

(16)

where x₁ and x₂ are the mole fractions of the components, M₁ and M₂ are the molar masses of components 1 and 2, ρ, ρ₁ and ρ₂ are the respective densities of the solution and of the pure components. The results of excess molar volumes are illustrated in Figure 1 and Figure 2.

The experimental excess molar volumes are negative for the DEG + DMSO system and positive for the MDEA + DMSO binary system in the whole composition range at all temperatures.

The negative values are a consequence of the following effects: (1) strong intermolecular interactions due to the charge-transfer complex, dipole-dipole and dipole-induced dipole interactions, and H-bonding between unlike molecules finally leading to more efficient packing in the mixture than in the pure liquids; (2) structural effects which arise from suitable interstitial accommodation giving a more compact structure of solutions [50].

The negative excess volume values for the DEG + DMSO system indicated that the volume of the mixture was less than the sum of the volumes of the pure components, possibly due to contraction of the mixing volume caused by structural effects and strong intermolecular interactions between DEG and DMSO. Similar behavior was observed by Qiaoet al. [12] for the binary system tri-ethylene glycol + dimethyl sulfoxide.

The value became less negative with increasing temperature and arrived at the minimum around molar fraction 0.40 for DEG at all temperatures. These values indicate that there is a maximum volume contraction on mixing DEG with DMSO at a rate of 2:3.

Dimethyl sulfoxide is a highly polar solvent, not forming H-bond networks and tending toward self-association [1]. The molecular dynamics simulations demonstrated that in liquid DMSO, the H-bonds C–H …O=S are formed [51]. Amines are moderately polar but not as polar as alcohols of comparable molecular weights, and the polar nature of N–H results in the formation of hydrogen bonds with other amine molecules, or other H-bonding systems [52,53]. In addition, DMSO can provide an S=O group and the hydroxylamines can provide OH or C-H groups for interactions [54].

The positive values for the MDEA + DMSO system indicate that there were no strong intermolecular interactions. The positive values are due to expansion of the solution volume due to mixing caused by the hydrogen bond rupture and dispersive interactions between unlike molecules [55]. These positive values of excess volume for the MDEA + DMSO system can be explained by the fact that DMSO forms a strong associative structure and by the self-association of MDEA molecules. The effect of temperature on the excess volumes shows a systematic decrease with rising temperature.

3.2.2. Viscosity Deviation

The viscosity deviation (Δη) values were calculated from the experimental data of viscosity using the equation:

$$\Delta \eta =\eta -\left(x_1{\eta }_1+x_2{\eta }_2\right)$$

(17)

where η is the dynamic viscosity of the mixture, x₁, x₂ and η₁, η₂ are the mole fractions and the dynamic viscosities of pure components 1 and 2, respectively.

The Δη values are shown in Figure 3 and Figure 4. The viscosity deviation values are negative at all investigated temperatures for both systems. The viscosity deviations may be generally explained by considering the following factors: (1) the difference in size and shape of the component molecules and the loss of dipolar association to a decrease in viscosity; (2) specific interactions between unlike molecules, such as H-bond formation, and charge transfer complexes may cause an increase in the viscosity of mixtures rather than in pure components. The former effect produces negative excess viscosity, and the latter effect produces positive excess viscosity [56]. For the DEG + DMSO system, the negative values of viscosity deviation indicate that the strength of specific interactions is not the only factor influencing the deviation in viscosity. The molecular size and shape of the components also play an important role [57]. For these systems the negative values of viscosity deviation indicate that the molecular size and shape of the components is a more important factor than the strength of specific interactions for determining the viscosity deviation.

The negative values of viscosity deviation for MDEA + DMSO corroborated with positive V^E values demonstrate that there were no strong molecular interactions.

The values of viscosity deviation decrease with an increase in temperature. An increase in temperature decreases self-association as well as the association between unlike components because of the increase in thermal energy [58].

The excess molar volumes and viscosity deviationof the binary systems can be represented by the Redlich–Kister [59] (Equation (18)) and Hwang [60] (Equation (19)) equations:

$$X^E=x_1{x}_2{\displaystyle \sum }_{k=0}^3{a}_k{\left(2x_1-1\right)}^k$$

(18)

$$X^E=x_1{x}_2\left(A_0+A_1{x}_1^3+A_2{x}_2^3\right)$$

(19)

where X^E represents either of the following properties: V^E, Δη; x₁, x₂ are the mole fractions of the components 1 and 2, respectively, and a_k, A₀, A₁, A₂ denote the polynomial coefficients.

In addition, the excess molar volumes were also correlated with the Myers and Scott [61] equation:

$$X^E=x_1{x}_2\frac{{{\displaystyle \sum }}_{k=0}^p{B}_k{z}_{12}^k}{1+{{\displaystyle \sum }}_{l=1}^m{C}_l{z}_{12}^l}$$

(20)

where X^E is V^E and z₁₂ = x₁ − x₂. B_k and C_l are polynomial coefficients.

The values of polynomial coefficients are given in

Table A4. Polynomial coefficients ¹ and standard deviations (σ) for the binary systems in the temperature range from 293.15 to 313.15 K.

Model	Parameters and σ	T/(K)
		293.15	298.15	303.15	308.15	313.15
VE/(cm3·mol−1) DEG (1) + DMSO (2)
Redlich-Kister	a0 a1 a2 a3 103·σ	−0.736 0.420 0.157 −0.384 3.0	−0.726 0.411 0.296 −0.422 3.5	−0.701 0.339 0.319 −0.328 2.7	−0.679 0.287 0.379 −0.307 3.7	−0.668 0.280 0.453 −0.198 2.4
Hwang	A0 A1 A2 103·σ	−0.785 0.545 −0.139 7.4	−0.821 0.703 0.071 8.0	−0.805 0.689 0.150 6.3	−0.803 0.717 0.285 6.3	−0.817 0.853 0.348 4.4
Myers and Scott	B0 B1 B2 C0 C1 103·σ	−0.730 −0.391 −0.240 1.122 1.001 2.9	−0.720 −0.343 0.105 1.060 0.693 3.3	−0.708 −0.003 −0.394 0.556 1.488 2.0	−0.680 −0.141 0.137 0.654 0.680 3.9	−0.666 0.004 0.518 0.410 0.018 2.6
MDEA (1) + DMSO (2)
Redlich-Kister	a0 a1 a2 a3 103·σ	1.436 0.164 −0.274 0.208 5.1	1.403 0.188 −0.307 0.250 5.3	1.364 0.211 −0.359 0.240 8.4	1.307 0.268 −0.411 0.264 10.0	1.259 0.315 −0.520 0.281 10.4
Hwang	A0 A1 A2 103·σ	1.527 −0.084 −0.647 5.2	1.505 −0.083 −0.737 5.6	1.483 −0.129 −0.830 8.2	1.444 −0.120 −0.977 9.7	1.432 −0.202 −1.186 10.1
Myers and Scott	B0 B1 B2 C0 C1 103·σ	1.428 −0.387 −1.759 −0.394 −1.078 3.8	1.389 −0.586 −1.874 −0.573 −1.152 5.4	1.348 −0.466 −1.742 −0.522 −1.073 8.4	1.287 −0.425 −1.836 −0.545 −1.162 7.9	1.234 −0.313 −1.788 −0.519 −1.125 8.2
Δη/(mPa·s) DEG (1) + DMSO (2)
Redlich-Kister	a0 a1 a2 a3 σ	−30.94 −8.67 −6.08 −6.46 0.11	−23.81 −7.84 −6.20 6.31 0.05	−18.47 −7.25 −2.65 −0.60 0.06	−13.15 −3.29 −1.35 −0.65 0.04	−10.22 −2.78 0.31 1.15 0.03
Hwang	A0 A1 A2 σ	−28.89 −21.19 4.89 0.11	−21.73 −20.30 3.67 0.07	−17.60 −12.42 5.41 0.06	−12.70 −6.00 2.40 0.03	−10.34 −2.39 3.29 0.04
MDEA (1) + DMSO (2)
Redlich-Kister	a0 a1 a2 a3 σ	−119.76 −45.73 −19.54 −54.82 0.63	−85.34 −35.93 −20.99 −43.35 0.39	−62.82 −22.03 −15.89 −42.66 0.37	−48.12 −17.44 −7.35 −27.20 0.26	−34.08 −11.65 −8.74 −23.83 0.19
Hwang	A0 A1 A2 σ	−113.24 −103.14 51.24 0.80	−78.34 −88.66 32.85 0.56	−57.52 −64.94 22.75 0.59	−45.67 −41.77 22.27 0.38	−31.17 −35.30 12.10 0.32

¹ Units: cm³·mol⁻¹ for V^E and mPa·s for Δη.

along with the standard deviation, σ, calculated with Equation (9). From the presented data it can be seen that, for both systems, the excess molar volume is best correlated using the Myers and Scott equation. The Redlich–Kister equation shows better results than the Hwang equation for correlating the viscosity deviation for both systems.

3.2.3. Apparent Molar Volume

The apparent molar volumes V_ϕ,1 and V_ϕ,2 of the binary systems were calculated with the equations [62]:

$$V_{\varphi ,1}=\frac{x_2{M}_2}{x_1}\frac{{\rho }_2-{\rho }_m}{{\rho }_2{\rho }_m}+\frac{M_1}{{\rho }_m}$$

(21)

$$V_{\varphi ,2}=\frac{x_1{M}_1}{x_2}\frac{{\rho }_1-{\rho }_m}{{\rho }_1{\rho }_m}+\frac{M_2}{{\rho }_m}$$

(22)

The values obtained in the temperature range from 293.15 to 313.15 K are listed in

Table A5. Apparent molar volumes of DEG, V_ϕ,1 (cm³·mol⁻¹), for binary systems DEG + DMSO and apparent molar volumes of MDEA, V_ϕ,1 (cm³·mol⁻¹), for binary system MDEA + DMSO in the temperature range from 293.15 to 313.15 K.

x1	T/(K)
	293.15	298.15	303.15	308.15	313.15
DEG (1) + DMSO (2)
0.0000 0.1062 0.2007	- 94.499 94.759	- 94.922 95.157	- 95.293 95.560	- 95.770 95.983	- 96.147 96.366
0.3034 0.4110 0.5108 0.5972 0.6955 0.8096 0.8819 1.0000	95.077 95.391 95.645 95.837 96.023 96.203 96.306 96.455	95.445 95.775 96.035 96.236 96.433 96.626 96.736 96.895	95.861 96.172 96.440 96.648 96.853 97.055 97.171 97.340	96.287 96.591 96.858 97.068 97.280 97.486 97.605 97.779	96.679 96.994 97.270 97.487 97.707 97.925 98.049 98.232
MDEA (1) + DMSO (2)
0.0000 0.1003 0.1967 0.2997 0.4006 0.5001 0.6020 0.6937 0.7983 0.8967 1.0000	- 114.274 113.424 112.488 111.671 110.936 110.265 109.730 109.186 108.731 108.310	- 114.764 113.859 112.975 112.167 111.429 110.760 110.226 109.682 109.226 108.805	- 115.141 114.243 113.405 112.618 111.886 111.229 110.706 110.169 109.719 109.304	- 115.450 114.619 113.843 113.053 112.343 111.700 111.183 110.654 110.208 109.797	- 115.770 115.008 114.263 113.511 112.815 112.182 111.671 111.151 110.711 110.305

and

Table A6. Apparent molar volumes of DMSO, V_ϕ,2 (cm³·mol⁻¹), for binary systems DEG + DMSO and apparent molar volumes of DMSO, V_ϕ,2 (cm³·mol⁻¹), for binary system MDEA + DMSO in the temperature range from 293.15 to 313.15 K.

x1	T/(K)
	293.15	298.15	303.15	308.15	313.15
DEG (1) + DMSO (2)
0.0000 0.1062 0.2007 0.3034 0.4110 0.5108 0.5972 0.6955 0.8096 0.8819 1.0000	71.014 70.966 70.899 70.832 70.780 70.752 70.752 70.765 70.725 70.792 -	71.339 71.304 71.244 71.166 71.124 71.090 71.095 71.120 71.111 71.195 -	71.656 71.633 71.585 71.522 71.462 71.432 71.438 71.466 71.467 71.533 -	71.989 71.968 71.917 71.862 71.801 71.767 71.764 71.808 71.799 71.899 -	72.322 72.304 72.254 72.201 72.145 72.114 72.111 72.158 72.211 72.327 -
MDEA (1) + DMSO (2)
0.0000 0.1003 0.1967 0.2997 0.4006 0.5001 0.6020 0.6937 0.7983 0.8967 1.0000	71.014 71.004 71.080 71.188 71.337 71.485 71.634 71.794 72.003 72.066 -	71.339 71.332 71.389 71.514 71.670 71.807 71.959 72.121 72.333 72.397 -	71.666 71.660 71.709 71.842 72.004 72.126 72.273 72.455 72.655 72.666 -	71.989 71.972 72.018 72.167 72.302 72.434 72.597 72.765 72.986 72.944 -	72.322 72.295 72.340 72.482 72.632 72.764 72.923 73.076 73.320 73.224 -

.

3.2.4. Partial Molar Volumes

Partial molar volumes were calculated using the following equations:

$$\overline{V_1}=V^E+V_1^0+\left(1-x_1\right){\left(\partial V^E/\partial x_1\right)}_{p,T}$$

(23)

$$\overline{V_2}=V^E+V_2^0-x_1{\left(\partial V^E/\partial x_1\right)}_{p,T}$$

(24)

where $V_1^0$ and $V_2^0$ are the molar volumes of pure components. The derivative ${\left(\partial V^E/\partial x_1\right)}_{p,T}$ in Equations (23) and (24) was obtained by differentiation of Equation (18), which leads to the following equations:

$$\overline{V_1}=V_1^0+x_2^2{\displaystyle \sum }_{k=0}^3{a}_k{\left(2x_1-1\right)}^k-2x_1{x}_2^2{\displaystyle \sum }_{k=1}^3{a}_k{\left(2x_1-1\right)}^{k-1}$$

(25)

$$\overline{V_2}=V_2^0+x_1^2{\displaystyle \sum }_{k=0}^3{a}_k{\left(2x_1-1\right)}^k+2x_1^2{x}_2{\displaystyle \sum }_{k=1}^3{a}_k{\left(2x_1-1\right)}^{k-1}$$

(26)

The calculated values of partial molar volumes are listed in

Table A7. Partial molar volumes $\overline{V_1}$ (cm³·mol⁻¹) for binary systems in the temperature range from 293.15 to 313.15 K.

x1	T/(K)
	293.15	298.15	303.15	308.15	313.15
DEG (1) + DMSO (2)
0.0000 0.1062 0.2007 0.3034 0.4110 0.5108 0.5972 0.6955 0.8096 0.8819 1.0000	94.262 94.243 94.286 94.375 94.490 94.600 94.687 94.770 94.837 94.862 94.877	94.773 94.679 94.675 94.728 94.820 94.918 95.001 95.082 95.150 95.176 95.192	95.142 95.067 95.067 95.115 95.197 95.284 95.358 95.431 95.494 95.519 95.535	95.635 95.533 95.513 95.541 95.606 95.681 95.748 95.816 95.875 95.900 95.915	95.966 95.888 95.876 95.904 95.964 96.033 96.096 96.161 96.221 96.246 96.263
MDEA (1) + DMSO (2)
0.0000 0.1003 0.1967 0.2997 0.4006 0.5001 0.6020 0.6937 0.7983 0.8967 1.0000	115.271 115.225 115.145 115.034 114.915 114.799 114.690 114.607 114.536 114.495 114.481	115.647 115.644 115.593 115.505 115.400 115.292 115.190 115.110 115.042 115.003 114.989	115.955 115.978 115.947 115.877 115.786 115.689 115.594 115.519 115.453 115.415 115.401	116.191 116.266 116.274 116.235 116.167 116.087 116.003 115.936 115.876 115.840 115.827	116.400 116.539 116.595 116.595 116.555 116.492 116.421 116.360 116.303 116.269 116.257

and

Table A8. Partial molar volumes $\overline{V_2}$ (cm³·mol⁻¹) for binary systems in the temperature range from 293.15 to 313.15 K.

x1	T/(K)
	293.15	298.15	303.15	308.15	313.15
DEG (1) + DMSO (2)
0.0000 0.1062 0.2007 0.3034 0.4110 0.5108 0.5972 0.6955 0.8096 0.8819 1.0000	71.014 71.007 70.992 70.974 70.954 70.933 70.907 70.863 70.774 70.688 70.471	71.338 71.329 71.313 71.293 71.274 71.258 71.241 71.211 71.146 71.078 70.897	71.666 71.656 71.639 71.616 71.593 71.573 71.554 71.527 71.475 71.425 71.295	71.989 71.979 71.960 71.935 71.910 71.889 71.871 71.849 71.809 71.770 71.669	72.322 72.313 72.293 72.267 72.242 72.224 72.213 72.206 72.202 72.200 72.189
MDEA (1) + DMSO (2)
0.0000 0.1003 0.1967 0.2997 0.4006 0.5001 0.6020 0.6937 0.7983 0.8967 1.0000	71.014 71.034 71.086 71.171 71.281 71.414 71.577 71.748 71.977 72.231 72.548	71.338 71.359 71.411 71.496 71.605 71.736 71.896 72.065 72.292 72.548 72.872	71.666 71.686 71.738 71.823 71.931 72.060 72.214 72.374 72.587 72.825 73.122	71.989 72.010 72.064 72.149 72.257 72.383 72.534 72.690 72.897 73.127 73.417	72.322 72.344 72.400 72.487 72.593 72.716 72.859 73.003 73.192 73.399 73.657

.

Our results show that for the DEG + DMSO system, the decrease in the DMSO concentration leads to the increase in the values of the apparent molar volumes and partial molar volumes of DEG, and the decrease in the values of the apparent molar volumes and partial molar volumes of DMSO. For the MDEA + DMSO system the decrease in the DMSO concentration leads to the decrease in the values of the apparent molar volumes and partial molar volumes of MDEA and the increase in the values of the apparent molar volumes and partial molar volumes of DMSO.

3.3. Thermodynamic Functions of Activation

The activation energy of viscous flow was calculated with the equations [63]:

$$\eta =\frac{hN}{V}exp\left(\frac{\Delta {\mathrm{G}}^{\ne }}{RT}\right)$$

(27)

$$\Delta {\mathrm{G}}^{\ne }=\Delta {\mathrm{H}}^{\ne }-T\Delta {\mathrm{S}}^{\ne }$$

(28)

where η is the viscosity of a liquid solution, h is Planck’s constant, N is Avogadro´s number, V is the molar volume of the solution, R is the universal gas constant, T is temperature,$\Delta {\mathrm{G}}^{\ne }$, $\Delta {\mathrm{H}}^{\ne }$ and $\Delta {\mathrm{S}}^{\ne }$ are the molar Gibbs energy, enthalpy and entropy of activation of viscous flow. The plots of ln(ηV/hN) versus 1/T are linear in the temperature range 293.15 to 313.15 K and the values of enthalpy of activation of viscous flow ($\Delta {\mathrm{H}}^{\ne }$) and entropy of activation viscous flow ($\Delta {\mathrm{S}}^{\ne }$) were obtained from the corresponding slopes and intercept. The values of $\Delta {\mathrm{G}}^{\ne }$ were also calculated. The values of thermodynamic functions of activation of viscous flow are listed in

Table 5. Values of ΔG^≠, ΔH^≠, ΔS^≠ for the binary mixtures.

x1	ΔH≠ (kJ/mol)	ΔS≠ (J/mol·K)	ΔG≠ (kJ/mol) T/(K)
			293.15	298.15	303.15	308.15	313.15
DEG (1) + DMSO (2)
0.0000 0.1062 0.2007 0.3034 0.4110 0.5108 0.5972 0.6955 0.8096 0.8819 1.0000	14.02 15.59 17.40 19.96 21.80 23.55 25.69 26.68 28.41 29.02 32.34	−2.01 0.26 3.49 9.58 13.10 16.72 21.91 23.06 26.52 27.12 35.69	14.61 15.51 16.34 17.15 17.96 18.65 19.27 19.91 20.64 21.07 21.88	14.62 15.51 16.33 17.10 17.80 18.57 19.16 19.80 20.50 20.93 21.71	14.63 15.51 16.31 17.05 17.83 18.48 19.05 19.68 20.37 20.80 21.53	14.64 15.50 16.29 17.01 17.77 18.40 18.94 19.57 20.24 20.66 21.35	14.65 15.50 16.27 16.96 17.70 18.32 18.83 19.45 20.11 20.53 21.17
MDEA (1) + DMSO (2)
0.0000 0.1003 0.1967 0.2997 0.4006 0.5001 0.6020 0.6937 0.7983 0.8967 1.0000	14.02 21.72 23.69 25.93 28.08 29.52 32.32 34.31 36.57 38.16 39.56	−2.01 16.02 19.72 24.08 28.27 30.13 36.46 40.39 45.18 48.10 49.62	14.61 17.02 17.91 18.87 19.79 20.69 21.63 22.47 23.32 24.06 25.01	14.62 16.94 17.81 18.75 19.65 20.54 21.45 22.26 23.10 23.82 24.76	14.63 16.86 17.71 18.63 19.51 20.39 21.26 22.06 22.87 23.58 24.51	14.64 16.78 17.61 18.51 19.37 20.24 21.08 21.86 22.64 23.34 24.27	14.65 16.70 17.52 18.39 19.23 20.09 20.90 21.66 22.42 23.10 24.02

. The values of $\Delta {\mathrm{G}}^{\ne }$ and $\Delta {\mathrm{H}}^{\ne }$ are positive for both binary systems and increase with the decrease in DMSO concentration in the solution at a constant temperature. The values of $\Delta {\mathrm{G}}^{\ne }$ at constant concentration decrease if the temperature increases, except for the pure DMSO.

The values of $\Delta {\mathrm{S}}^{\ne }$ are positive for all compoundsand binary mixtures except DMSO.

The positive $\Delta {\mathrm{H}}^{\ne }$. values decrease with increasing DMSO concentration, indicating that the viscous flow in DMSO is easier than in binary mixtures (DEG + DMSO, MDEA + DMSO) or in DEG. The $\Delta {\mathrm{S}}^{\ne }$ values decrease with increasing DMSO concentration for both analyzed systems, which reveals that the viscous flow is more ordered processing DMSO than in binary mixtures or in DEG.

4. Conclusions

Density and viscosity of the binary systems DEG (1) + DMSO (2) and MDEA (1) + DMSO (2) were determined at temperatures between 293.15 to 313.15 K and atmospheric pressure. The calculated V^E values are negative for the DEG (1) + DMSO (2) system and positive for the MDEA (1) + DMSO (2) system, while the calculated Δη were negative for both systems. Models from Grunberg–Nissan, Heric–Brewer, Wilson, Noda–Ishida and Eyring–NRTL have been used to calculate viscosity coefficients and were compared with experimental data. The results showed that the Eyring–NRTL model is adequate to describe the viscosities of the binary mixtures. The activation energies of viscous flow were calculated. The values of $\Delta {\mathrm{G}}^{\ne }$ and $\Delta {\mathrm{H}}^{\ne }$ are positive for both binary systems and the values of $\Delta {\mathrm{S}}^{\ne }$ are positive for all compounds and binary mixtures except DMSO.