- InChI
- InChI=1S/C6H14O/c1-5(2)7-6(3)4/h5-6H,1-4H3
- InChI Key
- ZAFNJMIOTHYJRJ-UHFFFAOYSA-N
- Formula
- C6H14O
- SMILES
- CC(C)OC(C)C
- Molecular Weight1
- 102.17
- CAS
- 108-20-3
- Other Names
-
- (iso-C3H7)2O
- 1,1'-Dimethyldiethyl ether
- 1-methyl-1-(1-methylethoxy)ethane
- 2,2'-OXYBIS-PROPANE
- 2,2'-Oxybispropane
- 2,4-dimethyl-3-oxapentane
- 2-ISOPROPOXYPROPANE
- Bis(isopropyl) ether
- Diiospropyl ether
- Diisopropyl oxide
- Ether isopropylique
- Ether, isopropyl
- ISOPROPYL ETHER
- Izopropylowy eter
- Propane, 2,2'-oxybis-
- UN 1159
- bis(1-methylethyl) ether
- ω : Acentric Factor.
- PAff : Proton affinity (kJ/mol).
- Tig : Autoignition Temperature (K).
- BasG : Gas basicity (kJ/mol).
- ΔcH°liquid : Standard liquid enthalpy of combustion (kJ/mol).
- Cp,gas : Ideal gas heat capacity (J/mol×K).
- Cp,liquid : Liquid phase heat capacity (J/mol×K).
- μ : Dipole Moment (debye).
- η : Dynamic viscosity (Pa×s).
- LFL : Lower Flammability Limit (% in Air).
- UFL : Upper Flammability Limit (% in Air).
- Tflash,cc : Flash Point (Closed Cup Method) (K).
- Tflash,oc : Flash Point (Open Cup Method) (K).
- ΔfG° : Standard Gibbs free energy of formation (kJ/mol).
- ΔfH°gas : Enthalpy of formation at standard conditions (kJ/mol).
- ΔfH°liquid : Liquid phase enthalpy of formation at standard conditions (kJ/mol).
- ΔfusH° : Enthalpy of fusion at standard conditions (kJ/mol).
- ΔfusH : Enthalpy of fusion at a given temperature (kJ/mol).
- ΔvapH° : Enthalpy of vaporization at standard conditions (kJ/mol).
- ΔvapH : Enthalpy of vaporization at a given temperature (kJ/mol).
- IE : Ionization energy (eV).
- ν : Kinematic viscosity (m2/s).
- log10WS : Log10 of Water solubility in mol/l.
- logPoct/wat : Octanol/Water partition coefficient.
- McVol : McGowan's characteristic volume (ml/mol).
- NFPA Fire : NFPA Fire Rating.
- NFPA Health : NFPA Health Rating.
- NFPA Safety : NFPA Safety Rating.
- Pc : Critical Pressure (kPa).
- Pvap : Vapor pressure (kPa).
- n0 : Refractive Index.
- ρl : Liquid Density (kg/m3).
- Inp : Non-polar retention indices.
- I : Polar retention indices.
- ΔfusS : Entropy of fusion at a given temperature (J/mol×K).
- S°liquid : Liquid phase molar entropy at standard conditions (J/mol×K).
- csound,fluid : Speed of sound in fluid (m/s).
- γ : Surface Tension (N/m).
- Tboil : Normal Boiling Point Temperature (K).
- Tc : Critical Temperature (K).
- λ : Liquid thermal conductivity (W/m×K).
- Tfus : Normal melting (fusion) point (K).
- Ttriple : Triple Point Temperature (K).
- Vc : Critical Volume (m3/kmol).
- Zc : Critical Compressibility.
- 1: Molecular weight from the IUPAC atomic weights tables.
Cheméo is a service of Céondo GmbH, since 2007, we provide simulation, modelling and software development services for the industry.
Do not hesitate to contact us for your projects.
Contents
- Physical Properties
- Temperature Dependent Properties
- Datasets
- Correlations
- Similar Compounds
- Mixtures
- Sources
Physical Properties
| Property | Value | Unit | Source |
|---|---|---|---|
| ω | 0.3310 | KDB | |
| PAff | 855.50 | kJ/mol | NIST |
| Tig | 716.48 | K | KDB |
| BasG | 828.10 | kJ/mol | NIST |
| ΔcH°liquid | -4010.40 ± 1.30 | kJ/mol | NIST |
| μ | 1.20 | debye | KDB |
| LFL | 1.40 | % in Air | KDB |
| UFL | 7.90 | % in Air | KDB |
| Tflash,cc | 247.04 | K | KDB |
| Tflash,oc | 245.37 | K | KDB |
| ΔfG° | -122.00 | kJ/mol | KDB |
| ΔfH°gas | [-319.00; -318.00] | kJ/mol |
|
| ΔfH°gas | -319.00 | kJ/mol | KDB |
| ΔfH°gas | -318.00 ± 3.00 | kJ/mol | NIST |
| ΔfH°liquid | -351.50 ± 1.40 | kJ/mol | NIST |
| ΔfusH° | 5.44 | kJ/mol | Joback Calculated Property |
| ΔvapH° | [32.10; 32.70] | kJ/mol |
|
| ΔvapH° | 32.26 | kJ/mol | NIST |
| ΔvapH° | 32.70 ± 0.50 | kJ/mol | NIST |
| ΔvapH° | 32.12 | kJ/mol | NIST |
| ΔvapH° | 32.10 ± 0.10 | kJ/mol | NIST |
| IE | [9.16; 9.32] | eV |
|
| IE | 9.20 ± 0.05 | eV | NIST |
| IE | 9.16 ± 0.05 | eV | NIST |
| IE | 9.20 ± 0.05 | eV | NIST |
| IE | 9.32 | eV | NIST |
| log10WS | [-1.10; -1.10] |
|
|
| log10WS | -1.10 | Aq. Sol... | |
| log10WS | -1.10 | Estimat... | |
| logPoct/wat | 1.820 | Crippen Calculated Property | |
| McVol | 101.270 | ml/mol | McGowan Calculated Property |
| NFPA Fire | 3 | KDB | |
| NFPA Health | 2 | KDB | |
| NFPA Safety | 1 | KDB | |
| Pc | [2832.00; 2875.10] | kPa |
|
| Pc | 2832.00 | kPa | KDB |
| Pc | 2832.00 ± 6.00 | kPa | NIST |
| Pc | 2875.10 ± 13.78 | kPa | NIST |
| Inp | [563.00; 624.00] |
|
|
| Inp | 593.00 | NIST | |
| Inp | 590.00 | NIST | |
| Inp | 594.00 | NIST | |
| Inp | Outlier 624.00 | NIST | |
| Inp | 563.00 | NIST | |
| Inp | 564.00 | NIST | |
| Inp | 570.00 | NIST | |
| Inp | 565.00 | NIST | |
| Inp | 568.00 | NIST | |
| Inp | 570.00 | NIST | |
| Inp | 602.00 | NIST | |
| Inp | 602.00 | NIST | |
| Inp | 590.00 | NIST | |
| Inp | 568.00 | NIST | |
| Inp | 598.00 | NIST | |
| Inp | 596.00 | NIST | |
| Inp | 598.00 | NIST | |
| Inp | 594.00 | NIST | |
| Inp | 603.00 | NIST | |
| Inp | 594.00 | NIST | |
| Inp | 594.00 | NIST | |
| Inp | 593.00 | NIST | |
| Inp | 564.00 | NIST | |
| I | [649.00; 682.00] |
|
|
| I | 652.00 | NIST | |
| I | Outlier 679.00 | NIST | |
| I | Outlier 682.00 | NIST | |
| I | 670.00 | NIST | |
| I | 667.00 | NIST | |
| I | 659.00 | NIST | |
| I | 658.30 | NIST | |
| I | 657.00 | NIST | |
| I | 655.40 | NIST | |
| I | 651.00 | NIST | |
| I | 649.00 | NIST | |
| I | 662.00 | NIST | |
| I | 657.00 | NIST | |
| I | 658.00 | NIST | |
| I | 659.00 | NIST | |
| I | 651.00 | NIST | |
| I | 649.00 | NIST | |
| S°liquid | [294.60; 304.60] | J/mol×K |
|
| S°liquid | 304.60 | J/mol×K | NIST |
| S°liquid | 294.60 | J/mol×K | NIST |
| Tboil | [340.70; 342.20] | K |
|
| Tboil | 341.66 | K | KDB |
| Tboil | 341.53 | K | Vapor l... |
| Tboil | 341.35 | K | Quatern... |
| Tboil | 341.55 | K | (Liquid... |
| Tboil | 341.40 | K | Isobari... |
| Tboil | 341.77 | K | Vapour-... |
| Tboil | 341.72 | K | Separat... |
| Tboil | 341.35 | K | Excess ... |
| Tboil | 341.35 | K | Vapor-L... |
| Tboil | 341.60 ± 0.30 | K | NIST |
| Tboil | 341.40 ± 0.30 | K | NIST |
| Tboil | 341.63 ± 0.20 | K | NIST |
| Tboil | 341.20 | K | NIST |
| Tboil | 341.50 | K | NIST |
| Tboil | 341.69 ± 0.12 | K | NIST |
| Tboil | Outlier 340.70 ± 0.50 | K | NIST |
| Tboil | 341.65 | K | NIST |
| Tboil | 341.15 ± 0.30 | K | NIST |
| Tboil | Outlier 340.80 ± 0.60 | K | NIST |
| Tboil | 341.55 ± 1.00 | K | NIST |
| Tboil | 341.60 ± 2.00 | K | NIST |
| Tboil | 341.42 ± 0.07 | K | NIST |
| Tboil | 341.15 ± 1.00 | K | NIST |
| Tboil | Outlier 342.20 ± 0.20 | K | NIST |
| Tc | [499.60; 500.32] | K |
|
| Tc | 500.32 | K | KDB |
| Tc | 500.30 | K | NIST |
| Tc | 499.60 ± 0.30 | K | NIST |
| Tc | 499.60 ± 0.30 | K | NIST |
| Tc | 500.32 ± 0.10 | K | NIST |
| Tc | 500.10 ± 0.30 | K | NIST |
| Tfus | [186.30; 187.65] | K |
|
| Tfus | 186.30 | K | KDB |
| Tfus | 186.75 | K | Aq. Sol... |
| Tfus | 187.65 | K | NIST |
| Tfus | 187.26 ± 0.05 | K | NIST |
| Ttriple | [186.30; 187.77] | K |
|
| Ttriple | 187.77 | K | KDB |
| Ttriple | 187.77 ± 0.06 | K | NIST |
| Ttriple | 186.30 ± 0.20 | K | NIST |
| Vc | [0.386; 0.386] | m3/kmol |
|
| Vc | 0.386 | m3/kmol | KDB |
| Vc | 0.386 ± 0.005 | m3/kmol | NIST |
| Zc | 0.2627820 | KDB |
Temperature Dependent Properties
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Cp,gas | [182.47; 219.11] | J/mol×K | [360.04; 449.98] |
|
|
T(K) Ideal gas heat capacity (J/mol×K) 180 190 200 210 220 400 450 | ||||
| Cp,gas | 182.47 | J/mol×K | 360.04 | NIST |
| Cp,gas | 191.01 | J/mol×K | 380.01 | NIST |
| Cp,gas | 199.33 | J/mol×K | 399.98 | NIST |
| Cp,gas | 209.60 | J/mol×K | 424.98 | NIST |
| Cp,gas | 219.11 | J/mol×K | 449.98 | NIST |
| Cp,liquid | [211.50; 232.04] | J/mol×K | [290.50; 339.89] |
|
|
T(K) Liquid phase heat capacity (J/mol×K) 210 215 220 225 230 300 320 340 | ||||
| Cp,liquid | 211.50 | J/mol×K | 290.50 | Speed o... |
| Cp,liquid | 216.31 | J/mol×K | 293.10 | NIST |
| Cp,liquid | 213.44 | J/mol×K | 295.44 | Speed o... |
| Cp,liquid | 216.74 | J/mol×K | 298.15 | NIST |
| Cp,liquid | 216.10 | J/mol×K | 298.15 | NIST |
| Cp,liquid | 215.28 | J/mol×K | 300.38 | Speed o... |
| Cp,liquid | 217.33 | J/mol×K | 305.32 | Speed o... |
| Cp,liquid | 219.37 | J/mol×K | 310.26 | Speed o... |
| Cp,liquid | 221.41 | J/mol×K | 315.20 | Speed o... |
| Cp,liquid | 223.46 | J/mol×K | 320.13 | Speed o... |
| Cp,liquid | 225.50 | J/mol×K | 325.07 | Speed o... |
| Cp,liquid | 227.65 | J/mol×K | 330.01 | Speed o... |
| Cp,liquid | 229.89 | J/mol×K | 334.95 | Speed o... |
| Cp,liquid | 232.04 | J/mol×K | 339.89 | Speed o... |
| η | [0.0002723; 0.0003646] | Pa×s | [283.15; 313.15] |
|
|
T(K) Dynamic viscosity (Pa×s) 2.80e-4 3.00e-4 3.20e-4 3.40e-4 3.60e-4 290 300 310 | ||||
| η | 0.0003646 | Pa×s | 283.15 | Viscosi... |
| η | 0.0003486 | Pa×s | 288.15 | Viscosi... |
| η | 0.0003340 | Pa×s | 293.15 | Viscosi... |
| η | 0.0003178 | Pa×s | 298.15 | Viscosi... |
| η | 0.0003001 | Pa×s | 303.15 | Viscosi... |
| η | 0.0002857 | Pa×s | 308.15 | Viscosi... |
| η | 0.0002723 | Pa×s | 313.15 | Viscosi... |
| ΔfusH | [11.03; 12.05] | kJ/mol | [186.30; 187.80] |
|
| ΔfusH | 11.03 | kJ/mol | 186.30 | NIST |
| ΔfusH | 12.04 | kJ/mol | 187.77 | NIST |
| ΔfusH | 12.05 | kJ/mol | 187.80 | NIST |
| ΔfusH | 12.05 | kJ/mol | 187.80 | NIST |
| ΔvapH | [29.10; 33.20] | kJ/mol | [300.50; 468.00] |
|
|
T(K) Enthalpy of vaporization at a given temperature (kJ/mol) 29 30 31 32 33 300 350 400 450 | ||||
| ΔvapH | 33.00 | kJ/mol | 300.50 | NIST |
| ΔvapH | 33.20 | kJ/mol | 303.00 | NIST |
| ΔvapH | 32.10 | kJ/mol | 319.00 | NIST |
| ΔvapH | 32.60 | kJ/mol | 324.50 | NIST |
| ΔvapH | 29.20 | kJ/mol | 324.50 | NIST |
| ΔvapH | 31.10 | kJ/mol | 328.00 | NIST |
| ΔvapH | 30.10 | kJ/mol | 335.50 | NIST |
| ΔvapH | 29.33 | kJ/mol | 341.40 | KDB |
| ΔvapH | 29.10 | kJ/mol | 341.50 | NIST |
| ΔvapH | 29.90 | kJ/mol | 400.00 | NIST |
| ΔvapH | 29.50 | kJ/mol | 468.00 | NIST |
| ν | [0.0000004; 0.0000005] | m2/s | [283.15; 313.15] |
|
| ν | 0.0000005 | m2/s | 283.15 | Kinemat... |
| ν | 0.0000004 | m2/s | 298.15 | Kinemat... |
| ν | 0.0000004 | m2/s | 313.15 | Kinemat... |
| Pvap | [3.21; 151.82] | kPa | [263.75; 354.88] |
|
|
T(K) Vapor pressure (kPa) 0 20 40 60 80 100 120 140 160 280 300 320 340 | ||||
| Pvap | 3.21 | kPa | 263.75 | Vapour ... |
| Pvap | 5.71 | kPa | 273.47 | Vapour ... |
| Pvap | 9.69 | kPa | 283.35 | Vapour ... |
| Pvap | 10.74 | kPa | 284.93 | Isother... |
| Pvap | 10.75 | kPa | 284.93 | Isother... |
| Pvap | 12.65 | kPa | 288.15 | Isother... |
| Pvap | 15.80 | kPa | 293.29 | Vapour ... |
| Pvap | 17.21 | kPa | 294.90 | Isother... |
| Pvap | 17.21 | kPa | 294.91 | Isother... |
| Pvap | 20.00 | kPa | 298.15 | Isother... |
| Pvap | 24.57 | kPa | 303.28 | Vapour ... |
| Pvap | 26.57 | kPa | 304.87 | Isother... |
| Pvap | 26.58 | kPa | 304.89 | Isother... |
| Pvap | 30.46 | kPa | 308.15 | Isother... |
| Pvap | 30.91 | kPa | 308.58 | The the... |
| Pvap | 37.26 | kPa | 313.25 | The the... |
| Pvap | 36.95 | kPa | 313.27 | Vapour ... |
| Pvap | 39.71 | kPa | 314.86 | Isother... |
| Pvap | 39.72 | kPa | 314.87 | Isother... |
| Pvap | 45.83 | kPa | 318.65 | The the... |
| Pvap | 53.85 | kPa | 323.25 | Vapour ... |
| Pvap | 56.12 | kPa | 324.17 | The the... |
| Pvap | 57.64 | kPa | 324.85 | Isother... |
| Pvap | 57.65 | kPa | 324.87 | Isother... |
| Pvap | 67.49 | kPa | 329.40 | The the... |
| Pvap | 76.24 | kPa | 333.22 | Vapour ... |
| Pvap | 81.42 | kPa | 334.85 | Isother... |
| Pvap | 81.41 | kPa | 334.85 | Isother... |
| Pvap | 81.57 | kPa | 334.98 | The the... |
| Pvap | 93.18 | kPa | 339.03 | The the... |
| Pvap | 95.31 | kPa | 339.73 | The the... |
| Pvap | 97.44 | kPa | 340.41 | The the... |
| Pvap | 104.96 | kPa | 343.18 | Vapour ... |
| Pvap | 112.36 | kPa | 344.84 | Isother... |
| Pvap | 112.39 | kPa | 344.85 | Isother... |
| Pvap | 151.81 | kPa | 354.87 | Isother... |
| Pvap | 151.82 | kPa | 354.88 | Isother... |
| n0 | [1.35667; 1.37358] | [283.15; 313.15] |
|
|
|
T(K) Refractive Index 1.36 1.36 1.37 1.37 1.38 290 300 310 | ||||
| n0 | 1.37358 | 283.15 | Volumet... | |
| n0 | 1.37126 | 288.15 | Densiti... | |
| n0 | 1.37084 | 288.15 | Volumet... | |
| n0 | 1.37093 | 288.15 | Densiti... | |
| n0 | 1.36812 | 293.15 | Volumet... | |
| n0 | 1.36510 | 298.15 | Vapor L... | |
| n0 | 1.36650 | 298.15 | Atmosph... | |
| n0 | 1.36537 | 298.15 | Densiti... | |
| n0 | 1.36520 | 298.15 | Isobari... | |
| n0 | 1.36652 | 298.15 | Isobari... | |
| n0 | 1.36524 | 298.15 | Densiti... | |
| n0 | 1.36540 | 298.15 | (Vapor ... | |
| n0 | 1.36520 | 298.15 | sobaric... | |
| n0 | 1.36644 | 298.15 | Vapor l... | |
| n0 | 1.36520 | 298.15 | Effect ... | |
| n0 | 1.36525 | 298.15 | Volumet... | |
| n0 | 1.36523 | 298.15 | Isobari... | |
| n0 | 1.36530 | 298.20 | Measure... | |
| n0 | 1.36242 | 303.15 | Volumet... | |
| n0 | 1.35956 | 308.15 | Volumet... | |
| n0 | 1.35954 | 308.15 | Densiti... | |
| n0 | 1.35944 | 308.15 | Densiti... | |
| n0 | 1.35667 | 313.15 | Volumet... | |
| ρl | [686.20; 728.82] | kg/m3 | [288.15; 328.15] |
|
|
T(K) Liquid Density (kg/m3) 690 700 710 720 730 290 300 310 320 | ||||
| ρl | 728.82 | kg/m3 | 288.15 | Volumet... |
| ρl | 724.00 | kg/m3 | 293.00 | KDB |
| ρl | 723.67 | kg/m3 | 293.15 | Volumet... |
| ρl | 723.80 | kg/m3 | 298.15 | Tie-Lin... |
| ρl | 719.17 | kg/m3 | 298.15 | Isother... |
| ρl | 718.23 | kg/m3 | 298.15 | Vapour-... |
| ρl | 718.30 | kg/m3 | 298.15 | Experim... |
| ρl | 718.30 | kg/m3 | 298.15 | Isobari... |
| ρl | 718.51 | kg/m3 | 298.15 | Volumet... |
| ρl | 718.24 | kg/m3 | 298.15 | Excess ... |
| ρl | 718.38 | kg/m3 | 298.15 | Excess ... |
| ρl | 719.17 | kg/m3 | 298.15 | Volumet... |
| ρl | 718.14 | kg/m3 | 298.15 | Phase e... |
| ρl | 718.62 | kg/m3 | 298.15 | Liquid ... |
| ρl | 718.46 | kg/m3 | 298.15 | Volumet... |
| ρl | 718.70 | kg/m3 | 298.15 | Excess ... |
| ρl | 718.51 | kg/m3 | 298.15 | Isother... |
| ρl | 718.38 | kg/m3 | 298.15 | Isother... |
| ρl | 713.51 | kg/m3 | 303.15 | Isother... |
| ρl | 713.10 | kg/m3 | 303.15 | Density... |
| ρl | 713.21 | kg/m3 | 303.15 | Volumet... |
| ρl | 707.90 | kg/m3 | 308.15 | Density... |
| ρl | 702.50 | kg/m3 | 313.15 | Density... |
| ρl | 702.59 | kg/m3 | 313.15 | Volumet... |
| ρl | 686.20 | kg/m3 | 328.15 | Volumet... |
| ΔfusS | [59.18; 64.09] | J/mol×K | [186.30; 187.77] |
|
| ΔfusS | 59.18 | J/mol×K | 186.30 | NIST |
| ΔfusS | 64.09 | J/mol×K | 187.77 | NIST |
| csound,fluid | [135.68; 986.38] | m/s | [303.08; 492.48] |
|
|
T(K) Speed of sound in fluid (m/s) 200 400 600 800 1000 300 350 400 450 | ||||
| csound,fluid | 986.38 | m/s | 303.08 | Speed o... |
| csound,fluid | 975.00 | m/s | 303.15 | Thermod... |
| csound,fluid | 976.00 | m/s | 303.15 | Thermod... |
| csound,fluid | 976.00 | m/s | 303.15 | Thermod... |
| csound,fluid | 976.00 | m/s | 303.15 | Thermod... |
| csound,fluid | 934.00 | m/s | 313.15 | Thermod... |
| csound,fluid | 932.00 | m/s | 313.15 | Thermod... |
| csound,fluid | 932.00 | m/s | 313.15 | Thermod... |
| csound,fluid | 932.00 | m/s | 313.15 | Thermod... |
| csound,fluid | 915.66 | m/s | 318.27 | Speed o... |
| csound,fluid | 889.00 | m/s | 323.15 | Thermod... |
| csound,fluid | 889.00 | m/s | 323.15 | Thermod... |
| csound,fluid | 889.00 | m/s | 323.15 | Thermod... |
| csound,fluid | 891.00 | m/s | 323.15 | Thermod... |
| csound,fluid | 892.00 | m/s | 323.15 | Thermod... |
| csound,fluid | 852.50 | m/s | 333.62 | Speed o... |
| csound,fluid | 790.74 | m/s | 347.96 | Speed o... |
| csound,fluid | 731.21 | m/s | 362.87 | Speed o... |
| csound,fluid | 662.26 | m/s | 378.14 | Speed o... |
| csound,fluid | 593.47 | m/s | 393.15 | Speed o... |
| csound,fluid | 552.35 | m/s | 402.97 | Speed o... |
| csound,fluid | 514.15 | m/s | 412.75 | Speed o... |
| csound,fluid | 469.11 | m/s | 422.75 | Speed o... |
| csound,fluid | 426.77 | m/s | 432.74 | Speed o... |
| csound,fluid | 384.46 | m/s | 443.46 | Speed o... |
| csound,fluid | 336.71 | m/s | 453.54 | Speed o... |
| csound,fluid | 315.85 | m/s | 457.54 | Speed o... |
| csound,fluid | 290.41 | m/s | 463.00 | Speed o... |
| csound,fluid | 263.51 | m/s | 468.31 | Speed o... |
| csound,fluid | 237.38 | m/s | 473.80 | Speed o... |
| csound,fluid | 210.25 | m/s | 478.69 | Speed o... |
| csound,fluid | 185.80 | m/s | 483.10 | Speed o... |
| csound,fluid | 162.27 | m/s | 487.42 | Speed o... |
| csound,fluid | 135.68 | m/s | 492.48 | Speed o... |
| γ | [0.01; 0.02] | N/m | [248.07; 373.17] |
|
|
T(K) Surface Tension (N/m) 0.01 0.01 0.01 0.02 0.02 0.02 0.02 250 300 350 | ||||
| γ | 0.02 | N/m | 248.07 | Surface... |
| γ | 0.02 | N/m | 253.23 | Surface... |
| γ | 0.02 | N/m | 258.10 | Surface... |
| γ | 0.02 | N/m | 263.18 | Surface... |
| γ | 0.02 | N/m | 268.33 | Surface... |
| γ | 0.02 | N/m | 273.46 | Surface... |
| γ | 0.02 | N/m | 278.50 | Surface... |
| γ | 0.02 | N/m | 283.18 | Surface... |
| γ | 0.02 | N/m | 288.18 | Surface... |
| γ | 0.02 | N/m | 293.16 | Surface... |
| γ | 0.02 | N/m | 298.10 | Surface... |
| γ | 0.02 | N/m | 298.20 | KDB |
| γ | 0.02 | N/m | 303.17 | Surface... |
| γ | 0.02 | N/m | 308.08 | Surface... |
| γ | 0.02 | N/m | 313.27 | Surface... |
| γ | 0.02 | N/m | 318.17 | Surface... |
| γ | 0.01 | N/m | 323.19 | Surface... |
| γ | 0.01 | N/m | 328.12 | Surface... |
| γ | 0.01 | N/m | 333.12 | Surface... |
| γ | 0.01 | N/m | 338.11 | Surface... |
| γ | 0.01 | N/m | 343.10 | Surface... |
| γ | 0.01 | N/m | 348.10 | Surface... |
| γ | 0.01 | N/m | 353.10 | Surface... |
| γ | 0.01 | N/m | 358.15 | Surface... |
| γ | 0.01 | N/m | 363.17 | Surface... |
| γ | 0.01 | N/m | 368.17 | Surface... |
| γ | 0.01 | N/m | 373.17 | Surface... |
Datasets
Viscosity, Pa*s
| Fixed | Measured | |
|---|---|---|
| Pressure, kPa - Liquid | Temperature, K - Liquid | Viscosity, Pa*s - Liquid |
| 20000.00 | 293.15 | 0.0004 |
| 40000.00 | 293.15 | 0.0005 |
| 60000.00 | 293.15 | 0.0005 |
| 80000.00 | 293.15 | 0.0006 |
| 100000.00 | 293.15 | 0.0007 |
| 20000.00 | 313.15 | 0.0003 |
| 40000.00 | 313.15 | 0.0004 |
| 60000.00 | 313.15 | 0.0005 |
| 80000.00 | 313.15 | 0.0005 |
| 100000.00 | 313.15 | 0.0006 |
| 20000.00 | 333.15 | 0.0003 |
| 40000.00 | 333.15 | 0.0003 |
| 60000.00 | 333.15 | 0.0004 |
| 80000.00 | 333.15 | 0.0005 |
| 100000.00 | 333.15 | 0.0005 |
| 20000.00 | 353.15 | 0.0003 |
| 40000.00 | 353.15 | 0.0003 |
| 60000.00 | 353.15 | 0.0004 |
| 80000.00 | 353.15 | 0.0004 |
| 100000.00 | 353.15 | 0.0005 |
| 100.00 | 293.15 | 0.0003 |
| 100.00 | 313.15 | 0.0003 |
| 100.00 | 333.15 | 0.0002 |
| Reference | ||
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Viscosity, Pa*s - Liquid |
| 243.15 | 100.00 | 0.0006 |
| 243.15 | 4660.00 | 0.0006 |
| 243.15 | 10070.00 | 0.0007 |
| 243.15 | 15370.00 | 0.0007 |
| 243.15 | 20860.00 | 0.0008 |
| 253.15 | 100.00 | 0.0005 |
| 253.15 | 4720.00 | 0.0006 |
| 253.15 | 9990.00 | 0.0006 |
| 253.15 | 15400.00 | 0.0006 |
| 253.15 | 20740.00 | 0.0006 |
| 263.15 | 100.00 | 0.0005 |
| 263.15 | 4470.00 | 0.0005 |
| 263.15 | 9490.00 | 0.0005 |
| 263.15 | 14490.00 | 0.0005 |
| 263.15 | 19640.00 | 0.0006 |
| 273.15 | 100.00 | 0.0004 |
| 273.15 | 4690.00 | 0.0004 |
| 273.15 | 10010.00 | 0.0005 |
| 273.15 | 15290.00 | 0.0005 |
| 273.15 | 20420.00 | 0.0005 |
| 283.15 | 100.00 | 0.0004 |
| 283.15 | 4700.00 | 0.0004 |
| 283.15 | 10100.00 | 0.0004 |
| 283.15 | 15460.00 | 0.0004 |
| 283.15 | 21360.00 | 0.0005 |
| 293.15 | 100.00 | 0.0003 |
| 293.15 | 4470.00 | 0.0003 |
| 293.15 | 9590.00 | 0.0004 |
| 293.15 | 14750.00 | 0.0004 |
| 293.15 | 20450.00 | 0.0004 |
| 303.15 | 100.00 | 0.0003 |
| 303.15 | 4440.00 | 0.0003 |
| 303.15 | 9500.00 | 0.0003 |
| 303.15 | 14650.00 | 0.0003 |
| 303.15 | 19650.00 | 0.0004 |
| 313.15 | 100.00 | 0.0003 |
| 313.15 | 4840.00 | 0.0003 |
| 313.15 | 10140.00 | 0.0003 |
| 313.15 | 15550.00 | 0.0003 |
| 313.15 | 21490.00 | 0.0003 |
| 323.15 | 100.00 | 0.0002 |
| 323.15 | 4760.00 | 0.0003 |
| 323.15 | 10370.00 | 0.0003 |
| 323.15 | 15480.00 | 0.0003 |
| 323.15 | 20780.00 | 0.0003 |
| 333.15 | 100.00 | 0.0002 |
| 333.15 | 4750.00 | 0.0002 |
| 333.15 | 10360.00 | 0.0003 |
| 333.15 | 15670.00 | 0.0003 |
| 333.15 | 20890.00 | 0.0003 |
| 343.15 | 130.00 | 0.0002 |
| 343.15 | 4390.00 | 0.0002 |
| 343.15 | 9530.00 | 0.0002 |
| 343.15 | 14740.00 | 0.0002 |
| 343.15 | 21230.00 | 0.0003 |
| 353.15 | 200.00 | 0.0002 |
| 353.15 | 4830.00 | 0.0002 |
| 353.15 | 10320.00 | 0.0002 |
| 353.15 | 15760.00 | 0.0002 |
| 353.15 | 21100.00 | 0.0002 |
| 363.15 | 230.00 | 0.0002 |
| 363.15 | 4730.00 | 0.0002 |
| 363.15 | 10170.00 | 0.0002 |
| 363.15 | 15830.00 | 0.0002 |
| 363.15 | 20860.00 | 0.0002 |
| 373.15 | 310.00 | 0.0002 |
| 373.15 | 4730.00 | 0.0002 |
| 373.15 | 9630.00 | 0.0002 |
| 373.15 | 15600.00 | 0.0002 |
| 373.15 | 21680.00 | 0.0002 |
| Reference | ||
Mass density, kg/m3
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Mass density, kg/m3 - Liquid |
| 283.15 | 100.00 | 733.83 |
| 288.15 | 100.00 | 728.69 |
| 293.15 | 100.00 | 723.51 |
| 298.15 | 100.00 | 718.29 |
| 303.15 | 100.00 | 713.03 |
| 308.15 | 100.00 | 707.73 |
| 313.15 | 100.00 | 702.38 |
| 318.15 | 100.00 | 697.07 |
| 323.15 | 100.00 | 691.61 |
| 328.15 | 100.00 | 686.17 |
| 333.15 | 100.00 | 681.0 |
| 283.15 | 5000.00 | 739.6 |
| 288.15 | 5000.00 | 734.61 |
| 293.15 | 5000.00 | 729.62 |
| 298.15 | 5000.00 | 724.67 |
| 303.15 | 5000.00 | 719.61 |
| 308.15 | 5000.00 | 714.61 |
| 313.15 | 5000.00 | 709.64 |
| 318.15 | 5000.00 | 704.53 |
| 323.15 | 5000.00 | 699.42 |
| 328.15 | 5000.00 | 694.18 |
| 333.15 | 5000.00 | 688.97 |
| 283.15 | 10000.00 | 744.9 |
| 288.15 | 10000.00 | 740.14 |
| 293.15 | 10000.00 | 735.37 |
| 298.15 | 10000.00 | 730.59 |
| 303.15 | 10000.00 | 725.79 |
| 308.15 | 10000.00 | 720.99 |
| 313.15 | 10000.00 | 716.16 |
| 318.15 | 10000.00 | 711.3 |
| 323.15 | 10000.00 | 706.46 |
| 328.15 | 10000.00 | 701.52 |
| 333.15 | 10000.00 | 696.58 |
| 283.15 | 15000.00 | 749.85 |
| 288.15 | 15000.00 | 745.3 |
| 293.15 | 15000.00 | 740.69 |
| 298.15 | 15000.00 | 736.05 |
| 303.15 | 15000.00 | 731.48 |
| 308.15 | 15000.00 | 726.79 |
| 313.15 | 15000.00 | 722.17 |
| 318.15 | 15000.00 | 717.51 |
| 323.15 | 15000.00 | 712.89 |
| 328.15 | 15000.00 | 708.19 |
| 333.15 | 15000.00 | 703.52 |
| 283.15 | 20000.00 | 754.49 |
| 288.15 | 20000.00 | 750.09 |
| 293.15 | 20000.00 | 745.62 |
| 298.15 | 20000.00 | 741.13 |
| 303.15 | 20000.00 | 736.81 |
| 308.15 | 20000.00 | 732.2 |
| 313.15 | 20000.00 | 727.77 |
| 318.15 | 20000.00 | 723.27 |
| 323.15 | 20000.00 | 718.83 |
| 328.15 | 20000.00 | 714.34 |
| 333.15 | 20000.00 | 709.85 |
| 283.15 | 25000.00 | 758.89 |
| 288.15 | 25000.00 | 754.61 |
| 293.15 | 25000.00 | 750.29 |
| 298.15 | 25000.00 | 745.92 |
| 303.15 | 25000.00 | 741.76 |
| 308.15 | 25000.00 | 737.29 |
| 313.15 | 25000.00 | 732.97 |
| 318.15 | 25000.00 | 728.67 |
| 323.15 | 25000.00 | 724.38 |
| 328.15 | 25000.00 | 720.04 |
| 333.15 | 25000.00 | 715.73 |
| 283.15 | 30000.00 | 763.08 |
| 288.15 | 30000.00 | 758.9 |
| 293.15 | 30000.00 | 754.71 |
| 298.15 | 30000.00 | 750.46 |
| 303.15 | 30000.00 | 746.43 |
| 308.15 | 30000.00 | 742.07 |
| 313.15 | 30000.00 | 737.92 |
| 318.15 | 30000.00 | 733.74 |
| 323.15 | 30000.00 | 729.58 |
| 328.15 | 30000.00 | 725.37 |
| 333.15 | 30000.00 | 721.21 |
| 283.15 | 35000.00 | 767.08 |
| 288.15 | 35000.00 | 763.01 |
| 293.15 | 35000.00 | 758.91 |
| 298.15 | 35000.00 | 754.77 |
| 303.15 | 35000.00 | 750.85 |
| 308.15 | 35000.00 | 746.63 |
| 313.15 | 35000.00 | 742.55 |
| 318.15 | 35000.00 | 738.49 |
| 323.15 | 35000.00 | 734.45 |
| 328.15 | 35000.00 | 730.4 |
| 333.15 | 35000.00 | 726.36 |
| 283.15 | 40000.00 | 770.91 |
| 288.15 | 40000.00 | 766.92 |
| 293.15 | 40000.00 | 762.93 |
| 298.15 | 40000.00 | 758.89 |
| 303.15 | 40000.00 | 755.09 |
| 308.15 | 40000.00 | 750.94 |
| 313.15 | 40000.00 | 746.98 |
| 318.15 | 40000.00 | 743.01 |
| 323.15 | 40000.00 | 739.08 |
| 328.15 | 40000.00 | 735.15 |
| 333.15 | 40000.00 | 731.23 |
| 283.15 | 45000.00 | 774.59 |
| 288.15 | 45000.00 | 770.68 |
| 293.15 | 45000.00 | 766.78 |
| 298.15 | 45000.00 | 762.82 |
| 303.15 | 45000.00 | 759.12 |
| 308.15 | 45000.00 | 755.05 |
| 313.15 | 45000.00 | 751.2 |
| 318.15 | 45000.00 | 747.34 |
| 323.15 | 45000.00 | 743.5 |
| 328.15 | 45000.00 | 739.67 |
| 333.15 | 45000.00 | 735.85 |
| 283.15 | 50000.00 | 778.13 |
| 288.15 | 50000.00 | 774.31 |
| 293.15 | 50000.00 | 770.48 |
| 298.15 | 50000.00 | 766.6 |
| 303.15 | 50000.00 | 763.0 |
| 308.15 | 50000.00 | 759.01 |
| 313.15 | 50000.00 | 755.21 |
| 318.15 | 50000.00 | 751.47 |
| 323.15 | 50000.00 | 747.72 |
| 328.15 | 50000.00 | 743.94 |
| 333.15 | 50000.00 | 740.18 |
| 283.15 | 55000.00 | 781.56 |
| 288.15 | 55000.00 | 777.77 |
| 293.15 | 55000.00 | 774.06 |
| 298.15 | 55000.00 | 770.25 |
| 303.15 | 55000.00 | 766.7 |
| 308.15 | 55000.00 | 762.79 |
| 313.15 | 55000.00 | 759.09 |
| 318.15 | 55000.00 | 755.41 |
| 323.15 | 55000.00 | 751.72 |
| 328.15 | 55000.00 | 748.05 |
| 333.15 | 55000.00 | 744.38 |
| 283.15 | 60000.00 | 784.88 |
| 288.15 | 60000.00 | 781.16 |
| 293.15 | 60000.00 | 777.49 |
| 298.15 | 60000.00 | 773.75 |
| 303.15 | 60000.00 | 770.24 |
| 308.15 | 60000.00 | 766.45 |
| 313.15 | 60000.00 | 762.83 |
| 318.15 | 60000.00 | 759.21 |
| 323.15 | 60000.00 | 755.59 |
| 328.15 | 60000.00 | 751.94 |
| 333.15 | 60000.00 | 748.24 |
| 283.15 | 65000.00 | 788.07 |
| 288.15 | 65000.00 | 784.42 |
| 293.15 | 65000.00 | 780.83 |
| 298.15 | 65000.00 | 777.14 |
| 303.15 | 65000.00 | 773.7 |
| 308.15 | 65000.00 | 769.97 |
| 313.15 | 65000.00 | 766.39 |
| 318.15 | 65000.00 | 762.85 |
| 323.15 | 65000.00 | 759.26 |
| 328.15 | 65000.00 | 755.64 |
| 333.15 | 65000.00 | 752.02 |
| Reference | ||
| Fixed | Measured | |
|---|---|---|
| Pressure, kPa - Liquid | Temperature, K - Liquid | Mass density, kg/m3 - Liquid |
| 100.00 | 293.15 | 723.5 |
| 1000.00 | 293.15 | 724.3 |
| 5000.00 | 293.15 | 729.1 |
| 10000.00 | 293.15 | 734.5 |
| 15000.00 | 293.15 | 739.6 |
| 20000.00 | 293.15 | 744.5 |
| 25000.00 | 293.15 | 749.0 |
| 30000.00 | 293.15 | 753.3 |
| 35000.00 | 293.15 | 757.4 |
| 40000.00 | 293.15 | 761.3 |
| 45000.00 | 293.15 | 765.0 |
| 50000.00 | 293.15 | 768.6 |
| 55000.00 | 293.15 | 772.1 |
| 60000.00 | 293.15 | 775.4 |
| 65000.00 | 293.15 | 778.6 |
| 70000.00 | 293.15 | 781.7 |
| 80000.00 | 293.15 | 787.6 |
| 90000.00 | 293.15 | 793.2 |
| 100000.00 | 293.15 | 798.5 |
| 110000.00 | 293.15 | 803.6 |
| 120000.00 | 293.15 | 808.4 |
| 130000.00 | 293.15 | 812.9 |
| 140000.00 | 293.15 | 817.3 |
| 100.00 | 298.15 | 718.3 |
| 1000.00 | 298.15 | 719.5 |
| 5000.00 | 298.15 | 724.5 |
| 10000.00 | 298.15 | 730.2 |
| 15000.00 | 298.15 | 735.6 |
| 20000.00 | 298.15 | 740.5 |
| 25000.00 | 298.15 | 745.2 |
| 30000.00 | 298.15 | 749.6 |
| 35000.00 | 298.15 | 753.7 |
| 40000.00 | 298.15 | 757.7 |
| 45000.00 | 298.15 | 761.6 |
| 50000.00 | 298.15 | 765.2 |
| 55000.00 | 298.15 | 768.7 |
| 60000.00 | 298.15 | 772.1 |
| 65000.00 | 298.15 | 775.4 |
| 70000.00 | 298.15 | 778.5 |
| 80000.00 | 298.15 | 784.5 |
| 90000.00 | 298.15 | 790.3 |
| 100000.00 | 298.15 | 795.6 |
| 110000.00 | 298.15 | 800.8 |
| 120000.00 | 298.15 | 805.6 |
| 130000.00 | 298.15 | 810.3 |
| 140000.00 | 298.15 | 814.6 |
| 100.00 | 313.15 | 702.4 |
| 1000.00 | 313.15 | 703.7 |
| 5000.00 | 313.15 | 709.3 |
| 10000.00 | 313.15 | 715.7 |
| 15000.00 | 313.15 | 721.6 |
| 20000.00 | 313.15 | 727.1 |
| 25000.00 | 313.15 | 732.0 |
| 30000.00 | 313.15 | 737.1 |
| 35000.00 | 313.15 | 741.5 |
| 40000.00 | 313.15 | 745.8 |
| 45000.00 | 313.15 | 749.9 |
| 50000.00 | 313.15 | 753.8 |
| 55000.00 | 313.15 | 757.6 |
| 60000.00 | 313.15 | 761.3 |
| 65000.00 | 313.15 | 764.8 |
| 70000.00 | 313.15 | 768.1 |
| 80000.00 | 313.15 | 774.3 |
| 90000.00 | 313.15 | 780.4 |
| 100000.00 | 313.15 | 786.0 |
| 110000.00 | 313.15 | 791.4 |
| 120000.00 | 313.15 | 796.4 |
| 130000.00 | 313.15 | 801.3 |
| 140000.00 | 313.15 | 806.0 |
| 100.00 | 333.15 | 680.4 |
| 1000.00 | 333.15 | 682.0 |
| 5000.00 | 333.15 | 688.8 |
| 10000.00 | 333.15 | 696.3 |
| 15000.00 | 333.15 | 703.1 |
| 20000.00 | 333.15 | 709.3 |
| 25000.00 | 333.15 | 715.0 |
| 30000.00 | 333.15 | 720.4 |
| 35000.00 | 333.15 | 725.5 |
| 40000.00 | 333.15 | 730.2 |
| 45000.00 | 333.15 | 734.7 |
| 50000.00 | 333.15 | 739.0 |
| 55000.00 | 333.15 | 743.1 |
| 60000.00 | 333.15 | 747.0 |
| 65000.00 | 333.15 | 750.8 |
| 70000.00 | 333.15 | 754.3 |
| 80000.00 | 333.15 | 761.2 |
| 90000.00 | 333.15 | 767.7 |
| 100000.00 | 333.15 | 773.6 |
| 110000.00 | 333.15 | 779.3 |
| 120000.00 | 333.15 | 784.6 |
| 130000.00 | 333.15 | 789.8 |
| 140000.00 | 333.15 | 794.7 |
| 1000.00 | 353.19 | 659.5 |
| 5000.00 | 353.19 | 667.5 |
| 10000.00 | 353.19 | 676.4 |
| 15000.00 | 353.19 | 684.4 |
| 20000.00 | 353.19 | 691.5 |
| 25000.00 | 353.19 | 698.0 |
| 30000.00 | 353.19 | 704.0 |
| 35000.00 | 353.19 | 709.6 |
| 40000.00 | 353.19 | 714.8 |
| 45000.00 | 353.19 | 719.7 |
| 50000.00 | 353.19 | 724.5 |
| 55000.00 | 353.19 | 728.9 |
| 60000.00 | 353.19 | 733.1 |
| 65000.00 | 353.19 | 737.2 |
| 70000.00 | 353.19 | 741.1 |
| 80000.00 | 353.19 | 748.4 |
| 90000.00 | 353.19 | 755.3 |
| 100000.00 | 353.19 | 761.6 |
| 110000.00 | 353.19 | 767.7 |
| 120000.00 | 353.19 | 773.4 |
| 130000.00 | 353.19 | 778.8 |
| 140000.00 | 353.19 | 784.0 |
| 1000.00 | 373.24 | 635.5 |
| 5000.00 | 373.24 | 645.5 |
| 10000.00 | 373.24 | 656.1 |
| 15000.00 | 373.24 | 665.3 |
| 20000.00 | 373.24 | 673.4 |
| 25000.00 | 373.24 | 680.8 |
| 30000.00 | 373.24 | 687.6 |
| 35000.00 | 373.24 | 693.8 |
| 40000.00 | 373.24 | 699.6 |
| 45000.00 | 373.24 | 705.0 |
| 50000.00 | 373.24 | 710.1 |
| 55000.00 | 373.24 | 714.9 |
| 60000.00 | 373.24 | 719.5 |
| 65000.00 | 373.24 | 723.9 |
| 70000.00 | 373.24 | 728.1 |
| 80000.00 | 373.24 | 735.9 |
| 90000.00 | 373.24 | 743.2 |
| 100000.00 | 373.24 | 750.0 |
| 110000.00 | 373.24 | 756.3 |
| 120000.00 | 373.24 | 762.3 |
| 130000.00 | 373.24 | 768.0 |
| 140000.00 | 373.24 | 773.3 |
| 1000.00 | 393.29 | 609.5 |
| 5000.00 | 393.29 | 622.1 |
| 10000.00 | 393.29 | 634.9 |
| 15000.00 | 393.29 | 645.7 |
| 20000.00 | 393.29 | 655.1 |
| 25000.00 | 393.29 | 663.4 |
| 30000.00 | 393.29 | 671.0 |
| 35000.00 | 393.29 | 677.9 |
| 40000.00 | 393.29 | 684.3 |
| 45000.00 | 393.29 | 690.2 |
| 50000.00 | 393.29 | 695.7 |
| 55000.00 | 393.29 | 701.0 |
| 60000.00 | 393.29 | 705.9 |
| 65000.00 | 393.29 | 710.6 |
| 70000.00 | 393.29 | 715.1 |
| 80000.00 | 393.29 | 723.5 |
| 90000.00 | 393.29 | 731.3 |
| 100000.00 | 393.29 | 738.3 |
| 110000.00 | 393.29 | 745.2 |
| 120000.00 | 393.29 | 751.3 |
| 130000.00 | 393.29 | 757.4 |
| 140000.00 | 393.29 | 763.0 |
| Reference | ||
| Fixed | Measured | |
|---|---|---|
| Pressure, kPa - Liquid | Temperature, K - Liquid | Mass density, kg/m3 - Liquid |
| 100.00 | 293.15 | 723.5 |
| 1000.00 | 293.15 | 724.6 |
| 5000.00 | 293.15 | 729.4 |
| 10000.00 | 293.15 | 734.9 |
| 15000.00 | 293.15 | 740.0 |
| 20000.00 | 293.15 | 744.8 |
| 25000.00 | 293.15 | 749.4 |
| 30000.00 | 293.15 | 753.7 |
| 35000.00 | 293.15 | 757.7 |
| 40000.00 | 293.15 | 761.6 |
| 45000.00 | 293.15 | 765.3 |
| 50000.00 | 293.15 | 768.9 |
| 55000.00 | 293.15 | 772.4 |
| 60000.00 | 293.15 | 775.7 |
| 65000.00 | 293.15 | 778.9 |
| 70000.00 | 293.15 | 782.0 |
| 80000.00 | 293.15 | 787.9 |
| 90000.00 | 293.15 | 793.5 |
| 100000.00 | 293.15 | 798.8 |
| 110000.00 | 293.15 | 803.9 |
| 120000.00 | 293.15 | 808.7 |
| 130000.00 | 293.15 | 813.2 |
| 140000.00 | 293.15 | 817.6 |
| 100.00 | 298.15 | 718.3 |
| 1000.00 | 298.15 | 719.6 |
| 5000.00 | 298.15 | 724.5 |
| 10000.00 | 298.15 | 730.2 |
| 15000.00 | 298.15 | 735.6 |
| 20000.00 | 298.15 | 740.5 |
| 25000.00 | 298.15 | 745.2 |
| 30000.00 | 298.15 | 749.6 |
| 35000.00 | 298.15 | 753.7 |
| 40000.00 | 298.15 | 757.8 |
| 45000.00 | 298.15 | 761.6 |
| 50000.00 | 298.15 | 765.2 |
| 55000.00 | 298.15 | 768.8 |
| 60000.00 | 298.15 | 772.2 |
| 65000.00 | 298.15 | 775.4 |
| 70000.00 | 298.15 | 778.6 |
| 80000.00 | 298.15 | 784.6 |
| 90000.00 | 298.15 | 790.3 |
| 100000.00 | 298.15 | 795.7 |
| 110000.00 | 298.15 | 800.8 |
| 120000.00 | 298.15 | 805.6 |
| 130000.00 | 298.15 | 810.3 |
| 140000.00 | 298.15 | 814.6 |
| 100.00 | 313.15 | 702.4 |
| 1000.00 | 313.15 | 703.8 |
| 5000.00 | 313.15 | 709.4 |
| 10000.00 | 313.15 | 715.8 |
| 15000.00 | 313.15 | 721.7 |
| 20000.00 | 313.15 | 727.2 |
| 25000.00 | 313.15 | 732.1 |
| 30000.00 | 313.15 | 737.1 |
| 35000.00 | 313.15 | 741.6 |
| 40000.00 | 313.15 | 745.9 |
| 45000.00 | 313.15 | 750.0 |
| 50000.00 | 313.15 | 753.9 |
| 55000.00 | 313.15 | 757.7 |
| 60000.00 | 313.15 | 761.3 |
| 65000.00 | 313.15 | 764.8 |
| 70000.00 | 313.15 | 768.1 |
| 80000.00 | 313.15 | 774.4 |
| 90000.00 | 313.15 | 780.5 |
| 100000.00 | 313.15 | 786.1 |
| 110000.00 | 313.15 | 791.4 |
| 120000.00 | 313.15 | 796.5 |
| 130000.00 | 313.15 | 801.4 |
| 140000.00 | 313.15 | 806.0 |
| 100.00 | 333.15 | 680.5 |
| 1000.00 | 333.15 | 682.1 |
| 5000.00 | 333.15 | 688.9 |
| 10000.00 | 333.15 | 696.4 |
| 15000.00 | 333.15 | 703.2 |
| 20000.00 | 333.15 | 709.4 |
| 25000.00 | 333.15 | 715.1 |
| 30000.00 | 333.15 | 720.5 |
| 35000.00 | 333.15 | 725.6 |
| 40000.00 | 333.15 | 730.3 |
| 45000.00 | 333.15 | 734.8 |
| 50000.00 | 333.15 | 739.1 |
| 55000.00 | 333.15 | 743.1 |
| 60000.00 | 333.15 | 747.1 |
| 65000.00 | 333.15 | 750.9 |
| 70000.00 | 333.15 | 754.4 |
| 80000.00 | 333.15 | 761.3 |
| 90000.00 | 333.15 | 767.7 |
| 100000.00 | 333.15 | 773.7 |
| 110000.00 | 333.15 | 779.4 |
| 120000.00 | 333.15 | 784.7 |
| 130000.00 | 333.15 | 789.9 |
| 140000.00 | 333.15 | 794.8 |
| 1000.00 | 353.19 | 659.5 |
| 5000.00 | 353.19 | 667.6 |
| 10000.00 | 353.19 | 676.5 |
| 15000.00 | 353.19 | 684.4 |
| 20000.00 | 353.19 | 691.5 |
| 25000.00 | 353.19 | 698.0 |
| 30000.00 | 353.19 | 704.0 |
| 35000.00 | 353.19 | 709.7 |
| 40000.00 | 353.19 | 714.8 |
| 45000.00 | 353.19 | 719.7 |
| 50000.00 | 353.19 | 724.6 |
| 55000.00 | 353.19 | 728.9 |
| 60000.00 | 353.19 | 733.2 |
| 65000.00 | 353.19 | 737.2 |
| 70000.00 | 353.19 | 741.1 |
| 80000.00 | 353.19 | 748.4 |
| 90000.00 | 353.19 | 755.4 |
| 100000.00 | 353.19 | 761.6 |
| 110000.00 | 353.19 | 767.8 |
| 120000.00 | 353.19 | 773.4 |
| 130000.00 | 353.19 | 778.8 |
| 140000.00 | 353.19 | 784.0 |
| 1000.00 | 373.24 | 635.6 |
| 5000.00 | 373.24 | 645.5 |
| 10000.00 | 373.24 | 656.1 |
| 15000.00 | 373.24 | 665.3 |
| 20000.00 | 373.24 | 673.5 |
| 25000.00 | 373.24 | 680.8 |
| 30000.00 | 373.24 | 687.6 |
| 35000.00 | 373.24 | 693.8 |
| 40000.00 | 373.24 | 699.6 |
| 45000.00 | 373.24 | 705.0 |
| 50000.00 | 373.24 | 710.1 |
| 55000.00 | 373.24 | 714.9 |
| 60000.00 | 373.24 | 719.5 |
| 65000.00 | 373.24 | 723.9 |
| 70000.00 | 373.24 | 728.1 |
| 80000.00 | 373.24 | 735.9 |
| 90000.00 | 373.24 | 743.2 |
| 100000.00 | 373.24 | 750.0 |
| 110000.00 | 373.24 | 756.3 |
| 120000.00 | 373.24 | 762.3 |
| 130000.00 | 373.24 | 768.0 |
| 140000.00 | 373.24 | 773.3 |
| 1000.00 | 393.28 | 609.5 |
| 5000.00 | 393.28 | 622.1 |
| 10000.00 | 393.28 | 635.0 |
| 15000.00 | 393.28 | 645.8 |
| 20000.00 | 393.28 | 655.2 |
| 25000.00 | 393.28 | 663.5 |
| 30000.00 | 393.28 | 671.1 |
| 35000.00 | 393.28 | 677.9 |
| 40000.00 | 393.28 | 684.3 |
| 45000.00 | 393.28 | 690.2 |
| 50000.00 | 393.28 | 695.8 |
| 55000.00 | 393.28 | 701.1 |
| 60000.00 | 393.28 | 705.9 |
| 65000.00 | 393.28 | 710.6 |
| 70000.00 | 393.28 | 715.2 |
| 80000.00 | 393.28 | 723.5 |
| 90000.00 | 393.28 | 731.3 |
| 100000.00 | 393.28 | 738.4 |
| 110000.00 | 393.28 | 745.3 |
| 120000.00 | 393.28 | 751.4 |
| 130000.00 | 393.28 | 757.4 |
| 140000.00 | 393.28 | 763.1 |
| Reference | ||
Speed of sound, m/s
Operational condition: Frequency, MHz = 3 (Liquid)
| Fixed | Measured | |
|---|---|---|
| Pressure, kPa - Liquid | Temperature, K - Liquid | Speed of sound, m/s - Liquid |
| 100.00 | 293.15 | 1019.71 |
| 20000.00 | 293.15 | 1161.24 |
| 40000.00 | 293.15 | 1274.5 |
| 60000.00 | 293.15 | 1369.29 |
| 80000.00 | 293.15 | 1454.22 |
| 100000.00 | 293.15 | 1528.73 |
| 100.00 | 303.15 | 974.32 |
| 20000.00 | 303.15 | 1122.56 |
| 40000.00 | 303.15 | 1240.38 |
| 60000.00 | 303.15 | 1337.63 |
| 80000.00 | 303.15 | 1423.43 |
| 100000.00 | 303.15 | 1501.88 |
| 100.00 | 313.15 | 930.24 |
| 20000.00 | 313.15 | 1086.83 |
| 40000.00 | 313.15 | 1207.91 |
| 60000.00 | 313.15 | 1308.13 |
| 80000.00 | 313.15 | 1396.71 |
| 100000.00 | 313.15 | 1474.97 |
| 100.00 | 323.15 | 887.83 |
| 20000.00 | 323.15 | 1051.9 |
| 40000.00 | 323.15 | 1177.1 |
| 60000.00 | 323.15 | 1278.96 |
| 80000.00 | 323.15 | 1368.68 |
| 100000.00 | 323.15 | 1448.65 |
| 100.00 | 333.15 | 847.29 |
| 20000.00 | 333.15 | 1017.78 |
| 40000.00 | 333.15 | 1146.81 |
| 60000.00 | 333.15 | 1252.38 |
| 80000.00 | 333.15 | 1343.16 |
| 100000.00 | 333.15 | 1423.5 |
| 20000.00 | 343.15 | 984.53 |
| 40000.00 | 343.15 | 1117.79 |
| 60000.00 | 343.15 | 1226.4 |
| 80000.00 | 343.15 | 1318.72 |
| 100000.00 | 343.15 | 1400.75 |
| 20000.00 | 353.15 | 953.14 |
| 40000.00 | 353.15 | 1090.71 |
| 60000.00 | 353.15 | 1200.36 |
| 80000.00 | 353.15 | 1294.59 |
| 100000.00 | 353.15 | 1378.37 |
| Reference | ||
Thermal conductivity, W/m/K
| Fixed | Measured | |
|---|---|---|
| Temperature, K - Liquid | Pressure, kPa - Liquid | Thermal conductivity, W/m/K - Liquid |
| 235.46 | 100.00 | 0.1259 |
| 235.54 | 100.00 | 0.1258 |
| 236.06 | 100.00 | 0.1259 |
| 236.15 | 30600.00 | 0.1369 |
| 236.25 | 5000.00 | 0.1280 |
| 236.29 | 10100.00 | 0.1300 |
| 236.33 | 5000.00 | 0.1275 |
| 236.44 | 20200.00 | 0.1331 |
| 236.45 | 20300.00 | 0.1337 |
| 236.53 | 29900.00 | 0.1364 |
| 236.67 | 5000.00 | 0.1277 |
| 236.70 | 10200.00 | 0.1305 |
| 236.80 | 20300.00 | 0.1337 |
| 236.92 | 30000.00 | 0.1363 |
| 237.15 | 10200.00 | 0.1302 |
| 254.40 | 20400.00 | 0.1276 |
| 254.47 | 30400.00 | 0.1314 |
| 254.66 | 5100.00 | 0.1220 |
| 254.73 | 100.00 | 0.1201 |
| 254.74 | 10000.00 | 0.1238 |
| 254.76 | 29500.00 | 0.1312 |
| 254.86 | 10200.00 | 0.1241 |
| 254.89 | 5300.00 | 0.1223 |
| 254.90 | 20100.00 | 0.1280 |
| 255.08 | 100.00 | 0.1205 |
| 255.13 | 10100.00 | 0.1236 |
| 255.14 | 5100.00 | 0.1221 |
| 255.26 | 100.00 | 0.1199 |
| 255.58 | 30100.00 | 0.1315 |
| 255.61 | 19900.00 | 0.1285 |
| 274.60 | 30000.00 | 0.1274 |
| 274.72 | 10100.00 | 0.1177 |
| 274.86 | 29900.00 | 0.1269 |
| 274.89 | 20000.00 | 0.1220 |
| 274.95 | 5100.00 | 0.1154 |
| 275.00 | 100.00 | 0.1129 |
| 275.02 | 10000.00 | 0.1178 |
| 275.17 | 30100.00 | 0.1271 |
| 275.19 | 5000.00 | 0.1150 |
| 275.25 | 10000.00 | 0.1175 |
| 275.30 | 100.00 | 0.1135 |
| 275.51 | 20100.00 | 0.1218 |
| 275.60 | 5000.00 | 0.1152 |
| 275.91 | 100.00 | 0.1131 |
| 276.04 | 20100.00 | 0.1219 |
| 294.58 | 100.00 | 0.1073 |
| 294.64 | 30100.00 | 0.1197 |
| 294.65 | 10000.00 | 0.1118 |
| 294.95 | 5000.00 | 0.1089 |
| 294.98 | 10000.00 | 0.1115 |
| 295.03 | 100.00 | 0.1071 |
| 295.13 | 20100.00 | 0.1161 |
| 295.14 | 30100.00 | 0.1199 |
| 295.27 | 30000.00 | 0.1198 |
| 295.32 | 10100.00 | 0.1111 |
| 295.35 | 5000.00 | 0.1085 |
| 295.60 | 20100.00 | 0.1160 |
| 295.70 | 100.00 | 0.1066 |
| 295.82 | 5000.00 | 0.1087 |
| 296.18 | 20100.00 | 0.1159 |
| 314.96 | 30000.00 | 0.1145 |
| 315.03 | 5000.00 | 0.1027 |
| 315.07 | 20000.00 | 0.1105 |
| 315.13 | 100.00 | 0.0993 |
| 315.24 | 30000.00 | 0.1144 |
| 315.26 | 20000.00 | 0.1099 |
| 315.35 | 10000.00 | 0.1050 |
| 315.39 | 5000.00 | 0.1023 |
| 315.48 | 100.00 | 0.0996 |
| 315.71 | 10000.00 | 0.1054 |
| 315.73 | 5100.00 | 0.1027 |
| 315.76 | 20000.00 | 0.1104 |
| 315.88 | 100.00 | 0.0994 |
| 315.98 | 30000.00 | 0.1144 |
| 316.26 | 10000.00 | 0.1050 |
| 334.99 | 10100.00 | 0.0998 |
| 335.01 | 5400.00 | 0.0959 |
| 335.11 | 20000.00 | 0.1038 |
| 335.23 | 100.00 | 0.0935 |
| 335.29 | 29900.00 | 0.1093 |
| 335.32 | 10100.00 | 0.0995 |
| 335.46 | 100.00 | 0.0932 |
| 335.51 | 30200.00 | 0.1094 |
| 335.68 | 19700.00 | 0.1043 |
| 335.72 | 30000.00 | 0.1096 |
| 335.84 | 5000.00 | 0.0960 |
| 335.84 | 10100.00 | 0.0995 |
| 335.94 | 100.00 | 0.0931 |
| 336.31 | 20100.00 | 0.1042 |
| 336.37 | 5200.00 | 0.0959 |
| 354.72 | 29900.00 | 0.1060 |
| 354.72 | 29900.00 | 0.1051 |
| 354.85 | 19700.00 | 0.1006 |
| 354.97 | 5000.00 | 0.0913 |
| 354.97 | 19800.00 | 0.1000 |
| 355.23 | 10100.00 | 0.0944 |
| 355.29 | 300.00 | 0.0865 |
| 355.33 | 10100.00 | 0.0944 |
| 355.45 | 5000.00 | 0.0916 |
| 355.47 | 20100.00 | 0.1001 |
| 355.56 | 5000.00 | 0.0910 |
| 355.66 | 300.00 | 0.0869 |
| 355.87 | 10000.00 | 0.0940 |
| 356.04 | 300.00 | 0.0866 |
| 356.04 | 29900.00 | 0.1056 |
| 374.75 | 30000.00 | 0.1021 |
| 374.95 | 29800.00 | 0.1021 |
| 375.12 | 20000.00 | 0.0959 |
| 375.24 | 400.00 | 0.0813 |
| 375.25 | 10000.00 | 0.0893 |
| 375.40 | 5100.00 | 0.0858 |
| 375.47 | 400.00 | 0.0812 |
| 375.55 | 30300.00 | 0.1026 |
| 375.57 | 20000.00 | 0.0957 |
| 375.61 | 10000.00 | 0.0889 |
| 375.75 | 5100.00 | 0.0853 |
| 375.87 | 400.00 | 0.0816 |
| 376.05 | 20000.00 | 0.0955 |
| 376.23 | 10000.00 | 0.0890 |
| 376.26 | 5100.00 | 0.0854 |
| Reference | ||
Correlations
| Property | Value | Unit | Temperature (K) | Source |
|---|---|---|---|---|
| Pvap | [1.33; 202.64] | kPa | [253.56; 362.50] |
The Yaw...
|
| Equation | ln(Pvp) = A + B/(T + C) | |||
| Coefficient A | 1.53410e+01 | |||
| Coefficient B | -3.27391e+03 | |||
| Coefficient C | -3.60730e+01 | |||
| Temperature range, min. | 253.56 | |||
| Temperature range, max. | 362.50 | |||
|
T(K) Vapor pressure (kPa) 0 50 100 150 200 300 350 | ||||
| Pvap | 1.33 | kPa | 253.56 | Calculated Property |
| Pvap | 2.95 | kPa | 265.66 | Calculated Property |
| Pvap | 6.02 | kPa | 277.77 | Calculated Property |
| Pvap | 11.49 | kPa | 289.87 | Calculated Property |
| Pvap | 20.67 | kPa | 301.98 | Calculated Property |
| Pvap | 35.33 | kPa | 314.08 | Calculated Property |
| Pvap | 57.75 | kPa | 326.19 | Calculated Property |
| Pvap | 90.74 | kPa | 338.29 | Calculated Property |
| Pvap | 137.72 | kPa | 350.40 | Calculated Property |
| Pvap | 202.64 | kPa | 362.50 | Calculated Property |
| Pvap | [6.74e-03; 2805.34] | kPa | [187.65; 500.05] |
KDB Vap...
|
| Equation | ln(Pvp) = A + B/T + C*ln(T) + D*T^2 | |||
| Coefficient A | 4.13028e+01 | |||
| Coefficient B | -4.89952e+03 | |||
| Coefficient C | -3.87085e+00 | |||
| Coefficient D | 1.96241e-06 | |||
| Temperature range, min. | 187.65 | |||
| Temperature range, max. | 500.05 | |||
|
T(K) Vapor pressure (kPa) 0 500 1000 1500 2000 2500 3000 200 300 400 500 | ||||
| Pvap | 6.74e-03 | kPa | 187.65 | Calculated Property |
| Pvap | 0.21 | kPa | 222.36 | Calculated Property |
| Pvap | 2.44 | kPa | 257.07 | Calculated Property |
| Pvap | 14.99 | kPa | 291.78 | Calculated Property |
| Pvap | 60.31 | kPa | 326.49 | Calculated Property |
| Pvap | 180.79 | kPa | 361.21 | Calculated Property |
| Pvap | 438.33 | kPa | 395.92 | Calculated Property |
| Pvap | 908.22 | kPa | 430.63 | Calculated Property |
| Pvap | 1670.92 | kPa | 465.34 | Calculated Property |
| Pvap | 2805.34 | kPa | 500.05 | Calculated Property |
Similar Compounds
![Propane, 2,2'-[ethylidenebis(oxy)]bis-.](data:image/png;base64,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)
Find more compounds similar to Diisopropyl ether.
Mixtures
- Diisopropyl ether + Pentane, 3-methyl-
- n-Hexane + Diisopropyl ether
- Diisopropyl ether + Heptane
- Diisopropyl ether + Butane, 1-chloro-
- Diisopropyl ether + Butane, 2-chloro-
- Diisopropyl ether + Propane, 1-chloro-2-methyl-
- Diisopropyl ether + Propane, 2-chloro-2-methyl-
- Diisopropyl ether + Pentane, 2,2,4-trimethyl-
- Methyl Isobutyl Ketone + Diisopropyl ether
- Methyl Isobutyl Ketone + Diisopropyl ether + Isopropyl Alcohol
- 1-Propanol + Diisopropyl ether
- Benzene + Diisopropyl ether
- Benzene + 1-Propanol + Diisopropyl ether
- Diisopropyl ether + 1-Propanol, 2-methyl-
- Benzene + Diisopropyl ether + 1-Propanol, 2-methyl-
- Diisopropyl ether + Ethanol
- Diisopropyl ether + Ethanol + Pentane, 2,2,4-trimethyl-
- Diisopropyl ether + Formamide, N,N-dimethyl-
- Toluene + Diisopropyl ether
- Diisopropyl ether + Benzene, 1,3-dimethyl-
Find more mixtures with Diisopropyl ether.
Sources
- KDB Pure (Korean Thermophysical Properties Databank)
- KDB Vapor Pressure Data
- Crippen Method
- Kinematic Viscosities for Ether + Alkane Mixtures: Experimental Results and UNIFAC-VISCO Parameters
- Measurement of Vapor Liquid Equilibrium for the DME + Diisopropyl Ether Binary System and Correlation for the DME + CO2 + Diisopropyl Ether Ternary System
- Viscosities of Binary Mixtures Containing Isomeric Chlorobutanes and Diisopropylether: Experimental and Predicted Values
- Phase equilibria for binary systems of octane boosters with 2,2,4-trimethylpentane
- Solubility of 9-fluorenone, thianthrene and xanthene in organic solvents
- Isothermal vapour liquid equilibria in the binary and ternary systems composed of 2-propanol, diisopropyl ether and 4-methyl-2-pentanone
- Total pressure and excess Gibbs energy for the ternary mixture di-isopropyl ether + 1-propanol + benzene and its corresponding binary systems at 313.15K
- Phase equilibria properties of binary and ternary systems containing di-isopropyl ether + isobutanol + benzene at 313.15K
- Vapor liquid equilibria for binary and ternary mixtures of diisopropyl ether, ethanol, and 2,2,4-trimethylpentane at 101.3 kPa
- (Vapor + liquid) equilibrium of binary mixtures formed by N,N-dimethyl formamide with some compounds at 95.1 kPa
- Vapour liquid equilibria, enthalpy of mixing of binary mixtures containing diisopropylether DIPE and monoaromatic hydrocarbons Experimental results and modelling
- Liquid liquid equilibria of ternary mixture (propargyl alcohol + diisopropyl ether +water)
- Effect of pressure and the capability of 2-methoxyethanol as a solvent in the behaviour of a diisopropyl ether isopropyl alcohol azeotropic mixture
- Measurement and correlation of vapor liquid equilibria for the system carbon dioxide diisopropyl ether
- Isothermal vapour liquid equilibria of binary systems of 1,2-dichloroethane with ethers
- Liquid liquid equilibria for the binary system of di-isopropyl ether (DIPE) +water in between 288.15 and 323.15K and the ternary systems of DIPE +water + C1 C4 alcohols at 298.15K
- Vapor liquid equilibria and interfacial tensions for the ternary system acetone + 2,2 -oxybis[propane] + cyclohexane and its constituent binary systems
- Isothermal vapor liquid equilibrium at 333.15K and excess molar volumes at 298.15K for the ternary system di-isopropyl ether + n-propyl alcohol + toluene and its binary subsystems
- Measurement and prediction of tie-line data for mixtures of (water + 1-propanol + diisopropyl ether): LLE diagrams as a function of temperature
- Phase equilibrium for the systems diisopropyl ether, isopropyl alcohol + 2,2,4-trimethylpentane and + n-heptane at 101.3 kPa
- Liquid + liquid equilibria for the quaternary systems of (water + acetic acid + mixed solvent) at 298.2 K and atmospheric pressure
- Experimental and predicted excess molar enthalpies of binary mixtures containing 2,2'-oxybis[propane], benzene, butan-1-ol, 2-methylpropan-1-ol, 2-methyl-2-ene-1-propanol at 303.15 K
- Liquid-liquid equilibrium for binary and ternary systems containing di-isopropyl ether (DIPE) and an imidazoliumbased ionic liquid at different temperatures
- Activity coefficients at infinite dilution of organic solutes in the ionic liquid 1-ethyl-3-methylimidazolium methanesulfonate
- Isothermal vapour-liquid equilibria and excess enthalpies for the binary mixtures containing an isomeric chlorobutane and diisopropyl ether
- Vapor-liquid equilibria at 333.15 K and excess molar volumes and deviations in molar refractivity at 298.15 K for mixtures of diisopropyl ether, ethanol and ionic liquids
- Quaternary phase equilibrium of water-carboxylic acid mixture (formic-propionic acid or acetic-propionic acid)-solvent liquid systems at 298.15 K
- Solubility of caprolactam in different organic solvents
- Vapour-liquid equilibria in binary and ternary systems composed of 2,3-dimethylbutane, diisopropyl ether, and 3-methyl-2-butanone at 313.15, 323.15 and 313.15 K
- Isobaric vapor liquid equilibrium and isothermal surface tensions of 2,2 -oxybis[propane] + 2,5-Dimethylfuran
- Experimental and theoretical study of interaction between organic compounds and 1- (4-sulfobutyl)-3-methylimidazolium based ionic liquids
- Ternary liquid-liquid equilibria of bis(trifluoromethylsulfonyl)-amidebased ionic liquids + 2-propanol + di-iso-propyl ether
- Experimental isobaric vapor-liquid equilibrium at atmospheric and sub-atmospheric pressures, excess molar volumes and deviations in molar refractivity from 293.15 K to 318.15 K of diisopropyl ether with methanol and isopropyl alcohol.
- Study of interaction between organic compounds and mono or dicationic oxygenated ionic liquids using gas chromatography
- Atmospheric densities and interfacial tensions for 1- alkanol (1-butanol to 1-octanol) + water and ether (MTBE, ETBE, DIPE, TAME and THP) + water demixed mixtures.
- Isobaric ternary vapour-liquid equilibrium of methanol(1) + diisopropyl ether(2) + isopropyl alcohol(3) along with methanol + isopropyl alcohol binary data at atmospheric and sub-atmospheric pressures
- Activity coefficients at infinite dilution of organic solvents and water in 1-butyl-3-methylimidazolium dicyanamide. A literature review of hexane/hex-1-ene separation
- Experimental and modeled volumetric behavior of linear and branched ethers
- High selective water/butan-1-ol separation on investigation of limiting activity coefficients with [P8,8,8,8][[NTf2] ionic liquid
- Speed of sound, density and derivative properties of diisopropyl ether under high pressure
- Separation of binary mixtures based on limiting activity coefficients data using specific ammonium-based ionic liquid and modelling of thermodynamic functions
- High pressure and high temperature volumetric properties of (2-propanol + diisopropyl ether) system
- Thermodynamics and activity coefficients at infinite dilution for organic solutes in the ionic liquid 1-butyl-1-methylpyrrolidinium dicyanamide
- New ionic liquid [P4,4,4,4][NTf2] in bio-butanol extraction on investigation of limiting activity coefficients
- Liquid-liquid equilibrium measurement and thermodynamics modeling for the systems water + thioglycolic acid + isopropyl ether/methyl tert-butyl ether at 298.15 and 308.15 K
- The behavior of mercury in water, alcohols, monoethylene glycol and triethylene glycol II. Elemental mercury solubility in alcohols, ethers and acetone; gas plant mercury distribution; and speciation in monoethylene glycol solution
- Ammonium ionic liquids in extraction of bio-butan-1-ol from water phase using activity coefficients at infinite dilution
- Volumetric properties of (N,N-dimethylformamide + aliphatic diethers) at Temperatures ranging from (298.15 to 358.15) K
- Quaternary (liquid + liquid) equilibria for (water + 1,1-dimethylethyl methyl ether + diisopropyl ether + toluene) at the temperature 298.15 K
- Systems with ionic liquids: Measurement of VLE and c1 data and prediction of their thermodynamic behavior using original UNIFAC, mod. UNIFAC(Do) and COSMO-RS(Ol)
- Phase equilibrium properties of binary and ternary systems containing di-isopropyl ether + 1-butanol + benzene at 313.15 K
- (Liquid + liquid) equilibria of (water + propionic acid + dipropyl ether or diisopropyl ether) at T = 298.2 K
- The thermodynamics of vaporization of ethyl tert-butyl ether, isobutyl tert-butyl ether, and di-isopropyl ether
- Volumetric properties of binary and ternary mixtures of diisopropyl ether, a,a,a-trifluorotoluene, 2,2,2-trifluoroethanol, and ethanol at a temperature 298.15 K and pressure 101 kPa
- Volumetric properties of binary mixtures of ethers and acetonitrile: Experimental results and application of the Prigogine Flory Patterson theory
- Isobaric (vapour + liquid + liquid) equilibrium data for (di-n-propyl ether + n-propyl alcohol + water) and (diisopropyl ether + isopropyl alcohol + water) systems at 100 kPa
- Thermodynamics and activity coefficients at infinite dilution measurements for organic solutes and water in the ionic liquid 1-butyl-1-methylpyrrolidinium tetracyanoborate
- Interactions of volatile organic compounds with the ionic liquid 1-ethyl-3-methylimidazolium tetracyanoborate
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 4-(2-methoxyethyl)-4-methylmorpholinium bis(trifluoromethylsulfonyl)-amide
- Measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-hexyl-3-methylimidazolium tetracyanoborate
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)-1-methylpiperidinium bis(trifluoromethylsulfonyl)-amide
- Measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-ethyl-3-methylimidazolium methanesulfonate
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)-1-methylpyrrolidinium bis(trifluoromethylsulfonyl)-amide
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 4-(2-methoxyethyl)-4-methylmorpholinium trifluorotris(perfluoroethyl)phosphate
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)- 1-methylpiperidinium trifluorotris(perfluoroethyl)phosphate
- Interactions of volatile organic compounds with the ionic liquids 1-butyl-1-methylpyrrolidinium tetracyanoborate and 1-butyl-1-methylpyrrolidinium bis(oxalato)borate
- Isothermal (vapour + liquid) equilibria for binary mixtures of diisopropyl ether with (methanol, or ethanol, or 1-butanol): Experimental data, correlations, and predictions
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-methoxyethyl)- 1-methylpyrrolidinium trifluorotris(perfluoroethyl)phosphate
- Measurements of activity coefficients at infinite dilution for organic solutes and water in N-hexylisoquinolinium thiocyanate, [HiQuin][SCN] using GLC
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 1-(2-hydroxyethyl)- 3-methylimidazolium trifluorotris(perfluoroethyl)phosphate
- Infinite dilution activity coefficients of volatile organic compounds in two ionic liquids composed of the tris(pentafluoroethyl) trifluorophosphate ([FAP]) anion and a functionalized cation
- Measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-butyl-1-methylpyrrolidinium tricyanomethanide
- Thermodynamic modeling of ternary and quaternary (liquid + liquid) systems containing water, FeCl3, HCl and diisopropyl ether
- Thermodynamics and activity coefficients at infinite dilution for organic solutes and water in the ionic liquid 1-butyl-1-methylmorpholinium tricyanomethanide
- Thermodynamics and activity coefficients at infinite dilution for organic solutes, water and diols in the ionic liquid choline bis(trifluoromethylsulfonyl)imide
- (Solid + liquid) phase equilibria of tetraphenyl piperazine-1,4-diyldiphosphonate in pure solvents
- Liquid density of oxygenated additive 2,4-dimethyl-3-oxapentane at pressures up to 140 MPa and temperatures from (293.15 to 393.29) K
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid 4-(3-hydroxypropyl)-4-methylmorpholinium bis(trifluoromethylsulfonyl)-amide
- (Liquid + liquid) equilibria for (water + 1-propanol + diisopropyl ether + octane, or methylbenzene, or heptane) systems at T = 298.15 K
- Activity coefficients at infinite dilution for organic solutes and water in 1-ethyl-1-methylpyrrolidinium lactate
- Activity coefficients at infinite dilution, physicochemical and thermodynamic properties for organic solutes and water in the ionic liquid ethyl-dimethyl-(2-methoxyethyl)ammonium trifluorotris-(perfluoroethyl)phosphate
- A 1-alkylcyanopyridinium-based ionic liquid in the separation processes
- Thermodynamics and selectivity of separation based on activity coefficients at infinite dilution of various solutes in 1-allyl-3-methylimidazolium bis{(trifluoromethyl)sulfonyl}imide ionic liquid
- Separation of aliphatic from aromatic hydrocarbons and sulphur compounds from fuel based on measurements of activity coefficients at infinite dilution for organic solutes and water in the ionic liquid N,N-diethyl-N-methyl-N-(2-methoxy-ethyl)ammonium bis(trifluoromethylsulfonyl)imide
- Thermodynamics and limiting activity coefficients measurements for organic solutes and water in the ionic liquid 1-dodecyl-3-methylimidzolium bis(trifluoromethylsulfonyl) imide
- Speed of sound measurements of di-isopropyl ether (DIPE) from 293.15 K to 673.15 K and up to 10 MPa
- Liquid densities and excess volumes of biofuel mixtures: (2-butanol + di-isopropyl ether) system at pressures up to 140 MPa and temperatures from 293.15 K to 393.28 K
- Separation of binary mixtures hexane/hex-1-ene, cyclohexane/cyclohexene and ethylbenzene/styrene based on limiting activity coefficients
- High pressure liquid densities and excess volumes of the (di-isopropyl ether + 1-hexanol) system
- Separation of water/butan-1-ol based on activity coefficients at infinite dilution in 1,3-didecyl-2-methylimidazolium dicyanamide ionic liquid
- Separation of binary mixtures hexane/hex-1-ene, cyclohexane/cyclohexene and ethylbenzene/styrene based on gamma infinity data measurements
- Activity coefficients at infinite dilution and physicochemical properties for organic solutes and water in the ionic liquid trihexyl-tetradecyl-phosphonium tricyanomethanide
- Thermodynamic study of molecular interaction-selectivity in separation processes based on limiting activity coefficients
- Liquid-liquid equilibrium for ternary systems of water + 2,2,3,3-tetrafluoro-1-propanol + isopropyl ether/tert-butyl methyl ether at 298.2, 308.2 K
- The use of ionic liquids for separation of binary hydrocarbons mixtures based on gamma infinity data measurements
- Speed of sound, density and derivative properties of binary mixtures HFE-7500 + Diisopropyl ether under high pressure
- Vapour-liquid equilibrium and extractive distillation for separation of azeotrope isopropyl alcohol and diisopropyl ether
- Separation of the mixture (isopropyl alcohol + diisopropyl ether + n-propanol): Entrainer selection, interaction exploration and vapour-liquid equilibrium measurements
- Density, viscosity, and speed of sound of binary liquid mixtures of vinyl acetate with butyl vinyl ether, diisopropyl ether, anisole and dibutyl ether
- Excess volumes, densities, speeds of sound and viscosities for the binary systems of diisopropyl ether with hydrocarbons at 303.15K
- Thermodynamic and acoustic properties of binary mixtures of ethers. III. Diisopropyl ether or oxolane with o- or m-toluidines at 303.15, 313.15 and 323.15 K
- Thermodynamic and acoustic properties of binary mixtures of ethers. IV. Diisopropyl ether or oxolane with N,N-dimethylaniline or N,Ndiethylaniline at 303.15, 313.15 and 323.15 K
- Thermodynamic and acoustic properties of binary mixtures of ethers. V. Diisopropyl ether or oxolane with 2- or 3-chloroanilines at 303.15, 313.15 and 323.15 K
- Correlation and prediction of the phase behavior and thermal properties of binary and ternary systems of 2,2 -oxybis[propane] + benzene, toluene, cyclohexane or n-heptane
- Tie-Line Data for Aqueous Mixtures of Butyric Acid with Diisopropyl Ether at Various Temperatures
- Activity Coefficients at Infinite Dilution of Organic Solutes and Water in Tributylethylphosphonium Diethylphosphate Using Gas Liquid Chromatography: Thermodynamic Properties of Mixtures Containing Ionic Liquids
- Measurement and Thermodynamic Modeling of Ternary (Liquid + Liquid) Equilibrium for Extraction of N,N-Dimethylacetamide from Aqueous Solution with Different Solvents
- High Pressure Volumetric Properties of the Binary Mixtures Di-isopropyl Ether + 2,2,4-Trimethylpentane
- High-Pressure Viscosity Measurements for the Binary Mixture HFE-7500 + Diisopropyl Ether
- Liquid-Liquid Equilibria of the System Water/Phosphoric Acid/ Diisopropyl Ether at (273.15, 283.15, and 293.15) K
- Excess Enthalpies of the Ternary Mixtures: Diisopropyl Ether + 3-Methylpentane + (Octane or Decane) at 298.15 K
- Vapor-Liquid Equilibria for the Binary Systems of Dimethoxymethane with Some Fuel Oxygenates
- Oxygenated Gasoline Additives: Saturated Heat Capacities between (277 and 355) K
- Excess Molar Volumes and Surface Tensions of Xylene with Isopropyl Ether or Methyl tert-Butyl Ether at 298.15 K
- Measurement of Activity Coefficients at Infinite Dilution of Benzene, Toluene, Ethanol, Esters, Ketones, and Ethers at Various Temperatures in Water Using the Dilutor Technique
- Densities and Viscosities for Binary and Ternary Mixtures of Diisopropyl Ether, Ethanol, and Methylcyclohexane
- Ternary and Quaternary Liquid-Liquid Equilibria of Water + Methanol + Diisopropyl Ether and Water + Methanol + Diisopropyl Ether + Toluene Mixtures
- Vapor-Liquid Equilibrium of Binary and Ternary Mixtures Containing Isopropyl Ether, 2-Butanol, and Benzene at T ) 313.15 K
- Densities, Viscosities, and Refractive Indices for Binary and Ternary Mixtures of Diisopropyl Ether, Ethanol, and 2,2,4-Trimethylpentane
- Solubility of Anthracene in Binary Diisopropyl Ether + Alkane Solvent Mixtures at 298.15 K
- Liquid-Liquid Equilibria for the Ternary System Water (1) + Acetic acid (2) + Diisopropyl Ether (3) at (293.15, 303.15, and 313.15) K
- Volumetric, Acoustic, and Refractive Properties of Isomeric Chlorobutanes with Diisopropyl Ether
- Thermodynamic and Acoustic Properties of Binary Mixtures of Ethers. 2. Diisopropyl Ether with Arylamines at (303.15, 313.15, and 323.15) K and Application of ERAS Model to Aniline Mixtures with Diisopropyl Ether and Oxolane
- Activity Coefficients at Infinite Dilution of Organic Compounds in Four New Imidazolium-Based Ionic Liquids
- Measurement and Calculation of Liquid Liquid Equilibria of Ternary and Quaternary Systems Containing Water, Propan-1-ol, and 2,2,4-Trimethylpentane (TMP) with 2,2'-Oxybis(propane) (DIPE) or Dimethyl Carbonate (DMC)
- Partition Coefficients of Organic Compounds in Four New Tetraalkylammonium Bis(trifluoromethylsulfonyl)imide Ionic Liquids Using Inverse Gas Chromatography
- Interactions of Volatile Organic Compounds with the Ionic Liquid 1-Butyl-1-methylpyrrolidinium Dicyanamide
- Evaluation of the Performance of Trigeminal Tricationic Ionic Liquids for Separation Problems
- Excess Volumes of Ternary Mixtures 2,2,4-Trimethylpentane + Diisopropyl Ether or Methyl tert-Butyl Ether + Methanol, Ethanol, or 1-Propanol at 298.15 K
- Solid Liquid Phase Equilibrium and Solubility of Dibenzo[b,d]furan and 9H-Fluoren-9-one in Organic Solvents
- Activity Coefficients at Infinite Dilution for Organic Compounds Dissolved in 1-Alkyl-1-methylpyrrolidinium Bis(trifluoromethylsulfonyl)imide Ionic Liquids Having Six-, Eight-, and Ten-Carbon Alkyl Chains
- Vapor Liquid Liquid Equilibria Measurements for the Dehydration of Ethanol, Isopropanol, and n-Propanol via Azeotropic Distillation Using DIPE and Isooctane as Entrainers
- Vapor Liquid Equilibrium for Ternary and Binary Mixtures of 2-Isopropoxypropane, 2-Propanol, and N,N-Dimethylacetamide at 101.3 kPa
- Activity Coefficients at Infinite Dilution for Organic Solutes Dissolved in Three 1-Alkyl-1-methylpyrrolidinium Bis(trifluoromethylsulfonyl)imide Ionic Liquids Bearing Short Linear Alkyl Side Chains of Three to Five Carbons
- Infinite Dilution Activity Coefficients of Solutes Dissolved in Two Trihexyl(tetradecyl)phosphonium Ionic Liquids
- Deduction of Physicochemical Properties from Solubilities: 2,4-Dihydroxybenzophenone, Biotin, and Caprolactam as Examples
- Solubility of Anthracene in Binary Diisopropyl Ether + Alcohol Solvent Mixtures at 298.15 K
- Isothermal VLE and VE at 303.15 K for the Binary and Ternary Mixtures of Di-isopropyl Ether (DIPE) + 1-Propanol + 2,2,4-Trimethylpentane
- Solubilities of Adefovir Dipivoxil in Different Binary Solvents at 298.15 K
- Determination and Correlation of Excess Molar Enthalpies of the Binary Carbon Dioxide + Diisopropyl Ether (DIPE) System at Temperatures from (298.15 to 308.15) K and Pressures from (5.0 to 7.5) MPa
- Isobaric Vapor-Liquid Equilibria for Binary and Ternary Mixtures of Diisopropyl Ether, 2-Propyl Alcohol, and 3-Methyl-1-Butanol
- Viscosity and Density Measurements of Diisopropyl Ether and Dibutyl Ether at Different Temperatures and Pressures
- Activity Coefficients at Infinite Dilution of Organic Compounds in 1-Butyl-3-methylimidazolium Tetrafluoroborate Using Inverse Gas Chromatography
- Activity Coefficients at Infinite Dilution of Organic Compounds in Trihexyl(tetradecyl)phosphonium Bis(trifluoromethylsulfonyl)imide Using Inverse Gas Chromatography
- sobaric Vapor-Liquid Equilibria for Binary and Ternary Mixtures of Diisopropyl Ether, 2-Propyl Alcohol, and n-Butyl Propionate at 101.3 kPa
- Isothermal Vapor-Liquid Equilibrium at 333.15 K and Excess Molar Volumes, Refractive Indices, and Excess Molar Enthalpies at 303.15 K for the Binary and Ternary Mixtures of Di-isopropyl Ether, Ethanol, and 2,2,4-Trimethylpentane
- Isobaric Vapor-Liquid Equilibria at 101.32 kPa and Densities, Speeds of Sound, and Refractive Indices at 298.15 K for MTBE or DIPE or TAME + 1-Propanol Binary Systems
- Partition Coefficients of Organic Compounds in New Imidazolium and Tetralkylammonium Based Ionic Liquids Using Inverse Gas Chromatography
- Thermal Conductivity of Liquid Diethyl Ether, Diisopropyl Ether, and Di-n-butyl Ether from (233 to 373) K at Pressures up to 30 MPa
- Surface Tension of Diethyl Ether, Diisopropyl Ether, and Dibutyl Ether
- Solubility of Avermectin B1a in Some Pure and Mixed Solvents from (278.2 to 318.2) K
- Study of Ether-, Alcohol-, or Cyano-Functionalized Ionic Liquids Using Inverse Gas Chromatography
- Thermodynamic Properties of Binary and Ternary Mixtures Containing Di-isopropyl Ether, 2-Propanol, and Benzene at T = 313.15 K
- Joback Method
- KDB
- Aqueous Solubility Prediction Method
- Estimated Solubility Method
- McGowan Method
- NIST Webbook
- The Yaws Handbook of Vapor Pressure
Note: Cheméo is only indexing the data, follow the source links to retrieve the latest data. The source is also providing more information like the publication year, authors and more.
Take the time to validate and double check the source of the data.
Outlier This icon means
that the value is more than 2 standard deviations away from the
property mean.