Physical Properties

HomeChapter 27: Physical PropertiesRules of Thumb for Chemical Engineers, 5th Editionby Stephen HallThis Excel workbook includes Visual Basic for Application function subroutines.Macros must be enabled for them to work.

Mixture ViscosityInputComponentmole%MWViscosity at 20C, cPn-hexane0.186.180.310n-heptane0.5100.210.409n-octane0.4114.230.5401.0CalculationsComponentmol% x MWwt%ln(viscosity)wt% x ln(mu)n-hexane8.620.08-1.1711829815(0.10)n-heptane50.110.48-0.8940401229(0.43)n-octane45.690.44-0.6161861394(0.27)104.421.00(0.80)Answer:0.451cP

Problem Statement:Calculate the viscosity of a mixture of n-hexane (10 mole%), n-heptane (50 mole%), and n-octane (40 mole%), at 20 degC

Emulsion ViscosityInputsContinuous PhaseViscosity20cPDispersed PhaseViscosity30cPVolume Fraction in the emulsion0.3OutputViscosity of the emulsion36.29cP

Problem Statement:Estimate the viscosity of an emulsion

Antoine CoefficientsProcedure1. Choose a fluid from the pull-down menu in cell C102. Enter row numbers to use for the calculation in cells A13:A153. Read answers in cells F13:F15FluidEthyl Alcohol12log10(p) = A - (B/(C+t))R2 fitMax ErrorrowTemp, Deg CVP, mm HgIntermediate:0.8188149022Over the data range0.99624.85%963.5400A7.9983294251Over the selected range1.0001.90%1197.51520B1524.1822731768121263800C218.9511066178RangeTotalData (from Perry's)Temp, CMean:16209,250.9Pressure, mm HgMethyl AlcoholPropaneTolueneAcetic AcidNitrogenAmmonian-Butanen-Pentanen-Hexanen-Heptanen-OctaneEthyl AlcoholPredictedSSreg^2SStotError11.0-44-128.9-26.7-17.2-226.1-109.1-101.5-76.6-53.9-34-14-31.30.80.06177444312621965.8493513185565042.539358424.85%125.0-25.3-115.4-4.46.3-221.3-97.5-85.7-62.5-34.5-12.78.3-124.30.49108191982610488.9858490485499420.363768614.02%1310.0-16.2-108.56.417.5-219.1-91.9-77.8-50.1-25-2.119.2-2.39.20.66224023982594721.0384922985409068.24685178.14%1420.0-6-100.918.429.9-216.8-85.8-68.9-40.2-14.19.531.5819.20.70352376072562684.7458686585224795.44294784.19%1540.05-92.431.843-214-79.2-59.1-29.2-2.322.345.11939.20.69900354542499042.6622514684855876.61355212.09%1660.012.1-8740.351.7-212.3-74.3-52.8-22.25.430.653.82659.70.09322951222434552.7386847584478051.26275230.51%17100.021.2-79.651.963-209.7-68.4-44.2-12.615.841.865.734.998.61.82552224532314509.2269369983763497.15992321.35%18200.034.8-68.469.580-205.6-57-31.21.931.658.783.648.4198.32.95904119562021288.2883717181949731.06971280.86%19400.049.9-55.689.599-200.9-45.4-16.318.549.67810463.5400.00148840078338234.12345680.00%110760.064.7-42.1110.6118.1-195.8-33.6-0.536.168.798.4125.678.4745.5209.523086343764706.37225721772341213.39072141.90%1111,520.084-25.6136.5143.5-189.2-18.718.85893124.8152.797.51,520.009999.999999999659766643.01234560.00%1123,800.0112.51.4178180.3-179.14.75092.4131.7165.7196.21263,800.004752400.0000000129712189.67901230.00%1137,600.013826.9215.8214-169.825.779.5124.7166.6202.8235.8151.87,713.712930.392855008837133324.54086042362913.140409441.50%11415,200.0167.858.1262.5252-157.650.1116164.3209.4247.5281.418316,083.1779883.436246359209181553.56040246679246.58103815.81%11522,800.0186.578.7292.8276.5-148.366.1140.6191.320324,327.92334470.2382062515648600.959363227316183.406886.70%11630,400.0203.594.831929778.921832,367.43870675.86308776945402811.540706534373239.9083626.47%11738,000.0214312.589.323040,118.54487939.440547671482132633.93227952807917.7133425.57%11845,600.022498.324249172.977842461212766170.6627192261285701.685611593773186.416947.84%1Error Sum24252287.05216525477459386.127274274216450.07138R20.9955723474209.523086343240158280.205536Same calculation procedure, but choosing from different mixture concentrations instead of a list of pure compounds0.9999991276Acetic Acid Concentration25%Fit:100.0%1log10(p) = A - (B/(C+t))rowTemp, Deg CVP, mm HgIntermediate:0.768492861312016.3A8.37741464071065178B1902.809859820817100743C245.5616982116Acetic Acid in Solutionmm HgMean:227.9deg C25 wt%50 wt%75 wt%PredictedSSreg^2SStoterror12016.315.715.316.30044774.560.00%22522.121.420.822.110.000113438642349.25626196620.05%33029.628.827.829.660.003927257539298.03986409520.21%43539.438.336.639.380.000418891135539.96641335940.05%54051.750.248.151.760.004000086231024.1560269480.12%64567656267.400.16319487225758.97440973630.60%75087.28580.186.990.044046236819855.59201392320.24%855110107102111.321.739239079313591.17569492911.20%960141138130141.310.09393546947498.43615795880.22%1065178172162178.0002490.010.00%1170223216203222.590.170155263228.22264354170.18%1275277269251276.410.34859842062353.17913452440.21%1380342331310340.971.06040348512784.87941222010.30%1485419407376417.951.107146335236118.1624024030.25%1590510497458509.210.631325489479132.75061047050.16%1695618602550616.801.4360631669151244.4867378940.19%17100743725666743.000265328.0099999990.00%6.8025674914809169.8577839690.99999159321.20%

Problem Statement:Calculate Antoine Coefficients

Relative HumidityInputDry bulb temperature100deg F37.7777777778deg C559.67deg RWet bulb temperature80deg F26.6666666667deg C539.67deg RPressure760mm HgConstantsCritical Pressure166818mm HgCritical Temperature1165.67deg REquation ParametersC04.39553K00.000367C1-0.0034691K11571C20.0000030721K232C3-0.0000000009Step-by-Step Calculation in Excel, Following the ProcedurePD1-1.941551197PW1-1.872169197PD20.9622754464PW20.8947297981PD3-0.1548492946PW3-0.1388346842KD3.2614049548KW3.2792559169PD49.0744948677PW26.2065928019PM5.7488412476OutputRH41.6941.69

Calculated using the VBA function subroutineProblem Statement:Given the air pressure and wet and dry bulb temperatures, calculate the relative humidity

IAPWSInputsTemperaturedeg K400Pressurebar, abs3Note: the answer "-1" is returned if the input data are outside the allowable rangePropertyDensity, single-phasekg/m3937.5118667997Specific internal energy, single-phasekJ/kg532.6637217373Specific enthalpy, single-phasekJ/kg532.9837176868Specific entropy, single-phasekJ/kg1.6011731544Specific isobaric heat capacity, single-phasekJ/(kg-K)4.2586014731Specific isochoric heat capacity, single-phasekJ/(kg-K)3.6347397535Dynamic viscosity, single-phasePa-s0.0002186116Thermal conductivity, single-phaseW/(m-K)0.683669863Boiling point as a function of pressureK406.6753579465Vapor pressurebar, abs2.457531863Density in saturation stateBoiling water as function of temperaturekg/m3937.4840056129Boiling water as function of pressurekg/m3931.8132266805Saturated steam as function of temperaturekg/m31.3692496283Saturated steam as function of pressurekg/m31.650749356Specific internal energy in saturation stateBoiling water as function of temperaturekJ/kg532.684429068Boiling water as function of pressurekJ/kg561.1334573255Saturated steam as function of temperaturekJ/kg2536.2313130812Saturated steam as function of pressurekJ/kg2543.1560209127Specific enthalpy in saturation stateBoiling water as function of temperaturekJ/kg532.9465702724Boiling water as function of pressurekJ/kg561.4554102571Saturated steam as function of temperaturekJ/kg2715.7115051688Saturated steam as function of pressurekJ/kg2724.8916665566Specific entropy in saturation stateBoiling water as function of temperaturekJ/kg1.6012249444Boiling water as function of pressurekJ/kg1.6717646729Saturated steam as function of temperaturekJ/kg7.0581217545Saturated steam as function of pressurekJ/kg6.991565929Specific isobaric heat capacity in saturation stateBoiling water as function of temperatureKj/(kg-K)4.2587468275Boiling water as function of pressureKj/(kg-K)4.2719935666Saturated steam as function of temperatureKj/(kg-K)2.2160192813Saturated steam as function of pressureKj/(kg-K)2.2618160537Specific isochoric heat capacity in saturation stateBoiling water as function of temperatureKj/(kg-K)3.6348004367Boiling water as function of pressureKj/(kg-K)3.602913726Saturated steam as function of temperatureKj/(kg-K)1.6415527886Saturated steam as function of pressureKj/(kg-K)1.6699853122Dynamic viscosity in saturation stateBoiling water as function of temperaturePa-s0.0002185974Boiling water as function of pressurePa-s0.0002068392Saturated steam as function of temperaturePa-s0.0000131925Saturated steam as function of pressurePa-s0.000013423Thermal conductivity in saturation stateBoiling water as function of temperatureW/(m-K)0.6836367699Boiling water as function of pressureW/(m-K)0.6836558602Saturated steam as function of temperatureW/(m-K)0.028347182Saturated steam as function of pressureW/(m-K)0.0292403892

Problem Statement:Demonstrate the use of IAWPS VBA functions to estimate the properties of water and steam

Gas SolubilityInputSelect gasCO2Temperature60deg C -- applicable range -45 C to 150 CLiquid Density840kg/m3 at 15.5 degCPressure1atm, absoluteVapor pressure of liquid0atm, absolute -- required if greater than 10% of total pressureOutputGas solubility in liquid1,495ppm by weightDataGasOstwald Coeffcient at 0CMolecular WeightHe0.014.003Ne0.02120.179H20.0392.0158N20.07528.0134Air0.09528.850334CO0.128.0104O20.1531.9988Ar0.2339.948CO2144.0098Kr1.383.8Xe2131.3NH32.817.0304NotesReference: "Rules of Thumb for Chemical Engineers"Calculation is performed in a Visual Basic for Applications function call named "GasSol"

Problem Statement:Estimate the solubility of a gas in petroleum liquid

Surface TensionInputChemicalBenzeneSurface Tension29.0dynes/cmSurface Tension temperature20.0CCritical temperature288.5CDesired Temperature100.0COutputSurface tension at 100.0 C19.0The measured surface tension for benzene at 100 C is 18.2 dynes/cm

Problem Statement:Determine the surface tension of benzene at 100 deg C. Its surface tension is 29 dynes/cm at 20 deg C and its critical temperature is 288.5 deg C

Thermo PropertiesInputWaterWaterPressurekPa200800TemperatureC300510OutputCompressibility FactorZ0.99560.9930Molar Heat Capacity, MCp (ideal-gas state), kJ/kmole-C at temperature, CCritical PropertiesGasMW-25010255075100125150Pc, atmTc, CPc, psiaTc, FAcetylene26.03839.8942.0242.7843.9345.6547.2448.7249.9851.1760.635.2890.695.3Air28.96429.0529.0729.0829.1029.1429.2029.2629.3429.4339.0-140.0573.1-220.0Ammonia17.03135.6335.6435.6435.6535.6535.6635.6735.6835.69111.5132.41,638.6270.3Argon39.94820.8820.8720.8620.8620.8520.8420.8220.8120.8048.1-122.3706.9-188.2Benzene78.11466.4474.0677.0381.6889.2296.76104.32111.32118.2047.9270.6703.9519.0Butane, iso-58.12483.4890.0892.6996.82103.62110.41117.34123.93130.5242.7151.8627.5305.3Butane, n-58.12485.2891.2793.6997.45105.33110.33117.02123.33130.4037.5152.1551.1305.7Butene, 1-56.10873.3679.5881.9685.6691.5197.31103.11108.49113.8639.7146.4583.4295.6Butene, cis-2-56.10867.6073.2775.4678.9384.5190.1595.85101.32106.8041.5162.4609.9324.4Butene, trans-2-56.10877.3382.5984.6387.8292.9898.17103.39108.43113.4640.5155.4595.2311.8Carbon dioxide44.01034.7035.9636.4137.1238.2139.2640.2941.2042.1072.831.11,069.987.9Carbon monoxide28.01029.0929.1229.1129.1529.1529.1929.2629.3229.4134.5-240.3507.0-400.5Ethane30.07047.1349.8850.9052.6755.7258.8262.1165.2968.5648.232.3708.390.1Ethylene28.05438.2540.9141.9445.5646.1248.7051.2853.7556.2149.79.3730.448.7Heptane, n-100.205142.94154.54159.01165.99177.14188.29199.40210.05220.5927.0267.1396.8512.7Hexane, n-86.178123.40133.30137.14143.11152.71162.31171.88181.08190.1929.3234.3430.6453.7Hydrogen2.01628.2928.6128.6926.5028.9629.0729.1329.1629.1812.8-239.9188.1-399.9Hydrogen sulfide34.07633.3133.6733.8234.0334.3834.7335.0835.4335.7988.2100.11,296.2212.1Methane16.04334.3034.9335.2035.7236.7437.8739.2040.5341.9945.8-82.5673.1-116.5Nitrogen28.01329.0829.1129.0929.1129.1229.1429.2029.2229.2833.5-146.9492.3-232.5Oxygen31.99929.1329.2429.2729.3629.4829.6529.8730.0530.2749.8-118.6731.9-181.4Pentane, iso-72.151101.90110.37113.68118.79127.34135.58144.03152.01160.0033.4187.2490.8369.0Pentane, n-72.151105.13112.60115.57120.21130.69136.16144.45152.18161.4533.3196.4489.4385.6Propane44.09764.1868.7870.6173.5278.5683.5988.8293.8298.3841.996.7615.8206.0Propylene42.08155.8859.9061.4663.9067.8371.7975.7679.5883.4045.691.8670.1197.3Water18.01533.3833.4733.4933.5733.6833.8334.0334.2134.42217.8373.93,200.1705.1Conversion: 1 Btu/lb-F = 4.1868 kJ/kg-CSource: GPSA, 12th Edition, exceptPerry's, exceptArgon: ASHRAE Fundamentals Handbook, 1997water: IAPWSisopentane: CAMEO Chemicals, NOAA, http://cameochemicals.noaa.gov/air: CodeCogs, http://www.codecogs.com/reference/engineering/thermodynamics/critical_temperature_and_pressure.phpNatural Gas0mole fracPcTcy*Pcy*TcMethane0.95245.8-82.543.6-78.5Ethane0.02548.232.31.20.8Propane0.00241.996.70.10.2Butane, iso-0.000342.7151.80.00.0Butane, n-0.000337.5152.10.00.0Pentane, iso-0.000133.4187.20.00.0Pentane, n-0.000133.3196.40.00.0Hexane, n-0.000129.3234.30.00.0Nitrogen0.01333.5-146.90.4-1.9Carbon Dioxide0.00772.831.10.50.2Oxygen0.000249.8-118.60.0-0.0Hydrogen0.00000112.8-239.90.0(0.0)Pseudo-Critical Pressure and Temperature45.88 atm-79.10 CAir0mole fracPcTcy*Pcy*TcNitrogen0.7833.5-146.926.1-114.6Oxygen0.2149.8-118.610.5-24.9Argon0.00948.1-122.30.4-1.1Water0.001217.8373.90.20.4Pseudo-Critical Pressure and Temperature37.24 atm-140.24 C

Problem Statement:Estimate the compressibility factor for steam at 200 kPa, 300 C and 800 kPa, 510 CFunction ZSI(P, T, Pc, Tc)' calculates compressibility factor, Z, using SI units' P = gas pressure, kPa' T = gas temperature, C' Pc = gas pseudo-critical pressure, atm' Tc = gas pseudo-critical temperature, C