Liquid densities of THF and excess volumes for the mixture with water in a wide temperature and pressure range

Schedemann, Andre; Ihmels, E. Christian; Gmehling, Jürgen

doi:10.1016/j.fluid.2010.05.004

Cited by 11 publications

(12 citation statements)

References 18 publications

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“…The values of MRD(ρ) obtained in this work for the calibration are comparable with those from the literature − as determined with an Anton Paar DMA HPM vibrating-tube densimeter, but unlike us, following discontinuous procedures of measurement and without considering the critical and vapor regions. As a consequence, the goal of our work is to get quasicontinuous PρT data along subcritical, critical, and supercritical regions of pure fluids and mixtures with adequate precisions and additionally, to be able to determine the limits of vapor–liquid equilibrium.…”

Section: Methodssupporting

confidence: 83%

Accurate Values of Some Thermodynamic Properties for Carbon Dioxide, Ethane, Propane, and Some Binary Mixtures

et al. 2011

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Quasicontinuous PρT data of CO(2), ethane, propane, and the [CO(2) + ethane] mixture have been determined along subcritical, critical, and supercritical regions. These data have been used to develop the optimal experimental method and to determine the precision of the results obtained when using an Anton Paar DMA HPM vibrating-tube densimeter. A comparison with data from reference EoS and other authors confirm the quality of our experimental setup, its calibration, and testing. For pure compounds, the value of the mean relative deviation is MRD(ρ) = 0.05% for the liquid phase and for the extended critical and supercritical region. For binary mixtures the mean relative deviation is MRD(ρ) = 0.70% in the range up to 20 MPa and MRD(ρ) = 0.20% in the range up to 70 MPa. The number of experimental points measured and their just quality have enable us to determine some derivated properties with satisfactory precision; isothermal compressibilities, κ(T), have been calculated for CO(2) and ethane (MRD(κ(T)) = 1.5%), isobaric expasion coefficients, α(P), and internal pressures, π(i), for CO(2) (MRD(α(P)) = 5% and MRD(π(i)) = 7%) and ethane (MRD(α(P)) = 7.5% and MRD(π(i)) = 8%). An in-depth discussion is presented on the behavior of the properties obtained along subcritical, critical, and supercritical regions. In addition, PuT values have been determined for water and compressed ethane from 273.19 to 463.26 K up to pressures of 190.0 MPa, using a device based on a 5 MHz pulsed ultrasonic system (MRD(u) = 0.1%). With these data we have calibrated the apparatus and have verified the adequacy of the operation with normal liquids as well as with some compressed gases. From density and speed of sound data of ethane, isentropic compressibilities, κ(s), have been obtained, and from these and our values for κ(T) and α(P), isobaric heat capacities, C(p), have been calculated with MRD(C(p)) = 3%, wich is within that of the EoS.

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Section: Methodssupporting

confidence: 83%

Accurate Values of Some Thermodynamic Properties for Carbon Dioxide, Ethane, Propane, and Some Binary Mixtures

et al. 2011

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“…[23] Other materials are usually composed of ash (4-6 wt %), proteins (2-3 wt %), acetic acid (2-4 wt %), sugar acids (1-2 wt %), and extractives (2-8 wt %) that were not quantified in this study. [24] Frozen stock of Saccharomyces cerevisiae (D 5 A) was prepared from plate monocultures that were transferred and cultured in a shaker incubator at 150 rpm and 38 8C in yeast peptone dextrose (YPD) media that contained yeast extract (10 …”

Section: Methodsmentioning

confidence: 99%

“…SSF combines the enzymatic hydrolysis of biomass to sugars with sugar fermentation to ethanol in a single step to reduce the endproduct inhibition of enzymes by high soluble sugar concentrations and thereby increase ethanol yields and titers. [10,21] In this study, SSF was applied to pretreated solids in 125 mL shake flasks at 4 wt % glucan loading; each flask contained 50 mL working volume and was fitted with a bubble trap and inoculated with the D 5 A strain of S. cerevisiae yeast along with Accellerase 1500. The ethanol yields obtained if SSF was applied to solids produced by DA and CELF pretreatments under optimized conditions compared to yields from an Avicel cellulose control at loadings of 5 and 15 mg enzyme g glucan À1 are shown in Figure 7 A and B.…”

Section: Simultaneous Saccharification and Fermentation Of Pretreatedmentioning

confidence: 99%

“…[6,9] Although each approach has itsa dvantages, incrementali mplementationc osts must be compensated by significanti mprovementsi nt otal sugarr ecoverya nd thea bility to achieveh igh yields of fuelsi nd ownstreamb ioconversion processesa tl ow enzyme loadings. We presenth ereanews olvent-basedp retreatments trategyc alledc o-solvent-enhanced lignocellulosic fractionation( CELF)t hate mploys aqueousT HF solutionst oe n-hanceD Ap retreatments ignificantly.D Ap retreatmenti saresearch andc ommercialp retreatmentb enchmark [10] as evidenced by itsw idea doption forp retreatment-relatedr esearch andc hoicef or techno-economica nalysesb yt he NationalR e-newableEnergyLaboratory(NREL) [11] as arelativelylow-costand effectivepretreatmentfor corn stoverand otherfeedstocks. [12] CELF employs THF because it is au nique polar aprotic solvent that is miscible with water over aw ide range of conditions and concentrationsa nd has the added benefit that it can be produced sustainably from biomass.…”

Section: Introductionmentioning

confidence: 99%

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Co‐solvent Pretreatment Reduces Costly Enzyme Requirements for High Sugar and Ethanol Yields from Lignocellulosic Biomass

et al. 2015

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We introduce a new pretreatment called co-solvent-enhanced lignocellulosic fractionation (CELF) to reduce enzyme costs dramatically for high sugar yields from hemicellulose and cellulose, which is essential for the low-cost conversion of biomass to fuels. CELF employs THF miscible with aqueous dilute acid to obtain up to 95 % theoretical yield of glucose, xylose, and arabinose from corn stover even if coupled with enzymatic hydrolysis at only 2 mgenzyme gglucan (-1) . The unusually high saccharification with such low enzyme loadings can be attributed to a very high lignin removal, which is supported by compositional analysis, fractal kinetic modeling, and SEM imaging. Subsequently, nearly pure lignin product can be precipitated by the evaporation of volatile THF for recovery and recycling. Simultaneous saccharification and fermentation of CELF-pretreated solids with low enzyme loadings and Saccharomyces cerevisiae produced twice as much ethanol as that from dilute-acid-pretreated solids if both were optimized for corn stover.

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“…The calibration was carried out at a pressure just above ambient and at different temperatures for various mole fractions of H 2 O. The mixture density was obtained from the work of Schedemann et al 117 Considering the reproducibility in the response peak area, the standard relative uncertainty in the peak area response for H 2 O was, on average, 2.0% while the standard relative uncertainty in the calculated amount of H 2 O at each given pressure and temperature was estimated to be 0.2%.…”

Section: Introductionmentioning

confidence: 99%

Experimental and Modeling Study of the Phase Behavior of (Methane + CO₂+ Water) Mixtures

et al. 2014

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In this work we report phase equilibrium measurements on the system (methane + carbon dioxide + water) carried out with a high-pressure quasi-static-analytical apparatus. The measurements have been made under conditions of two-phase vapor-liquid equilibrium, three-phase vapor-liquid-liquid equilibrium (VLLE), and four-phase vapor-liquid-liquid-hydrate equilibrium. The compositions of three coexisting fluid phases have been obtained along eight isotherms at temperatures from (285.15 to 303.5) K and at pressures up to either the upper critical end point (UCEP) or up to the hydrate formation locus. Compositions of coexisting vapor and liquid phases have been obtained along three isotherms at temperatures from (323.15 to 423.15) K and pressures up to 20 MPa. The quadruple curve, along which hydrates coexist with the three fluid phases, was also measured along its entire length. The VLLE data obtained for this mixture have been compared with the predictions of the statistical associating fluid theory for potentials of variable range (SAFT-VR), implemented with the square-well potential and using parameters fitted to pure-component and binary-mixture data. Specifically, we used the SAFT-VR parameters reported by Mı́guez and co-workers [Mı́guez, J. M.; dos Ramos, M. C.; Piñeiro, M. M.; Blas, F. J. J. Phys. Chem. B 2011, 115, 9604]. The pressure along the quadruple curve was compared with the predictions of two different thermodynamic models. Furthermore, a detailed study of the ternary mixtures was carried out based on comparison with available ternary data of the type (CO2 + n-alkane + water) and available data for the constituent binary subsystems. In this way, we analyzed the observed effects on the solubility when the n-alkane component was changed or a third component was added.

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Liquid densities of THF and excess volumes for the mixture with water in a wide temperature and pressure range

Cited by 11 publications

References 18 publications

Accurate Values of Some Thermodynamic Properties for Carbon Dioxide, Ethane, Propane, and Some Binary Mixtures

Accurate Values of Some Thermodynamic Properties for Carbon Dioxide, Ethane, Propane, and Some Binary Mixtures

Co‐solvent Pretreatment Reduces Costly Enzyme Requirements for High Sugar and Ethanol Yields from Lignocellulosic Biomass

Experimental and Modeling Study of the Phase Behavior of (Methane + CO₂+ Water) Mixtures

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Liquid densities of THF and excess volumes for the mixture with water in a wide temperature and pressure range

Cited by 11 publications

References 18 publications

Accurate Values of Some Thermodynamic Properties for Carbon Dioxide, Ethane, Propane, and Some Binary Mixtures

Accurate Values of Some Thermodynamic Properties for Carbon Dioxide, Ethane, Propane, and Some Binary Mixtures

Co‐solvent Pretreatment Reduces Costly Enzyme Requirements for High Sugar and Ethanol Yields from Lignocellulosic Biomass

Experimental and Modeling Study of the Phase Behavior of (Methane + CO2+ Water) Mixtures

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Experimental and Modeling Study of the Phase Behavior of (Methane + CO₂+ Water) Mixtures