A Study of Molecular Diffusion in Polymer Solutions by a Microinterferometric Method

Total Page:16

File Type:pdf, Size:1020Kb

A Study of Molecular Diffusion in Polymer Solutions by a Microinterferometric Method Scholars' Mine Masters Theses Student Theses and Dissertations 1966 A study of molecular diffusion in polymer solutions by a microinterferometric method Girish T. Dalal Follow this and additional works at: https://scholarsmine.mst.edu/masters_theses Part of the Chemical Engineering Commons Department: Recommended Citation Dalal, Girish T., "A study of molecular diffusion in polymer solutions by a microinterferometric method" (1966). Masters Theses. 5757. https://scholarsmine.mst.edu/masters_theses/5757 This thesis is brought to you by Scholars' Mine, a service of the Missouri S&T Library and Learning Resources. This work is protected by U. S. Copyright Law. Unauthorized use including reproduction for redistribution requires the permission of the copyright holder. For more information, please contact [email protected]. ii ABSTRACT A microinterferometric method was used to study the effect of solute concentration on the diffusion coefficient in polymer solutions and also to d etermine the effect of polymer concentration on the dif­ fusion coefficient. The polyacrylonitrile-dimethylforruamide system was used as a means of dete rmining the accuracy of the experimental apparatus and procedure. The non-ionic, water soluble polymer, hydrox~thyl cellulose (commercially known as Na.trosol), was used to study this effect with urea and D-glucose as the solutes. The results obtained for the polyacrylonitrile-dimethylform­ amide s ystem were in close agreement with the results obtained by Secor, which meant that the experimental techniqu.e is accurate enou.gh to give r eproducible data. The differential diffusion coefficient in­ creased with the increase in solute concentration in all cases. The effect of solute concentration on the differential diffusion coefficient was found to be s imilar for various polymer concentrations and dif­ ferent solutes. The integral diffusion coefficient temained almost constant for the concentration range of the solutes used in this work. No effect of polymer concentration on the integral diffusion coefficient could be deduced from the experimental data. iii TABLE OF CONTENTS Page LIST OF FIGURES v LIST OF TABLES viii NOMENCLATURE ix I. INTRODUCTION 1 II. LITERATURE REVIEW 4 Theory Of Diffusion 4 Laws of Diffusion 5 Techniques for the Measurement of Diffusivity • 10 Steady State Diffusion. • • • •••• 1 1 Free Diffusion ..•••.•• 13 Restricted Diffusion . .••• . 17 Optical Techniques .. 17 Schlieren Methods ...•••• 17 Interferometric Methods ...•• . 19 The Optical Wedge Technique ••• 21 III. EXPERIMENTAL 25 Mate rials . ... 25 Expe rimental Apparatus ..... 2 5 Preparation Of Optical Wedge 28 Microscope ... ..... · . · · · · · · · · · 31 Concentration Measurement Apparatus . 31 Expe rimental Procedure. .. 34 Procedure For Obtaining Experimental Interference Pattern.• .. .. 34 Measurement Of Concentration .. .. .. .. 35 Computation Technique . .. 39 Evaluation Of The Integral . ... 40 Evaluation Of The Concentration Gradient 44 Data and Results . 46 IV. DISCUSSION . .. ... 48 Effect Of Solute Concentration .•. 48 Effect Of Polymer Concentration On Integral Diffusi vities • • •••.•• . ••••••..•.••• . 63 Experimental Equipment • •••••••••• • ••• 65 Prediction of Diffusi vity of a Solute in Very Dilute Solutions • • • • • • • • • • • • • • • • • • • • • • 6 7 iv Page v. CONCLUSIONS...••• . 68 VI. RECOMMENDATIONS . 70 VII. APPENDICES ....... 71 Appendix A - Derivation Of Formula For Diffusion Coefficient Appendix B - Materials .....•. 77 Appendix C - Data and Results •. 78 Appendix D - Computer Programs 92 Appendix E - Integration of Concentration­ distance Curves •••.•... 107 Appendix F - Evaluation Of Concentration Gradient ............. 112 Appendix G - Measurement of Interference Pattern ••. •.• .• 11 5 VIII. BIBLIOGRAPHY .•.• . 117 IX. ACKNOWLEDGMENT • . 119 X. VITA .•............ 120 v LIST OF FIGURES Figure Page 2. 1 Schematic Diffusion Cell for Steady-state Diffusion 12 2. 2 Free Diffusion. The Initial Arrangement of Solutions in the Cell at t = 0, and Concentration Gradie nt Curves at a later time , t1 14 2.3 Restricted Diffusion. Concentration Curve for a time, t2, after the concentrations have changed appreciably at the ends of the Cell 18 2.4 The Optical Wedge 22 3. 1 Schematic Drawing of Experimental Apparatus 27 Experimental Apparatus Assembly 29 3.3 Preparation of the Optical Wedge for Diffusion Measurements 30 3.4 Microscope used for the Experiment 32 3. 5 Abbe-Spencer Refrac tomete r use d for M easure­ ment of Refractive Inde x as a Function of Con centration 33 3. 6 Light-inte rference P atterns Observed During a D iffu sion Experiment 36 3 .7 Experimental Interference Patte rn at t = 11 seconds, for System 4. 37 3.8 Experimental Interference Patte rn at t = 15 seconds , fo r System 8. 38 3.9 Refractive Inde x (Sodium D-line ) of Solutions of Polyacrylonitrile in Dimethylformamid e at 25°C 41 3. 10 Expe rimental Concentration Profile for Poly­ acrylonitrile-Dimethylformamide System at t = 90 seconds 42 vi Figure Page c 3. 11 Evaluation of .Jo(' x dC 45 3. 12 Experimental Concentration Gradient as a Function of Distance for Polyacrylonitrile­ Dimethylformarnide System at t = 90 Seconds 47 4. 1 Effect of Concentration on the Diffusion Coefficient for Solutions of Polyacrylonitrile in Dimethyl­ formamide at 77°F, with t = 90 seconds 49 4. 2 Diffu~ivity versus concentration for 0. 8% Natrosol in Water with Urea as Solute, at 77°F, with t = 12 seconds. 51 4. 3 Diffusivity versus Concentration for 0. 8% Natrosol in Water with D-Glucose as Solute, at 770F, with t = 15 seconds. 52 4.4 Diffusivity versus Concentration for 1. 0% Natrosol in Wa ter with Urea as Solute, at 77°F, with t = 15 54 4.5 Diffusivity versus Concentration for 1. 0% Natrosol in wate r with D-Glucose as Solute, at 77°F, with t = 15 s e conds 55 4. 6 Diffusivity versus Concentration for 1. 88% Natrosol in Wate r with Urea as Solute, at 77°F, with t = 10 seconds 56 4.7 Diffusivity versus Concentration for 1. 88% Natrosol in Water with D-G1uc ose as Solute , at 77°F, with t = 30 seconds 57 4.8 Diffusivity versus Concentration for 2. 5% Natrosol in Water with Urea as Solute, at 77°F, with t = 11 Seconds 58 4.9 Diffusivity versus Concentration for 2. 5% Natrosol in Wa t e r with D-Glucose as Solute, at 77°F, with t = 1 7 S e conds 59 4. 10 Diffusivity versus Concentration for 3 . 51% Natrosol in Water with Urea as Solute, at 77°F, with t = 10 seconds 60 vii Figure Page 4. 11 Diffusivity versus Concentration for 3. 51% Natrosol in Water with D-Glucose as Solute, at 77°F, with t = 16 seconds. 61 4. lZ Integral Diffusivity as a Function of Polymer Concentration for Natrosol-Water Systems. 63 E. 1 Evaluation of De from a Concentration-distance Curve Using Equation (Z. ZZ). 109 E. Z Evaluation of the .Jor.~ X dC. 110 F. 1 Concentration Profile for System 3, at t = 16 Seconds. 114b G. 1 A Sketch of Experimental Interference Pattern, showing how to measure the Fringe Pattern. 116 viii LIST OF TABLES Table Page 3. 1 Polymeric Systems Used for the Study. 26 c. 1 Polymeric Systems Used for the Study. 79 c. 2 Data and Results for System 1. 80 c. 3 Data and Results for System 2. 81 C.4 Data and Results for System 3. 82 c. 5 Data and Results for System 4 . 83 c. 6 Data and Results for System 5. 84 c. 7 Data and Results for System 6. 85 c . 8 Data and Results for System 7. 86 c. 9 Data and Results for System 8. 87 c. 10 Data and Results for System 9. 88 c. 11 Data and Results for System 10. 89 c. 12 Data and Resulty for System 11. 90 c. 13 Values of Integrated Diffusivities, D, for the Systems Studied. 91 F. 1 Comparison of Concentration Gradients Obtained by Two Different Methods. 114 F. 2 Average Absolute Percentage Deviation of Observed Concentrations from Those Predicted by Gompertz Equation and Davis' Method. 114a ix NOMENCLATURE A = area under the curve of concentration versus distance, (gm./100 cc. soln. )em. a = intercept of straight line that results when (x - x 1 ) / § is plotted against x. a' = cross-sectional area, sq. em. a 1, a 2 , a 3 = constants in Gompertz equation. b = slope of straight line that results when (x - x 1 )/ § is plotted against x . C = concentration of solute, gm. Icc. C 0 = initial concentration of solute, gm. Icc. c' = concentration of solute at original interface, gm. Icc. c = concentration of solute, gm./100 cc. D = molecular diffusion coefficient of a solute, sq. em. /sec. D = integral {average) diffusion coefficient of a solute, sq. em. I sec. Dnn = diffusion coefficient of a solute in a non-Ne wtonian fluid, sq. cm. / sec. d = distance between adjacent bright fringes, em. h = h eight, em. M = molecular weight. N = diffusion flux, gm. I sq. em. sec. -' N = diffusion flux in vector notation, gm. /sq. em. sec. n = refractive index of solution. no = refractive index of solvent. X r = x/2 ~~ Boltzmann's variable, ern. I (sec. ) 112 T = absolute temperature, °K. t = time, seconds. V = volume, cu. ern. w = weight fraction of solute. X = fractional area occupied, sq. ern. x = coordinate, corresponds to distance, ern. y = coordinate, corresponds to concentr ation of solute, gm. / c c . y I = small angle of deflection, rad. z = coordinate, corresponds to depth of the medium, em. Subscripts A = solute A. A' = rese r vo1r. A ' . B = solvent B. B ' = reservo1r. B' . c = at some concentration C. Co = at initial concentration C 0 • cp = prope rties or parameters of the continuous phase portion of the non-Newtonian fluid. i = i th sol ute. t = at time t. x = direction x. y = direction y. xi z = direction z. 1, 2 = positions 1 and 2 in a system. Greek Letters and Other Symbols a = intercept, Gompertz equation. A = change in property.- 9 = wedge angle, minutes or rad. ~ = wave length, mi.J.
Recommended publications
  • Air-Sea Gas Exchange
    Air-Sea Gas Exchange OCN 623 – Chemical Oceanography 17 March 2015 Readings: Libes, Chapter 6 – pp. 158 -168 Wanninkhof et al. (2009) Advances in quantifying air-sea gas exchange and environmental forcing, Annual Reviews of Marine Science © 2015 David Ho and Frank Sansone Overview • Introduction • Theory/models of gas exchange • Mechanisms/lab studies of gas exchange • Field measurements • Parameterizations Why do we care about air-water gas exchange? . Globally, to understand cycling of biogeochemically important trace gases (e.g., CO2, DMS, CH4, N2O, CH3Br) . Regionally and locally . To understand indicators of water quality (e.g., dissolved O2) . To predict evasion rates of volatile pollutants (e.g., VOCs, PAHs, PCBs) Factors Influencing Air-water Transfer of Mass, Momentum, Heat From SOLAS Science Plan and Implementation Strategy Basic flux equation Concentration gradient Flux (mol cm-3) (mol cm-2 s-1) “driving force” Gas transfer velocity (cm s-1) “resistance” k: Gas transfer velocity, piston velocity, gas exchange coefficient Cw: Concentration in water near the surface Ca: Concentration in air near the surface α: Ostwald solubility coefficient (temp-compensated Bunsen coeff) Basic conceptual model Turbulent atmosphere C Atmosphere a Laminar Stagnant Cas Boundary Layer zFilm Cws (transport by Ocean molecular diffusion) Cw Turbulent bulk liquid F = k(Cw-αCa) Air/water side resistance Magnitude of typical Ostwald solubility coefficients He ≈ 0.01 Water-side resistance O2 ≈ 0.03 CO2 ≈ 0.7 DMS ≈ 10 Air- and water-side resistance CH3Br
    [Show full text]
  • Modes of Mass Transfer Chapter Objectives
    MODES OF MASS TRANSFER CHAPTER OBJECTIVES - After you have studied this chapter, you should be able to: 1. Explain the process of molecular diffusion and its dependence on molecular mobility. 2. Explain the process of capillary diffusion 3. Explain the process of dispersion in a fluid or in a porous solid. 4. Understand the process of convective mass transfer as due to bulk flow added to diffusion or dispersion. 5. Explain saturated flow and unsaturated capillary flow in a porous solid 6. Have an idea of the relative rates of the different modes of mass transfer. 7. Explain osmotic flow. KEY TERMS diffusion, diffusivity, and. diffusion coefficient dispersion and dispersion coefficient hydraulic conductivity capillarity osmotic flow mass and molar flux Fick's law Darcy's law 1. A Primer on Porous Media Flow Physical Interpretation of Hydraulic Conductivity K and Permeability k Figure 1. Idealization of a porous media as bundle of tubes of varying diameter and tortuosity. Capillarity and Unsaturated Flow in a Porous Media Figure 2.Capillary attraction between the tube walls and the fluid causes the fluid to rise. Osmotic Flow in a Porous Media Figure 3.Osmotic flow from a dilute to a concentrated solution through a semi-permeable membrane. 2. Molecular Diffusion • In a material with two or more mass species whose concentrations vary within the material, there is tendency for mass to move. Diffusive mass transfer is the transport of one mass component from a region of higher concentration to a region of lower concentration. Physical interpretation of diffusivity Figure 4. Concentration profiles at different times from an instantaneous source placed at zero distance.
    [Show full text]
  • Visualizing Molecular Diffusion Through Passive Permeability
    COCHBI-1072; NO. OF PAGES 9 Available online at www.sciencedirect.com Visualizing molecular diffusion through passive permeability barriers in cells: conventional and novel approaches 1 1 1,2 1,3 Yu-Chun Lin , Siew Cheng Phua , Benjamin Lin and Takanari Inoue Diffusion barriers are universal solutions for cells to achieve exist at a variety of cellular structures, including the distinct organizations, compositions, and activities within a nuclear envelope, the annulus of spermatozoa, the lead- limited space. The influence of diffusion barriers on the ing edge of migrating cells, the cleavage furrow of divid- spatiotemporal dynamics of signaling molecules often ing cells, and the budding neck of yeast, as well as in determines cellular physiology and functions. Over the years, cellular extensions such as primary cilia, dendritic spines, the passive permeability barriers in various subcellular locales and the initial segment of the neuronal axon [1 ,6 ,7]. have been characterized using elaborate analytical techniques. While some diffusion barriers exist constitutively in cells, In this review, we will summarize the current state of knowledge others are highly dynamic. The importance of diffusion on the various passive permeability barriers present in barriers is further underscored by the various human mammalian cells. We will conclude with a description of several diseases which result from their dysfunction [3,6 ,8,9]. conventional techniques and one new approach based on chemically inducible diffusion trap (CIDT) for probing Diffusion barriers can be categorized into two major permeable barriers. classes based on the substrates they affect: lateral diffu- Addresses sion barriers and permeability barriers. Lateral diffusion 1 Department of Cell Biology, Center for Cell Dynamics, School of barriers localize in membranes and restrict the movement Medicine, Johns Hopkins University, United States 2 of molecules within the membrane plane such as trans- Department of Biomedical Engineering, Johns Hopkins University, membrane proteins and membrane lipids [1 ].
    [Show full text]
  • On the Molecular Diffusion Coefficients of Dissolved , And
    Available online at www.sciencedirect.com Geochimica et Cosmochimica Acta 75 (2011) 2483–2498 www.elsevier.com/locate/gca À On the molecular diffusion coefficients of dissolved CO2; HCO3 , 2À and CO3 and their dependence on isotopic mass Richard E. Zeebe ⇑ School of Ocean and Earth Science and Technology, University of Hawaii at Manoa, 1000 Pope Road, MSB 504, Honolulu, HI 96822, USA Received 21 August 2010; accepted in revised form 7 February 2011; available online 13 February 2011 Abstract À The molecular diffusion coefficients of dissolved carbon dioxide ðCO2Þ, bicarbonate ion ðHCO3 Þ, and carbonate ion 2À ðCO3 Þ are fundamental physico-chemical constants and are of practical significance in various disciplines including geochem- istry, biology, and medicine. Yet, very little experimental data is available, for instance, on the bicarbonate and carbonate ion diffusion coefficient. Furthermore, it appears that no information was hitherto available on the mass-dependence of the dif- fusion coefficients of the ionic carbonate species in water. Here I use molecular dynamics simulations to study the diffusion of the dissolved carbonate species in water, including their dependence on temperature and isotopic mass. Based on the simu- À 2À lations, I provide equations to calculate the diffusion coefficients of dissolved CO2; HCO3 , and CO3 over the temperature range from 0° to 100 °C. The results indicate a mass-dependence of CO2 diffusion that is consistent with the observed 12 13 CO2= CO2 diffusion ratio at 25 °C. No significant isotope fractionation appears to be associated with the diffusion of À 2À the naturally occurring isotopologues of HCO3 and CO3 at 25 °C.
    [Show full text]
  • Diffusion in Porous Media – Measurement and Modeling
    Fakultät Maschinenwesen | Institut für Energietechnik | Professur für Technische Thermodynamik Institutslogo Lecture Series at Fritz-Haber-Institute Berlin „Modern Methods in Heterogeneous Catalysis“ 09.12.2011 Diffusion in porous media – measurement and modeling Cornelia Breitkopf for personal use only! Diffusion – what is that? Diffusion – what is that? From G. Gamow „One, Two, Three…Infinity“ The Viking Press, New York, 1955. Dresden, Frauenkirche 2010 Diffusion – application to societies in: Diffusion – application to societies Diffusion – first experiment Robert Brown Robert Brown, (1773-1958) “Scottish botanist best known for his description of the natural continuous motion of minute particles in solution, which came to be called Brownian movement.” http://www.britannica.com/EBchecked/topic/81618/Robert-Brown Diffusion – first experiment Robert Brown “In 1827, while examining grains of pollen of the plant Clarkia pulchella suspended in water under a microscope, Brown observed minute particles, now known to be amyloplasts (starch organelles) and spherosomes (lipid organelles), ejected from the pollen grains, executing a continuous jittery motion. He then observed the same motion in particles of inorganic matter, enabling him to rule out the hypothesis that the effect was life- related…..” http://en.wikipedia.org/wiki/Robert_Brown_(botanist) Diffusion – short history http://www.uni-leipzig.de/diffusion/pdf/volume4/diff_fund_4(2006)6.pdf Diffusion – short history A. E. Fick “Adolf Eugen Fick (1829-1901) was a German physiologist. He started to study mathematics and physics, but then realized he was more interested in medicine. He earned his doctorate in medicine at Marburg in 1851.” “In 1855 he introduced Fick's law of diffusion, which governs the diffusion of a gas across a fluid membrane.” http://en.wikipedia.org/wiki/Adolf_Fick Diffusion – short history Albert Einstein (1879-1955) Marian von Smoluchowski (1872-1917 was a phyiscist.
    [Show full text]
  • Augmenting CO2 Absorption Flux Through a Gas–Liquid Membrane Module by Inserting Carbon-Fiber Spacers
    membranes Article Augmenting CO2 Absorption Flux through a Gas–Liquid Membrane Module by Inserting Carbon-Fiber Spacers Luke Chen 1 , Chii-Dong Ho 2,*, Li-Yang Jen 2, Jun-Wei Lim 3,* and Yu-Han Chen 2 1 Department of Water Resources and Environmental Engineering, Tamkang University, Tamsui, New Taipei 251, Taiwan; [email protected] 2 Department of Chemical and Materials Engineering, Tamkang University, Tamsui, New Taipei 251, Taiwan; [email protected] (L.-Y.J.); [email protected] (Y.-H.C.) 3 Department of Fundamental and Applied Sciences, HICoE-Centre for Biofuel and Biochemical Research, Institute of Self-Sustainable Building, Universiti Teknologi PETRONAS, Seri Iskandar, Perak Darul Ridzuan 32610, Malaysia * Correspondence: [email protected] (C.-D.H.); [email protected] (J.-W.L.); Tel.: +886-2-26215656 (ext. 2724) (C.-D.H.) Received: 18 September 2020; Accepted: 19 October 2020; Published: 22 October 2020 Abstract: We investigated the insertion of eddy promoters into a parallel-plate gas–liquid polytetrafluoroethylene (PTFE) membrane contactor to effectively enhance carbon dioxide absorption through aqueous amine solutions (monoethanolamide—MEA). In this study, a theoretical model was established and experimental work was performed to predict and to compare carbon dioxide absorption efficiency under concurrent- and countercurrent-flow operations for various MEA feed flow rates, inlet CO2 concentrations, and channel design conditions. A Sherwood number’s correlated expression was formulated, incorporating experimental data to estimate the mass transfer coefficient of the CO2 absorption in MEA flowing through a PTFE membrane. Theoretical predictions were calculated and validated through experimental data for the augmented CO2 absorption efficiency by inserting carbon-fiber spacers as an eddy promoter to reduce the concentration polarization effect.
    [Show full text]
  • Effect of Molecular Structure on Diffusion of Alcohols Through Type-A Zeolite Pores (0.5 Nm)
    Journal of Materials Science and Engineering A 11 (4-6) (2021) 48-55 doi: 10.17265/2161-6213/2021.4-6.003 D DAVID PUBLISHING Effect of Molecular Structure on Diffusion of Alcohols through Type-A Zeolite Pores (0.5 nm) Bryan Fernández-Solano and Julio F. Mata-Segreda Biomass Laboratory, School of Chemistry, University of Costa Rica 11501-2060, Costa Rica Abstract: Drying kinetics for alcohol-soaked type-A zeolite (pore size 0.5 nm) was determined at 50 °C for 12 small-molecule alcohols (from C1 to C10). The second-phase of drying of wet porous materials reports on the mass-transfer characteristics within the solid matrices. This stage follows pseudo first-order kinetics (k1), and the second-order rate constant k2 = k1/(fluxional area) was found to correlate with the surface tension of the liquids imbibing the solid matrix (p < 0.002). k2 values decrease along the homologous linear alcohols, and branched-chain alcohols diffuse faster than their linear analogues due to their lower surface tensions. No independent contribution was found from the molecular size of the alcohols in the experiment reported here. Characteristic velocity and enthalpy of vaporisation of the liquids were not found to be significant independent variables, either. The find agrees with the notion that liquid movement in pores is governed during the drying processes by the liquid chemical potential gradient between the pore space and gas phase above the porous particle surfaces, this gradient being a function of the molecular cohesion of -1 -2 the moving liquid front (surface tension, ). The results can be expressed by the linear Gibbs-energy relation log (k2/s ·m ) = (2.5 ± 0.5) - (1.6 ± 0.2) 102 (/J·m-2).
    [Show full text]
  • Determination of Diffusion Coefficient in Droplet Evaporation Experiment
    Determination of Diffusion Coefficient in Droplet Evaporation Experiment Using Response Surface Method Xue Chen, Xun Wang, Paul G. Chen, Qiusheng Liu To cite this version: Xue Chen, Xun Wang, Paul G. Chen, Qiusheng Liu. Determination of Diffusion Coefficient in Droplet Evaporation Experiment Using Response Surface Method. Microgravity Science and Technology, Springer, 2018, 30, pp.675-682. 10.1007/s12217-018-9645-2. hal-02112826 HAL Id: hal-02112826 https://hal.archives-ouvertes.fr/hal-02112826 Submitted on 29 Apr 2019 HAL is a multi-disciplinary open access L’archive ouverte pluridisciplinaire HAL, est archive for the deposit and dissemination of sci- destinée au dépôt et à la diffusion de documents entific research documents, whether they are pub- scientifiques de niveau recherche, publiés ou non, lished or not. The documents may come from émanant des établissements d’enseignement et de teaching and research institutions in France or recherche français ou étrangers, des laboratoires abroad, or from public or private research centers. publics ou privés. Determination of Diffusion Coefficient in Droplet Evaporation Experiment Using Response Surface Method Xue Chen1 · Xun Wang2 · Paul G. Chen3 · Qiusheng Liu4,5 Abstract Evaporation of a liquid droplet resting on a heated substrate is a complex free-surface advection-diffusion problem, in which the main driving force of the evaporation is the vapor concentration gradient across the droplet surface. Given the uncertainty associated with the diffusion coefficient of the vapor in the atmosphere during space evaporation experiments due to the environmental conditions, a simple and accurate determination of its value is of paramount importance for a better understanding of the evaporation process.
    [Show full text]
  • Membrane Gas Separation
    Membrane Gas Separation Membrane Gas Separation YURI YAMPOLSKII A.V. Topchiev Institute of Petrochemical Synthesis, Moscow, Russia BENNY FREEMAN University of Texas at Austin, Austin, TX, USA A John Wiley & Sons, Ltd., Publication This edition fi rst published 2010 © (2010) John Wiley & Sons Ltd Registered offi ce John Wiley & Sons Ltd, The Atrium, Southern Gate, Chichester, West Sussex, PO19 8SQ, United Kingdom For details of our global editorial offi ces, for customer services and for information about how to apply for permission to reuse the copyright material in this book please see our website at www.wiley.com. The right of the author to be identifi ed as the author of this work has been asserted in accordance with the Copyright, Designs and Patents Act 1988. All rights reserved. No part of this publication may be reproduced, stored in a retrieval system, or transmitted, in any form or by any means, electronic, mechanical, photocopying, recording or otherwise, except as permitted by the UK Copyright, Designs and Patents Act 1988, without the prior permission of the publisher. Wiley also publishes its books in a variety of electronic formats. Some content that appears in print may not be available in electronic books. Designations used by companies to distinguish their products are often claimed as trademarks. All brand names and product names used in this book are trade names, service marks, trademarks or registered trademarks of their respective owners. The publisher is not associated with any product or vendor mentioned in this book. This publication is designed to provide accurate and authoritative information in regard to the subject matter covered.
    [Show full text]
  • Models for Air–Water Gas Transfer
    Tellus (1984), 36B, 92-100 Models for air-water gas transfer: an experimental investigation By KIM HOLMEN, Department of Meteorology,' University of Stockholm, Arrhenius Laboratory, S-106 91 Stockholm, Sweden and PETER LISS, School of Environmental Sciences, University of East Anglia, Norwich, NR4 7TJ, England (Manuscript received August 16; in final form November 14, 1983) ABSTRACT The air-water transfer velocities for H,, He and Xe have been measured simultaneously in laboratory-tank experiments. Using average values from the existing literature data for the molecular diffusivities of the gases, the transfer velocities are found to vary with the diffusivity raised to the power 0.57. This exponent is in reasonable agreement with the findings from other laboratories, as well as field studies, provided average diffusivities are used consistently. Although interpretation is limited by uncertainties in presently available diffusion coefficients, the results may be interpreted as supportive of both the surface-renewal and boundary-layer models of air-water gas exchange, but they provide little evidence for the appropriateness of the film model. 1. Introduction In it, the main body of the fluid (liquid or gaseous) is assumed to be well mixed, the rate of interfacial The air-water transfer of gases which are transfer being determined by molecular diffusion of sparingly soluble in water and do not react rapidly the gas molecules across a stagnant layer (or film) in the aqueous phase is controlled by processes in of fluid (thickness z) adjacent to the surface. In this the near-surface water (Liss, 1973). Gases for model, the rate of gas exchange, expressed in terms which this applies include 0,, CO,, the inert gases, of a transfer velocity k, (defined as the flux of gas CO, CH,, CHJ, (CH,),S, freons and other low 'x' per unit of concentration gradient driving its molecular weight halocarbons.
    [Show full text]
  • Investigating Fuel-Cell Transport Limitations Using Hydrogen Limiting Current
    Lawrence Berkeley National Laboratory Recent Work Title Investigating fuel-cell transport limitations using hydrogen limiting current Permalink https://escholarship.org/uc/item/1f9147nv Journal International Journal of Hydrogen Energy, 42(19) ISSN 0360-3199 Authors Spingler, FB Phillips, A Schuler, T et al. Publication Date 2017-05-11 DOI 10.1016/j.ijhydene.2017.01.036 License https://creativecommons.org/licenses/by-nc-nd/4.0/ 4.0 Peer reviewed eScholarship.org Powered by the California Digital Library University of California Investigating Fuel-Cell Transport Limitations using Hydrogen Limiting Current Franz B. Spingler, Adam Phillips, Tobias Schuler, Michael C. Tucker, Adam Z. Weber Energy Conversion Group, Energy Technologies Area, Lawrence Berkeley National Laboratory, 1 Cyclotron Road, Berkeley CA 94720, USA Reducing mass-transport losses in polymer-electrolyte fuel cells (PEFCs) is essential to increase their power density and reduce overall stack cost. At the same time, cost also motivates the reduction in expensive precious-metal catalysts, which results in higher local transport losses in the catalyst layers. In this paper, we use a hydrogen-pump limiting- current setup to explore the gas-phase transport losses through PEFC catalyst layers and various gas-diffusion and microporous layers. It is shown that the effective diffusivity in the gas-diffusion layers is a strong function of liquid saturation. In addition, it is shown how the catalyst layer unexpectedly contributes significantly to the overall measured transport resistance. This is especially true at low catalyst loadings. It is also shown how the various losses can be separated into different mechanisms including diffusional processes and mass- dependent and independent ones, where the data suggests that a large part of the transport resistance in CLs cannot be attributed to a gas-phase diffusional process.
    [Show full text]
  • 1 3. Molecular Mass Transport 3.1 Introduction to Mass Transfer 3.2
    3. Molecular mass transport 3.1 Introduction to mass transfer 3.2 Properties of mixtures 3.2.1 Concentration of species 3.2.2 Mass Averaged velocity 3.3 Diffusion flux 3.3.1 Pick’s Law 3.3.2 Relation among molar fluxes 3.4 Diffusivity 3.4.1 Diffusivity in gases 3.4.2 Diffusivity in liquids 3.4.3 Diffusivity in solids 3.5 Steady state diffusion 3.5.1 Diffusion through a stagnant gas film 3.5.2 Pseudo – steady – state diffusion through a stagnant gas film. 3.5.3 Equimolar counter diffusion. 3.5.4 Diffusion into an infinite stagnant medium. 3.5.5 Diffusion in liquids 3.5.6 Mass diffusion with homogeneous chemical reaction. 3.5.7 Diffusion in solids 3.6 Transient Diffusion. 3.1 Introduction of Mass Transfer When a system contains two or more components whose concentrations vary from point to point, there is a natural tendency for mass to be transferred, minimizing the concentration differences within a system. The transport of one constituent from a region of higher concentration to that of a lower concentration is called mass transfer. The transfer of mass within a fluid mixture or across a phase boundary is a process that plays a major role in many industrial processes. Examples of such processes are: (i) Dispersion of gases from stacks (ii) Removal of pollutants from plant discharge streams by absorption (iii) Stripping of gases from waste water (iv) Neutron diffusion within nuclear reactors (v) Air conditioning Many of air day-by-day experiences also involve mass transfer, for example: 1 (i) A lump of sugar added to a cup of coffee eventually dissolves and then eventually diffuses to make the concentration uniform.
    [Show full text]