ANNUAL REVIEW
ALBERT GOMEZPLATA THOMAS M. REGAN
Mass Transfer Advances in mass transfer fundamentals published during 1967 and 1968. A section on membrane transport appears for the first time
based on an exponential dependence on concentration. He points out that very serious errors are made when concentration dependence is neglected. I n his continuing study of thermal diffusion, Emery presents the results of a parallel-plate thermal diffusion column packed with glass wool and operated in continuous flow (76A).
he format of this review is the same as that used in
Tthe last annual review by Bischoff and Himmelblau
[IND.ENG.CHEM.,60 (l), 66-74 (1968)l. A few modifications have been made. Of these, we note in particular that interest tables have been expanded to include transfer between swarms of particles and a continuous phase (Table D-4), as well as membrane transport in Table I. Molecular Diffusion
Arnold and Toor (2A) extended previous work to include experimental studies in a bounded system and numerical studies of the nonlinear diffusion equations in both bounded and unbounded systems. Two-dimensional models for transport in the lower layers of the atmosphere were presented by Poppendick (36A). He illustrates the usefulness of the models by applications to air pollution and climatology. A note by Shrier (42A) reinforces the continued use of the Wilke-Chang correlation for dissolved gases in liquids. A solution to the generalized Stefan problem was presented by Grinberg (27A) for the freezing of a liquid and related problems such as those of heat conduction and diffusion. I n polymer systems, Goldstein and Laurence (79A) considered activity corrections, and Li and Gainer (30A) developed an expression to predict diffusion coefficients from heat of mixing and viscosity data. Scattergood and Lightfoot (47A) showed the importance of the commonly neglected isotopic interaction in an ion exchange system through an experimental and theoretical study utilizing a phenomenological approach cast in the form of the Stefan-Maxwell equation. Cullinan (77A) continued his work in predicting diffusion coefficients based on the absolute rate theory. He offered a relationship for the diffusion coefficient of a dilute species in a mixture of two solvents based on the linear additivity of the frictional activation energy (70A). The intrinsic mobilities and interdependent fluxes in multicomponent isothermal diffusion in simple and complex Darken systems is clearly discussed by Carman ( 5 4 6A). Hansen (23A) presents simple correction factors for rapid calculation of the true diffusion coefficients obtained by the absorption and desorption methods
Turbulent Diffusion and Dispersion
Several studies have utilized liquid jet experiments to obtain transport coefficients of dissolved gases in a liquid. Duda and Vrentas (6B), through a rigorous analysis of jet hydrodynamics, developed a technique to analyze jet absorption data and concluded that the technique is rapid and accurate. Davies and Ting (4B) report on an experimental study that supports the Levich theory of eddy behavior of an interface for COZ and Hz absorption into a turbulent water jet. They observed that the mean concentration of gas absorption increases with flow rate for a turbulent jet, in contrast to the decrease commonly observed for laminar jets. Capps and Rehm (3B) offer an empirical correlation for determining the velocity distribution and momentum eddy diffusivity profiles in pipes, based on the surface roughness as the key parameter. Predictions compare with available data to within *I% over the entire flow region. Hughmark (77B), in a comment on previous work of San and Hanratty, examines the effect of high Schmidt numbers on the limiting value of eddy diffusivity close to a wall. Gill (32B) continued his studies of laminar dispersion in capillaries by reporting experimental findings on combined natural and forced convection in vertical tubes. He also commented and developed a solution (77B) for the problem of transient mass dispersion in fully developed laminar flow. I n a continuation of his work on the performance of packed beds, Shulman (38B) reports on liquid flow patterns and velocities in packed beds. Two experimental studies utilizing pulse techniques measured axial dispersion (7B) and radial dispersion (27B) in packed beds. Aunicky (7B) considers longitudinal mixing of liquids in bends and presents a design equation to evaluate the percentage increase in the dispersion coefficient because of a bend. Estrin and Schmidt (8B) give a theoretical study of the Higbie penetration model applied to unsteady gas absorption with irreversible first-order reactions. The effect of mixing on reactor performance is considered by VOL. 6 0
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TABLE A-I.
GASEOUS DIFFUSION
TABLE B-I.
BASIC TURBULENT DIFFUSION AND DISPERSION
Theoretical, T , or experimental, E Ref.
Syrtern or topic
Theoretical,
T,01
Unsteady diffusion of methane-argon-hydrogen in Loschmidt apparatus Transient diffusion in composite slab Transition between Knudsen and molecular diffusion in ternary mixture Calculation of diffusion coefficients Ethylene gas in HzO at Z O O , 25', 30OC by absorbing in laminar H20 jet Temperature dependence of gas pair diffusivity Transport models for lower layers of atmosphere Predicting gas diffusivities in liquids Diffusion through a stagnant gas Mass transfer coefficients in gas boundary layer Nondiffusing species in turbulent gas phase
2A 7A
T, E T
T T
14A 22A
E E
24A 25A 36A 42A 43A 45A 46A
T T T
T T
Cellular model based on large scale eddies Generalized penetration theory with effect of velocity components Concentration and temperature distribution in entrance region Axial diffusion with pulsed flow Transfer to falling liquid films Transfer into turbulent and laminar jets Velocity distribution in smooth and rough pipes Eddy diffusivity close to a wall Transient dispersion in laminar flow Narurai and forced convection in vertical capillaries
TABLE B-2. TABLE A-2.
(Primarily Experimental Data and Method) Ref.
Subject
25-65OC 2-6OoC
3A 4A
25OC
37A
Gas dispersion in packed beds Transfer in fluidized packed beds Quasi-homogeneous model for packed beds Liquid flow patterns and velocities in packed beds Transfer from packing surface at low Reynolds numbers Gravity effect on correlations of mass transfer in packed columns Note on the applicability of dispersion results to packed beds
Technique
Temp.
Concd. aqueous K O H Aromatic and cycloparaffin hydrocarbons in H20 Hexamethylenetetramine aqueous solutions Self-diffusion of Na + in ethylene glycol-HS0 and glycerol-
Diaphragm cell Capillary cell
Osmotic coefficientsof polystyrenesulfonates Octamethylcyclotetrasiloxanebenzene Octamethylcyclotetrasiloxanecarbon tetrachloride Ni-ammonium sulfate-HS0
Differential osmometry
32A
Gouy interferometer
33A
Zeiss interferometer 25OC Radioactive tracer
34A
Gouy interferometer
Ha0
TABLE B-3.
Self-diffusion of liquid COSand propane
Reduced T of 0.8, 0 . 9 0.97 25oc
Osmotic coefficients for HClOaLiClOa-HnO HCIOa-NaC104-H20, LiCIOc NaCIOp-Hz0
TABLE A-3.
40A
ToPic
Ref, 1A 5A, 6 A QA-l3A, 3 7 A 19.4
21A 23A 26A 28A 30A 35A 3QA 41A 44A
T
54
168
128 28 4 8 , 68 3B 178 1 18 328
Theoretical, T , or experimental, E E E T E E
Ref. 7B 238, 288,338 228 388 318 1QB 27B
DISPERSION I N EQUIPMENT Theoretical T , or expertmental, E Ref.
Subject Longitudinal dispersion in pipelines Dispersion in fluid-bed reactors Longitudinal dispersion in sieve trays Effect of pressure on longitudinal dispersion in gas-bubble columns Design of apparatus with axial mixing Longitudinal mixing in bends
E E E E
.. E
3QB 30B 298 18B 58 IB
TABLE B-4.
CHEMICAL REACTOR APPLICATIONS
Subject Note on the axial dispersion model Exact and approximate solution of the dispersion equation Penetration theory applied to unsteady gas absorption Influence of packing on backmixing Influence of mixing on reactor performance Recycle reactor to simulate incomplete mixing On the definition of"backmixing" and reply Simulation of reactor with incomplete mixing
Theoretical, T , or erperimental, E
... T T T, E T
... ... T
Ref. 36B 248-268 88
378 150 348 148, 24B 138
THERMAL DIFFUSION Theoretical, 07
System or topic
experimental, E
Ref.
Twin bulb method for He-Ne-COz Continuous flow in packed thermal diffusion column Variation of nonisothermal diffusion coefficients
E,T E E
15A 16A 17A
TABLE A-5.
IOB 35B
LIQUID DIFFUSION
Equation for multicomponent systems with chemically similar pairs Interdependent fluxes in multicomponent systems Prediction of diffusion coefficients Activity correction in polymer systems Solution of the Stefan problem Concentration-dependent diffusion coefficients Osmotic coefficients of tungstosilicic acid Analytical solution with nonlinear boundary conditions Diffusion in polymer solutions Liquid metal diffusion coefficient Convective diffusion in the small penetration approximation Isotope interaction shown in ion exchange membrane An examination of the Nernst-Plank model
TABLE A-4.
38A
Ref.
DISPERSION IN POROUS MEDIA
LIQUID DIFFUSION
System
experimental, E
Subject
Horn and Parish (75B) for the case of general kinetics by means of the adjoint variables of optimization theory. Their thorough study includes an examination of the plug flow, series, and Taylor models. Mecklenburgh and Hartland (24B-26B) present a numerical comparison of exact and approximate methods for the solution of the dispersion equation with chemical reaction terms.
EXPERIMENTAL TECHNIQUES Method
Ref.
Pressure change in gaseous diffusion Vertical column open to different compartments at ends Ag+ and Ag(SOa)9- by rotating disk method A filter paper diaphragm technique
18A 20A 27A 29A
INDUSTRIAL A N D E N G I N E E R I N G CHEMISTRY
General Mixing Processes in Flow Systems
As an extension of his former work with particulate systems, Gal-Or (9C) presented a theory for the case of coupled heat and multicomponent mass transfer in dispersions and suspensions. Proposed normalized size
distributions are compared with experimental results of bubble size distributions in gas-liquid dispersion. The Residence Time Distributions (RTD) of different models proposed to simulate mixing effects in reactors have been investigated. The R T D matching approach to account for mixing effects has been applied to recycle reactors (39C), stirred tanks (45C)’ staged stirred tanks (38C), internal reflux systems (43C), and gas-solid moving beds (44C). The moments of the R T D have been evaluated for the cases of series stirred tanks with backmixing (23C) and for fixed bed multistaged processes with linear kinetics (36C). Howarth (76C) used a new technique for measuring coalescence frequency in an agitated tank based on the transients in mean drop size resulting from a stepwise reduction in agitation intensity. Other experimental studies in stirred tanks have considered the level of mixing (7C), mixing time (72C, 74C, 77C, 28C), and droplet size. Miller (37C) reports an experimental investigation of particle mass transfer in baffled agitated tanks. His results include a general correlation based on the Frossling equation. This study is recommended for designers since it suggests scale-up criteria. A good review of single phase gas and liquid mixtures, including dispersion in packed and fluidized beds and some hybrid type of contactors, is presented by Gunn (77C). Pyle and Harrison (37C) show through experimentation and clever deduction that the two-phase theory of fluidization is not rigorous. Fluidized bed models based on their analysis might give better correlations. A sophisticated model for fluidized bed reactors is presented by Mireau and Bischoff (32C). A pulse technique for studying mixing in a fluidized bed has been employed by Sandblom (47C) and Yoshida and Kunii (50C). Other mixing studies are listed in Table C-4. For an excellent review of mixing, refer to Oldshue’s Annual Reviews (34C).
TABLE C-1.
Theoretical, T , or Expertmental, E
Subject Residence time distribution (RTD) Recycle reactor Stirred tank Staged stirred tanks Systems with internal reflux Gas-solid moving bed Moments of residence time distributions Sta ed tanks with backmixing Muftistage process Distribution functions to describe eddy renewal model Effect of R T D on performance of fluidized bed Coupled heat and mass transfer with residence time and size distribution in dispersions
T
Ref.
T+E
39C $2g
T T
43C 44C
T T T E
23C 36C 26C 24C
T, E
QC
M I X I N G I N STIRRED TANKS
TABLE C-2.
Theoretical, T , or Experimental E
Subject Level of mixing in continuous flow vessel Mixing by recirculation Power input and mixing time Coalescence frequency Power requirements and drop size with screen blade turbine Scale-up parameters for fixed solute surfaces Gas agitation of liquid
Ref.
T, E E E E
7c 12c 14c 76C
E E E
21C, 22C 37C 28C
M I X I N G I N FLUIDIZED BEDS
TABLE C-3.
Theoreticsl Expirirnenlal, T , or Subject Solids mixing by single bubble Response of gas to a stimulus Pulse technique using particle temperature as a tracer Investigation of two-phase theory of fluidization Mixing and contacting models Backmixing and chemical reaction Longitudinal solid mixing in a screen-packed bed Mixing of solids in adjacent beds Equations of motion Flow patterns in spouted beds Mixing in three-phase bed Review of mixing in packed and fluidized beds
TABLE C-4.
interphase Mass Transfer
Theoretical studies of interphase liquid mass transfer have included the surface stretch model applied to uniform wave motion (380)’falling films at low Reynolds number (720)’ and the effect of surfactants on the transfer rate in laminar films (70). The experimental studies summarized in Table D-1 deal mostly with surface characteristics of films as they influence the mass transfer rate. The Graetz problem for turbulent flow between parallel plates with nth order reactions on one wall has been solved by Solbrig and Gidaspow (790) to estimate the effect of diffusion on the rate of reaction. Their solution applies to turbulent flow with a well-defined isothermal catalytic surfaces. Smith and Winnick
AGE DISTRIBUTION FUNCTIONS
E
Ref.
E E
49c 50C 41c
E T, E
37C 32C 27C 20c 3c
T T E E
1c
T E E
...
30C 47C,48C 1 IC
OTHER M I X I N G APPLICATIONS Theoretical, T , or Ewperimentol,
Subject Mixins in stage contactors*
rnlumns fG-L)
E
Ref.
E E
13c 18C 35C,46C 2c
E E
Mixing in porous medium with stagnant zones Mixing in periodic countercurrent pracesses Washing of liquid retained in granular solids Dynamic behavior of isothermal crystallizer Modeling problems in mass transfer equipment Influence of mixing on solid-to-liquid transfer with chemical reaction Effect of vapor mixing on tray efficiency Drying of solid spheres with fine solid particles Effect of mixing on liquid-liquid extraction Effect of mixing and diffusion of high viscosity fluid in stirred tanks and extruders Analysis of polycondensation reactor Review of mixing a
G
3
2QC
15C 1 IC
42C 40C 4c 8C 6C 1oc
33c 79c 34c
gas, L = liquid, S = solid
VOL. 6 0
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DECEMBER 1 9 6 8
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TABLE D-3.
TRANSFERTO AND FROM SINGLE DROPS, BUBBLES OR SOLID PARTICLES Subject
Ref.
Primarily Theoretical
TABLE D-1.
GENERAL INTERPHASE MASS TRANSFER Theoretical, T , or Experimental, E
Subject
Ref.
Primarily Theoretical Transfer with moving interface Transfer to falling films a t low Reynolds number Application of surface stretch model to uniform wave motion in falling films Effect of surface-active materials on transfer in laminar films Transfer under oscillatory fluid flow Effect of surface resistance on penetration theory Over-all coefficient for a system containing a solid phase O n recent correlation of mass transfer data Comments and reply on diffusion in a homogeneous fluidized bed
T
20 720
T
380
T T T T
70 360 750
E,
T
Modes of aerosol particle motion Dissolving of stationary gas bubble in liquid Force on spherical evaporating particle due to motion and temperature gradients Rate equation for molecular diffusion in stagnant drop Shape of drop or bubble at low Reynolds number Mass transfer to drop or bubbles at high Reynolds number Transport to sphere Profile of a growing droplet Sphere or drop approaching a surface Transport and wake phenomena
Reviews
60
..*
390
...
370
...
560 850 770 7 0 290 180 520 30 SOD 920 710
E E E E E E E E E
...
...
Adsorption processes Coefficientsfor gas-liquid transfer in packed columns Transfer a t interfaces Transport equations for transfer in liquid films
120 660 170,700 340
TABLE D-2. SIMULTANEOUS INTERPHASE TRANSFER AND CHEMICAL REACTION Subject
260 410 670 140 530 320 4 0 , 160 550
Primarily Experimental Large or cap bubbles Sphere or drop approaching a surface Experimental method to study (G-L) Drag coefficients (L-G) Transport coefficients (G-L,S-L,S-G) Terminal velocity for noncontaminated (L-L) Micron thick samples of liquid surfaces Mass and heat transfer from rigid spheres
Primarily Experimental Correlation of effect of surface roughness Drying in granular beds Evaluating phase diffusion resistance for thin films Transfer across mobile interfaces Transfer through horizontal liquid films in wavy motion Absorption of gases in liquids Transfer in wetted-wall column with stirred film Effect of interfacial turbulence in liquid extraction Hydrodynamics of film and ripple flow Transfer in cocurrent pipe flow Scale-up problems in mass transfer equipment
80 100
Reactants or order
Primarily Experimental Acetylation of alkyl chlorides with sodium acetate Carbon dioxide absorption in sodium chloride solution Oxidation of methane to Fluidized bed as reactor formaldehyde Carbon dioxide in concenAbsorption in novel constant-interface apparatus trated alkaline solution Mass transfer driving force for a system Carbon dioxide in sodium with a chemical reaction hydroxide Effect of slurry particle geometry and state of aggregation Absorption with reaction in packed bed
Primarily Theoretical Film penetration models with chemical 1st order reaction for spheres and surfaces Turbulent transfer with reaction in a flat Arbitrary order duct
Ref.
680
Reviews Gas absorption from bubbles Heat and mass transfer from spheres
Subject General heterogeneous flow Basic equations includin the second law Design equations for tan%-typecontactor Review with foreign references Agitated stage-contactors Effective interfacial area (L-L) Size distribution (G-L,L-L,L-L) Fluid and particle motion (S-L) Holdup and flooding (G-L) Bubble columns (all G-L) Size from porous plate distributor holdup Velocity distribution Friction factors Coalescence Transfer coefficients
460 620
Liquid-liquid contactors (all L-L)
590
780 790
110
250
TABLE D-4. TRANSFER BETWEEN A CONTINUOUS PHASE AND A DISCONTINUOUS PHASE OF D ISCRETE PART ICLES
Fluidized b e d s Holdu of solid particles Transgr coefficients between phases (S-G) Hydromechanical model Transfer coefficient at wall (S-L) Dynamics of adsorption and desorption (S-G)
650
l S D , 300, 8 3 0 , 8 2 0 , 870 40,330 930 90 270, 640, 860 88D 540 400
Radial behavior of dispersed droplets in packed bed Transfer coefficients in extraction units Transfer coefficients in pulse-perforated-plate columns Air-agitated contactors Other Spray column with dense packing of drops Air flotation of hexavalent chromium Perforated plate column-froth and foam study Slurry reactor-behavior of solid particles Effect of droplet size-age distribution Effect of mass transfer on drop size distribution
Ref.
810 740 350
220 1 4 0 , 4 3 0 , 80D 750, 760 730
470,480,570 4 7 0 , 500 500 490 570 600
420 23'0, 5 8 0 , 26 43 0
450 890
510 280 670
210
a40 310 690 840 910 50
Albert Gomezplata is Professor and Thomas M . Regan is Assistant Professor in the Department of Chemical Engineering, University of Maryland, College Park, M d . AUTHORS
56
I N D U S T R I A L A N D E N G I N E E R I N G CHEMISTRY
~~~
( 7 8 0 ) extended the film penetration theory to describe mass transfer with chemical reaction in a spherical drop system and a surface resistance system. The kinetics of the reaction of sodium acetate particles with an alkyl chloride were observed to change from first to zero order by Polinski and Huang (680) when they adjusted the particle geometry and state of aggregation of the solid phase. They offer the explanation of a change in controlling step from mass transfer to reaction, and propose that osmotic diffusion is occurring inside the pores. T h e studies of transport to single particles are numerous. Large cap bubbles have received considerable experimental attention (790, 300, 820, 830, 8 7 0 ) because of their important role in fluidized beds. Calderbank ( 7 7 0 ) , in the third part of a review series, includes mass transfer properties of bubbles. Mass and heat transfer from spheres was reviewed by Galloway and Sage (250). Thorsen et al. (880) found that noncontaminated drops of organic liquid falling through water had a greater terminal velocity then previously reported. Brock ( 8 0 ) reports on some new modes of aerosol motion (photodiffusiophoresis) . The important area of transfer between a continuous phase and a discontinuous phase of discrete particles (drops, bubbles, or solid particles) is catagorized by type of contactor in Table D-4. A key variable for estimating mass transfer from bubbles and drops is the interfacial area or drop size distribution. Kawecki et al. (430) point to the necessity of measuring the bubble size distribution in various portions of a vessel to make an accurate estimate of the interfacial area. For a flow system, they found a distinct but not very large influence of volumetric flow rate on the gas interfacial area. I n a continuous reactor, Fernandes and Sharma (220) found the effective interfacial area to be practically the same as in a batch reactor operated under similar conditions. Koide and co-workers (470-500) have made considerable progress in the evaluation of the properties of bubble swarms.
~
TABLE E-I.
~
~~
PHASE TRANSITIONS Theoretical, T , or Experimental, E Ref.
Tobit ~~
~
~
T, E T
Vapor-phase fugacity coefficients for 114 binary systems Evaporation rates of sprays Kinetics of crystallization Evaporation coefficients by jet tensimeter Liquid droplet evaporation with surface impurities Sublimation with slip flow
IE 2E 3E 8E
T E E E
-
IIE 9E
TABLE E-2. SIMULTANEOUS MASS AND HEAT TRANSFER Theoretical, T , or Experimental, E
System or Topic Rigid spheres Parametric pumping Void fraction in random beds of equilateral cylinders Diffusion and conduction in granular beds Foam-type heat and mass exchanger Interphase heat and mass transfer and the Onsager relations Catalytic packed tube Forced convection on a flat plate
TABLE F.
T
Ref. 4E 5 E , QE 6E 7E IOE 12E 73E 14E
E, T E T E
T T T
INTERFACIAL PHENOMENA Theoretical,
T?or
Expenmental, E
Topic Diffusion and the adsorption-desorption antagonism Multilayer model for surface transport of adsorbed gases Gas-solid over-all mass transfer coefficient Scale-up of adsorber by simulation Vapor-liquid transport Gas-solid adsorption (primarily experimental) Role of surfactants in gas-liq., 1iq.-liq. system Adsorption a t 1iq.-liq. interface Solid-gas sublimation Gas desorption through surface-active monolayers Interfacial turbulence (COrmonoethanolamine) Nonlinear temperature profiles in surface tensiondriven flow Dyeing rates in organic fibers Interphase mass and energy transfer with surface reactions Diffusion of strontium and cobalt ions in pure NaCl crystals H2 diffusionin quartz
Ref.
T
3F
T T T
4F 5F 6F 7F-9F, 13F, 77F, 24F ZF, 1OF 17F 14F, 15F, 18F, 19F 16F ZOF 22F
T,E
T, E E, T E, T
E E E, T
E
23F 25F
T
2lF
E, T
IF 12F
E
Simultaneous Heat and Mass Transfer
Parametric pumping, a dynamic adsorptive separation technique utilizing the coupled transport action of periodic, synchronous cycling of thermal and chemical gradients, suffered the loss of its pioneering investigator, R. H. Wilhelm, this past year. Wilhelm and his coworkers illustrated the technique (143) by separating the mixtures toluene-n-heptane and NaC1-H20. Jenczewski and Myers, in a preliminary report (5E), point out the extension of parametric pumping to the separation of gas mixtures. Standart offered a second installment of his series (72E) on “The Second Law of Thermodynamics for VOL. 6 0
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DECEMBER 1 9 6 8
57
TABLE G-1.
Heterogeneous Flow Systems,” and dealt specifically with the problems of formulating the describing equations for interphase heat and mass transfer. Hughmark commented on the effect of the Reynolds and Schmidt numbers in correlations for heat and mass transfer from rigid spheres (4E).
PORE D I FFUSION Theoretical,
Interfacial Phenomena
T , 07
Exfierimental, E Ref.
Subject ~
~~~
__
~~~~
Uniform diffusivity in a nickel base steam-hydrocarbon reforming catalyst Afiotropic diffusivities in pressed boehmite pellets Surface transport of gases on platinum-alumipa Correlation between solid shapes and diffusion rates Effective diffusivity in porous solids Adsorptivity of active carbon Propane from He on activated alumina Adsorption of normal paraffins by a 5A molecular sieve Surface diffusion of chemisorbed Hz on Ni
2G 3G 6G 14G 15G 16G 20G 21G 22G
TABLE G-2. PORE DIFFUSION EFFECTS ON CHEMICAL REACTION
Effectiveness factors Diffusion and reaction in pores Surface transport effects Isobutylene hydration in cation exchange resin Ion exchange functionality in cross-linked polymers Effect of intraparticle temperature gradient Influence of external diffusion Rate of poisoning Transport limitations within catalysts Zeolite-catalyzed alkylation of benzene with ethylene Selectivity in cylindrical catalyst
Theoretical, T,, 07 Experimental E
Ref.
T
IG,12G, 13G
T
4G, 7G, SG, IOG, 23G
T E
5G
E, T
24G 1 7G 17G 18G 19G
T T T E
8G
25G 26G
TABLE H-I. MASS TRANSFER I N BOUNDARY LAYER FLOW Ref.
Subject T h e effect of mass addition in the laminar boundary layer of a n absorbing-emitting gas Heat and mass transfer in a reacting laminar boundary layer in the presence of multicomponent diffusion Discussions of mass transfer coefficients in gas laminar boundary layer along a flat plate
4H 14H 1SH
TABLE H-2. BOOKS AND REVIEWS RELATED T O MASS TRANSFER Topic
Ref.
Absorbers Partitioning a t the liquid-liquid interface Diffusion and chemical reaction in catalysis and absorption Fixed and fluidized bed reactors Transfer processes with a high mass flux Transport through biological barriers Separation processes Chemistry and physics of interfaces Molecular theories of liquids and mixtures Diffusion in pelleted catalysts Mass transfer and the second law Industrial gas cleaning Heterogeneous catalysis Liquid-liquid extraction
lH, 5H
~
58
2H
3H 6H 7H 8H S H , 7OH 1lH 12H 73H 15H 16H 17H 7 8H
INDUSTRIAL A N D E N G I N E E R I N G CHEMISTRY
Sada and Himmelblau (20F) investigated the reduction in gas desorption through surface-active monolayers on a water substrate. Their results showed that gas transport coefficients are related nonlinearly to surface coverage. I n a short communication, Danckwerts and Tavares-da Silva ( 8 F ) support and discuss the observation of convective currents when C 0 2 is absorbed by solutions of monoethanolamine. Vidal and Acrivos (23F) used linear stability theory to study the effect of nonlinear preconvective profiles on the magnitude of the critical Marangoni number for the case of surface tension-driven flow in evaporating liquid layers. Their analytical prediction was in good agreement with measured Marangoni numbers. Membrane Transport
Interest has grown in the area of membrane transport, due largely to the desalination effort and the medical application in artificial kidneys and membrane oxygenators. For information about the medical application area, the reader is referred to past volumes of the “Transactions of the American Society for Artificial Internal Organs,” “Proceedings of the Conference of Engineering in Medicine and Biology,” and “The Artificial Kidney” (41). I n future reviews, individual papers will be cited in this area. Kaufmann and Leonard ( 7 7 1 ) report on the intramembrane transport properties of carbohydrates in cellophane. They determined the matrix of phenomenological coefficients and showed that the tortuosity factor was not a simple geometric property of the membrane but rather related to the solute polymer interactions. The Monte Carlo technique was applied by Piekaar and Clarenburg (271) to a random array of cylinders as a model for an aerosol filter. Litt and Smith, in a short paper (791), outline a method of determining membrane permeability based on membrane rotation. By exposing an electrode ~~
TABLE I.
MEMBRANE TRANSPORT
Subject Reverse osmosis (hyperfiltration) Aerosol filters Separation of liquid mixtures Vapor permeability through polymers Permeability measurement technique Ion-selective properties of sintered glass Charge density of membranes (review) Intramembrane transport, phenomenological approach Electro-osmosis Volume flow through membrane Interfacial mass transport Anomalous osmosis with anion exchange membranes Transport in ultrafine capillaries Artificial kidney
Ref. 41, 7‘21, 731, 231-281, 301 141, 271, 221 161, 771 81 11, 191, 201 21, 31, gI
291 111 181 151 101
71 61
51
covered with membrane to an oxygen atmosphere, Aiba et al. (IZ) obtained a rapid determination of oxygen permeability. T h e technique gave good agreement for membranes with higher oxygen permeability.
f.,
REFER ENCES MOLECULAR DIFFUSION (1A) Albright J. E “Equations for the Description of Isothermal Diffusion in Multicompdnent &stems Containing Pairs of Chemically Equivalent Components,” J . Phys. Chem., 72, 11-15 (1968). (2A) A y o l d , K . R., and Toor, H . L., “Unsteady Diffusion in Ternary Gas Mixtures, A.I.Ch.E. J., 13, 909-914 (1967). (3A) Bhatia, R . N., Gubbins, K . E., and Walker, R. D., “Mutual Diffusion in Concentrated Aqueous K O H Solutions,” Trans. Faraday Soc., 64, 2091-2099 (1968). (4A) Bonoli, L., and Witherspoon, P. A.,“Diffusion of Aromatic and C cloparaffin Hydrocarbonsin H 2 0 from 2 to 60°,” J . Phys. Chem., 72,2532-2534 (1J68). (5A) Carman, P. C., “Intrinsic Mobilities and Interdependent Fluxes in Multicomponent Isothermal Diffusion. I . Simple Darker Systems,” ibid., pp 17071712. (6A) Carman P. C “Intrinsic M o es and Interdependent Fluxes in Multicomponent ’ I s o t h e k a l Diffusion. Complex Darker Systems,” ibid., 17131721. (7A) Concus, P., and Olander, D . R “Transient Diffusion in a Composite Slab,” Znt. J . Heat Mars Transfer, 11, 610-i)13 (1968). (SA) Costantino L. Crescenzi V and Vitagliano, V., “Differential Diffusion Coefficients of H&amethylehete?ramine Aqueous Solutions,” J . Phys. Chem., 72, 149-152 (1968). (9A) CulliEan H. T J r “Composition Dependence of Binary Diffusion Co7,519-520 (1968). efficient, I&. ENG.”CH&.,FUNDAM., (10A) Cullinan, H. T., Jr., “A Prediction Theory for Diffusion in Mixed Solvents,” A.Z.Ch.E. J., 13, 1171-1174 (1967). (11A) Cullinan H . T. Jr., “Predictive of Multicomponent Diffusion Coefficients,” Can. J . Chem.’Eng., 4.5, 377-381 (1967). (12A) Cullinan, H. T., Jr., and Cusick, M . R., IND. ENG.CHEM.,FUNDAM., 6 , 72 (1967). (13A) Cullinan H T. Jr. and Mortimer, R . G., “Comments and A Reply on Reference 12A,” ;bid.: 7, i30-332 (1968). (14A) Cunningham R. S and Geankoplis C. J “Diffusion inTbree-Component Gas Mixtures in ;he T r k t i o n Region Bktwee; Knudsen and Molecular Diffusion,’’ ibid., pp 429-432. (15A) Deb, S. K., and Barua, A. K “ ( H e Ne C o t ) by Two-Bulb Method,” Trans. Faraday Soc., 64, 358-362 (i468). (16A) DiCave, S., and Emery, A. H., Jr., “Continuous Flow in Packed Thermal Diffusion Columns,” A.I.Ch.E. J., 13, 1077-1080 (1968). (17A) DiCave, S. and Emery A. H. Jr., “Variation of Nonisothermal Diffusion Coefficients,” I& ENG.CH&., F U ~ D A M 7,. 95-99 , (1968). (18A) Gavalas, G. R., Reamer, H . H., and Sage, B. H., “Experimental Technique. Diffusion Coefficients in Hydrocarbon Systems. Homogeneous Phases a t Elevated Pressures,” ibid., pp 306-312. (19A) Goldstein, C., and Laurence R . L “Activity Corrections to Diffus in Polymetric Materials,” A.Z.Ch.k. J., 14: 357-357 (1968). (20A) Graff, R. A., and Drew, T. B., “Experimental Technique. Steady-State Method for the Measurement of Ternary Liquid Diffusion,” I N D .ENG. CHEM., FUNDAM.,7, 490-497 (1968). (21A) Grinberg G. A. “Solution of the Generalized Stefan Problem for the Freezing of a‘ Li uid’ and Related Problems in Heat Conduction, Diffusion, Etc.,” SOU. Phyr.-&ch. Phys., 12, 1169-1174 (1968). (22A) Gupta G. P. and Saxena, S. C., “Calculation of Viscosity and Diffusion Coefficient: of Nohpoiar Gas Mixtures a t Ordinary Pressures,” A.Z.Ch.E. J., 14, 519-520 (1968). (23A) Hansen, C. M. “Measurement of Concentration-Dependent Diffusion 6 , 609-614 Coefficients. T h e Edponential Case,” IND.END. CHEM.,FUNDAM., (1967). “Diffusion Coefficients of Ethylene Gas in H20,”, (24A) Hug A. and Wood T J . Chem. Eng.’Data, 13, 25i-259 (1968). (25A) Ivakin, B. A,, Suetin, P. E., and Plesovskikh, V. P., “Temperature Dependence of the Diflusion Coefficient of Certain Gas Pairs,” Sou. Phys.-Tech. Phys., 12, 1403-1404 (1968). (26A) Johnson I S. Jr. and Rush R . M . “Osmotic Coefficientsof Tungstosi icic Acid,” J . Phis: C h e k , ?2,360-362’(1968).’ (27A) Johnson R. R M and Sprio M;, :‘Diffusion Coefficients of A g + and Ag(SO&a- dy the Rotatyng Disk Metkod,’ tbid., 71, 3784-3790 (1967). (28A) Kochina N. N “Solution of Diffusion Problem with Non-Linear Boundary Conditions,” >okl. .&ad. Nauk. SSSR,174,305 (1967). (29A) Kreeyoy, M . M., and Wewerka, M “A Filter Paper Dia hragm Technique for Diffusion Coefficients,” J . Phys. Chem:: 71,4150-4152 (19677. (30A) Li, S. U.,and Gainer, J. I>., “Diffusion in Polymer Solutions,” IND. END. CHEM.,FUNDAM., 7,433-440 (1968). (31A) Marcinkowsky, A. E., Phillips, H. O., and Kraus, K. A., “Properties of Organic-Water Mixtures. VII. Self-Diffusion Coefficients of Na + i n Ethylene Glycol-Water and Glycerol-Water Mixtures a t 2S°C,” J . Phys. Chem., 72, 12011203 (1968). (32A) Marinsk J A. and Chu P. “ T h e Osmotic Properties of Polystyrensulfonates, I. ‘?Le OsAotic Coefficiehts,” ibid., 71, 4352-4359 (1967). (33A) Marsh K . N. “Mutual Diffusion in Octamethylcyclotetrasiloxane,” Trans. Faraday 64, 89i-901 (1968). (34A) Mullin, J. W., and Osman, M . M . , “Diffusivity, Density, Viscosity, and Refractive Index of Ni Ammonium Sulfate Aqueous Solutions,” J. Chem. Eng. Data, 12, 516 (1967). (35A) Pasternak, A. D., and Olander, D. R., “Diffusion in Liquid Metals,” A I . Ch.E. J., 13,1052-1057 (1967). (36A) Pop endick H. F. “Two Dimensional Transport Models for the Lower Layers o r t h e Atkosphe;e,” Znt. J . Heat Mass Transfer, 11, 67-69 (1968). (37A) Raedel, A. A., and Porai-Koshits A. B “Calculation of Liquid Phase Diffusion Coefficients,” Zh. Prikl. Khim.,i o , 456“(1967). (38A) RobiFson R C. and Stewart W. E., “Self-Diffusion i n Liquid C O Z and Propane, IN;. END. HEM., FUNDAM., 7, 90-95 (1968). (39A) Ruckenstein E and Berbente, C. P “The Equation of Convection Diffusion and Its Solution) in’ the Small Penetrayion Approximation,” A.I.Ch.E. J., 13, 1205-1207 (1967).
+ +
Sot.:
(40A) Rush, R . M., and Johnson, J. S., “Is0 iestic Measurements of the Osmotic and Activity Coefficient for the System H & O I - L ~ C ~ O I - H ~ OHC10~-NaCI04H z O and LiCIOa-NaC104-Ht0,” J . Phys. Chem., 72, 767 (1966). (41A) Scattergood, E. M., 2nd Lightfoot, E. N., “Diffusional Interaction in a n Ion-Exchange Membrane, Trans. Faraday Soc., 64,1135 (1 968). (42A) Shrier, A. L “Note on Predicting Diffusivities of Gases in Liquids,” Chem. Eng. Sci., 22, 139i) (1967). (43A) Stevenson, W. H., “On a Trans ort Equation Describing Steady Diffusion Through a Stagnant Gas,” A.I.Ch.E. 14, 350-351 (1968). (44A) Turner, J. C., and Snowdon, C. B., “Liquid Side Mass Transf:: Coefficients in Ion Exchange. An Examination of the Nernst-Plank Model, Chern. Eng. Sci., 23, 221-230 i1968). (45A) Wakao, N., Fujishiro, S., “Discussions on Mass Transfer Coefficients-for Gas Laminar Boundary Layer Along a Flat Plate,” Kagaku Kogaku, 5,4-7 (1967). (46A) Wason D. T and Wilke C. R. “Role of Concentration Level of the Nondiffusing SieciEs ‘in T u r b u l e h GaH-Phase Mass Transfer a t Ordinary Mass Transfer Rates, A.Z.Ch.E. J.,14, 577-583 (1968).
TURBULENT DIFFUSION AND DISPERSION (1B) Aunicky, Z “ T h e Longitudinal Mixing of Liquids in Bends,” Can. J . Chem.
Ene., 46, 27-31) (1968). (2B) Banerjee, S., Scott, D . S., and Rhodes, E., “Mass Transfer to Falling Wavy Liquid Films In Turbulent Flow,” IND.END.CHEM.,FUNDAM., 7, 22-27 (1968). (3B) Ca ps, D 0. and Rehm, T. R., “An Empirical Expression for the Turbulent Flow Gelociiy Distribution,’’ IND.END.CHEM.,PRGCESS DES. DEVELOP., 7, 311313 (1968). (4B) Davies, .I. T., and Ting, S. T., “Mass Transfer Into Turbulent Jets,” Chem. En!. Sci., 22, 1539-1548 (1967). (5B) Dit’man, V. V., “Mass Transfer Apparatus Design Taking Into Account Axial Mixins and the Scheme of Flow for Linear Equilibrium Relationship,” Teor. O m . Khim., 1, 100 (1967). (6B) Duda, J. L., and Vrentas, J. S., “Laminar Liquid Jet Diffusion Studies,” A.I.Ch.E. J., 14, 286-294 (1968). (7B) Edwards, M. F., and Richardson, J. F., “Gas Dispersion in Packed Beds,” Chem. Eng. Sci.,23, 109-123 (1968). (8B) Estrin, J., and Schmidt, E. H., Jr., “Penetration Theory Applied to Unsteady Gas Absorption with Irreversible First-Order Reaction,” A.Z.Ch.E. J., 14, 678-681 (1968). (10B) Fortescue, G E., and Pcarson J. R . A. “ O n Gas Absorption Into a Turbulent Liquid,” dhem. Eng. Sci., 22,’1163-117k (1967). (11B) Gill W N. “A Note on the Solution of Transient Dispersion Problems,” Proc. Ro;. So;. . A: .298., 335-339 (1967). (12B) Harris, H. G., Jr., and Goren, S . L., “Axial Diffusion in A Cylinder with Pulsed Flow,” Chem. Eng. Sci., 22,1571-1576 (1967). (13B) Harris, I. J., “ T h e Simulation of Single Phase Tubular Reactors with Incomplete Reactant Mixing,” Can. J . Chem. Eng., 46,66-69 (1968). (14B) Hartland, S., and Mecklenburgh, J. C., “ T h e Concept of Backmixing,” Chem. Eng. Sci., 23, 186-187 (1968). (15B) Horn, F. J. M., and Parish, T. D., “ T h e Influence of Mixing on Tubular Reactor Performance,” ibid., 22, 1549-1560 (1967). (16B) Howell, J. A,, Sparrow, E. M., and Schmal, M., “Concentration, Tem era ture and Reaction Surfaces in Laminar T u b e Flow with Radially Stepwise Tnlei Distribution,” ibid., pp 1383-1387. (17B) Hughmark, G. A.,“Eddy Diffusivity Close to a Wall,” A.I.Ch.E. J., 14, 352 (1968). (18B) Ishii, T., a$ Takeya G. “Longitudinal Mixing in a Gas Bubble Column Under Pressure, Kagaku kogaku, 5 , 212-213 (1967) (Engl.). (19B) Jackson, G. S., and Marchello, J. M., “Correlation of Gravitational Force for Absorption in Packed Columns,” IND.ENC. CHEM.,PROCESS DES. DEVELOP., 7, 359-361 (1968). (20B) Klinkenberg, A., “The Concept of Backmixing,” Chem. Eng. Sci., 23, 92 (1968). (21B) Komasawa, I., Histani, S., and Otake, T., “Some Experimental Studies on the Radial Behaviors of Dispersed Droplets in a Liquid-Liquid Packed Bed,” Kagaku Kogaku, 5 , 182-186 (1967) (Engl.). (22B) Kuchanov, S. I., and Pismen, L. M., “A Quasi-Homogeneous Model of a Packed Bed Reactor,” Teor. O m . Khim., 1,124 (1967). (23B) Levsb, I. P., Niyazov, M . I., Krainer, N . I., and Ganikhanova, F. F., “Mass Transfer in Absorbers with Fluidized Packed Beds,” Int. Chem. Eng., 8, 379-380 (1968). (24B) Mecklenburgh, J C and Hartland S “Design ofReactors with Backmixing. I. Exact Methods,” Chem: Eng. Sci.,23, 571’65 (1968). (25B) .Mecklenburgh, J., C., and Hartland, S., “Design of Reactors with Backmixing. 11. Approximate Methods,” ibid., pp 67-80. (26B) ,Mecklenburgh, J. C., and Hartland, S., “Design of Reactors with Backmixing. 111. Numerical Difference Between Differential and Stagewise Models,” ibid., pp 81-86. (27B) Mellish, W. G . “Applicability of Dispersion Results t o Packed Columns,” A.Z.Ch.E. J.,14, 668 (1968). (28B), Miss??, Y., and Yamada, N. “Oxidation of Calcium Sulfite in a Gas-LiquidSolid Fluidized Bed,” Kagnku Kogbku, 5 , 34-35 (1967) (Engl.). (29B) ,Miyamhi, T., I m a i , H., and Kubo, K., “Longitudinal Dispersion of Liquid on Travs.” . Sieve .~~ , ibtd.. nu 20-24. (30B), Miyauchi, T., p j i , H., and Saito K “Fluid and Particle Dispersion i n Fluid-Bed Reactors, J . Chem. Eng. JapLn, 1;’72-77 (1968). (31B) Petrovic Louis J and Thodos, George, “Mass Transfer in the Flow of Gases ThroAgh Packkb Beds. Low Reynolds Number Region,” IND. ENO. CHEM.,FUNDAM., 7, 274-280 (1968). (32B) Reejhsinghani, N. S Barduhn, A. J., and Gill, W. N., “Laminar Dispersion in Capillaries. Part V.” Experiments on Combined Natural and Forced Convection in Vertical Tubes,” A.I.Ch.E. J., 14, 100-109 (1968). (33B) Reiss L. P. “Cocurrent Gas-Liquid Contacting in Packed Columns,” IND.ENG.’CHEM.,’PROCESS DES.DEVELOP., 6,486-499 (1967). (34B) Rippin, D. W . T . , “ T h e Recycle Reactor as a Model of Incomplete Mixing,” IND.ENO.CHEM.,FUNDAM., 6,488-492 (1967). (35B) Ruckenstein E., “A Generalized Penetration Theory for Unsteady Convective Mass Transfkr,” Chem. Eng. Sci., 23, 363-371 (1968). (36B). Schenk, J. “Note Sur La Theorie D u Reacteur Piston Avec Dispersion Axiale,” ibtd,, i 2 , 1525-1526 (1967). (37B) Shuki, A. R., Corrigan, T. E., and Dean, M . J., “Chemical Reactors. Influence of Packing on Eflective Reactor Volume,” IND. END. CHEM.,PROCESS DES.DEVELOP., 7,433-434 (1968). (38B) Shulman, H. L., and Mellish, W . G., “Performance of Packed Columns: Part V I I I . Li uid Flow Patterns and Velocities in Packed Beds,” A.Z.Ch.E. J., 13, 1137-1140 71967). ~
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(39B) Sittel C. N. Jr. Threadgill W. D., and Schnelle, K . B., Jr., “Longitudinal Dispersio; for T w b h e n t Flow h Pipes,” IND. ENO.CHEM.,FUNDAM., 7, 39-43 (1968).
GENERAL MIXING PROCESSES IN FLOW SYSTEMS (1C) Anderson, T. B., and Jackson, R., “ A Fluid Mechanical Description of Fluidized Beds. Equations of Motion,” IND.ENO.CHEM.,FUNDAhl., 6 , 527-539 (1967). (2C) Barton, P., McCormick, R. H., and Penske, M . R . “Ammonia A Versatile Liquid Extraction Solvent,” IND.ENO.CEIEM., PROCESS 6 ~ sDEVELOP)., . 7,366-371 (1 968). (3‘2) Baskakov, S. P., and Grinpel’man, E. Ya., “Mixing of hlaterials in Adjacent Fluidized Beds,” Inrh. Fir.Zh., 11, 601 (1966). (4C) Blasinski, H . and Boss J. “ T h e Influence of Mixing on the Coefficient of Solid-to-Liquid ’Mass Tra)nsf& with Accompanying Chemical Reaction. I. Attempts at Experimental Verification of Models of Transfer with Simultaneous Chemical Reaction,” Inl. Chem. Engr., 8 , 53-59 (1968). (5C) Chang, D. H., and Bixler, H . J . “Washing of the Liquid Rctained by Granular Solids,” A.I.Ch.E. J., 13, 1058-io66 (1967). (6C) Ciborowski J. and Wolny A. “Drying of Wet Solid Spheres Through Contact with Dry bide Solid P a r h e 6 During Mixing,” Int. J . Heot Mars Y‘mns/er, 11, 255-265 (1968). (7C) Cloutier L. and Cholette A . ”Effect of Various Parameters on the Level of Mixing i; Cdntinuous Flow’Sys;ems,’’ Con. J . Chem. Eng., 46, 82-88 (1968). (8C) Diener, D. A., “Calculation of Effect of Vapor Mixing on Tray Efficiency,” IND.END.CHEY.,PROCESS DES.DEVELOP., 6,499-503 (1967). (9s)Gal-Or, B., “Coupled Heat and Multicomponent Mass Transfer in Particulate Systems with Residence Time and Size Distribution,” Inl. J . He01 M a s s Tranifer, 11, 551-565 (1968). (1OC) Goncharenko, G. K., and Gorlinskaya, A. P “Influence of Degree of Mixing on Mass Transfer in Liquid-Liquid Extraction,””Zh. Pi&. Khim., 40, 594 (1967). (11C) Gunn, D. J., “Mixing in Packed and Fluidized Bed,” The Chem. Engr., 219, 153 (1968). (12C) Harrell, J. E., and Perona, J. J., ”Mixing of Fluids in Tanks ofLarge Lengthto-Diameter Ratio by Recirculation,” I N D .ENG.CHEM.,PROCESS DES. DEVELOP., 7, 464-468 (1968). (13C) Hartland, S., “Backmixing in a Morris Contactor,” l r a n s . Inst. Chem. Eng., 45, 353-359 (1967). (14’2) Hoogendoorn, C. J.,and Den, Hartog, A . P. “Model Studies on Mixers in the Viscous Flow Region,” Chem. Eng. Sci., 22, 1684-1699 (1967). (15C) Horn, F. J. M., and May, R . A., “Effect of Mixing on Periodic Countercurrent Processes,” I N D .ENG.CHEM.,FUNDAM,, 7, 349-354 (1968). (16C) Howarth, W. J., “Measurement of Coalescence Frequency in an Agitated Tank,” A.I.Ch.E. J., 13, 1007-1013 (1967). (17C) Inoue, I., and Sato, K., “Circulation Time Distribution in a Stirred Vessel,” Kagaku Kognku, 5, 121-124 (1967) (Eng.). (18‘2) Ischikawa, Y., Akachi, Y., and Makino, K . “ O n the Longitudinal Mixing Characteristics of the Gas Bubble Column with Pkrforated Plates,” ibid.,pp 179182. (19C) Kilkson, H., “Generalization of Various Polymerization Problems. T h e Concept ofFlow Influx,” I N D . E K G . CHEM.,FUNDAY., 7,354-363 (1968). (2OC) Kim Y. E. Lee C. S. and Kang, W. K . “Longitudinal Solid Mixing in a Screen Packed Fiuidized Beh;’ J . Korean Init. &em. Eng., 5, 205-208 (1968). (21C) Kim, Y. E., Shin, K . S., and Kang, TV. K . “A Study of Liquid Mixing on Screen Blade Turbine Impeller (I),’’ ibid., pp 201-204. (22C) King, Y. E., Shin, K . S., and Kang, W. K., ibid., pp 209-213. (23‘2) Klinkenberg, A., “Moments of Residence Time Distributions for Cascades of Stirred Vessels with Backmixing,” Chem. Eng. Sci.,23, 175-181 (1968). (24‘2) Kobayashi, H., Arai, F., and Izawa, K., “Performance of Gas-Solid Fluidized Bed Catalytic Reactors in Relation to Its Residence Time Distribution Characteristics,” Kagoku Kogaku, 5 , 28-34 (1967) (Engl.). (26’2) Kovasy, K., “Different Types of Distribution Functions to Describe a Random Eddy Surface Renewal Model,” Chem. E n g . Sci., 23, 90-91 (1968). (27C) Latham, R., Hamilton, C. and Potter D. E.. “Backmixing and Chemical Reaction in Fluidized Beds,” d i t . Chem. En;., 13, 666-670 (1968). (28C) Lebrer, I. H., “Gas Agitation of Liquids,” I N D ,ENG.CHEY.,PROCESS DES. DEVELOP.,7, 226-239 (1968). ( 2 9 C ) Levich, V. G., Markin, V. S., and Chismadjev, Yu. A.,”On Hydrodynamic Mixing in a Model of a Porous Medium with Stagnant Zones,’’ Chem. Eng. Sci., 22, 1357-1367 (1967). (30‘2) Mamuro, T., and Haltori, H., “Flow Pattern of Fluid in Spouted Beds,” J . Chem. Eng. Japan, 1, 1-5 (1968). (31C) Mill:r, D. N., “Scale-up of Agitated Vessels-Mass Transfer From Fixed Surfaces, Chem. Eng. Sci., 22, 1617-1626 (1967). (32C). y i r e a u , J.,,P., and Bischoff, K . B., “Mixing and Contacting Models for Fluidized Beds, A.Z.Ch.E. J., 13, 839-845 (1967). (33C) Ohya, H., and Miyauchi, T.,“Mixing and Diffusion in High Viscous Fluid,” Kagaku Kogaku, 5, 118-20 (1967) (Engl.). (34C) Oldshue, J. Y., “Annual Review of Mixing,” IND. ENG. CHEM.,5 9 (111, 58-70 (1967) and 60 ( l l ) , 24-35 (1968). (35C) Otake, T., Tone, S., and Matsuo, H., “,Mixing Characteristics of Solids in Stirred Moving Beds,” K q a k u Kogaku, 5 , 134-138 (1967). (36C) Petho, A , , “Mean and Variance of Residence Time Distributions in Fixed Bed Multistage Exchange Processes of Linear Kinetics,” Chem. Eng. Sci., 22, 1793-1801 (1967). (37C) Pyle, D. L., and Harrison, D., “An Experimental Investigation of the T w o Phase Vheory of Fluidization,” ibid., pp 1199-1207. (38C) Rehakova, M., and Novasad, Z., “Residence Time Distribution and Fractional Conversion for a Multistage Reactor with Backmixing Between Real Stages,” ibid., 23, 139-145 (1968). (39C) Rippin, D. W. T., “ T h e Recycle Reactor as a Model of Incomplete Mixing,” I N D .END.CHEX.,FUNDAM., 6,488-492 (1967). (40C) Rozen, A. M., Aksel’rod, L. S . , and Dil’man, V. V.,“Some Modeling Problems in the Development of Mass-Transfer Equipment,” Int. Chem. Engr., 8 , 243-252 (1 968). (41C) Sandblom,: H., “ T h e Pulse Technique for Investigating Solid Mixing in a Fluidized Bed, Brit.Chem. Ens., 13,677-679 (1968). (42C) Sherwin, 41. B., Shinnar, R., and Katz, S . , “Dynamic Behavior of the Well Mixed Isothermal Crystallizer,” A.I.Ch.E. J . , 13, 1143-1 154 (1967). (43C) Shinnar, R., and Nlaor, P., “Residence Time Distribution in Systems with Internal Reflux,” Chern. Eng. Sci., 22, 1369-1381 (1967). (44C) Srimathi, C. R., and Bhat, G. M., “Evaluation of Residence Time for a Gas-Solid Interface Moving Bed System,” Brit. Chem. Eng., 12, 1597-1599 (1 967).
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(45C) Takamutsu, T., and Sawada, T., “ O n Mixing Models of Continuous Stirred Tank,” Kagoku Kognku, 5 , 163-166 (1967) (Engl.). (46C) Tone, Z., Higuchi, Tamura, S., Otake, T., “Mixing Characteristics of Solids by Impellers in Multiple-Moving Beds,” ibid., pp 67-171. (47C) Vail, Yu. K., Manakov, h’. Kh., and Manshilin, V. V. “Turbulent Mixing in a Three-phase Fluidized Bed,” Int. Chem. Engr., 8, 293-296’(1968). (48‘2) Vail, Yu. K., Manakov, K.Kh., and Manshilin, V. V.,”Turbulent Agitation in a Three-phase Fluidized Bed,” ibid., pp 516-520. (49C) Woollard, I. Is. M., and Potter, 0. E., “Solids Mixing in Fluidized Beds,” A.I.Ch.E. J., 14, 388-391 (1968). (50C) Yoshida, K., and Kunii, D., “Stimulus and Response of Gas Concentration inBubbling Fluidized Beds,” J . Chem. Eng. Jupon, 1, 11-16 (1968).
INTERPHASE MASS TRANSFER (1D) Angelo, J. B., and Lightfoot, E. N., “Mass Transfer Across Mobile Interfaces,” A.I.Ch.E. J., 14, 531, 540 (1968). (2D) Apelblat, A . , and Katchalsby, A,, “Mass Transfer with a Moving Interface,” Int. J . Heal Masr,TronJfer, 11, 1053-1067 (1968). (3D) Bakker, C. A . P., Fentener Van Vlissingen H . F., and Beek, \.\T. J “The Influence of the Driving Force in Liquid-Liqujd Extraction-A Study 6f Mass Transfer With and Without Intcrfacial Turbulence Gnder Well-Defined Conditions,” Chem. Eng.Sci., 22, 1349-1355 (1967). Settling of a Fluid Sphere Toward a Flat (5D) Bayens, C. A . , and Laurence, R . L., “Communication. Effect of Mass Transfer on Drop Formation,” IND.END.CHEM.,FUNDAM,, 7, 521-522 (1968). (6D) Bomshtein, V. E., Planovskii, A . N., and Egorov, N. N., “Over-all Mass Transfer Coefficient for Systems of a Solid Phase;” Int. Chem. Engr,, 8 , 413-414 (1968). (7D) Boyadzhiev K h . Levich, V.. and Krylov V. “ T h e Effect of Surface Active Materials on M’ass Tkansfer in Laminar Film $lo!%:,” ibid., pp 393-396 (1968). (8D) Brock, J. R., “Some New hlodes of Aerosol Particle Motion: Phctodiffusiophoresis,” J . Phis. Chem., 72, 747-749 (1968). (9D) Buzzard J. L. and Nedderman R . h?. ”The Drag Coefficients of Liquid Droplets A c h z r a t h g Through Air,”’Chem. E’ng. Sci., 22, 1577-1586 (1967). (10D) Cable, M., “ T h e Dissolving of Stationary Gas Bubbles in a Liquid,” ibid., pp 1393-1398. ( l l D ) Calderbank, P. H., ”Review Series No. 3. Gas Absorption from Bubbles,” The Chem. Engr., 212, 209-233 (1967). ( l 2 D ) Carter, J. FY. “Developments in Adsorption Processes,” Brit, Chem. Eng., 13, 229-234 (1968)). (13D) Cheh, H . Y., and Tobias, C. TV;: “Mass Transfer to Spherical Drops or Bubbles at High Reynolds Number, TND. EXC. CHEY.,F U N D A M7,. , 48-52 (1968). (14D) Chen, H . T., and Middleman, Stanley, “Drop Size Distribution in Agitated Liquid-liquid Systems,” A.2.Ch.E. J., 13, 989-995 (1967). (15D) Coughlin, R . W., “Surface Resistance in Transport from Vapor to Liquid,” Chem. Eng. Sci., 22, 1503-1511 (1967). (16D) Cox, R . C., and Brenner, H . , “ T h e Slow Motion of a Sphere Through a Viscous Fluid Towards a Plane Surface. 11. Small Gap Widths, Including Inertial Effects,” ibid., pp 1753-1777. (17D) Cratin, P. D. “Partitioning at the Liquid-Liquid Interface,” IND, ENO, CHEH.,60 (9), 14-i9 (1968). (18D) Danckwerts, P. V., ” T h e Absorption of Gases in Liquids,” Teor. Osn. Khim., 1, 31 (1967). (19D) Davenport, W.G., Richardson, F. D., and Bradshaw, A. V., “Spherical Cap Bubbles in Low Density Liquids,” Chem. Eng. Sci.,22, 1221-1234 (1968). (20D) Dickinson, Dean R., and Marshall, W. R., Jr., “ T h e Rates of Evaporation ofSprays,” A.I.Ch.E. J., 14, 541-552 (1968). (21D) Fernandes, J. B., and Sharma 51. M . , “Air-Agitated Liquid-Liquid Contactors,” Chem. Eng.Sci., 23, 9-16 ( l b i 8 ) . (22D) Fernandes, J.B., and Sharma M. M. “Effective Interfacial Area in Agitated Liquid-Liquid Contactors,” ibid.,i2, 1267L3482 (1967). (23D) Fridland, M. F “Mass-Transfer Coefficients in Fluidized Systems,” Int. Cfimz. Engr., 7, 598-6z4 (1967), (24D) Fridland, M . F., “Mass Transfer Coefficients in Fluidized Systems,’’ Khim. i Tekh. Topl. i Masel, 5, 7 (1967). (25D) Gal,l,oway, J. R . , and Sage, B. H., Thermal and Material Transfer from Spheres, Int. J . Heat M a s s Transfer, 11, 539-549 (1968). (26D) Gardner, G. C., “Force on a Small Spherical Evaporating Particle in Its Pure Vapor Due to Motion and Temperature Gradients,” Chem. Eng. Sci., 23, 29-40 (1968). (27D) Golding J. A. Gravdon W. F., and Johnson, A. I., “Mass Transfer from Single Bubblis Undkr Dishlatlon Conditions,” Trans. Inst. Chem. Eng., 46, 172-176 (1968). (28D) Goncharenko, G . K . , and Gotlinskaya, A. P., “Influence of Degree ofMixing on Mass Transfer in Liquid-Liquid Extraction,” Zh. Przkl. Khim. 40, 594 (1967). (29D) Goren, S . L., and Mani, R . V. S., “Mass Transfer Through Horizontal Liquid Films in Wavy Motion,” A.I.Ch.E. J., 14, 57-61 (1968). (30D) Grace, J. R., and Harrison, D., “The Influence of Bubble Shape on the Rising Velocities of Large Bubbles,” Chem. Eng. Scz., 22, 1337-1347 (1967). (31D) Grieves, R . B., and Ettelt, G. A,, “Continuous Dissolved-Air Ion Flotation ofHexavalent Chromium,” A.I.Ch.E. J., 13,1167-1171 (1967). (32D) Halligan, J. E., and Burkhart, L. E., ”Determination of the Profile of a Growing Droplet,” ibid.,14, 411-414 (1968). (33D) Hartland, S., “The Approach of a Liquid Drop to a Flat Plate,” Chem. Eng. Sci., 22, 1675-1687 (1967). (34D) Hobler, T., and Kidzierski, S., “Analysis of the Equations of Mass Transfer in the Liquid Phase in the Flow- of Liquid Down a TVall,” Int. Chem. Engr., 7, 654-666 (1967). (351)) Hodossy, L., “Momentum, Heat, and Mass Transfer in Two-Phase Flow,” tbid., 8, 427-438 (1968). (36D), Horn, F. J. >I.. and Kipp, K . L., Jr., “Mass Transport Under Oscillatory Fluid Flow Conditions,” Chem. Eng. Sci., 22, 1879-1880 (1967). (37D) Houghton, G., and Ruckenstein, E., “Correspondence,” I N D .END.CHRM., FUNDAM., 6 , 617-619 (1967). and Lightfoot, E . N . , “ M a s s Transfer to Falling Films. I. (38D) Howard, D . W., Application of the Surface Stretch Model to Uniform Wave Motion,” A.I.Ch.E. J . , 14, 458-467 (1968). (39D) Hubbard, D. W., “Correlations of Mass Transfer Data: Comments on an Article by Son and Hanratry,” ibid., pp 354-355. (40D) Hughmark, G. A,, ;‘Mass and Heat Transfer from Rigid Spheres,” ibid., 13, 1219-1221 (1967).
(41D) Jury, S. H., “An Improved Version of the Rate Equation for Molecular Diffusionin a Dispersed Phase,” ibid., pp 1124-1 126. (42D) Kalinowski, B., “ A p p m a t e Determination of the Hold-up Time of Granular Materials in the luidized Phase in a Continuously Operating Reactor,” Znt. Chem. Enqr., 8, 224-229 (1968). (43D) Kawecki, W., Reith, T., Van Heuven, J. W., and Beek, W. J., “Bubble Size Distribution in the Impeller Region of a Stirred Vessel,” Chem. Eng. Sci., 22, 1519-1523 (1967). (44D) Kehat, E., and Letan, R., “Operation of a S ray Column with a Dense DES. 7, 385-389 (1968). Packing ofDrops,” IND.ENO.CHEM.,PROCESS (45D) King, D. H., and Smith, J. W., “Wall Mass Transfer in Liquid-Fluidized Beds,” Con. J . Chem. Eng., 45, 329-333 (1967). (46D) Koba ashi, T., Inoue, H., and Yagi, S., “The Abnormality of the Rate of COz Gas ibsorption into the Concentrated Alkaline Solution,” Kagaku Kogaku, 5 , 211-32 (1967( (Engl.). (47D) Koide, K., Hirahara, T., and Kubota, H., “Average Bubble Diameter, Slip Velocity and Gas Hold-up of Bubble Swarms,” ibid., pp 38-42. (48D) Koide, K., Kato, S., Taraka Y. and Kubota H., “Bubbles Generated from Porous Plates,” J . Chem. Eng. Jap& 1: 51-56 (19681. oide K . and Kubota H. “Friction Factor in Vertical Bubble and Slug‘‘i?JwK Ka&u kogaku, 5, 73:77 (1967) (Engl.). (SOD) Koide K., and Kubota, H.,“Gas Hold-up Distribution and Liquid Viscosity Distribution on Bubble Flow in Vertical Columns,’’ ibid., pp 77-81. (5lD) Komasawa, I., Hisatani, S., and Otake, T., “Some Experimental Studies on T+ Radial Behavior of Dispersed Droplets in a Liquid-Liquid Packed Bed,” ibbd., pp 182-186. (52D) Kulov, N. N., and Malyusov, V. A., “Mass Transfer in Wetted-Wall Column With Stirred Liquid Film,” Teor. Om. Khim. Tekh., 1, 213 (1967). (53D) Lee, K., and Barrow, H., “Transport Processes in Flow Around a Sphere With Particular Reference to the Transfer of Mass,” Znt. J. Heat Mass Transfer, 11, 1013-1026 (1968). (54D) MacInt re F. “Bubbles: A Boundary Layer ‘Microtome’ for MicronThick Sampgs bf a Liquid Surface,” J . Phys. Chem., 72, 589-592 (1968). (55D) M a p v e y R H . and MacLatchy C. S., “Mass Transfer and Wake Phenomena, A.Z.6h.E. J.: 14,260-265 (19i8). (56D) Mahato, B. K., and Shemilt, L. W., “Effect of Surface Roughness on Mass Transfer,” Chrm. Eng. Sci., 23, 183-185 (1968). (57D) Marrucci, G., and Nicodemo, L., “Coalescence of Gas Bubbles in Aqueous Solutions of Inorganic Electrolytes,” ibid., 22, 1257-1256 (1967). (58D) Martyushin, I. G., “Hydromechanical Model of Non-Homogeneous Fluidized Bed,” Zu.Prikl. Khim., 40, 589 (1967). (59D) McConkey, B. H., and Wilkinson, P. R., “Oxidation of Methane to Formaldehyde in a Fluidized Bed Reactor,” IND.ENC.CHEM.,PROCESS DES.DEVELOP., 6, 436-440 (1967). (60D) Men’shikov, V. A,, “Phase Contact Surface and Mass Transfer in Bubbling Reactors,” Khim. i Tekh. TOPI.Masel., 3, 25 (1967). (6?,D) M i auchi T Ohya H Kikuchi, H., Hashizume, H., and Kagawa K Mass +ransf& Siudy in’ P&e-Perforated Plate Columns,” Kagaku Kogaiu, 5: 108-111 (1967) (English). (62D) Mutriskov, A. Ya., and Maminov, 0. V., “Problems in Analyzing Processes of MassTransfer with Chemical Reaction,” Znt. Chem. Engr., 8, 410-412 (1968). (63D) Namkoony, S., Chung, W. C., and Moon, S. G., “Measurement of Gas Cross Flow Coefficient Between a Bubble and Emulsion Phases in a Gas-Solid Fluidized Bed.” J . Korean Znst. Chem. Ene.. 5.97-102 11967). . , (64D) Noordsij, P., and Rotte, J. W.,“MassTransfer Coefficients to a Rotating and to a Vibrating Sphere,” Chem. Eng. Sci.,22, 1475-1481 (1967). (65D) Onda, K., Sada, E., an,$ Takeuchi, H., “Gas Absorption With Chemical Reaction in Packed Columns, J . Chem. Eng. Japan, 1,62-66 (1968). (66D) Onda, K., Takeuchi, H., and Okumoto, Y., “Mass Transfer Coefficients Between Gas and Liquid Phases in Packed Columns,” ibid., pp 56-62. (67D) Pan, F. Y . and Acrivos A. “Shape of a Dro o r Bubble at Low Reynolds Number,” IND.’ENC.CHEM.,&DAM., 7,227-232 968). (68D) Polinski, L., and Huang, I-D., “Role of Slurry Particle Geometry and State of Aggregation in Changing the Kinetics of a Reacting Slurry System. Acetylation of Alkyl Chlorides with Sodium Acetate,” IND.ENC.CHEM.,PROCESS DES.DEVELOP., 6,432-436 (1967). (69D) Redwine, D. A,, Flint, E. M., and Van Winkle, M., “Froth and Foam Height Studies. Small Perforated Plate Distillation Column,” ibid., pp 525-532. (70D) Ross, S., “Chemistry and Physics of Interfaces,” IND.ENO.CHEM.,60 (9), 12-13 (1968). (71D) Rozen:, A. M., “Scaling-u Problems in Development of Mass Transfer Apparatus, Teor. Om. Khim. TeKh., 1,459 (1967). (72D) Ruckenstein, E., and Berbente, C., “Mass Transfer to Falling Liquid Films at Low Reynolds Numbers,” Znt. J . Heat Mass Transjer, 11,743-753 (1968). (73D) Rushton J. H. and Bimbinet J. J., “Hold-up and Flooding in Air Liquid Mixing,” Can: J. Chlm. Eng., 46,16121 (1968). (74D) Schaftlein, R. W., and Russell, T. W., “Two-Phase Reactor Design,” I N D . END.CHEM., 60 (5), 12-27 (1968). (75D) Schwartzberg, H. G., and Treybal, R . E., “Fluid and Particle Motion in Turbulent Stirred Tanks. I. Fluid Motion,” IND. ENO. CHEM.,FUNDAM., 7, 1-6 (1968). (76D) Schwartzberg, H . G., and Treybal, R. E., “Fluid and Particle Motion in Turbulent Stirred Tanks. 11. Particle Motion,” ibid., pp 6-12. (77D) Shafronovskii, A. V., and Ruchinskii, V. P. “Method of Evaluating Phase Diffusion Resistance for Thin Film Mass Tranbfer,” Tear. Osn. Khim., 1, 1 1 1 (1967). (78D) Smith, J. L., and Winnick, J., “Film-Penetration Models for Mass Transfer with Chemical Reaction,” A.Z.Ch.E. J., 13, 1207-1209 (1967).
EVEL LOP.,
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(79D) Solbrig, C. W., and Gidaspow, D., “Turbulent Mass Transfer with an Arbitary Order Surface Reaction in a Flat Duct,” Znt. J . Heat Mass. Transfer, 11, 155-180 (1968). (BOD) S row F. B., “Drop Size Distributions in Strongly Coalescing Agitated L i q u i x L i q h d Systems,” A.Z.Ch.E. J., 13, 995-998 (1967). (81D) Standart, G., “ T h e Moment of Momentum and Electrochemical Equations for Heterogeneous Flow Systems,” Ch,em. Eng. Sci., 22, 1409-1416 (1967) and “The Second Law of Thermodynamics for Heterogeneous Flow Systems. I. Basic Relations and the Curie Theorem,” ibid., pp 1417-1438. (82D) Stewart, P. S. B., “Isolated Bubbles in Fluidized Bed-Theory and Experiment, Trans. Inst. Chem. Eng., 46, 60-66 (1968). (83D) Stewart, P. S. B., “Prediction of Voidage Fraction Near Bubbles in Fluidized Beds,” Chem. Eng. Sci., 23, 396-397 (1968). (84D) SugaEuma T Yamanishi, T “Behavior of Solid Particles in Bubble Columns, K o g h h g a k u , 5, 203-268 (1967) (Engl).
(85D) Suzuki M. and Maeda S. “ O n the Mechanism of Drying of Granular Beds ‘Mass’Tradsfer from DisLoniinued Sources,”’ J. Chem. Eng. Japan, 1, 26-31 (1968). (86D) Svinaryov, V. A “Mass Transfer Between a Spherical Solid and Turbulent Gas Flow,” Znzh. Fi.z.’>h., 12, 10 (1967) (87D) Szekely J. and Martins G . P. “On the Behavior of Gas Bubbles in Liquids a t Reduced h ; s u r e s , ” Chem.’Eng. S k , 23,398-399 (1 968). (88D) Thorsen G Stordalen R . M and Terjesen, S. G. “On the Terminal Velocity of Circuyating and dscillatini Liquid Drops,” ibid., bp 41 3-426. (89D) Todes, 0 . M., and Lezin, Yu. S. “Dynamics of Continuous Adsorption and Desorption i n a Fludized Bed with Non-Linear Isotherm,” Znt. Chem. Engr., 7. 577-581(1967). , , (90D) Tudose R F. Savenau T. and Cristian G “Transfer Processes Between Immiscible Liqiid;. T h e H;dr;dynamics of *ilmFlow,” ibid., pp 637-642. (71D) Valentas, K. J., and Amundson, N. R., “Influence of Droplet Size-Age Distribution on Rate Processes in Dispersed Phase Systems,’’ IND.ENO.CHEM., FUNDAM., 7, 66-72 (1968). (92D) Watkinson, A. P., and Cavers, S. D. “Mass Transfer Between Liquids in Cocurrent Pipeline Flow,” Can. J. Chem. Erzg., 45,258-263 (1967). (93D) Zieminski, S. A., and Raymond, D. R “Experimental Study of theBehavior of SingleBubbles,” Chem. Eng. Sci., 23, 17-28 (1968). SIMULTANEOUS H E A T AND MASS TRANSFER (1E) Chueh, P. L., and Prausnitz, J. M., “Vapor-Liquid Equilibria at High Pressures. Vapor-Phase Fugacit Coefficients in Nonpolar and Quantum-Gas Mixtures,” IND.END.CHEM., 6,492-498 (1967). (2E) Dickinson, D. R., and Marshall, W. R., Jr., “The Rates of Evaporation of Sprays,” A.Z.Ch.E. J., 14, 541-552 (1968). (3E) Han, C. D., “Evaluation of Some of the Kinetic Parameters in Crystallization,” Chem. fing. Sci., 23,321-330 (1968). (4E) Hughmark, G. A. “Mass and Heat Transfer from Rigid Spheres,” A.1.Ch.E. J.,13,1219-1221 (19k7). (5E) Jenczewski, T. J., and Myers, A. L., “Parametric Pumping Separates Gas Phase Mixtures,” ibid., 14,509 (1 968). (6E) Kondelik, P., Horak J., and Tesarova, J., “Heat and Mass Transfer in Heterogeneous Catalyst:. Variation of Local Void Fraction in Randomly Packed Beds of E ullateral Cylinders,” IND.END.CHEM.,PROCESS DES.DEVELOP., 7, 250-252 (1 9683. (7E) Kuchanov, S. I., Levich, V. G., and Pis’men, L. M., “Transverse Diffusion and Heat Conduction in Granular Beds,” Znt. Chem. Engr., 8,162-167 (1968). (BE) Maa, J. R., “Evaporation Coefficient of Liquids,” IND.ENO.CHEM.,FUNDAM., 6, 504-518 (1967). (9E) Munakata, T., Nagasue, H., and Doi, K., “Mass Transfer in Tube Within Slip Flow Region a t Low Pressure,” Kagaku Kogaku, 5, 7-10 (1967). (10E) Sakra T. Pilar A Plisek J and Stejokol J. “Study of a Tubular FoamType Hea; anh Mas; Ex’change;,”’>nt. Chem. En&., , ; 204-208 (1968). (11E) Shih, Y., and Coughanowr D. R. “Eva oration of Liquid Containing Surface Impurities,” A.Z.Ch.E. J.,’14, 5021507 (1f68). (12E) Standart, G., “ T h e Second Law of Thermodynamics for Heterogeneous Flow Systems-11. Interphase Heat and Mass Transfer and the Onsager Relations,’’ Chem. Eng. Sci., 22, 1627-1653 (1967). (13E) Tone, S., and Atake, T., “Analytical Prediction of Concentration and Temperature Profiles i n the Catalytic Packed Tube,” Kagaku Kogaku, 5, 171-178 (1967). (14E) Wilhelm, R . H., Rice, A. W., Rolke, R. W., and Sweed, N. H., “Parametric Pumping. Dynamic Princi le for Separating Fluid Mixtures,” IND. ENO. CHEM.FUNDAM., 7,337-349 8968). (15E) Zeh, D. W., and Gill, W. N., “Heat Transfer and Binary Diffusion with Thermodynamic Coupling in Variable Property Forced Convection on a Flat Plate,” A.Z.Ch.E. J.,15, 140-147 (1967).
JUNDAM.,
INTERFACIAL PHENOMENA (1F) Allnatt, A. R., and Pantelis, P., “Isothermal Diffusion of Strontium and Cobalt Ions in Pure NaCl Crystals and Reconsideration of the Soret Effect,” Trans. Faraday Sac., 64, 2100-2105 (1968). (2F) Aristov, B. G., and Kiselev, A. V., “Adsorption of Nz and Ar Vapors on Surfaces of Nonspecific Adsorbents-Gra hitized Carbon Black, Polyethylene, and Polytetrafluoroethylene,” CoIloid J . U.J.S.R., 29,465-470 (1967) (Engl.). (3F) Baret, J. F., “Kinetics of Adsorption from a Solution-Role of Diffusion and of the Adsorption-Desorption Antagonism,” J. Phyr. Chem., 72, 2755-2758 (1968). (4F) Bell, W. K., and Brown, L. F., “A Multilayer Model for the Surface Transport of Adsorbent Gases,” ibid., pp 2365-2370. (5F) Bomshtein, V. E., Planovskii, A. N., and Egorov, N. N., “Over-all Mass Transfer Coefficients for Systems with a Solid Phase,” Znl. Chem. Engr., 8, 413-414 (1968). (6F) Chen, J. W., Buege, J. A., Cunningham, F. L., and Northam, J. I., “Scale-up of a Column Adsorption Process hy Computer Simulation,” IND. ENO. CHEM., PROCESS DES.DEVELOP., 7,26-31 (1968). (7F) Coughlin, R . W., “Surface Resistance in Transport From Vapor to Liquid,” Chem. Eng. Sci., 22, 1503-1511 (1967). (8F) Danckwerts, P. V., and Tavares-da Silva, A., “Surfaces Instability During the Absorption of COSby Monoethanolamine Solutions,” ibid., pp 1513-1514. (9F) Davies G. A Ponter, A. B., and Craine K “The Diffusion of COz in Organic Liquids,;’ Can. J . Chem. Eng., 45,372-336 (i967). (10F) Day, R . E., and Parfitt, G . D., “Adsorption of Ethanol, n-Octanol, and nDodecanol or Defined Rutile Surfaces from Binary Liquid Mixtures with pXylene and n-Heptane,” Trans. Faraday Soc., 64,815-822 (1968). (11F) Elenkov, D., “Influence of Surface-Active Additives on Mass Transfer in Gas-Liquid and Liquid-Liquid,” Teor. Om. Khim. Tekh., 1,176 (1967). (12F) Garland, J. K., and Schroeder, J. W., “Rate of H2 Diffusion in RoomTemperature Irradiated Quartz,” J . Phys. Chem., 72, 2277-2278 (1968). (13F) Jhaveri, A. S., and Sharma, M . M “Absorption of Oxy en in Aqueous Alkaline Solutions of Sodium Dithionite,” b e m . Eng. Sci.,23, 1-8 8968). (14F) Lawrence, J., and Parsons, R., “Adsorption at the Hg/Formic Acid Interphase,” Tmnr. Faraday Soc., 64, 1656-1678 (1968). (15F) Lawrence, J., and Parsons, R., “Specific Adsorption a t the Mercury/ Sulpholane Interface,” ibid., pp 751-770. (16F) Munakata, T., Nagasue, H., and Doi, K., “Mass Transfer in Tube Within Slip Flow Region a t Low Pressure,” Kagaku Kogaku, 5 , 7-10 (1967) (Engl.). (17F) Onda, K., Kobayashi, T., and Nagase, T., “Rate of Absorption of CO? bx Sodium Carhonate Solution Containing Amino Acids or Arsenious Acid, Znt. Chem. Engr., 8,520-526 (1968).
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(18F) Parsons, R., and Symo:s, P. C., “Adsorption of Sulphur Containing Species a t rhe Hg/H20 Interphase, Trans. Faraday SOC.,64, 1077-1092 (1968). (19F) Payne, R., “Specific Adsorption of Chloride Ions at the Hg/Aqueous Solution Interface,” ibid., pp 1638-1655. (20F) Sada E and Hiinmelblau D . M “Transport of Gases Through Insoluble Monolay&” A.I.Ch.E. J., 13, 8)60-865”(1967). (21F) Standart, G., “The Eflect of Surface Chemical Reactions on Interphase Mass and Energy Transfer,” Chem. Eng. Sci., 22, 1635-1662 (1967). (22F) Thomas, 1%‘. J., and Nicholl, E. McK., “An Optical Study of Interfacial Turbulence Occurring During the Absorption of Con Into Monoethanolamine,” tbid.. DD 1877-1878. (23F) Vidal, A , , and Acrivos, A,, “Eflect of Nonlinear Temperature Profiles on the Onset of Convecrion Driven by Surface Tension Gradients,” INn, ENG.CHEM., FUXDAM., 7, 53-58 (1968). (24F) Volgin, B. P., Efimova, T. F., and Gofman, M. S., “Absorption of Sulfur Dioxide by Ammonium Sulfite-Bisulfite Solution in a Venturi Scrubber,” Int.Chem. Engr., 8, 113-119 (1968). (25F) Weisz, P. B., and Zollinger, H., “Adsorption-Diffusion in Heterogeneous Systems. Part IV. Dyeing Rates in Organic Fibers,” Tranr. Faraday SOC., 64, 1693-1 700 (1968). , . I
PORE DIFFUSION IN SOLIDS (1G) Bischofl, K . B., “Eflectiveness Factors and Temperature Distributions for Catal st Particles in Non-Uniform Environments,” Chem. Eng. Sa.,23, 451-456
(10H) Pratt, H. R . C., “Countercurrent Separation Processes,” American Elsevier Publishing Co., New York, N . Y., 1967. (11H) Ross, S., “Chemistry and Physics of Interfaces,” IND.END.CHEM.,60 ( 9 ) , 12-13 (1968). (12H) Rowlinson, J. S., “Molecular Theories of Liquid and Mixtures,” ibid., 59 (121, 28-33 (1967). (13H) Satterfield, C. N., y d Cadle, P. J., ”Diffusion in Commercially Manufactured Pelleted Catalysts, INn. Exo. CHEM.,PROCESS DES.DEVELOP., 7, 256-260 (1968).
(14H) Sergeev G. T. “Heat and Mass Transfer in a Reacting Laminar Boundary Layer in the bresenie of Multi-Component Diffusion,” Irrt. Chem. Engr.? 8, 233-239
(1968). (15H) Standart, G., “The Second Law of Thermodynamics for Heterogeneous Flow Systems-111. Effect of the Conditions of Mechanical Equilibrium and Electroneurrality on Simultaneous Heat and Mass Transfer and the Prigogine Theorem,” Chem. Eng. Sci., 23, 279-285 (1968). (16H) Strauss, W., “Industrial Gas Cleaning,” Vol. 8, Pergamon Press, N e w York, IN. Y., 1967. (17H) Thomas, J. M., and Thomas W. J “Introduction to the Principles of Heterogeneous Catalysis,” Academi: Press,’kew York, N. Y., 1967. (18H) Vashist, P. N., and Beckmann R . B. “Liquid-Li uid Extraction,” I N n . END.C ~ ~ ~ . , 5 9 ( 1 1 ) , 7 1 -(1967) 7 9 anh 60(11j,43-51 ( 1 9 6 8 . (1 9H) Wakao, N.,and Fujishiro, S. “Discussions on Mass Transfer Coefficient,” Kaqaku K ~ g ~ k5,4-7 u, (1967) (Engl.’).
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(2G) Cadle, P. J., and Satterfield, C. N., “Uniformity of Diffusivirv in a Nickel Base Steam-H drocarbon Reforming Catalyst,” IND.ENC. CHEM.,’F u N n A M . , 7, 189-192 (1968r. (3G) Cadle, P. J., and Satterfield, C. I%., “Anisotropic Diffusivities in Pressed Boehmite Pellets,” zbzd., pp 192-197. (4G) Coughlin, R . \V., “A Heat Transfer Analogy for Diffusion and First-Order Chemical Reactionin a Catalyst Pore,” A2.Ch.E. J., 13,1031-1033 (1967). ( j G ) Foster, R . N., and Butt, J. B., “Some Surface Transport Effects o n Activity in Diffusionally Limited Catalytic Systems,” IND. END. CXEM.,FuNnAx., 6 , 481-488 (1967). , , (6G) Gclbi:, D. “The Surface Transport of Various Gases on a Platinum-Alumina Catalyst, Cheh. Ens. Sci., 23, 41-49 (1968). (7G) Gunn, 1s. J., “Diffusion and Chemical Reaction in Catalysis and Absorption,” zbzd., 22, 1439-1455 (1967). (81;) Gupta, V. P., and Douglas, M‘. J.. h?., “Diffusion and Chemical Reaction in Isobutylene Hydration Within Cation Exchange Resin,” A.I.Ch.E. J., 13, 883-889 (1967). (9G) Hudgins, R. R., “A General Criterion for .4bsence of Diffusion Control in a n Isothermal Catalyst Pellet,” Chem. Eng. Sci., 23, 93-94 (1968). (10G) Hudson, J. L., “Transient Multicomponent Diflusion with Heterogeneous Reaction,” A.1.Ch.E. J., 13, 961-964 (1967). (11G) Irving, J . P., and Butt, J. B., “An Experimental Study of the Effect of Intraparticle Temperature Gradients on Catalyric Acrivity,” Chem. Eng. Sci., 22, 18591873 (1967). (12G) Ishida, M., and Wen, C. Y., “Eflectiveness Factors and Instability in SolidGas Keactions,” zbid., 23, 125-137 (1968). (13G) Kasaoka, S., and Sakata, Y., “Effeciiveness Factors with Shape-Differences of Catalyst Particles,” Kugaku Kogaku, 5,24-28 (1967) (Engl.). (14G) Kasaoka, S., Sakata, Y., and Nitta, K . “Unsteady State Diffusion Within Porous Solid Particles,” J .Chem. E n g . Jnpon,’l, 32-37 (1968). (15G) Kawazoe, K., and Sugiyama, I., “On Effective Diffusivities inPorousSolids,” Kagaku Kognku, 5,151-154 (1967) (Engl.). (16G) Kim, B. W., “A Study on the Adsorptivity of Active Carbon,” J . Korean Inrt. Chem. Eng., 5,77-95 (1967). (17G) Levich, V.,,G., “Influence of External Diffusion Resistance on Process in Porous Catalyst, Doki. Akad. ??auk, S.S.S.R., 171, 406 (1966). (18G) Olson, J. H., “Rates of Poisoning in Fixed-Bed Reactors,” I N n . ENG,CHEM., FUNDAM., 7, 185-188 (1968). (19G) Petersen, E. E., “On the Use of Criteria for Determining Transport Limitations Within Heterogeneous Catalysts,” Chem. Eng. Sci.,23, 94-96 (1 968). (20G) Rimpel, A. E., Jr., Camp, D. T., Kostecki, J. A,, and Canjar, L. N., “Kinetics of Physical Adsorption of Propane from Helium on Fixed Beds of Activated Alumina,” A.2.Ch.E. J., 14, 19-24 (1968). (21G) Roberts, P. V., and York, R . “rldsorption of Narmal Paraffins f r o m Binary Liquid Solutions by 5a Molecula; Sieve Adsorbent, INn. ENG.CHEM.,PROCESS DES.DEVELOP., 6,516-525 (1967). (22G) Satteyfield, C. N., and Iino, H., “Surface Diffusionof Chemisorbed Hydrogen on Nickel, I N D EKG. . CHEM.,FENDAM., 7,214-218 (1968). (23G) Shendalman, L. H., “A Kinetic Theory of Catalysis and Mass Transfer in a Cylinder,” A.I.Ch.E. J . , 14, 599-605 (1968). (24G) Small, H., ”Chemical Modification of Crosslinked Polymers. New Approach to Synthesis of Ion Exchange and Chelating Resins,” IND.ENG.CHEM., Pnon. RES.DEVELOP., 6 , 147-150 (1967). (25G) Venuto, P. B., and Hamiiron, L. A., “Reverse Molecular-Size Selectivity and Aging I n a Zeolite-Catalyzed Alkylation,” ibid., pp 190-192. (26G) TVakao, N., and Fujiishiro, S., “Selectivity of Successive Reaction in Cylindrical Catalyst,” Kagaku Kogaku, 5 , 63-66 (1967) (Engl.).
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(81) Henley, E. J., and dos Santos, M. L., “Permeation of Vapors Through Polymers a t Low Temperature and Elevated Pressures,’’ A.I.Ch.E. J., 13, 1117-1119 (1967). (91) Hersh, L. S., “Ionic Membranes. I . Surface Sulfonic Acid Groups on Porous Glass: A Potentiometric Study,” J . Phys. Chem., 72, 2195-2199 (1 168). (101) Kaufmann, T. G., and Leonard, E. F., “AMechanismof Interfacial hiass Transfer in Membranc Transport,” ii.1.Ch.E. J., 14, 421-425 (1968). (111) Kaufmann, T. G., and Leonard, E. F., “Studies of Intramembrane Transport: A Phenomenological Approach,” ibid., pp 110-1 17. (121) Kimura, S., and Sourirajan, S., “Concentration Polarization Effects in Reverse Osmosis Using Porous Cellulose Acetate Membranes,” IND.E s c . Cmhl., PROCESS DES.DEVELOP., 7, 41-48 (1968). (131) Kimura, S., and Sourirajan, S., “Performance of Porous Cellulose Acetate Membranes During Extended Continuous Operation Under Pressure in the Reverse Osmosis Process Using Aqueous Solurions,” zbid., pp 197-206. (141) Kirsh, A . A,, and Fuks, N. A,, “Investigations of Fibrous Aerosol Filters Resistance of Systems of Parallel Cylinders,” Colloid J . U.S.S.R., 29, 504-507 (1967) (Engl.). (151) Kobatake, Y., Yuasa, M., and Fujita, H., “Studies of hlembrane Phenomena. VI. Further Study ofVolume Flow,” J . P h p . Chem.. 72, 1752-1757 (1968). (161) Kubica, J., Kucharski, M., and Stelmaszek, J., ”Separation of Liquid >fixtures by the Permeation Method. 111. Separation of Aqueous Solutions,” Int. Chem. Engr., 8 , 81-85 (1968). (171) Kucb,arski, M., and Stelmaszek, J., “Separation of Liquid Mixtures by Permeation, ibid., 7, 618-622 (1967). (181) Lakshminarayanaiah, N., and Subrahmanyan, V., “Current Dependence of H20 Transport in Cation-Exchange Membranes,” J. Phyr. Chem., 72, 12531258 (1968). (191) Lirt, M., and Smith, W. G., “Artificial Membranes: .4 New Type of Cell for Measuring Diffusion Resistance,”Science, 160, 201-202 (1968). (201) Nakano, Y., Tien, C.: and Gill: W. K.,“Nonlinear Convection Diffusion: A Hyperfiltration Application,” z1.I.Ch.E. J., 13, 1092-1098 (1967). (21I ) Piekaar, H . W.,and Clarenburg, L. A,, “Aerosol rilters-Pore Size Distribution in Fibrous Filters,” Chem. Eng. Sci., 22, 1399-1408 (1967). (221) Piekaar, H . W., and Clarenburg, L . A,, “Aerosol Filters-The Tortuosity Factor in Fibrous Filters,” ibid., pp 1817-1 827. (231) Shor, A. J., Kraus, K . A., Johnson, J. S., Jr., Cooney, J. L., and Rabe “Correspondence. Hyperfiltration. Comments and a Reply on Reference 231,” I E D . ENG.CHEM., FUNDAM., 7, 527-528 (1968). (241) Shor, A . J., Kraus,,K. A., Johnson, J. S., Jr., and Smith, W . T., Jr., “Hyperfiltration. Concentration Polarization in Tubular Systems with Dynamically Formed Membranes,” ibid., pp 44-48. (251) Shor, A. J., Kraus, K. A,, Smith, W . T., Jr., and Johnson, J. S . , Jr., “Hyperfiltration Studies. XI. Salt Rejection Properties of Dynamically Formed Hydrous Zirconium (IV) Oxid hlembranes,” J. Phys. Chem., 72, 2200-2206 (1968). (261) Sourirajan, S., and Kimura, S., “Correlations of the Reverse Osmosis Separation Data for the System Glycerol-water Using Porous Cellulase Acetate Membranes,“ IND.END.CHEM.,PROCESS DES.DEVELOP., 6 , 504-516 (1967). (271) Srinivasan, S., Tien, C., and Gill, W. N., “Simultaneous Developments of Velocity and Concentration Profiles in Reverse Osmosis Systems,” Chem. Eng. Sci., 22, 417-433 (1967). (281) Thomas, D . G., and Watson, J. S., “Hyperfiltration. Reduction of Concentration Polarization of Dynamically Formed Hyperfiltration Membranes by Detached Turbulence Promoters,” IND.END.CIIEM.,PROCESS DES.DEVELOP., 7, 397-401 (1968). (291) Yuasa, M . , Kobatake, Y., and Fujita, H., “Studies of Membrane Phenomena. V I I . Effective Charge Densities of Membranes,” J . Phys. Chem., 72, 2871-2876 (1968). (301) Zeh, D . H., and Gill, W. N., “Convection Diffusion in Stagnation Flow with a n Imperfect Semipermeable Interface,” A.I.Ck.E. J.,13, 1014-1016 (1967).
