bluuebunny/crossref_metadata_2025_split huggingface dataset:
Evolution of gas from liquids flowing through porous media
Authors: Hunt E. B. , Berry V. J. 
Published: June 2004

AbstractThe production of oil and gas by pressure depletion involves both the formation of bubbles and the diffusion of gas from the liquid phase into these bubbles. Studies were undertaken to outline in detail the process of bubble formation when the driving force is small. This work shows that the formation of bubbles is a random process which can, however, be described by a simple probability distribution function. Also, calculations have been made to determine how fast gas will diffuse into uniformly distributed gas bubbles.These results make it possible to describe the manner in which a gas phase is established during the pressure depletion process. In this process the rate of pressure decline is the most important factor influencing the total number of bubbles produced. Laboratory tests have substantiated the finding that in certain types of porous media the amount of oil recovered is sensitive to the number of bubbles formed.
Correlating kinetic data in reactors: Application to tertiary Butanol dehydration
Authors: Black J. H. , Wright J. H. , Coull James 
Published: June 2004

AbstractThe reactor‐unit concept proposed by Hurt is extended in this paper to include fractional‐order reactions and to show the effect of volume change on the system. Equations defining the reactor unit for homogeneous and heterogeneous reactions are derived.The catalytic dehydration of tertiary butanol was chosen as a means of studying the validity of the extended reactor‐unit concept. The experimental investigation was conducted over a wide range of flow rates, catalyst bed heights, and temperatures. The result of the application of this modified reactor‐unit expression to the correlation of the data was excellent.
Material transport in turbulent gas streams: Radial diffusion in a circular conduit
Authors: Lynn Scott , Corcoran W. H. , Sage B. H. 
Published: June 2004

AbstractExperimental studies of the mixing of coaxial streams of a natural gas and air at atmospheric pressure were made at Reynolds numbers of 44,000 and 79,000 under conditions where the turbulent‐velocity profile of nearly uniform flow was altered as little as feasible by the blending of the two streams.Total diffusivities of natural gas in air for the region near the center of the conduit were computed from the data for turbulent, steady, nonuniform flow. The total diffusivities were found to be rather complicated functions of the conditions of flow. Limitations in the configuration of the apparatus did not permit a study of the behavior of the total diffusivities to be made over as wide a range of flow rates as would be necessary to investigate the large‐scale trends indicated by this study.
Liquid‐liquid extraction in a pulsed perforated‐plate column
Authors: Li W. H. , Newton W. M. 
Published: June 2004

AbstractLiquid extractions of benzoic acid–toluene solutions by means of water were studied under varying flow rates of both solvents in a 2‐in. perforated‐plate column to which pulsations of different frequencies and amplitudes were applied. Studies on reversal of the phase of the dispersion were made. With fixed flow rates of both solvents, the rate of extraction increased much more rapidly when the flow through the perforation became turbulent. The results are correlated by means of Reynolds number based on the flow through the perforations and are calculated from the product of the frequency and amplitude of the pulsations.
Effect of concentration level on mass transfer rates
Authors: Westkaemper L. E. , White Robert R. 
Published: June 2004

AbstractCarbon tetrachloride was evaporated into a stream of air over ranges of gas concentration from 0 to 0.70 mole fraction carbon tetrachloride, Reynolds number from 600 to 15,000, and Schmidt number from 0.23 to 1.17. The data were correlated by an equation and also by a computer solution to the differential equation describing mass transfer from values of eddy viscosity and eddy diffusivity obtained from the literature.
Vapor‐liquid equilibria of nitrogenargon‐oxygen mixtures
Authors: Latimer R. E. 
Published: June 2004

AbstractThe equations and graphs presented here for the vapor‐liquid equilibrium of the nitrogen‐argon‐oxygen low‐temperature system are based on published binary and ternary experimental data involving mixtures of nitrogen, argon, and oxygen, and on careful thermodynamic study over a period of years of accurate plant‐performance data on tall, large air‐rectifying columns operating near the minimum reflux ratios. The plants have achieved separations that are impossible according to some of the published equilibrium data, and thus the plant data have made a major contribution toward the preparation of this paper.
Axial mixing of binary gas mixtures flowing in a random bed of spheres
Authors: McHenry K. W. , Wilhelm R. H. 
Published: June 2004

AbstractMeasurements are reported on axial mixing of binary gas mixtures at room temperature and atmospheric pressure in a random bed of spherical particles. By means of the Fick's Law equation for diffusion an axial Peclet number, dp U/Ez (where dp is particle diameter, U is interstitial velocity, and Ez is axial eddy diffusivity), was computed in terms of the ratio of the amplitudes of a sinusoidal concentration wave at the inlet and outlet of the bed. An experimental method was devised to eliminate end effects in the system. For the gas systems H2N2 and C2H4N2 and for Reynolds numbers between 100 and 400 the mean of twenty‐one determinations of axial Peclet number was 1.88 ± 0.15. This value is in excellent agreement with a value of 2.0 predicted theoretically on the assumption that the bed acts as a series of n perfect mixers, where n is the number of particles traversed between inlet and outlet.Axial diffusivity for turbulent flow of gases among particles is about sixfold larger than radial diffusivity, previously determined. It is suggested that axial diffusivity may not, perhaps, be neglected in contacting devices, such as adsorbers and catalytic reactors.
Heats of mixing of liquids
Authors: Schnaible H. W. , Van Ness H. C. , Smith J. M. 
Published: June 2004

AbstractExperimental data are presented for the heats of mixing of liquids at 25°C. and 1 atm. pressure for ten binary and five ternary systems. For nonpolar binary systems a two‐constant equation has been developed which correlates the data within experimental accuracy. Several equations which have been proposed for the calculation of ternary heats of mixing from binary data are tested for the systems studied. The method of Jost and Röck (4) for determining the constants in power‐series functions from experimental data is considered.
Densities of liquid‐acetone‐water solutions up to their normal boiling points
Authors: Thomas K. T. , McAllister R. A. 
Published: June 2004

AbstractThe densities of acetone‐water liquid solutions have been measured over the entire composition range from 20°C. to within 3° to 7°C. of the normal boiling point of the mixture. The density was measured with a Robertson pycnometer (13), which was modified slightly. The density values are thought to be accurate to within ±0.00005 density units. The technique for determining density values of the volatile mixture near the boiling temperature is given in some detail. The refractive index (nD25) of pure acetone has been redetermined and equals 1.35596 ± 0.00003.
A study of laminar‐flow heat transfer in tubes
Authors: Gross Joseph F. , Van Ness H. C. 
Published: June 2004

AbstractThe general problem of heat transfer to fluids in laminar flow in tubes is discussed, a new procedure for the measurement of local laminar‐flow heat transfer coefficients is described, and an empirical equation is presented for the correlation of data for local heat transfer rates to liquids flowing upward in laminar flow in vertical tubes under conditions of constant heat flux at the tube wall.
Ion exclusion equilibria in the system glycerol–sodium chloride–water–Dowex‐50
Authors: Shurts Edward L. , White Robert R. 
Published: June 2004

AbstractIon exclusion is an operation in which an ion exchange resin is used to separate an electrolyte from a nonelectrolyte in a polar solvent. An ion exchange resin tends to absorb a nonelectrolyte and to exclude an electrolyte. This is described quantitatively by the equilibrium distribution of the electrolyte, the nonelectrolyte, and the solvent between the resin phase and the liquid phase surrounding the resin.As no ternary distribution data applicable to ion exclusion are available, and only a few binary data have been published, a principal purpose of this investigation was to determine the distribution data for a typical system: glycerol‐sodium chloride‐water‐Dowex‐50.
Separation of liquids by thermal diffusion
Authors: Powers John E. , Wilke C. R. 
Published: June 2004

AbstractData were obtained in flat‐plate continuous‐flow thermogravitational columns to check the theory developed by Furry, Jones, and Onsaer and a modification of this theory proposed by the authors. Separations of ethyl alcohol–water and benzene–n‐heptane mixtures were measured, flow rate, column length, temperature difference, spacing between plates, and inclination of the plates being varied in the experiments. Theory and data are in qualitative agreement for the range of variables studied. Quantitative agreement exists between theory and experiment in the region of practical design for liquid‐thermal‐diffusion plants.Equations to aid in the design of thermal‐diffusion plants are developed, and a plant to treat 1,000 bbl./day of a liquid aromatic‐aliphatic mixture is designed and costs are estimated.
Radioisotope technique for the determination of flow characteristics in liquid‐liquid extraction columns
Authors: Markas S. E. , Beckmann R. B. 
Published: June 2004

AbstractA radioisotope technique has been utilized to study the point holdup of the dispersed phase and some operational flow characteristics in a packed countercurrent liquid‐liquid extraction tower. The system used was toluene‐water and the packing was Raschig rings. The toluene dispersed phase was tagged with gamma‐radiating iodine‐131.The study revealed that holdup experiences a hysteresis cycle with variations of the continuous‐phase flow rate. Correlating equations are presented for “total” and permanent holdup, below loading, to account for this hysteresis. Entrance effects and flow maldistribution effects are readily determined by the method utilized. Displacement studies demonstrated that no simple “operational” dispersed‐phase flow holdup exists, but rather a complex dispersed‐phase movement, which involves all the “nonhysteresis” permanent holdup.
Flow of steam‐water mixutures in a heated annulus and through orifices
Authors: Hoopes John W. 
Published: June 2004

AbstractValues of total pressure drop are presented for the flow of vaporizing water in an internally heated 1‐in. I.D. by 1½‐in. O.D. annulus at mass velocities of 270 to 1,440, lb./(sec.)(sq.ft.), pressures of 9 to 180 lb./sq. in., and up to 0.34 fraction by weight vaporized. The total heated length over which boiling took place was as large as 6 ft. There is no evidence of “sonic” pressure jumps at the outlet. The results for the annulus mentioned lie within +30 to −11% of the Lockhart‐Martinelli curve at higher qualities and with ±45% of the correlation at lower qualities where the actual quality is more uncertain. A simplified correlation in terms of quality and volume fraction of liquid predicted the two‐phase frictional pressure drops with an average error of 41%.It was found that the ratio of the two‐phase pressure drop through a 0.3‐in. orifice to the drop with no vaporization was approximately a linear function of the quality in thevena contractabut was only one tenth to one third as great as would be predicted if the mixture were to expand as a homogeneous fluid. Prediction of orifice presure drops is improved if slip between vapor and liquid is considered.
Mass transfer in a continuous‐flow mixing vessel
Authors: Humphrey D. W. , Van Ness H. C. 
Published: June 2004

AbstractMass transfer coefficients have been determined for the dissolution of Na2S2O3·5H2O crystals in water under conditions of turbulent agitation in a mixing vessel. The dissolution was carried out in a steady‐flow process in which the area of selt crystals and the concentration of the solution in the mixing vessel were constant during each run. A comparison is made with previously unpublished results for batch runs in a similar system, and a method is developed for calculating the surface area of salt particles suspended in the mixing vessel under steady‐flow conditions.
Ion exchange separation of gram quantities of americium from a kilogram of lanthanum
Authors: Armstrong D. E. , Asprey L. B. , Coleman J. S. , Keenan T. K. , LaMar L. E. , Penneman R. A. 
Published: June 2004

AbstractThe separation of 4.5 g. of americium from approximately a kilogram of light rare earths (primarily lanthanum) was achieved on a pilot plant scale by chromatographic displacement of the mixture from Dowex‐50 resin with 0.1% ammonium citrate at pH 8 into hydrogen‐form Dowex‐50. The americium collected into a narrow band and was eluted free from lanthanum but contained an equal weight of cerium. A 6‐ and a 2‐in.‐diam. column were used in tandem. Use of a final column with a much smaller diameter would have permitted a cleaner separation from cerium, but this was left for a laboratory‐scale separation by a different process. Precipitation, which was observed in the columns during the first runs, was later avoided entriely by use of high flow rates both initially and during the transfer between columns. No adverse effects were noted from ∼15 curies of alpha activity.
Effect of water vapor on the catalytic oxidation of nitric oxide
Authors: Kircher Omer , Hougen O. A. 
Published: June 2004

AbstractExtension of the kinetics of the catalytic oxidation of nitric oxide on activated carbon and silica gel confirms the rate‐controlling step postulated by previous workers. The effect of variables including water vapor on the reaction rate is expressed by an equation containing the constants a, b, c, and w, which have been evaluated for both catalysts at 30°, 45°, and 60°C. The effect of water vapor is to reduce the reaction by reversible adsorption on the active sites of the catalyst. The value of w is dependent on temperature but independent of water‐vapor concentration up to a relative humidity of 20%. Above 20% the value of w for activated carbon increases greatly with relative humidity, in agreement with the effect of capillary adsorption at high water contents.
Heat transfer coefficients for condensing organic vapors of pure components and binary mixtures
Authors: Pressburg Bernard S. , Todd James B. 
Published: June 2004

AbstractThe behavior of the film coefficient of heat transfer for the condensation of organic vapor mixtures was investigated experimentally to establish a satisfactory basis for applying the Nusselt equation to binary systems. Five ideal and nonideal pairs, all of which gave miscible condensates, were studied; the work was carried out under conditions of almost total condensation on a horizontal condensing surface designed to comply as rigidly as possible with the conditions for which Nusselt's equation is valid.The same behavior was observed for all systems and all concentrations studied: the experimental coefficients fell between those for the pure components and followed the behavior pattern for pure components when the temperature difference was taken as that between the bubble point of the condensate and the surface temperature, rather than between the dew point or the measured vapor temperature and the surface temperature, Correlation of the film coefficient showed it to vary approximately linearly with composition if the coefficients were compared at a constant value of the temperature difference, defined as above. This permits determination of the coefficient for a mixture by interpolation between the coefficients for the pure components, which are easily obtained, in preference to making the calculations with the properties of the mixture obtained by laborious and uncertain weighting of the corresponding properties of the pure components.When results are interpreted in the light of the theories of Colburn and Drew, the presence of a vapor‐phase resistance to heat and mass transfer, as postulated by them, is indicated.
Two‐phase, steam‐water critical flow
Authors: Isbin H. S. , Moy J. E. , Da Cruz A. J. R. 
Published: June 2004

AbstractTwo‐phase critical flow of steam‐water mixtures has been investigated over a pressure range from 4 to 43 1b./sq.in. abs. and a quality range from saturated vapor to 1% (weight) vapor. Discharges were measured from 1/4‐,1/2‐, 3/4‐, and 1‐in. pipes and from annuli of intermediate cross‐sectional areas. The experimental mass flow rates are always grteater than the values calculated on the basis of a homogeneous flow model. Several empirical methods for correlating the data were determined, and comparisons are presented of the predictions of several analytical flow models.
Behavior of suspended particles in a turbulent fluid
Authors: Friedlander S. K. 
Published: June 2004

AbstractHeat and mass transfer and coagulation are considered as related to the mean‐square relative velocity between particle and fluid uR2 and eddy diffusion as described by the mean‐square particle displacement, Xp2. The mathematical methods used are similar to those employed in the early calculations of the Brownian motion.The mean‐square relative velocity is obtained as a function of particle characteristics, intensity of turbulence, and a fluid correlation coefficient. In the limiting case of equal particle and fluid density uR2 = 0, and for very heavy particles uR2 → uF2.A general expression for the eddy diffusivity is obtained is obtained which reduces to the same form as that of the fluid for the stationary state. However, the correlation coefficient to be used in the calculations depends on uR2. As a first approximation, it can be assumed that at a sufficiently long time from the introduction of the particles, fluid and particle diffusivities are equal.For short times after injection, the particle spread may be much less than that of the fluid. An illustrative calculation for the initial spreading of a jet of suspended particles is offered. In all cases an effort is made to organize the available experimental data within the framework of the theory.
Determination of the chemical properties of an oxide catalyst in a closed system
Authors: Holland C. D. , Murdoch P. G. 
Published: June 2004

AbstractThe bulk chemical properties of an impregnated chromia‐alumina catalyst with respect to several gases, CO, CO2, C3H6, were determined as a function of the degree of oxidation of the surface of the catalyst. The importance of the results lies in the demonstration that a simple method described herein can be used to obtain significant data on catalytic surfaces. Briefly, the prior adsorption of oxygen by the catalyst tended to promote the adsorption of carbon monoxide and to prohibit the adsorption of carbon dioxide. Far more carbon monoxide was adsorbed by the highly oxidized surface than could be accounted for on the basis of adsorbed carbon dioxide. The quantity of propylene adsorbed also increased with an increase in the oxidation of the surface. The results are explained on the basis of two types of adsorbed oxygen atoms.
Effects of bubbling and stirring on mass transfer coefficients in liquids
Authors: Johnson D. L. , Saito Hirotaro , Polejes J. D. , Hougen O. A. 
Published: June 2004

AbstractIn the hydrogenation of α‐methylstyrene by means of a suspended palladium‐alumina catalyst in a stirred reactor the mass transfer of hydrogen through the liquid is the rate‐controlling step and the resistance to chemical reaction at the catalyst surface is negligible except at extremely rapid rates of stirring. This system therefore provides an excellent means of establishing the effects of operating variables and mechanical construction on mass transfer coefficients in liquids in stirred reactors. It is convenient to consider the total resistance to mass transfer as consisting of two separate resistaces: in the liquid adjoining the bubbles and in the liquid adjoining the suspended solid particles; thus R = Rb + Rs.A general equation was evaluated from experimental data based upon unit volume of liquid.
Effect of liquid physical properties and flow rates on the surface area of sprays from a pressure atomizer
Authors: Consiglio J. A. , Sliepcevich C. M. 
Published: June 2004

AbstractThe effects of the physical properties and volume flow rate of liquids on the surface area of sprays produced by a pressure type of atomizing nozzle were determined experimentally. the specific surface area of the sprays is correlated by an equation of two dimensionless groups in terms of the variables surface tension to the −1.0 power, kinematic viscosity to the −0.4 power, and volume flow rate to the 2.4 power. The volume flow rate is correlated by an equation of two dimensionless groups containing the variables viscosity to the 0.17 power, density to the −0.58 power, and spray pressure to the 0.42 power. The conversion of compression energy to surface‐area energy appears to be constant at approximately 0.1%.
Kinetics of aldehyde hydrogenation: Vapor‐phase flow system and supported nickel catalyst
Authors: Oldenburg C. C. , Rase Howard F. 
Published: June 2004

AbstractA kinetic study of the catalytic vapor‐phase hydrogenation of three aldehydes (acetaldehyde, propionaldehyde, and n‐butyraldehyde) was made at low conversions with a commercial supported nickel catalyst. A simple initial rate equation was determined and found to agree with a mechanism suggested by the ideal kinetics of Hougen and known experimental evidence. By means of this equation the relative reactivities of the aldehydes were compared and found to agree with the predictions of organic theory. An improved reactor designed to ensure isothermal operation is described.
Continuous‐flow stirred tank reactors: Solid‐liquid systems
Authors: Mattern R. V. , Bilous Olegh , Piret Edgar L. 
Published: June 2004

AbstractThe theory and design of continuous stirred tank reactors are extended to the complex but industrially important field of continuous‐heterogeneous‐reaction systems. The present investigation is concerned with the elementary process occurring when solid particles and a liquid flow into and from a single reactor or a chain of these reactors. The equations are developed for dissolution processes, and the theoretical size distributions and specific areas are confirmed experimentally. Performance is also related to operating conditions and reactor design.
Control of flow distribution by mixing headers
Authors: Hyman Seymour C. , Gruber Alan R. , Joseph Leon 
Published: June 2004

AbstractThe coolant flow distribution among parallel passages in a nuclear reactor (or boiler or heat exchanger) can be very sensitive to variations in heat input, channel dimensions, etc. In a previous paper this flow sensitivity was defined in terms of certain partial derivatives, which were related by analytical expressions to fluid properties and operating characteristics. Flow sensitivity contributes largely to potential malfunction, reduced efficiency, or failures. The use of valves and orifices was quantitatively evaluated for supercritical water in the earlier paper. The scope of this paper is to consider the utility of mixing headers. These mixing chambers are located along the flow passage as a common receiver for parallel flow from many channels. The headers, in turn, supply subsequent lengths of heated passages in parallel. Analytical expressions are derived for the effect of headers on flow, outlet‐fluid enthalpy, and channel‐wall temperatures. The limiting cases of minimum and complete mixing in the headers are considered and numerical results for water at supercritical pressures are given to show the marked increase in stability obtained by use of intermediate mixing headers.