Mass transfer rates between oil slicks and water

The results of a laboratory wind-wave tank study are reported in which the rate of mass transfer of a tracer (phenol) from a synthetic oil slick to the underlying water was measured at wind speeds from 0 to 9 m/s. Estimates were made of the mass transfer coefficients in the oil and water phases at the oil-water interface. The results indicate that the rate of hydrocarbon dissolution from a slick is controlled by the water phase mass transfer coefficient which is usually less than 1 cm/h. Whereas mass transfer coefficients at air-water interfaces show a marked increase at wind speeds of approximately 3 m/s due to wave formation, when oil is present its damping effect delays this transition to approximately 7 m/s. It can be inferred that (i) dissolution is considerably slower than evaporation for reasonably volatile compounds, (ii) dissolution will have a negligible effect on slick composition, (iii) the concentrations of soluble hydrocarbons established in the water column under the slick by direct dissolution are small and unlikely to result in significant toxicity, and (iv) that the dominant mechanism of transfer of soluble hydrocarbons into the water column is probably from dissolution of dispersed oil particles.     

Characterization of the evaporation rates of complex hydrocarbon mixtures under environmental conditions

The characterization of the evaporation rate of complex hydrocarbon mixtures, such as commercial oil fractions, under environmental conditions is discussed. It is shown that the relevant thermodynamic quantity is the total volume of vapour (per unit of initial oil mass) removed under isothermal differential distillation conditions (V m³/kg) as a function of the mass fraction of the oil remaining (F). Plots of F versus V for various isothermal conditions can be used to estimate evaporation rates since it is shown that V is equivalent to the group K_sA_sτ_s/Ms where K_s is the evaporation mass transfer coefficient (m/s), A_s is the spill area (m²), τ_s is the evaporation time (s) and M_s is the spill mass (kg). The basis of a methodology for estimating environmental evaporation rates is thus outlined. Methods of obtaining V versus F data are discussed, with calibrated wind tunnel evaporations being preferred. The estimation of evaporation rates under spreading and non-isothermal conditions and the analogous dissolution process are discussed briefly.     

Microbial uptake of diesel oil sorbed on soil and oil spill clean‐up sorbents

Sorbent effects in the microbial uptake of diesel oil were determined for black cotton soil (BCS) and two oil spill clean‐up sorbents, ie peat sorb and spill sorb. Biodegradation studies were conducted in mass transfer limited batch slurry microcosms using microorganisms capable of direct interfacial uptake of diesel oil. Under identical loading conditions, the amounts of diesel oil initially loaded on the various sorbents were 178, 288 and 649 mg g^?1 for BCS, spill sorb and peat sorb, respectively. Total biodegradation of sorbed diesel was comparable for all the sorbents (45–52 mg), however, the biodegradation rates were significantly different. Peat sorb demonstrated a distinct initial lag phase, the biodegradation rate in spill sorb was initially slower, whereas biodegradation at a high rate commenced immediately for BCS. The maximum biodegradation rates observed for BCS, spill sorb and peat sorb microcosms were 7.9, 5, and 2.9 mg day^?1, respectively. Thus, the maximum biodegradation rate increased as the diesel oil loading decreased. Our results indicate that spill clean‐up sorbents have greater bioavailability limitations compared with soils and this is linked with their significantly higher loading capacity and internal porosity. Copyright © 2005 Society of Chemical Industry     

Influence of unsteady mass transfer on dynamics of rising and sinking droplet in water: Experimental and CFD study

Experimental and numerical investigations were conducted to study the effect of unsteady mass transfer on the dynamics of an organic droplet released in quiescent water. The situation is important and relevant to deep sea oil spill scenario. The droplet contains two components, one is heavier (immiscible) than water and other is lighter (miscible). When released, with an initial mixture density (890–975 kg/m³) lower than that of surrounding water, droplet rises in the column. The mass transfer of lighter solute component into water causes the droplet density to increase and droplet sinks when the density exceeds that of water. A mass‐transfer correlation accounting for the loss of the solute, based on Reynolds, Grashoff, and Schmidt numbers was developed. A two‐dimensional axisymmetric Computational Fluid Dynamics (CFD) model accounting for species transport was developed to emulate the experimental observations. The study also helped in identifying dominant mass‐transfer mechanisms during different stages of droplet motion. © 2014 American Institute of Chemical Engineers AIChE J, 61: 342–354, 2015     

A fundamental wax deposition model for water‐in‐oil dispersed flows in subsea pipelines

Water‐in‐oil dispersions frequently form in subsea oil pipeline transportation and their presence affects the wax deposition rate in subsea pipelines. A fundamental model for wax deposition on the wall of water‐in‐oil dispersed phase flow pipelines has not been developed. Dispersed water droplets can affect the heat and mass transfer characteristics of wax deposition and alter the deposit growth rate. In this study, wax deposition from water‐in‐oil dispersed flows is comprehensively modeled using first principles of heat and mass transfer. The role of the dispersed water phase on the heat and mass transfer aspects of wax deposition is analyzed. The developed model predicts different effects of the water volume fraction and droplet size on the wax deposition rates in laboratory flow loop experiments and in field scale wax deposition processes. © 2017 American Institute of Chemical Engineers AIChE J, 63: 4201–4213, 2017     

Evaporation of Pure Droplets in the Convective Regime Under High Mass Flux

An analytical expression analogous to the D² law was introduced, based on a mass transfer consideration, to describe the evaporation of pure droplets in the convective regime based on the Ranz-Marshall-type correlation for the Sh number. Comparison was made to single droplet drying experiments of pure water. It was found that the effect of mass transfer coefficient depression is significant under the high mass flux condition from the droplet. An expression was obtained to approximate the total time required for complete evaporation of a pure droplet. This expression can be used as a quick computation tool for more fundamental studies on droplet evaporation under controlled ambient conditions.     

Improvement of heat removal in solid‐state fermentation tray bioreactors by forced air convection

BACKGROUND: Heat removal is one of the major constraints in large‐scale solid‐state fermentation (SSF) processes. The effect of internal air circulation by forced convection on heat and water transfer has not been studied in SSF tray bioreactors. Formulation of a mathematical model for SSF requires a good estimation of the mass and heat transfer coefficients. RESULTS: A stainless steel tray bioreactor (80.6 L capacity) was used. Aspergillus niger C28B25 was cultivated under SSF conditions on an inert support. Temperature, moisture content, biomass and substrate concentrations were measured. Water and energy integral balances were used to estimate the heat and mass transfer coefficients involved in the process. The Reynolds number (N_Re) in the headspace of the tray bioreactor ranged from 2.5 to 2839, which increased the global heat transfer coefficient from 4.2 to 6.9 (W m^?2 K^?1) and the mass transfer coefficient from 1.0 to 2.1 (g m^?2 s^?1). Mathematical model predictions of the temperature and moisture content of the fermentation bed showed a high goodness‐of‐fit with the experimental results. CONCLUSIONS: This is the first report describing the effect of N_Re of air in the headspace of a SSF tray bioreactor on the heat and mass transfer coefficients and temperature regulation in SSF. Copyright © 2011 Society of Chemical Industry     

Characterization of isotherms and thin-layer drying of red kidney beans,Part II: Three-dimensional finite element models to estimate transient mass and heat transfer coefficients and water diffusivity

Three-dimensional finite element models with consideration of shrinkage and irregular shape were developed to estimate the relationships among the transient heat and mass transfer coefficients, the transient water diffusivity, and the temperature and moisture content of the red kidney beans being dried under different drying conditions. An equation was developed to calculate the transient mass transfer coefficient using the measured time–moisture content data. This calculated transient mass transfer coefficient was further used to calculate the transient heat transfer coefficient. To verify the predicted temperature on the surface of the red kidney beans, surface temperature was measured using a handhold infrared thermometer. These measured temperature and time–moisture content data were used to determine the transient water diffusivity using the least square method when the red kidney bean kernel experienced a shrinkage during drying. Strong relationship among the transient heat and mass transfer coefficients, the water diffusivity, and the ratio of the transient heat and mass transfer coefficients was revealed. This relationship could be used to predict temperature and moisture content of the red kidney beans during the entire drying period. The Lewis number?=?27, and the ratio of the transient heat over mass transfer coefficients was 10765?J?m^?3?k^?1 at 30 and 40°C, and 10729?J?m^?3?k^?1 at 50°C. Shrinkage did not significantly influence the value of the estimated transient water diffusivity.     

Effect of Chemical Reaction and Mass Transfer on Ozonation of the Azo Dyes Reactive Black 5 and Reactive Orange 96

Ozonation of wastewater containing azo dye has been studied to evaluate the enhancement of ozone mass transfer from O₂O₃ gas into water with the presence of chemical reactions in a bubble column reactor. Experiments were performed at different initial dye concentrations and at various gas flow rates. C.I. Reactive Black 5 (RB 5) and C.I. Reactive Orange 96 (RO 96) have been chosen as representative model substances being found in wastewater from textile-finishing wastewater. Results show that the rate of ozone mass transfer increases with increasing initial dye concentration and gas flow rate. Consequently, an enhancement factor E for ozone mass transfer with chemical reaction could be calculated which increases with dye concentration. The chemical reaction between ozone and dye enhanced the mass transfer within the liquid film of the gas liquid boundary. The greatest enhancement factor for wastewater containing RO 96 of 2050 mgL^?1 is E = 15.4 compared with E = 9.1 for RB 5 of 3800 mgL^?1, both for gas flow rates of 19 Lh^?1. For lower gas flow rates, higher enhancement factors were observed, particularly for RO 96.     

超临界压力水在垂直上升内螺纹管中的传热特性

在压力22.5～30 MPa,质量流速430～1200 kg·m^-2·s^-1,内壁热负荷284～719 kW·m^-2范围内,对超临界压力水在均匀加热垂直上升内螺纹管内的传热特性进行了实验研究,得到了内螺纹管内超临界压力水的传热特性,分析了压力、热负荷和质量流速变化对内螺纹管壁温及传热系数的影响,探讨了拟临界区的传热机理,并给出了能用于工程实际的传热实验关联式。实验结果表明：垂直上升内螺纹管中超临界水具有良好的传热特性。在低焓值区内螺纹管壁温随焓增平缓增加,而在高焓值区壁温随焓增的升高明显。由于热物性的剧烈变化,超临界水在拟临界焓值区发生了明显的传热强化。压力与热负荷的增大以及质量流速的减小均会导致内螺纹管壁温的升高和传热系数的减小,使得传热强化现象削弱,甚至出现传热恶化。     

Heat and Mass Transfer at the Wall of a Square Mechanically Stirred Gas-Liquid-Solid Catalytic Reactor

Wall mass and heat transfer rates in a square gas-sparged, mechanically stirred reactor were measured by the electrochemical technique under the effect of various geometrical and hydrodynamic variables. For the 45° impeller, the mass transfer data fit the equation Sh = 0.7Sc^0.33Re^0.2Re_g^0.5 with an average deviation of ±6.9 %. For the 90° impeller, the data fit the equation Sh = 0.95Sc^0.33Re^0.14Re_g^0.53 with an average deviation of ±7.5 %. Gas sparging enhanced the wall mass transfer rates by factors of up to 2.61 and 3 for the 90° and 45° impellers, respectively, with a significant decrease in the total power consumption. The contribution of the present results to the operation of multiphase mechanically agitated vessels in different aspects is outlined.     

Mass Transfer of Ozone Using a Microporous Diffuser Reactor System

An ozone reactor was constructed using a tubular gas diffuser made of microporous stainless steel to significantly reduce gas bubble size and increase overall mass transfer area. Overall mass transfer coefficient, K_La [s ^?1], was correlated with gas (G) and liquid (L) flow rates using K_La = AL^αG^β , with A = 3.96 × 10 ⁸ [s^?1], α = 1.53, and β = 0.40, with L and G in [m ³s^?1]. The reactor is essentially plug flow at high G or L. This system achieves one of the highest ozone mass transfer rates observed in the literature.     

Experimental research on convection–condensation heat transfer characteristics and sootblowing operation strategy of waste heat recovery heat exchanger for dryer exhaust

Abstract

In this study, air/water vapor mixture with ash particles was used to simulate actual dryer exhaust gas. An experimental study of the convection–condensation heat transfer characteristics of air/vapor mixtures with ash particles across horizontal tube-bundles was conducted under various water vapor mass fractions and concentrations of ash particles. The variation of convection–condensation heat transfer coefficient with time presented four different types, as follows: almost did not change with time; decreased first, then reached stable values; decreased continuously in the experimental time; and decreased rapidly, decreased slowly, and decreased rapidly, with potential to increase again. In general, the convection–condensation heat transfer coefficient decreased with increasing concentration of ash particles and increased with increasing water vapor mass fraction. The reducing effect on the convection–condensation heat transfer coefficient by ash deposition would be weakened by increasing the water vapor mass fraction, but the heat exchanger would be blocked further easily by increasing the concentration of ash particles. Then, a distribution diagram was drawn to present different types of convection–condensation heat transfer curves under various working parameters. Sootblowing operation strategies were proposed under different working conditions to provide reference for the actual operation of the waste heat recovery heat exchanger for dryer exhaust.     

Effect of pitch-to-diameter ratio on the natural convection heat transfer of two vertically aligned horizontal cylinders

Natural convection heat transfer experiments were conducted for two parallel horizontal cylinders using various pitch-to-diameter ratios (P/D) from 1.02 to 9 for the Prandtl numbers between 2014 and 8334 and Rayleigh numbers between 7.3×10⁷ and 4.5×10¹⁰. Based upon analogy concept, mass transfer rate were measured instead of heat transfer rates by measuring the limiting current of the cathodic deposition of copper from acidified copper sulfate solution. The mass transfer rates for the lower cylinders were unaffected by the presence of the upper cylinders, and agreed well with the prediction from existing heat transfer correlations developed from a single horizontal cylinder. The Nusselt number ratios of the upper to lower cylinders increased with P/D. The ratios were less than 1 at P/D values less than about 1.5 for laminar flows, but the ratios were almost 1 at a P/D very close to 1 for turbulent flows. The variation of the ratios with P/D becomes steep with higher Prandtl numbers, which is confirmed by numerical simulations using the FLUENT program. The plating pattern that appeared on the surface of the cylinder revealed local mixed convection heat transfer. The area covered by thin lines, denoting the flow separation on top of the upper cylinder, increased for laminar but decreased for turbulent flow due to the laminarization phenomena in turbulent mixed convection.     

Heat transfer in co-current vertical two-phase flow

Heat transfer in co-current two-phase upflow and downflow of air–water has been investigated in a 25.8 mm electrically heated vertical pipe at 172.3 kPa for water mass velocities of 54 to 172 kg/m²s and gas flow rates of 0 to 1.322 × 10⁻² m³/s. It was found that although the injection of air in the liquid flow increased the two-phase heat transfer coefficients significantly for both systems, upflow coefficients were generally higher than those for downflow for the same liquid flow rate. This could have important implications in the design of some chemical reactors and heat engineering processes. Changes in heat transfer rates were found to occur at the flow pattern transition boundaries. Two-phase heat transfer coefficients were well correlated by an expression based on dimensional analysis for both upflow and downflow.     

Heat and Mass Transfer in Fry Drying of Wood

This article describes the coupled heat and mass (water, oil) transport phenomena in parallelepiped samples of beech (Fagus sylvatica) fried in peanut oil between 120 and 180°C. The aim was to evaluate the suitability of simultaneous fry drying and oil impregnation as an alternative wood treatment process. Water loss and oil impregnation were continuously assessed during the process. Temperature and pressure were measured at the center of the sample. The water in the peripheral layers of the wood vaporizes at atmospheric pressure. The water at the center of the wood vaporizes at overpressures of the order of 2.8 × 10⁵ Pa. High fluxes of water were recorded of about 0.006 kg/(m²s). The impregnated oil can amount to 20% of the mass of the removed water.     

Dispersion and Mass Transfer Effects on the Performance of an Immobilized Lipase Packed Bed Reactor During the Hydrolysis of Rice Bran Oil

The performance of an immobilized packed bed reactor for the hydrolysis of rice bran oil has been investigated and can be well described by a dispersion model with an average standard deviation of 0.0388. Global mass transfer coefficients estimated using the model and experimental data ranged from 0.095‐0.482 min^?1, depending on substrate flow rates. A dimensionless mass transfer correlation between the Sherwood number and the Reynolds number was obtained as NSh = 3.96 ×NRe^2.07.     

Mixed convection heat and Mass transfer in a vertical channel with film evaporation

Numerical results are presented for effects of latent heat transport associated with film vaporization on laminar mixed convection heat and mass transfer in a vertical channel with a half channel width b = 0.01 m. The influences of the inlet liquid mass flowrate and wall temperature on the film vaporization and the associated heat and mass transfer characteristics are examined for air-water and air-ethanol systems with gas Reynolds number Re_g = 2000. Predicted results obtained by including transport in the liquid film are contrasted with those where liquid film transport is neglected, showing that the assumption of an extremely thin film made in Lin et al. (1988) and Yan and Lin (1989) is only valid for systems having small liquid mass flow rates. Additionally, it is found that the interfacial heat flux is predominantly determined by latent heat transfer connected with film evaporation.     

Studies on the liquid-liquid interfacial mass transfer process using holographic interferometry

This paper aims at the interfacial phenomena of liquid-liquid mass transfer and its characteristic. By using the real-time holographic technique, the concentration distributions on the aqueous side were obtained according to holographic diagrams of mass transfer of ethanol through the interface of oil and water at different initial concentrations. Furthermore, the concentrations near the interface and the mass transfer coefficients were attained. A correlation of concentration near the interface to the concentration of the solute in the oil side was proposed. An approach of interfacial energy with solute concentration was established, and the calculated results are at good agreement with the experimental data. It is indicated that the liquid-liquid mass transfer process is approximately in accordance with two-film theory, the interfacial performance may be changed by the addition of the solute, and the interface of liquid-liquid is nonequilibrium thermodynamically during the mass transfer process. __________ Translated from Chemical Engineering (China), 2007, 35(6): 1–3 [译自: 化学工程]     

Numerical simulation of CO2 absorption into aqueous methyldiethanolamine solutions

The CO₂ absorption rate into aqueous N-methyldiethanolamine solutions was measured using a stirred cell with a flat gas-liquid interface. The measurements were performed in the temperature range of 293.15 to 333.15 K for various amine concentrations and CO₂ partial pressures. A numerical model of mass-transfer with complex chemical reactions based on the film theory was developed to interpret the experimental results. The model predictions have been found to be in good agreement with the experimental values of CO₂ absorption rates. A comparison is made between the enhancement factor predicted from the detailed model and the approximate solution of mass transfer equations with chemical reaction. The numerical results indicate that under the present experimental conditions, the effect of the reaction between CO₂ and OH^? on the observed mass transfer rates is negligible. The detailed mass transfer model was used for simulating the CO₂ absorption process in terms of the enhancement factor under a variety of operating conditions.