Particle-fluid heat transfer and dispersion in fluidised beds

The dynamic response of a gas fluidised bed has been measured for a range of particle sizes of lead glass ballotini and a range of particle Reynolds numbers. A dispersion model has been formulated that includes the effects of gas and particle mixing, fluid-to-particle heat transfer and intraparticle thermal conductivity, and the dynamic thermal response in theory has been found by solving the partial differential equations in the Laplace transform domain. The coefficient of thermal dispersion, the particle-to-fluid heat transfer coefficient and the intraparticle thermal conductivity have been found for the experimental response by non-linear regression. The coefficient of axial dispersion was found to be large and the particle to fluid heat transfer coefficients agreed with an established correlation for fixed and fluidised beds. The intraparticle thermal conductivity agreed with literature values for lead glass, the estimates showed no trend with flowrate, and the standard deviation of the estimate was three times smaller than the deviation found from similar experiments in fixed beds.     

Thermal dispersion and wall heat transfer in packed beds

A new analysis showing the effect of axial and radial thermal dispersion and wall thermal resistance upon heat transfer to fixed beds of solids is presented. By application of this theory and non-linear regression, coefficients of axial and radial dispersion and wall heat transfer coefficients are calculated from experimental measurements of radial temperature profiles in fixed beds heated at the wall.The experiments have been performed for beds packed with glass and with metallic particles within the particle Reynolds number range from 1 to 400.The calculated coefficients are compared with experimental values reported by other workers. Some differences are attributed to the neglect of axial dispersion in the work of others, but other differences are significant in that, for example, thermal characteristics of fixed beds of metallic particles differ from those of non-metallic particles.     

Packed bed thermal dispersion models and consistent sets of coefficients

Previous experimental and theoretical work has shown that the numerous one- and two-phase packed bed dispersion models can be regarded to be equivalent in describing important aspects of fixed bed behaviour. This paper is concerned with the problem of how thermal model coefficients for any other model are obtained if a set of reliable coefficients is known for one particular model from experimental results.The results of this analysis agree with observations made during the past decades that the Nusselt numbers are particularly sensitive to small changes of the axial dispersion coefficients and that—depending on the model—they differ considerably. While this is the case for the range of lower Reynolds numbers (say Re < 200), the models converge at high Reynolds numbers since dispersion effects become increasingly negligible. At very low Reynolds numbers (Re < 10), packed beds are dominated by the effective quiescent conductivity.     

Measurements of particle-to-gas heat transfer coefficients from one-shot thermal responses in packed beds

By applying the technique of one-shot thermal input, particle-to-gas heat transfer coefficients have been obtained for glass beads-air system in the range of Reynolds number from 5 to 229. The obtained heat transfer coefficients are well represented by a correlation, eqn (14), proposed by Wakao et al. Sensitivity test on the experimental results shows that at low flow rates the particle-to-gas heat transfer cannot be a controlling step in the overall heat transfer process.     

Forced convection in cross flow of power law fluids over a tube bank

The forced convective heat transfer characteristics for incompressible power-law fluids past a bundle of circular cylinders have been investigated numerically. The cylinder-to-cylinder hydrodynamic interactions have been approximated via a simple cell model. The momentum and energy equations have been solved using a finite difference based numerical method for a range of physical and kinematic conditions. The role of the two commonly used thermal boundary conditions, namely, constant temperature or constant heat flux, on heat transfer characteristics has also been studied. Extensive numerical results elucidating the effect of shear-thinning viscosity on the values of Nusselt number have been obtained for Peclet numbers ranging from 1 to 5000, Reynolds number in the range 1-500, flow behaviour index 1?n?0.5 and three values of voidages, namely, 0.4, 0.5 and 0.6, typical of tubular heat exchangers and tube banks. Under all conditions, varying levels of enhancement in Nusselt number are observed due to shear-thinning behaviour. The surface averaged Nusselt number shows strong dependence on the values of voidage, power-law index, Reynolds and Peclet numbers. The paper is concluded by presenting comparisons with the scant experimental results available in the literature.     

空气横掠波纹管束的流动与传热性能

引　言管壳式换热器是石油化工行业应用十分广泛的换热设备 ,它具有易于制造、耐压高等特点 .但是普通管壳式换热器换热效率低 ,因此开发高效传热元件对管壳式换热器的进一步推广应用具有十分重要的意义 .采用翅片管换热器可以大大强化换热 ,但是阻力也增加很多 ,并且容易积垢 ,影响使用 .近年来开发的波纹管换热器由于加工方便、易于制造而越来越受到人们的重视[1～ 4 ] .但对于流体横掠波纹管束时流动传热性能的研究却少见报道 .本文对如图 1所示的波纹管束组成的换热器进行了实验测定 ,研究了 3种排数的阻力与换热规律 ,为设计换热器提供…     

Experimental laminar falling film heat transfer coefficients on a large diameter horizontal tube

A test rig was designed and fabricated to measure local heat transfer coefficients from a large-diameter, steam-heated horizontal tube to thin falling films of water. The results of the experiments generally support the theory developed by Rogers for laminar film conditions, which were found to persist up to film Reynolds numbers of about 2000. Agreement between theoretical predictions of heat transfer coefficients and the measured values is reasonable for the thermal boundary layer development region, but measured values are about 20% lower than predicted values in the developed region. The lower values in the developed region are attributed mainly to measured film thicknesses being greater than predicted values.     

振动流化床与浸没水平管平均传热特性理论分析与实验研究

在二维流化床(240mm×80mm)中,以平均粒径dp为1.83mm的玻璃珠为物料,研究了振动流化床与浸没水平管间传热规律;考察了流化数、振动频率、床高、水平管管径等因素对平均传热系数的影响。采用自制探头对浸没加热管束和振动流化床层间平均传热系数进行实验测定,利用颗粒团模型,建立了振动流化床层与浸没水平管间平均传热模型,并对平均传热系数的理论预测值与实验测定值进行了比较。结果表明:计算值与实验值吻合较好,误差在±15%范围内。在较高流化数、低振动频率时,实验值处于理论值上方;随着振动频率、管径增大,平均传热系数实验值逐渐趋于理论预测值甚至低于理论预测值。结果可为带浸没水平管的振动流化床设计和研究提供参考。     

Accuracy enhancement of thermal dispersion model in prediction of convective heat transfer for nanofluids considering the effects of particle migration

A thermal dispersion model is utilized for simulation of convective heat transfer of water-TiO₂ nanofluid for laminar flow in circular tube. Concentration distribution at cross section of the tube was obtained considering the effects of particle migration, and this concentration distribution was applied in the numerical solution. Numerical solution was done at Reynolds numbers of 500 to 2000 and mean concentrations of 0.5 to 3%. Meanwhile, an experimental study was conducted to investigate the accuracy of the results obtained from the numerical solution. Non-uniformity of the concentration distribution increases with raising mean concentration and Reynolds number. Thereby, for mean concentration of 3%, at Reynolds numbers of 500 and 2000, the concentration from wall to center of the tube increases 2.6 and 30.9%, respectively. In the dispersion model, application of non-uniform concentration distribution improves the accuracy in prediction of the convective heat transfer coefficient in comparison with applying uniform concentration.     

Pellet heat transfer coefficients in packed beds: Global and local values

Pellet heat transfer coefficients in a packed bed have been obtained, both for specific individual pellets and for the entire bed. They are referred to as local and global values, respectively. It appears that the local values are scattered around the global value. This is due to the heat transfer coefficient of individual pellets being statistically distributed, as a result of the randomnes of the packing. At low Reynolds numbers, both global and local values fall well below Nu = 2, which is the lower limit for a single sphere in absence of convection. In the literature, this behaviour has been attributed i.a. to axial dispersion and fluid maldistribution. However, these phenomena cannot explain why the same behaviour is observed in slurries. The fact that the local values fall below Nu = 2 would suggest that neither of these explanations is valid for packed beds.     

Particle-to-fluid transfer coefficients and fluid diffusivities at low flow rate in packed beds

The assumption of temperature/concentration being center-symmetric in solid particles in packed beds was found to be faulty at low flow rate. The anomalously low transfer coefficients measured at low Reynolds numbers were considered to result from the erroneous assumption. When the fundamental equations based on the assumption of center-symmetry are adopted as a matter of convenience, however, (1) much larger axial fluid dispersion coefficients, as given by eqn (42), should be substituted, and (2) particle-to-fluid transfer coefficients may be assumed as Nusselt/Sherwood number > 1 in the range of Reynolds number 0–1.     

Evaluating resistance coefficients of straight‐through diaphragm control valves

Despite the extensive use of straight‐through diaphragm valves in many diverse industrial applications, very few studies of frictional pressure loss for straight‐through diaphragm valves have been reported in the open literature. The few that are available are for fully opened valves based on the tacit assumption that different sized diaphragm valves are geometrically similar. In this study, the pressure drops across five straight‐through diaphragm valves were measured in four aperture positions. Resistance coefficients were determined by experimentally establishing pressure gradients upstream and downstream of the valves. The experiments were carried out using Newtonian and non‐Newtonian fluids over a wide range of Reynolds numbers with the emphasis on obtaining laminar flow data. The Hooper 2‐k correlation was corroborated and found to be valid at Reynolds numbers <10 for straight‐through diaphragm valves. At higher Reynolds numbers the resistance coefficient is shown to be dependent on the size and the opening of the valve. Three different approaches (domain separation, simple summation, and selective combination) using a two‐constant model to predict the experimental resistance coefficients were explored. Comparison of the correlations with experimental data and existing models has shown that the simple summation two‐constant model approach has substantial merit. Considering the complexities of accounting for the valve size, the valve opening position, the type of fluid over a Reynolds number range of 0.1–100 000, this model gives pipeline design engineers a simple, semi‐empirical correlation for the estimation of resistance coefficients of straight‐through diaphragm control valves.     

Experimental research on stabilities,thermophysical properties and heat transfer enhancement of nanofluids in heat exchanger systems

Stable TiO₂-water nanofluids are prepared by a two-step method, stabilities of nanofluids are investigated by precipitation method and transmittance method respectively, and thermal conductivities and viscosities are also measured. An experimental system for studying the heat transfer enhancement of nanofluids is established, and heat transfer and flow characteristics of TiO₂-water nanofluids in heat exchanger systems with a triangular tube and circular tube are experimentally studied. The effects of nanoparticle mass fractions (ω=0.1 wt%-0.5 wt%) and Reynolds numbers (Re=800-10000) on the heat transfer and flow performances of nanofluids are analyzed. Fitting formulas for Nusselt number and resistance coefficient of nanofluids in a triangular tube are put forward based on the experimental data. The comprehensive performances of nanofluids in a triangular tube are investigated. It is found that nanofluids in a triangular tube can significantly improve the heat transfer performance at the cost of a small increase in resistance coefficient compared with that in a circular tube, especially the resistance coefficients are almost the same between different nanoparticle mass fractions at turbulent flow. It is also found that the comprehensive evaluation index η decreases with Reynolds number at laminar flow but a critical maximum value appears at turbulent flow.     

THE EFFECT OF HETEROGENEOUS DRAG REDUCING SURFACTANT IN DRAG AND HEAT TRANSFER REDUCTION IN CRUDE OIL SYSTEMS

Pilot scale experiments have been performed to study the effect of a heterogeneous surfactant into the drag and heat transfer coefficient in crude oil pipelines. The effects of surfactant concentration, pipe diameter, Reynolds number and temperature were studied in this research program.

An extensive set of data was obtained for heat transfer and friction coefficients for a heterogeneous surfactant known as MDR-2000. A wide range of Reynolds numbers were covered and experiments were conducted for many different Prandtl numbers. All drag and heat transfer reduction experiments were performed in the same installation using the same measurement techniques which facilitates the assessment of the trends caused by the various parameters studied.

Typical results showed that the friction coefficient was reduced by half at the optimum concentration. While, the heat transfer coefficient was reduced even more dramatically.     

Frequency response of different size concentric tube heat exchangers

The frequency response of a concentric tube heat exchanger was investigated theoretically, and experimentally, on four different size heat exchangers. Transfer functions, for the response of both shell and tube fluid outlet temperatures to disturbances in either flow rate were derived. Experimental results for water-glycol systems show that the mathematical model accurately predicts the frequency response of large heat exchangers operated at high Reynolds numbers. However, the attenuation and phase shift of the fluid outlet temperatures become significantly greater than predicted by the model when heat exchanger size is decreased or experimental conditions are changed to increase axial mixing.     

Thermal performance of tubular heat exchanger with multiple twisted-tape inserts

The paper presents an experimental investigation on enhanced heat transfer and pressure loss characteristics by using single, double, triple, and quadruple twisted-tape inserts in a round tube having a uniform heat-fluxed wal . The investigation has been conducted in the heat exchanger tube inserted with various twisted-tape numbers for co-and counter-twist arrangements for the turbulent air flow, Reynolds number (Re) from 5300 to 24000. The typical single twisted-tape inserts at two twist ratios, y/w=4 and 5, are used as the base case, while the other multiple twisted-tape inserts are at y/w=4 only. The experimental results of heat transfer and pressure drop in terms of Nusselt number (Nu) and friction factor (f), respectively, reveal that Nu increases with the increment of Re and of twisted-tape number. The values of Nu for the inserted tube are in a range of 1.15–2.12 times that for the plain tube while f is 1.9–4.1 times. The thermal enhancement factor of the inserted tube under similar pumping power is evaluated and found to be above unity except for the single and the double co-twisted tapes. The quadruple counter-twisted tape insert provides the maximum thermal performance.     

Influence of heat flux and Reynolds number on the entropy generation for different types of nanofluids in a hexagon microchannel heat sink

Based on the Second Law of Thermodynamics, the entropy generation is studied for laminar forced convection flow of different nanoparticles(Al_2 O_3, CuO and SiO_2) mixed with water through a hexagon microchannel heat sink(HMCHS). The effects of different heat fluxes and Reynolds numbers on the entropy generation for different nanofluids, volume fractions and nanoparticles diameter are investigated. The heat flux is in the range of 125 to 500 kW·m~(-2) and the Reynolds numbers vary between 200 and 1500. The thermal, frictional and total entropy generations are calculated by integrating the volumetric rate components over the entire HMCHS. The results clearly show that the rise in the heat flux leads to an increase in the thermal entropy generation for nanofluids and pure water but they don't have any influence on the frictional entropy generation. Moreover, when the Reynolds number increases, the frictional entropy generation increases while the thermal entropy generation decreases. The results revealed that at low heat fluxes and high Reynolds numbers, pure water gives the lowest entropy generation, while at high heat flux the nanofluid has to be used in order to lower the overall irreversibility.     

Convective heat and mass transfer coefficient measurements and correlations for particle beds using temperature and humidity step changes with air flow through a test bed

In this paper, transient responses of a porous urea particle bed subject to a step change in the inlet temperature or humidity for a forced convective air flow through the particle bed are investigated to determine the convective heat and mass transfer coefficients inversely by comparing the measured time constant with the predicted characteristic time constant, which is a function of the convection coefficients and Reynolds number. The experimental results show, that although both the time constants for temperature and humidity step changes are dependent on Reynolds number, the temperature response time constant (35-1300 s) is much larger than the humidity response time constant (4-25 s) for the Reynolds number range of 300-5. The surface adsorption of water vapor is very rapid but the absorption inside the porous urea particle is slowed by a very low internal effective diffusion coefficient within the particles whereas the very low Biot number for heat transfer in the particles implies a complete thermal interaction with the air flow throughout each particle and a much larger time constant. Empirical correlations of the Chilton-Colburn j-factor and Nusselt number versus Reynolds number are compared with the correlations of other researchers. These new correlations, which include an uncertainty analysis, imply much lower convective coefficients than those reported previously in the literature.     

微/小圆柱针肋热沉传热特性

圆柱形微/小针肋热沉热阻由底板及微/小肋热传导热阻、冷却液与肋间对流换热热阻以及冷却液吸热焓变热阻等组成。以去离子水为冷却液,恒定热流下,进行了叉排排布的不同尺寸的微/小圆柱形针肋热沉的单相强制对流传热实验,实验Re为100～1000,加热功率为50～300 W。实验表明：微/小圆柱形针肋热沉的Nu随Re和加热功率的增大而增大,当Re=600时对