鼓泡塔列管传热系数的测量与估算

在φ500 mm×5000 mm的冷模实验装置中,使用自制传热探头,对无内构件的空塔和安装31根竖直换热列管的鼓泡塔内列管传热系数进行了测量.实验表明,列管传热系数随表观气速的增加而增大,传热系数沿径向呈抛物型分布,垂直列管内构件的加入使得传热系数的径向分布变得更为陡峭.基于表面更新理论,结合鼓泡塔内气含率和液速分布的测量及计算结果,提出了计算传热系数的数学模型.该模型既可以用于空塔的局部传热系数与平均传热系数计算,也可以用于安装列管束的局部传热系数与平均传热系数计算.模型计算值与实验数据符合良好,最大相对误差为5.62％.     

基于传热系数的高温循环流率测量方法研究

循环物料流率是循环流化床锅炉中重要的设计和运行参数,但其热态在线测量一直是难点。基于换热原理进一步改进和完善了在线测量循环流率的方法,通过热态试验研究了影响高温颗粒与管壁之间传热系数的因素,并且利用热态试验数据和Borodulya等提出的对流传热系数预测模型进行了关联式推导,从而将传热系数和颗粒流率相关联。结果发现,传热系数的影响因素包括颗粒流率、颗粒温度、颗粒粒径等;热态试验测量得到的物料流率值与预设值的误差在±25%内;在实际流率工况下,该方法可以将物料流率和传热系数一一对应,在较宽的流率变化范围内都具有良好的预测能力。根据研究结果,测量中传热系数确定后,由计算模型可以获得物料流率,即实现高温物料流率的测量。换热法测量循环流率的原理简单,成本低廉,通过研究进一步提升了其实用性,在循环流化床锅炉的循环流率测量领域具有广阔的应用前景。     

流体流过填充床层冷却之传热系数

填充床层之传热系数包括二重阻力,即床层内部的传热阻力和床层与管壁界面间薄膜的传热阻力。本文以空气和水为传热介质,使其流过填充床层冷却,改变操作条件和床层构造,考察了Pr准数,床层高度、填充物的导热系数和形状对於传热系数的影响。由於高速固定床接触反应器和填充热交换器逐渐在工业上取得了应用,高线速下的传热数据需要迫切,因此试验的范围采用了较大的Re准数。 玻璃或磁质等低导热系数球状填充物的传热系数可归纳成: 试验范围: D_p/D_t=0.08～0.5; L/D_t=10～30; Re=250～6500; Pr=0.722～4.8 铜、铁等高导热系数球状填充物的传热系数可归纳成: 试验范围; D_p/D_t=0.1～0.5;　Re=300～10,000; 　 L/D_t=10～30 在此范围内所有试验皆经过二次以上的重复试验,误差一般不大於5%。 以圆柱体为填充物的传热系数,仅须将修正Re准数中的几何量D_p,改成与圆球具有相同的几何表面面积的球径D_p即可。 以上二式说明流体的物理性质即Pr准数对传热系数的影响不很显著,床层高度对传热系数的影响:低导热系数填充物的传热系数随L/D_t比率之减小而逐渐增大,L/D_t>30,影响甚微,L/D_t=20,误差约7%,L/D_t=10,误差可达15%;高导热系数填充物的传热系数随L/D_t的增大略有增大的趋势,但影响     

高温小直径固定床传热特性的研究

根据实验数据,提出了计算小直径固定床的有效导热系数λer和壁传热系数α_w的三种方法。 实验结果指出λ_(eλ)和α_w与Re_p·Pr呈线性关系,其斜率取决于d_p/d_t。由实验还可得到:在较高温度下,床层的平均温度对线性关联式的截距的影响更显著。     

间接加热式列管回转干燥机传热系数的测试方法

在对列管回转干燥机内传热过程进行深入分析的基础上,设计了简便、可靠的实验系统,并运用非稳态传热理论导出列管壁面与物料颗粒间的传热系数与被测量参数的关系式,从而建立了一套用于间接加热式列管回转干燥机的加热管壁面与物料颗粒间传热系数的测试方法。实验装置的传热系数测量结果显示,列管壁面与颗粒间的瞬时传热系数随筒体转动呈现周期性的变化规律,随着列管位置的升高,传热系数呈逐渐降低的趋势。通过对测试结果的误差分析表明,对传热系数测量精度影响最大的因素是紫铜管表面积,其余依次为壁面升温速率、加热电流、列管壁面温度和物料温度的测量。对常见的6种运行工况的传热系数测试结果进行了可靠性分析,结果表明,所产生的最大相对误差小于3.5%,壁面升温速率的测量误差是总误差的主要构成部分。     

二次曲线拟合法波纹管管内传热系数研究

针对波纹传热表面结构复杂难以测量管壁温度的特点,提出了二次曲线拟合法测量波纹管传热系数的方法,研究结构参数对波纹管传热特性的影响规律,为开发和设计结构合理的波纹管换热器提供依据。用W illson拟合曲线分离法,对一定的结构参数波纹管经一次拟合建立传热特性与介质物理性质的准数关系式。在此基础上,对不同的结构波纹管进行实验,并对实验结果进行二次拟合确定结构参数的影响。用该方法得到的波纹管对流传热系数准数关联式,在实验范围内计算误差小于15%。减小侍测侧与非侍测侧传热系数的比值,可进一步提高测量精度。     

管内插入物强化高粘液体传热

在Pr=135和雷诺数为300～3500条件下,对10种不同类型和参数的插入物进行传热及流阻实验、机理分析和性能评价,分析表明对于高粘液体传热,置换型插入物是最适宜的类型。又通过分析插入物传热和阻力特性对其效益的影响,指出以节省面积或功耗为目的时,用插入物强化传热的途径应当是尽可能提高传热系数,特别是低雷诺数下的传热系数,插入物引起的阻力增加可由降低雷诺数来补偿,最后以交叉锯齿带插入物的开发作为实例,说明上述两点结论的作用及其工业应用的可行性。     

内加热搅拌釜中改进型INTER-MIG桨的传热性能

通过实验与数值模拟,以水为工作介质,在直径D=0.5 m的内盘管加热搅拌釜中对双层正交排列的改进型INTER-MIG浆搅拌器不同转速下的温度场、盘管外侧的温度边界层及传热系数进行研究. 结果表明,实验与数值模拟的温度误差在2 K以内;搅拌釜内温度从上到下、从内到外呈升高趋势,最大温差基本保持在1 K之内;根据实验数据拟合得盘管外侧传热系数的关联式为Nu=0.0337Re0.925Pr1/3(d/D)0.1(dco/D)0.5,计算与实测值的平均偏差为7.64%;盘管外侧温度边界层平均厚度为3.66 mm,在合理范围内.     

镨掺杂铁酸铋粉晶的结构和磁性研究

Pr掺杂的BiFeO3粉晶是由溶胶凝胶方法制备的,掺杂浓度为0≤x≤0.5.分别用X光衍射和综合物性测量系统对Bi1-x Prx FeO3粉晶样品的结构和磁性进行了测量和分析。分析结果表明,Pr掺杂与其他稀土元素掺杂明显不同.随着Pr掺杂量的增加,母体BiFeO3的结构由菱形R3c相变为正交Pnma相的过程中,出现了稳定的PbZrO3型正交Pbam过渡相.另外,随着掺杂浓度的增大,Bi1-x Prx FeO3的磁性逐渐增强,剩余磁化强度Mr在相变边界处有最大值,并且在进入Pnma相后逐渐减小。     

压力对气体强制对流传热系数的影响

根据对流传热系数的计算公式,分别计算了不同压力下的对流传热系数,计算结果与实际操作的结果差别很大,说明了在对流传热系数关联式中应加入压力的修正系数。     

池式核沸腾中的“界面汽化热阱”效应

采用扩散极限电流技术 ( LDCT)与传热测定同时进行的实验方法分析了池核沸腾中的“界面汽化热阱”效应。传热实验所测定的是池核沸腾的总换热系数 ,由 LDCT测定并以类比原理可以获得对流传热系数 ,两者差值即为“界面汽化热阱”效应。实验结果表明 ,沸腾时 ,“界面汽化热阱”效应随热流率的提高而显著增大。对以 LDCT法测得的对流传热数据进行关联 ,获得了准数式。     

Heat transfer behavior of melting polymers in laminar flow field

Heat transfer coefficients were investigated by insertion of a probe into melting polymers under laminar flow at 200–240°C and a flow velocity of 0.5–2.7 mm/sec. The average heat transfer coefficients of melting polypropylene (PP) and polystyrene (PS) were found to be 160–220 W/m·°C and 180–270 W/m·°C, respectively. These coefficients show remarkable dependence on flow velocity, and the average heat transfer coefficient of PS is about 13%–23% higher than that of PP. When the flow velocity of flowing melting PP and PS exceeds about 0.078mm/sec, heat transfer by convection becomes dominant, whereas under lower flow velocities, since the equivalent conduction layer thickness δ′ in which the quiescent state without flow approaches infinity, heat transfer by conduction becomes dominant. The Prandtl number (Pr) and Nusselt number (Nu) of melting PP are 125–133 × 10⁶ and 38.6–51.4, respectively, and those of melting PS are 63–64 × 10⁶ and 42.3–61.3. In the case of constant flow velocity, the Peclet number (Pe) and Stanton number (St) are dependent on the specific heat of melting polymer. Polym. Eng. Sci. 44:423–432, 2004. © 2004 Society of Plastics Engineers.     

釜外和釜内螺旋半圆管夹套内流体流动与换热性特性

The physical models of the outer and inner half coil jackets were simplified to two types of coiled ducts.The mathematic models of incompressible fluid at the condition of laminar flow and heat transfer in the two types of jackets for cooling process reactor were set up and solved by the semi-implicit method for pressure linked equa-tions consistent (SIMPLEC) algorithm based on a control volume method.The flow and temperature fields were given and the effects of Dean and Prandtl numbers on flow and heat transfer were studied.The results show that flow in the inner half coil jacket is found to exhibit transition of secondary flow pattern from two vortices to four vortices when the Dean number increases,but that in the outer half coil jacket is not found.The critical Dean num-ber is about 96.The inner half coil jacket has stronger heat transfer ability than the outer half coil jacket and this superiority is more evident with larger Prandtl number.However,as the Dean number is greater than 105,the flow resistance enhances more severely in the inner jacket than the outer jacket.For both jackets,the centers of the heated wall are the poorest for heat transfer.     

Mixed convection heat transfer in porous media in the non-darcy regime

In this study mixed convection heat transfer in a homogeneous porous duct of square cross section in a horizontal orientation is examined. Results from a generalized Forchheimer model are compared with that from the Darcy model. The heat transfer rate and the flow behavior depend on the following parameters: Grashof number, Gr = Q'gβKa/kv², an axial flow pressure drop parameter, ζ = (aK/vμ)dp'/dz', an inertial parameter ξ = mK/a, appearing in the Forccheimer model and the Prandtl number, Pr = C_pμ/k. In the Darcy limit, ξ → 0, the role of the axial flow parameter, λ is reduced to a mere scale factor and the flow behavior is determined by a single parameter, λ = Gr · Pr. Both the Darcy and the Forchheimer models exhibit dual solutions and a hysteresis behavior over a certain range of Gr. Such parametric dependence can be used as an additional tool along with carefully designed experiments to determine the importance of inertial and Prandtl number effects on convective heat transfer in porous media.     

Laminar film boiling on a porous vertical wall with uniform suction velocity

Laminar free convection film boiling on a porous vertical wall with uniform suction or blowing is analysed using boundary layer theory. The solutions are obtained assuming suction or blowing to be a disturbance superposed on the isothermal, impermeable wall case. Using a parameter involving the suction or blowing velocity, universal functions are derived for various values of Prandtl Number and c_p(T_w — T_sat)/h_fgPr. These universal functions can be used to estimate the heat transfer rate in the presence of suction or blowing. As expected, suction increases the heat transfer rate while blowing decreases the heat-transfer. Even small velocities of suction or blowing could significantly affect the heat transfer. It is also found that the effects of suction or blowing are more pronounced at lower wall superheats.     

Laminar forced convection in the thermal entrance region of curved pipes with uniform wall temperature

The thermal entrance region heat transfer problem for fully developed laminar flow in curved pipes with uniform wall temperature is approached by an alternating direction implicit method for the parabolic energy equation for a flow regime with Dean number ranging from 0 to an order of 100. This work represents an extension of the classical Graetz problem in straight tubes to curved pipes. The graphical results for temperature developments in the form of temperature profiles through the horizontal and vertical planes, isothermals and local Nusselt number variations in the thermal entrance region are presented in such a way as to illustrate clearly the interaction between the secondary flow and the developing temperature field for Prandtl numbers of 0.1, 0.7, 10 and 500. For a given Dean number, the effect of Prandtl number is to shorten the thermal entrance length (I/Gz) and the temperature field develops rather rapidly with large Prandtl number. The effect of Dean number is similar to that of Prandtl number with Dean number effect becoming much more appreciable at high Prantdl numbers than at low Prandtl number.     

多头与单头螺旋槽管传热准数方程关联法

本文提出一种多头与单头螺旋槽管管内单相流体对流传热准数方程的关联法,对普兰特数Pr从0.7到35的三种介质——空气、水及甘油与水的混合物进行了管内传热准数方程的关联,其关联形式较简单,关联效果良好,适用于工程计算,也有助于传热理沦的研究.     

人工糙管中湍流传热与温度分布

以横肋管为典型人工糙管,空气为试验介质,恒热流操作,进行湍流传热时径向温度分布和传热特性的测定,试验Re为20000～70000.所得湍流核心区温度分布可以对数分布律和温度亏损律表示,式中常数与粗糙几何参数有关.由测得的温度分布和速度分布计算了湍流粘度和湍流导温系数.此外,还进行了温度脉动特性的测定.传热系数测定结果表明,人工粗糙管比光滑管强化150%～300%,传热膜系数可用简单关联式估算Nu/Nu_s=1+26(k/d)~(0.49)(S/K)~(-0.46)式中Nu_s=0.022Re~(0.8)Pr~(0.5)     

Laminar Flow and Heat Transfer Characteristics in Jackets of Triangular Flow Channels

Laminar flow and heat transfer characteristics of jacketed vessel with triangular flow channels were numerically studied under hydrodynamically and thermally fully developed conditions. Constant heat flux at theheated wall was assumed. The numerical program code interms of vorticity, stream function, axial velocity com ponent and energy equations was written based on a finite volume method. Based on the numerical results, the flow and temperature field were given, and the effects of Dean and Prandtl numbers on flow and heat transfer were ex amined, and the correlations of flow resistance and mean Nusselt number were developed for the jacket. The results show that the structure of secondary flow is steady two vortices in the investigated range of dimensionless curvatureratio and Reynolds number. Two peaks of local Nusselt number increase significantly with Prandtl and Dean num ber increasing, but the local Nusselt numbers near two ends and at the center of the heated wall increase only slightly. The center and two ends of heated wall are the poor positions for heat transfer in the jacket. Compared with the outer half coil jacket at the same area of heated wall, curvature radius, Reynolds number and Prandtl number, e jacket of triangular flow chmnel has lower flow resistance and less mean Nusselt number.