High-order targeted essentially non-oscillatory scheme for two-fluid plasma model

The weakly ionized plasma flows in aerospace are commonly simulated by the single-fluid model,which cannot describe certain nonequilibrium phenomena by finite collisions of particles,decreasing the fidelity of the solution.Based on an alternative formulation of the targeted essentially non-oscillatory(TENO)scheme,a novel high-order numerical scheme is proposed to simulate the two-fluid plasmas problems.The numerical flux is constructed by the TENO interpolation of the solution and its derivatives,instead of being reconstructed from the physical flux.The present scheme is used to solve the two sets of Euler equations coupled with Maxwell's equations.The numerical methods are verified by several classical plasma problems.The results show that compared with the original TENO scheme,the present scheme can suppress the non-physical oscillations and reduce the numerical dissipation.

Temperature and current sensitivity extraction of optical superconducting transition-edge sensors based on a two-fluid model

Optical superconducting transition-edge sensor(TES)has been widely used in quantum information,biological imaging,and fluorescence microscopy owing to its high quantum efficiency,low dark count,and photon number resolving capability.The temperature sensitivity(α_(I))and current sensitivity(β_(I))are important parameters for optical TESs,which are generally extracted from the complex impedance.Here we present a method to extractα_(I)andβ_(I)based on a two-fluid model and compare the calculated current-voltage curves,pulse response,and theoretical energy resolution with the measured ones.This method shows qualitative agreement that is suitable for further optimization of optical TESs.

Anisotropic Plane Symmetric Two-Fluid Cosmological Model with Time-Varying G and A

We investigate a two-fluid anisotropic plane symmetric cosmological model with variable gravitational constant G（t） and cosmological term A（t）. In the two-fluid model, one fluid is chosen to be that of the radiation field modeling the cosmic microwave background and the other one a perfect fluid modeling the material content of the universe. Exact solutions of the field equations are obtained by using a special form for the average scale factor which corresponds to a specific time-varying deceleration parameter. The model obtained presents a cosmological scenario which describes an early acceleration and late-time deceleration. The gravitation constant increases with the cosmic time whereas the cosmological term decreases and asymptotically tends to zero. The physical and kinematical behaviors of the associated fluid parameters are discussed.

REVIEW ON MATHEMATICAL ANALYSIS OF SOME TWO-PHASE FLOW MODELS

The two-phase flow models are commonly used in industrial applications, such as nuclear, power, chemical-process, oil-and-gas, cryogenics, bio-medical, micro-technology and so on. This is a survey paper on the study of compressible nonconservative two-fluid model, drift-flux model and viscous liquid-gas two-phase flow model. We give the research developments of these three two-phase flow models, respectively. In the last part, we give some open problems about the above models.

Experimental Determination and Modeling of Bubble Size Distributions in Bubble Columns

Using a five point conductivity technique local values of bubble size,bubble velocity and gas fractionhave been experimentally determined in a 288 mmID and 4.3 m high bubble column as a function of axial andradial position for the air/water and CO2/N2/aqueous MDEA systems.The experimental results are comparedwith predictions from a fundamental two-fluid model.The implementation of a non-steady lateral drag term inthe two-fluid model has been shown.In addition to improving the physical realism of the model,it is found togive slight improvements in the predictions of the distributions of local bubble size.Predictions of bubble size arefound in reasonable agreement with experimental values in the heterogeous flow regime,whereas they are stil1found to be unreliable at low gas velocities.Local void predictions are found in reasonable agreement with experi-mental values,but deviations occur in the homogeneous flow regime towards the wall.This is attributed to defi-ciencies in the simplified bubble size

Assessment of coal gasification in a pressurized fixed bed gasifier using an ASPEN plus and Euler–Euler model

With the help of Aspen Plus,a two-dimensional unsteady CFD model is developed to simulate the coal gasification process in a fixed bed gasifier.A developed and validated two dimensional CFD model for coal gasification has been used to predict and assess the viability of the syngas generation from coal gasification employing the updraft fixed bed gasifier.The process rate model and the sub-model of gas generation are determined.The particle size variation and char burning during gasification are also taken into account.In order to verify the model and increase the understanding of gasification characteristics,a set of experiments and numerical comparisons have been carried out.The simulated results in the bed are used to predict the composition of syngas and the conversion of carbon.The model proposed in this paper is a promising tool for simulating the coal gasification process in a fixed bed gasifier.

A THREE-FLUID MODEL OF THE SAND-DRIVEN FLOW

The sand-driven flow is studied from the continuum viewpoint in this paper. The crux of this work is how to model the stresses of the particle phase properly. By analysing the two-fluid model which usually, works in solving gas-particle two-phase .flow,. we find that this model has many. deficiencies for studying the sand-driven flow,even for the simplest case- the steady, two-dimensional fully-developed flow.Considering this, we have proposed the three-fluid model in which the upward particles and the downward-particles ore regarded as two kinds of fluids respectively.It is shown that the three-fluid model is better than the two-fluid model in reflecting the internal structure of the flow, region and the influence of the boundary situations on the flow. and it is advantageous to find an approximate solution in that the main components of the particle-phase stresses can be explicitly expressed by those variables in the three-fluid model.In the end, the governing equations as well as the boundary. conditions for the three-fluid model are provided with a discussion.

An improved semi-empirical friction model for gas-liquid two-phase flow in horizontal and near horizontal pipes

Pressure drop and liquid hold-up are two very important fluid flow parameters in design and control of multiphase flow pipelines.Friction factors play an important role in the accurate calculation of pressure drop.Various empirical and semi-empirical closure relations exist in the literature to calculate the liquid-wall,gas-wall and interfacial friction in two-phase pipe flow.However most of them are empirical correlations found under special experimental conditions.In this paper by modification of a friction model available in the literature,an improved semiempirical model is proposed.The proposed model is incorporated in the two-fluid correlations under equilibrium conditions and solved.Pressure gradient and velocity profiles are validated against experimental data.Using the improved model,the pressure gradient deviation from experiments diminishes by about 3%;the no-slip condition at the interface is satisfied and the velocity profile is predicted in better agreement with the experimental data.

Prediction of pressure gradient and hold-up in horizontal liquid-liquid pipe flow

This paper aims to propose correlations to predict pressure gradient,friction factor and fluid phase hold-up in liquid-liquid horizontal pipe flow.To develop the correlations,experiments are conducted using high viscous oils(202 and 630 mPa⋅s)in a steel pipe of length 11.25 m and length-to-diameter ratio of 708.In addition,the experimental data from the literature comprising wide range of flow and fluid properties is analyzed.For the analysis,the liquid-liquid pipe flow data is categorized into two as:stratified and dispersed.The existing friction factor correlations are modified to incorporate the effects of viscosity of the oil phase,interfacial curvature(contact/wetting angle-in lieu of material of the pipe)and fluid phase fraction.In the two-fluid model of stratified flow,the wall stress and interfacial stress correlations are substituted with superficial velocities of fluids and superficial Reynolds numbers of fluid phases replacing fluid phase velocities and fluid Reynolds numbers.Similarly,for dispersed flow,an effective Reynolds number is described as the sum of superficial Reynolds number of oil and water phases.Substituting the generally employed mean or mixture Reynolds number with the effective Reynolds number into the existing single-phase turbulent flow friction factor correlation,an effective friction factor for oil-water flow is proposed.Employing the proposed correlations,the pressure gradient across the oil-water flow and hold-up volume fraction are predicted with significant reduction in error compared with that of conventionally employed correlations.The average error and standard deviation values of−7.06%,20.72%and 0.31%,18.79%are found for stratified flow and dispersed flow respectively.

Validation of an improved two-fluid model with particle rotation for gas-solid fluidized bed

Gas-solid fluidized beds are widely applied in chemical and process engineering.It is of significance to establish a reasonable and effective mathematical model to explore the hydrodynamics of gas-particle system for industrial applications.As a less computationally demanding alternative to the discrete descriptions,two-fluid model considering kinetic theory of granular flow is often adopted to describe the fluidized behaviors of particles,but it cannot characterize the rotation of particles and its influence on the fluidized behaviors.In this study,to address the rotation effect of the fluidized particles,a two-fluid model combining the classical fluid and micropolar fluid is established,namely CMTFM.In the CMTFM,classical fluid is used to describe the motion of gas phase,while micropolar fluid is adopted to describe the motion of particle phase,and the rotation of particles and its influence on the hydrodynamics of the gas-particle system are characterized by the degree of freedom of microrotation and the improved drag force based on micropolar viscosities.In the calculation of the gas-solid bubbling fluidized bed,we investigated the influence of the microstructure parameters,particle-particle collision restitution coefficient and inlet velocity,and the results are compared to those from TFM model and experiments.Through the analysis,it manifests that pressure drop and expansion height of the fluidized bed under the consideration of the microrotation effect are closer to the experiments,which demonstrates the feasibility and advantage of the classical-micropolar two-fluid model.

液固流化床中颗粒流动特性的数值模拟

应用欧拉-欧拉双流体模型,液相采用k-ε湍流模型,同时考虑液固两相间耦合作用,数值模拟液固流化床内液固两相流动,研究了液体密度和粘度对液固流化床内流动特性的影响.研究结果表明,液固流化床内液体、颗粒混合比较均匀,呈现散式流态化特性.颗粒轴向速度随着液体密度和粘度的增大而增大,并且在床内分布趋势相同.数值模拟得到床层膨胀高度的结果与Babu等人公式计算值相吻合.

湍动流化床内气固两相流动特性的数值模拟

采用欧拉-欧拉双流体模型,颗粒动理学方法模拟颗粒脉动流动和k-ε双方程模型模拟气相湍流流动,考虑气固两相间耦合作用,数值模拟湍动流化床内气固两相流动行为,获得颗粒浓度和颗粒速度分布.计算结果表明湍动流化床呈现下部密相区、上部稀相区的颗粒分布特性。在密相区,沿床径向方向颗粒浓度在床中心处低、壁面逐渐增高;在稀相区颗粒浓度分布较均匀.沿轴向方向颗粒浓度呈底部浓度高、顶部浓度低的"S"型分布。

高固体流率循环流化床内气体-颗粒团聚物流动特性

采用Euler/Euler双流体模型、颗粒动理学方法模拟颗粒相流动,k-ε双方程模型模拟气相湍流流动,同时采用以颗粒团聚物直径为定性尺寸的气?固曳力计算方法,数值模拟高固体流率循环流化床内颗粒的湍动流化特性。计算结果表明,考虑颗粒团聚物影响的模型能准确地反映出床内颗粒湍动流化的宏观规律。颗粒间摩擦应力对固相应力贡献较小。模拟结果获得的空隙率和颗粒浓度分布与实验结果相吻合,同时,预测出颗粒团聚物的分布规律。

鼓泡塔内气液两相流动力特性数值模拟研究

利用CFD软件模拟的方法研究鼓泡塔内气液两相流动力特性,为鼓泡塔的设计提供依据。采用欧拉-欧拉双流体模型分别结合标准k-ε紊流模型和RNG k-ε紊流模型对鼓泡塔内气液两相流进行数值模拟,并使用Phase Coupled SIMPLE算法进行速度与压力耦合求解。比较鼓泡塔内轴截面(y=0)处不同高度液相速度和气相速度的变化情况,发现速度沿径向呈现出抛物线分布,沿水深方向越接近通气孔,速度越大,且气相速度整体大于液相速度。通过将z=0.28 m处的垂向液相速度与实验值比较,得出欧拉-欧拉双流体模型结合标准k-ε紊流模型模拟鼓泡塔气液两相流动力特性优于RNG k-ε模型,且发现上升力对模拟结果有显著的影响。

聚丙烯环管反应器的流体力学模拟

采用颗粒动力学为基础的Euler-Euler双流体模型研究反应器内液固相的流动力学特性.通过fluent软件,采用标准k-ε模型描述流体的湍流状态、Gidaspow曳力模型描述流体的相互作用力,运用SIMPLE算法求解速度场.结果表明：在5～9m/s的浆液速度范围内,环管反应器直管段的固相体积分数分布均匀,弯管段的固相体积分数分布不均匀;浆液速度增大,其固相体积分数分布的非均匀性增加;当固相体积分数为0.35时,浆液密度为563～571千克/立方米.通过对速度场的分析可知,上升管中段的流速为6～7.5 m/s,速度呈对称分布;下降管中段的流速为5～8 m/s,速度呈非对称分布.计算结果与工厂实际生产情况接近,表明欧拉双流体模型能有效地描述环管反应器内浆液流动形态.

循环流化床煤粉气化炉内气固三维流动特性数值模拟

采用基于气相k-ε湍流模型、颗粒相颗粒动理学模型的欧拉-欧拉双流体模型,对循环流化床煤粉气化炉内气体和颗粒两相三维流动特性进行了冷态数值模拟,得到了炉内颗粒体积分数、颗粒速度的分布情况以及进料管与回料管的颗粒扩散距离。模拟结果表明,循环流化床煤粉气化炉内呈现下部密相区、上部稀相区的颗粒分布特性。

基于MECST气固相间曳力模型的气体-颗粒团聚物流动特性的数值研究

由颗粒非均匀流动结构中各个尺度内能量守恒的角度出发,建立了气固两相流系统的整体和局部参数与气固相间曳力的相互关系,提出了基于颗粒悬浮输送能量最小(MECST)气固相间曳力模型;并将其应用于欧拉-欧拉双流体模型中,数值模拟循环流化床提升管内气体-颗粒-颗粒团聚物的流动特性。考察了时均颗粒相密度和颗粒质量流率沿径向的分布;颗粒浓度、提升管压降沿轴向的分布以及颗粒团聚物在提升管内的分布特性。模拟结果表明,颗粒相密度、颗粒质量流率以及提升管压降与实验结果相吻合;与能量最小多尺度气固相间曳力模型的颗粒浓度和颗粒拟温度的结果相比,MECST气固相间曳力模型得到的颗粒浓度较低,从而使颗粒拟温度减小。

低速下不同入口位置塔式曝气池气液两相数值模拟

为了研究不同入口下塔式曝气池气液两相流动规律,采用欧拉双流体模型耦合群体平衡模型(PBM,population balance model),在对计算域网格及气相分布与实验验证的基础上,研究了四种距离曝气池底部中心不同位置处的入口对曝气池内气液两相流动的影响,探讨了气含率、气泡数密度、液相水平速度等流体动力学性质,以期为塔式曝气池设计提供指导和依据.研究结果表明:欧拉双流体模型耦合PBM的模拟结果优于单一气泡尺寸的欧拉双流体模型;曝气池内气含率、气相分布、旋涡强度、液相水平速度均受入口位置影响;当入口位置逐渐远离曝气池中心时,气相分布逐渐呈之字形,旋涡强度增大,气含率及气泡羽流周期则先增大后减小;入口位置对气泡数密度无明显影响,气泡数密度在气泡直径5.95 mm下分布最多.

循环流化床锅炉燃烧过程仿真研究

建立循环流化床锅炉(circulating fluidized bed boiler,CFBB)的二维几何模型,采用欧拉双流体模型与离散相模型相结合的方法对CFBB燃烧过程进行仿真分析。根据仿真所得锅炉内部床料颗粒、煤粉颗粒分布情况以及气相温度场、浓度场等多物理场分布特点,得出结论:同时使用欧拉双流体模型与离散相模型具有可行性;在CFBB燃烧过程中,内部煤粉的火焰位置是变化的。下一步的研究重点是CFBB三维几何模型的仿真分析。

Two-fluid modeling of Geldart A particles in gas-fluidized beds

We have investigated the effect of cohesion and drag models on the bed hydrodynamics of Geldart A particles based on the two-fluid （TF） model. For a high gas velocity U0 = 0.03 m/s, we found a transition from the homogeneous fluidization to bubbling fluidization with an increase of the coefficient C1, which is used to account for the contribution of cohesion to the excess compressibility. Thus cohesion can play a role in the bed expansion of Geldart A particles. Apart from cohesion, we have also investigated the influence of the drag models. When using the Wen and Yu drag correlation with an exponent n = 4.65, we find an under-prediction of the bed expansion at low gas velocities （U0 = 0.009 m/s）. When using a larger exponent （n = 9.6）, as reported in experimental studies of gas-fluidization, a much better agreement with the experimental bed expansion is obtained. These findings suggest that at low gas velocity, a scale-down of the commonly used drag model is required. On the other hand, a scale-up of the commonly used drag model is necessary at high gas velocity （U0 = 0.2 and 0.06 m/s）. We therefore conclude that scaling the drag force represent only an ad hoc way of repairing the deficiencies of the TF model, and that a far more detailed study is required into the origin of the failure of the TF model for simulating fluidized beds of fine powders.