轴向水─水混合式加热器在供热中的应用

本文从应用角度出发，对轴向水－水混合式加热器的实用性进行了分析，并与数种其他加热器进行了技术性能比较。     

晶体管混频器混频增益的简化计算

本文介绍一种方法简单、便于学生理解的分析晶体管混频器混频增益的简化计算方法.该方法从晶体管的电流方程入手,通过分析晶体管混频器的混频原理,得到了输出中频电流和混频跨导、混频增益的简明数学表示.通过对典型混频器电路的仿真,验证了该方法的有效性.该方法与传统的时变偏置电压分析方法相比,混频跨导和混频增益容易求得,解决了以往混频跨导基本是一个概念参数而难以确定具体数值的问题.     

Mixing of low-dose cohesive drug and overcoming of pre-blending step using a new gentle-wing high-shear mixer granulator

The objective of this study was to examine the influence of drug amount and mixing time on the homogeneity and content uniformity of a low-dose drug formulation during the dry mixing step using a new gentle-wing high-shear mixer. Moreover, the study investigated the influence of drug incorporation mode on the content uniformity of tablets manufactured by different methods. Albuterol sulfate was selected as a model drug and was blended with the other excipients at two different levels, 1% w/w and 5% w/w at impeller speed of 300?rpm and chopper speed of 3000?rpm for 30?min. Utilizing a 1?ml unit side-sampling thief probe, triplicate samples were taken from nine different positions in the mixer bowl at selected time points. Two methods were used for manufacturing of tablets, direct compression and wet granulation. The produced tablets were sampled at the beginning, middle, and end of the compression cycle. An analysis of variance analysis indicated the significant effect (p?相似文献   

Lightnin静态混合器内气泡分散流体动力学特性实验研究

以Lightnin静态混合器（LSM）内水-空气气液两相体系为研究对象,在连续相水表观速度U_L=0.071~0.127 m/s和离散相空气表观速度U_G=0.007~0.042 m/s的条件下,研究内径100 mm的LSM内气液两相湍流流动阻力与气泡分散水动力学行为。使用分辨率为1920×1080的高速相机Revealer-2F04M采集混合器内不同轴向窗口的气泡群演化过程。结果表明：当U_L<0.085 m/s和U_G=0.025~0.042 m/s时,LSM内的流型为泡状流。随着气泡群流经混合元件数的增加,气泡群的Sauter平均直径d₃₂逐渐减小。当液体表观速度U_L≤0.085 m/s时,Sauter平均直径d₃₂随气体表观速度的增加先减小后增大;U_G =0.028 m/s时d₃₂达到局部最小值,53%的气泡直径d_B/D₀在0.02~0.05范围内。Sauter平均直径、内径与无量纲停留时间τ之间的关系满足d₃₂/D₀=0.031τ^-0.14We^-0.41。平均气含率α的增大显著增加了单位体积内气泡数量密度,加剧气泡与元件表面碰撞频率,增大旋涡二次流强度,导致摩擦系数显著降低;采用Lockhart-Martinelli方法对实验数据回归,得到气液两相流压降预测常数C的关联式：C=5.26×10⁵U_G^-0.91/Re^0.74。     

烟花药剂自动混药技术

为提高烟花自动生产线中最易出现爆炸的混药工序的安全性及混药质量,提出滚筒制备发射药、响药的技术。介绍混药机的主要功能,分析其工作原理和结构,给出其工艺流程,列出混药滚筒及有效装载容量的计算方法。结果表明：该技术能实现烟花药剂的自动混药及出药功能,保证药剂混合均匀,配比精确,实现人机隔离和无人化生产,达到预期的设计要求,并已应用于双响炮自动装药装配生产线中。     

潜水搅拌器安装角度对搅拌效果的影响

研究潜水搅拌器水平安装角度对搅拌池内流场的影响,建立不同的水平安装角度,通过Fluent对潜水搅拌机的搅拌槽内流场进行三维数值模拟,得出不同方案的速度分布情况.利用UDF模块,分别计算流场中流速达到搅拌效果的有效搅拌流体体积及其占整个流场体积的百分比,通过比较,选出最优的潜水搅拌器安装方案,提出了评价潜水搅拌器效能及其安装布置优劣的新方法——有效搅拌域法,利用此方法,使潜水搅拌器的搅拌效果分析更加准确.     

转矩流变仪RC90系统的技术与应用

介绍了转矩流变仪的发展、基本原理和应用。各种混合器、单螺杆挤出机、双螺杆挤出机、模具和后挤出机系统都能与RC90装配。RC90可用于对材料的熔融性能和热稳定性、颜料分散性、交联、固化和硫化性能以及挤出可加工性能等的研究。     

Flow patterns in granulating systems

Particle flow patterns were investigated for wet granulation and dry powder mixing in ploughshare mixers using Positron Emission Particle Tracking (PEPT). In a 4-l mixer, calcium carbonate with mean size 45 μm was granulated using a 50 wt.% solution of glycerol and water as binding fluid, and particle movement was followed using a 600-μm calcium hydroxy-phosphate tracer particle. In a 20-l mixer, dry powder flow was studied using a 600-μm resin bead tracer particle to simulate the bulk polypropylene powder with mean size 600 μm. Important differences were seen between particle flow patterns for wet and dry systems. Particle speed relative to blade speed was lower in the wet system than in the dry system, with the ratios of average particle speed to blade tip speed for all experiments in the range 0.01–0.25. In the axial plane, the same particle motion was observed around each blade; this provides a significant advance for modelling flow in ploughshare mixers. For the future, a detailed understanding of the local velocity, acceleration and density variations around a plough blade will reveal the effects of flow patterns in granulating systems on the resultant distribution of granular product attributes such as size, density and strength.     

Non-equilibrium particle motion in the vicinity of a single blade

The motion of sand particles close to a single moving blade was investigated using Positron Emission Particle Tracking (PEPT) during the period in which the free bed surface profile was evolving to an equilibrium shape. The area affected by the blade was divided into active and inactive regions and these were analysed separately. The characteristic heart-shape of the active region in the plan view was determined. An approximately 10-particle-diameter wide velocity transition zone is found between the two regions. While the tracer particle is in the inactive region moving away from the blade, the time dependence of the axial displacement is well described by a logarithmic relationship. The probability of particle movement towards the centre of the blade was quantified using a “central tendency” index. The calculated central tendency shows maxima at each side of the blade. The separation of the two maxima, which indicates the width of the active region, increases with fill level but is independent of rotational speed.     

Instability due to Viscosity Stratification Downstream of a Centerline Injector

A common injector geometry upstream of a static mixer is the centerline injector. A flow instability can arise due to viscosity differences between the injected core‐flow and the outer co‐flow. This instability can adversely affect the effectiveness of the mixing operation. An experimental investigation of miscible viscosity‐stratified flow in a circular geometry was performed using Laser Induced Fluorescence (LIF) and Particle Image Velocimetry (PIV). The experimental results for the stable region agree with the analytical results. The unstable region exhibits different modes depending on the viscosity ratio, volume flux ratio, and Reynolds number. The modes include wavy core‐flow with fissures and wavy core‐flow with core breakup. The time‐averaged experiment velocity profiles for the unstable core indicate a broadening of the jet at the centerline, which is consistent with the LIF visualization.