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1.
在直径为0.476m的椭圆底圆柱形搅拌槽内,以水/航空煤油及水/环己烷为实验体系,研究了Rushton涡轮式搅拌桨(RT-6)、六半椭圆管涡轮式搅拌桨(HEDT)、折叶轴流式搅拌桨及翼形轴流式搅拌桨(CBY)的6种不同组合桨的液-液分散特性,用取样法测定了分散相体积分数的轴向分布及体系澄清时间。结果表明,组合桨中的底桨在液-液分散中发挥了主要作用。单位体积输入功率相同时,底桨为CBY的组合桨进行液-液分散后,液滴的平均滴径最小,体系澄清时间较长;底桨为HEDT的组合桨的分散效果次之;底桨为RT-6的组合桨因滴径分布较宽,虽然平均滴径最大,但澄清时间也较长。 相似文献
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以水-煤油及水-环己烷为体系,研究Rushton涡轮桨(RT),半椭圆管涡轮(HEDT)及翼形轴流式桨(CBY)的6种不同组合桨的液-液分散特性。测定了不同输入功率时分散相体积分率沿轴向及径向的分布。结果表明:当搅拌槽内液位与槽径之比达1.5,在相同输入功率时,三层桨的液液分散性能优于两层桨,功率准数较低的CBY组合桨在输入功率0.8kW/m~3时,槽内的轴向及径向分散相体积分率达到稳定的均匀分布。而功率准数较大的RT组合桨需要在输入功率1.8kW/m~3才能达到槽内分散相的均匀分布。 相似文献
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多层桨搅拌槽内气-液两相局部气含率研究 总被引:1,自引:1,他引:0
在直径0.48 m的椭圆底搅拌槽中,研究了以半椭圆管盘式涡轮(HEDT)为底桨、上两层为四叶翼型轴流桨下压操作(WHD)的组合桨(HEDT+2WHD)在搅拌槽内沿径向和轴向的局部气含率分布及不同表观气速对局部气含率的影响.局部气含率沿轴向分布比较均匀,仅在底桨附近有一个极大值,其它位置局部气含率差异较小.随着表观气速增... 相似文献
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以水为液相,玻璃珠为固相,在固-液搅拌槽内比较了传统径向流Rushton桨、轴向流下推式45°六斜叶桨以及新型半折叶搅拌桨的功耗、泵送能力和对固体颗粒的悬浮效果。并应用CFD (Computational fluid dynamics)方法研究了不同搅拌桨操作下颗粒的轴向速度分布。结果表明:在相同转速下,Rushton桨的功耗最大,新型半折叶桨与下推式45°六斜叶桨的功耗接近;新型半折叶桨的流量准数最大,泵送能力最强;在固-液体系中,新型半折叶桨与下推式45°六斜叶桨的流型类似,但3种桨中新型半折叶桨对固体颗粒的悬浮效果最好。 相似文献
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搅拌槽内粘稠物系中气液相间氧传递 总被引:1,自引:0,他引:1
以发酵罐中气液相间氧传递为背景,考察了搅拌槽内搅拌器形式、物系流变性质、通气搅拌操作条件等对假塑性粘稠物系中氧传递过程的影响。结果表明,这些因素主要通过改变气体分散状态和相间传质面积来影响氧传递速率。根据气泡在搅拌槽内不均匀分布现象,多层搅拌下气液相间传质过程可以用气泡运动分区分布模型来描述。它说明了采用轴向流桨和涡轮桨组合的搅拌形式在氧传递方面的优越性,为强化发酵罐中供氧指明一条有效途径 相似文献
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从实验和数值模拟两方面对搅拌槽内中高黏物系条件下的气含率、气泡尺寸大小和传质特性等进行综述。讨论了搅拌桨型、操作条件、黏度或非牛顿性对气液分散特性的影响。阐明了径流式搅拌桨和上翻式轴流桨的组合能减小气穴,更适合中低黏物系的搅拌;搅拌转速比通气量的影响效果更明显,转速增加使气泡的分布均匀性变好,而提高通气速度会产生大气泡,使气泡分布不均匀程度增加;黏度或非牛顿性的增加可以改变气泡的碰撞频率,气泡平均尺寸减小。最后讨论了针对中高黏物系的计算流体力学模型的修正方法,并且展望了此领域的研究发展方向。 相似文献
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《高校化学工程学报》2021,35(3)
为将改进型三斜叶-Rushton组合桨高效应用于实际工程,通过计算流体动力学(CFD)对装配改进型三斜叶-Rushton组合桨搅拌槽内的流场进行了模拟研究,与三斜叶-Rushton组合桨进行了对比;并通过粒子图像测速(PIV)技术研究该组合桨槽内搅拌转速n、桨叶间距C2及离底距离C1的变化对流场产生的影响。结果表明当转速为100r×min~(-1)时能有效改善槽底和上桨叶区域的混合效果,槽内速度分布相对均匀,实验结果和模拟结果吻合效果较好;模拟结果表明改进型三斜叶桨的泵吸效果较三斜叶桨更强,能有效缩小搅拌槽底部和内壁附近的低速区域,槽内混合效果更好;实验结果表明当桨叶间距为0.25h时,槽内速度分布更合理;当离底距离为0.3h时,上桨叶区的较低速区域进一步缩小。 相似文献
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螺带式搅拌器传热性能参数的研究 总被引:1,自引:0,他引:1
用实验方法讨论了螺带叶轮对从罐壁到混合液体内层传热时,所需功率和传热系数的影响因素,得出了螺带式搅拌桨直径与搅拌罐直径之比d/D=0.93~0.95,搅拌桨螺距与直径之比p/d=0.24~0.26时混合效率最高。通过搅拌罐高径比对传热系数影响的研究,表明了叶轮位于距离罐底1/2H附近时,其传热系数最大,得出了Nu/(Re^0.5Pr^0.33Vi^0.14)随着(H/D)^-0.47的增加而减小。 相似文献
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The heat transfer coefficient between a suspension of FCC particles and a horizontal cylindrical heat transfer probe inserted into the riser or the standpipe of a CFB has been quantified. With the heat transfer probe located in the riser 4.75 meters above the L-valve, and solids mass flux varied between 0 to 100 kg/(m2·s), the heat transfer coefficient ranged from 70 W/(m2·K) to 475 W/(m2·K). On a plot of heat transfer coefficient versus solids mass flux, three zones have been identified, which correspond to the difference in the flow structure of the solids around the heat transfer probe as the solids mass flux increases. Also, measurements were taken of the radial solids flux in two orthogonal directions using an isokinetic sampling system. The data shows the asymmetry due to the perturbations introduced by the heat transfer probe. Finally, the heat transfer in the downcomer was investigated. It has been found that the magnitude of the heat transfer coefficient in the downcomer is dominated by the solids flux; variation in gas bypassing in the standpipe has little effect. Results obtained by traversing the heat transfer probe across the diameter of the standpipe suggest that the heat transfer coefficient is nearly independent of radial position within the standpipe. 相似文献
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对垂直管内高粘假塑性流体传热进行了实验研究,所得实验数据与前人工作做了比较,并建立了考虑轴向变粘度效应的传热关联式. 相似文献
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针对二氧化碳作为制冷剂在微细通道内两相流沸腾换热进行了实验与理论研究,采用红外成像观测与传热系数实验研究,定量与定性地分析了热通量2~35 kW·m-2,饱和温度-10~10℃工况时,内径为1、2、3 mm圆管内的传热系数。实验结果表明:当质量流率增加时干涸起始干度逐渐降低,当质量流率小于临界值时,干涸现象结束之后,传热系数随着质量流率增加基本维持不变,而当质量流率大于临界值时,干涸现象结束之后,随着质量流率增加传热系数相应增加;随着管径增加,干涸发生的质量流率越小,临界热通量越大,同时管径越小传热系数越高。 相似文献
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Shuichi Tezura Akihiro Kimura Masanori Yoshida Kazuaki Yamagiwa Akira Ohkawa 《Journal of chemical technology and biotechnology (Oxford, Oxfordshire : 1986)》2008,83(5):763-767
To develop an enhanced form of solid‐liquid apparatus, an unbaffled agitated vessel has been constructed, fitted with an agitation system using an impeller whose rotation alternates unsteadily in direction, i.e. a forward‐reverse rotating impeller. In this vessel, solid‐liquid mass transfer was studied using a disc turbine impeller with six flat blades. The effect of impeller rotation rate as an operating variable on the mass transfer coefficient was evaluated experimentally using various geometrical conditions of the apparatus, such as impeller diameter and height, in relation to the impeller power consumption. Mixing of gas above the free surface into the bulk liquid, i.e. surface aeration, which accompanied the solid‐liquid agitation, was also investigated. Comparison of the mass transfer characteristics between this type of vessel and a baffled vessel with a unidirectional rotating impeller underscored the sufficient solid‐liquid contact for prevention of gas mixing in the forward‐reverse rotation mode of the impeller. Copyright © 2008 Society of Chemical Industry 相似文献
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The effects of superficial gas velocity (0.5 to 4.5 m/s), solid circulating rate (0 to 40 kg/m2·s), suspension density (0 to 19 kg/m3) and particle sizes (83, 103, 163, 236 μm) on the bed-to-wall heat transfer coefficient have been determined in a downer reactor (0.1 m I. D. × 3.5 m high). Bed-to-wall heat transfer coefficient increases with increasing suspension density. The heat transfer coefficient by gas convection played a significant role, especially at lower solid circulation rates or suspension densities and larger particle sizes. At a given particle suspension density in the downer reactor, the heat transfer coefficient increases with decreasing particle size. A model is proposed to predict the bed-to-wall heat transfer coefficient in a downer reactor. 相似文献
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Properties of gas—liquid dispersion and mixing of seven types of impellers were studied and compared in a stirred vessel with aeration. New correlations for the properties including critical dispersion impeller speed, dispersion regime, power consumption, gas hold-up, discharge flow number and discharge efficiency have been developed. The fluid/wall heat transfer was also studied with several types of dual impeller combinations. There is a critical impeller speed which determines how aeration changes the heat transfer coefficient. Operating conditions influence heat transfer interactively by three factors, which can be expressed by proper dimensionless variables. 相似文献
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Ik Sang Shin Sung Mo Son Dae Ho Lim Yong Kang Heon Jung Ho Tae Lee 《Korean Journal of Chemical Engineering》2010,27(3):1015-1020
Characteristics of heat transfer were investigated in pressurized slurry bubble column reactors whose diameter was either
0.051, 0.076, 0.102 or 0.152 m (ID) and 1.5 m in height, respectively. Effects of gas velocity (U
G
), solid contents (S
C
), pressure (P), liquid viscosity (μ
L
) and column diameter (D) on the heat transfer coefficient (h) between the immersed vertical heater and the column were determined.
Multiple effects such as UG and D, P and D, μ
L
and D, and S
C
and D on the value of heat transfer coefficient were discussed. Temperature fluctuations were also measured and analyzed
by adapting chaos theory, which was used to explain the effects of operating variables on the heat transfer in the column.
The heat transfer coefficient increased with increasing gas velocity, pressure or solid content in the slurry phase, but decreased
with increasing liquid viscosity or column diameter. The decrease trend of h with increasing column diameter was somewhat
sensitive when the gas velocity was relatively high (U
G
⩾12 cm/s). The effects of column diameter on the h value became almost linear when the operating pressure (P=4−10 kg
f
/cm2), liquid viscosity (μ
L
=20−38 mPa·s) or solid content in the slurry phase (S
C
=10−20 wt%) was relatively high and gas velocity was relatively low, within these experimental conditions. The heat transfer
coefficient was well correlated in terms of dimensionless groups as well as operating variables. 相似文献
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A simple formula is provided to estimate viscosity of glass using parallel plate viscometry well above 108 Pa·s, which is the upper limit of the recommended range. The formula is based on computational studies that account for viscoelastic material behavior and frictional slip that justify using linear interpolation to estimate viscosity between established upper and lower bounds. The formula accounts for variations in friction coefficient and cylinder aspect ratio for viscosity from 107 to 1011 Pa·s. 相似文献