• 한국환경과학회지
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• 제5권1호
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• pp.93-102
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• 1996

Hydrodynamic characteristics such as gas holdup, liquid circulation velocity and bed expansion in a hexagonal inverse fluidized bed were investigated using air-water system by changing the ratio ($A_d$/$A_r$) of cross-sectional area between the riser and the downcomer, the liquid level($H_1$/H), and the superficial gas velocity($U_g$). The gas holdup and the liquid circulation velocity were steadily increased with the superficial gas velocity increasing, but at high superficial gas velocity, some of gas bubbles were carried over to a downcomer and circulated through the column. When the superficial gas velocity was high, the $A_d$/$A_r$ ratio in the range of 1 to 2.4 did not affect the liquid circulation velocity, but the maximum bed expansion was obtained at $A_d$/$A_r$ ratio of 1.25. The liquid circulation velocity was expressed as a model equation below with variables of the cross-sectional area ratio($A_d$/$A_r$) between riser to downcomer, the liquid level($H_1$/H), the superficial gas velocity($U_g$), the sparser height[(H-$H_s$)/H], and the draft Plate level($H_b$/H). $U_{ld}$ = 11.62U_g^{0.75}$${(\frac{H_1}{H})}^{10.30}$${(\frac{A_d}{A_r})}^{-0.52}$${(\frac({H-H_s}{H})}^{0.91}$${(\frac{H_b}{H})}^{0.13}$

• Journal of Advanced Marine Engineering and Technology
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• 제29권4호
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• pp.377-383
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• 2005

This paper deals with the flow characteristics of air-water two-phase flow in a vertical tube of 10mm I.D. and 600mm in length at an adiabatic condition. The obtained experimental data were covered with the liquid superficial velocity ranging from 0.095m/s to 2.56m/s. and the gas superficial velocity ranging from 0.032m/s to 21.08m/s. The effects of the gas and liquid superficial velocity on the flow pattern transitions, frictional pressure drop, and film thickness and gas-liquid interface roughness were also examined. It was found that the film thickness increased and the liquid film wave length was more longer with the liquid superficial velocity $j_L$ increasing at $j_G$ constant. It was also showed that the frictional pressure drops were experienced in three regions. namely increasing region(bubbly flow), decreasing region (Taylor bubble and slug flows) and re-increasing region (annular flow).

• 한국안전학회지
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• 제8권4호
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• pp.120-126
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• 1993

This work was carried out to investigate the effects of solid mass flow rate, mean particle diameter and mesh number of screen packing material on minimum carrying velocity, which defined as the superficial gas velocity of the upper limit of chocking phenomenon. Vertical pneumatic conveying was studied on a 4.6cm 1. D. pipe, 180cm in length. Experiments were performed in both the empty and the screen-packed pipe. It was also examined the effect of superficial gas velocity, solid mass flow, mean particle diameter, and mesh number of packing material on pressure drop. Minimum carrying velocity in screen packed-pipe was lower than that in an empty pipe. besides minimum carrying velocity was decreased with increase in mesh number of screen packing material. The pressure drop In vortical packed-pipe was Increased with superficial gas velocity, mean particle diameter, and mesh number of screen packing material.

• 한국신재생에너지학회:학술대회논문집
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• 한국신재생에너지학회 2009년도 춘계학술대회 논문집
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• pp.876-879
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• 2009

Fischer-Tropsch 합성 반응과 같은 slurry bubble column reactor에서는 반응 속도를 증진시키기 위해서는 서로 다른 상간의 접촉 면적을 최대화함으로써 물질 전달을 원활하게 유지하여야 한다. 특히 Fischer-Tropsch 합성 반응에서는 반응물인 기체가 촉매로서 기능하는 고체 표면으로의 external mass transfer가 효과적으로 이루어져야 하기 때문에 반응기 내의 기체의 거동뿐만 아니라 고체인 촉매의 분포에 대한 연구가 활발하게 이루어지고 있다. 따라서 본 연구에서는 반응기 내에 기체의 superficial velocity를 변화시키면서 기체의 hold up 뿐만 아니라 고체 입자의 분포특성에 대하여 관찰하였다. Superficial velocity가 증가함에따라 gas hold up의 경우, 일정하게 증가하다가 6 cm/sec 이상에서 그 증가폭이 감소하였다. 즉 6 cm/sec이상에서 turbulent flow regime을 형성하였다. 또한 고체입자의 분포 역시 기체의 superficial velocity가 증가함에따라 보다 균일하게 되는 것을 확인할 수 있었다.

• 한국환경과학회지
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• 제6권1호
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• pp.25-31
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• 1997

The variations of gas hold-up, overall volumetric oxygen mass transfer coefficients and liquid circulation velocity in an internal loop reactor were investigated to manifest scale-up effect. The relationship between superficial gas velocity and gas hold-up were found as Ugr = 0.045 $\varepsilon$r in the pilot-scale and Ugr = 0.056 $\varepsilon$r in the bench-scale reactor. The overall volumetric oxygen mass tractsfer coefficient, KLa was slightly increased in the pilot-scale than in the bench-scale reactor. Flow regime was changed from the bubble flow to the churn-turbulent flow when the superficial gas velocity reached to 3.5 - 4 cm/sec in the pilot-scale.

• 설비공학논문집
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• 제19권6호
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• pp.441-446
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• 2007

An experimental study on the countercurrent two-phase flow in narrow rectangular channels has been peformed. Countercurrent flow limitation (CCFL) was investigated using air and water in 760mm long, 100mm wide, vertical test sections with 1 and 3mm channel gaps. Tests were systematically performed with downward liquid superficial velocities and upward gas velocities covering 0 to 0.125 and 0 to 3.5m/s ranges, respectively. As the gap width of rectangular channel increased the CCFL water superficial velocity decreased for the given air superficial velocity. Slight increase of the air superficial velocity resulted in the abrupt decrease of water velocity when $j_g=2{\sim}4m/s$. The critical superficial velocity of air, at which the downward flow of water was no longer allowed, also decreased with the increase of gap width. The experimental results were compared with the previous correlations, which were mainly for round tubes, and the qualitative trends were found to be partially acceptable. However the quantitative discrepancies were hardly neglected. New correlation of CCFL was developed and showed good agreement with the experimental data.

• 한국입자에어로졸학회지
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• 제13권2호
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• pp.79-85
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• 2017

실험실 규모의 유동층 반응기(Length=0.25m, Diameter=0.05m)에서 고부가가치 물질인 희유금속 산화물 $NiO/MoO_3/MoS_2$의 공탑속도에 따른 최소유동화 속도 및 압력손실 경향을 확인하였다. 시료의 L/D 1, 2, 3 변화에 따른 Superficial gas velocity 0.07~0.45 m/s 범위에서 $NiO/MoO_3/MoS_2$의 L/D 1, 2, 3에서의 평균 압력손실은 Decreasing flux에서 290~1952 Pa, Increasing flux에서 253~1925 Pa로 나타났다. Wen이 제시한 이론값과 실험데이터를 비교해본 결과, 0.021~0.36배 차이나는 것을 확인하였다. 이번 결과를 통하여, 희유금속 산화물을 실제 현상에서 적용 가능한 운전조건을 결정할 수 있었다.

• Environmental Engineering Research
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• 제19권4호
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• pp.345-354
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• 2014

In this paper, effects of physical configurations and operating conditions on bubble column performance were analyzed in terms of bubble hydrodynamic and mass transfer parameters. Bubble column with 3 different dimensions and 7 gas diffusers (single / multiple orifice and rigid / flexible orifice) were applied. High speed camera and image analysis program were used for analyzing the bubble hydrodynamic parameters. The local liquid-side mass transfer coefficient ($k_L$) was estimated from the volumetric mass transfer coefficient ($k_La$) and the interfacial area (a), which was deduced from the bubble diameter ($D_B$) and the terminal bubble rising velocity ($U_B$). The result showed that the values of kLa and a increased with the superficial gas velocity (Vg) and the size of bubble column. Influences of gas diffuser physical property (orifice size, thickness and orifice number) can be proven on the generated bubble size and the mass transfer performance in bubble column. Concerning the variation of $k_L$ coefficients with bubble size, 3 zones (Zone A, B and C) can be observed. For Zone A and Zone C, a good agreement between the experimental and the predicted $K_L$ coefficients was obtained (average difference of ${\pm}15%$), whereas the inaccuracy result (of ${\pm}40%$) was found in Zone B. To enhance the high $k_La$ coefficient and absorption efficiency in bubble column, it was unnecessary to generate numerous fine bubbles at high superficial gas velocity since it causes high power consumption with the great decrease of $k_L$ coefficients.

• Korean Chemical Engineering Research
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• 제55권5호
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• pp.698-703
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• 2017

Bubble flow characteristics in fluidized beds were analyzed by CPFD simulation. A fluidized bed, which had the size of $0.3m-ID{\times}2.4m-high$, was modeled by commercial CPFD $Barracuda^{(R)}$. Properties of bed material were $d_p=150{\mu}m$, ${\rho}_p=2,330kg/m^3$, and $U_{mf}=0.02m/s$. Gas was uniformly distributed and the range of superficial gas velocity was 0.07 to 0.16 m/s. Two other geometries were modeled. The first was a three-dimensional model, and the other was a two-dimensional model of $0.01m{\times}0.3m{\times}2.4m$. Bubble size and rising velocity were simulated by axial and radial position according to superficial gas velocity. In the case of three-dimensional model, simulated bubble rising velocity was different from correlations, because there was zigzag motion in bubble flow, and bubble detection was duplicated. To exclude zigzag motion of bubble flow, bubble rising velocity was simulated in the two-dimensional model and compared to the result from three-dimensional model.

• Korean Chemical Engineering Research
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• 제52권4호
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• pp.516-521
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• 2014

고점성이며 낮은 표면장력 매체로 구성된 기포탑에서 축방향 국부 열전달 계수와 총괄 열전달 계수에 대해 고찰하였다. 기체공탑유속(0.02~0.10 m/s), 액체 점도($0.1{\sim}0.3Pa{\cdot}s$) 그리고 액체 표면장력($66.1{\sim}72.9{\times}10^{-3}N/m$)이 국부 및 총괄 열전달 계수에 미치는 영향을 검토하였다. 열전달 영역은 기포탑 내부 열원과 기포탑 간의 열전달계로 구성하였다. 즉, 기포탑의 중앙에 수직 열원을 설치하여 내부 열원으로 하였다. 열전달 계수는 주어진 운전조건에서 열원에 제공되는 열량과 내부 열원과 기포탑 간의 온도차를 연속적으로 측정하여 결정하였다. 국부 열전달 계수는 기체공탑유속이 증가함에 따라 증가하였으나 기체 분산판으로 부터의 축방향 거리가 증가함에 따라, 액체의 표면장력이 증가함에 따라 감소하였다. 총괄 열전달 계수는 기체공탑유속이 증가함에 따라 증가하였으나 액상의 점도와 표면장력이 증가함에 따라서는 감소하였다. 총괄 열전달 계수는 기체공탑유속, 액상의 점도와 표면장력의 함수로 상관계수 0.91의 상관식을 얻을 수 있었으며 넛셀 수, 레이놀즈 수, 플란틀 수 그리고 웨버 수의 함수로 상관계수 0.92의 상관식으로 나타낼 수 있었다. $$h=2502U^{0.236}_{G}{\mu}^{-0.250}_{L}{\sigma}^{-0.028}_L$$ $$Nu=325Re^{0.180}Pr^{-0.067}We^{0.028}$$.