Absorption in vertical stream tubes with swirl bodies

1983 ◽  
Vol 48 (3) ◽  
pp. 854-860
Author(s):  
Kurt Winkler ◽  
František Kaštánek ◽  
Freimut Storz ◽  
Jan Kratochvíl ◽  
Antonín Havlíček
Keyword(s):  
Mass Transfer ◽  
Transfer Coefficient ◽  
Mass Transfer Coefficient ◽  
Mixing Conditions ◽  
Two Phase ◽  
Liquid Load ◽  
Interfacial Areas ◽  
Experimental Values ◽  
Superficial Gas Velocity ◽  
Vertical Tubes

The absorption of oxygen from air into water has been measured in vertical tubes with swirl bodies in the inlet part. The tubes were of 70 mm I.D. and of height H with diameter ratio H/D ≦ 22. The two-phase flow was directed upward. Superficial gas velocity was ωG = 10 to 35 m s-1 and specific liquid load QLE = 13 to 80 m3m-2h-1. Values of the liquid-side mass transfer coefficient were determined as ratios of experimental values of volumetric mass transfer coefficient and specific interfacial areas, which were measured earlier. Murphree efficiencies were obtained with experimentally determined Peclet numbers considering the real mixing conditions of the liquid phase.

The gas side mass transfer coefficient in the turbulent flow in a packing with a significant dependence of the interfacial area on the density of irrigation

1984 ◽  
Vol 49 (12) ◽  
pp. 2756-2762
Author(s):  
Jan Červenka ◽  
Václav Kolář
Keyword(s):  
Mass Transfer ◽  
Transfer Coefficient ◽  
Mass Transfer Coefficient ◽  
Gas Flow ◽  
Interfacial Area ◽  
Two Phase ◽  
Expanded Metal ◽  
Significant Dependence ◽  
Experimental Values ◽  
Density Of Irrigation

A theoretically derived relationship has been applied for the gas-side mass transfer coefficient to experimental values of kG. The experimental data have been obtained under the two-phase flow of gas and liquid in a plane vertical packing manufactured of the expanded metal sheet. This packing exhibits a significant dependence of the extent of interfacial area, and hence the geometry of the channel available for gas flow, on the density of irrigation.

scholarly journals Hydrodynamics and Mass Transfer in a Concentric Internal Jet-Loop Airlift Bioreactor Equipped with a Deflector

Energies ◽  
2021 ◽  
Vol 14 (14) ◽  
pp. 4329
Author(s):  
Radek Šulc ◽  
Jan Dymák
Keyword(s):  
Mass Transfer ◽  
Transfer Coefficient ◽  
Mass Transfer Coefficient ◽  
Liquid System ◽  
Gas Holdup ◽  
Gas Velocity ◽  
Liquid Phase Mass Transfer ◽  
Homogenization Time ◽  
Standard Design ◽  
Superficial Gas Velocity

The gas–liquid hydrodynamics and mass transfer were studied in a concentric tube internal jet-loop airlift reactor with a conical bottom. Comparing with a standard design, the gas separator was equipped with an adjustable deflector placed above the riser. The effect of riser superficial gas velocity uSGR on the total gas holdup εGT, homogenization time tH, and overall volumetric liquid-phase mass transfer coefficient kLa was investigated in a laboratory bioreactor, of 300 mm in inner diameter, in a two-phase air–water system and three-phase air–water–PVC–particle system with the volumetric solid fraction of 1% for various deflector clearances. The airlift was operated in the range of riser superficial gas velocity from 0.011 to 0.045 m/s. For the gas–liquid system, when reducing the deflector clearance, the total gas holdup decreased, the homogenization time increased twice compared to the highest deflector clearance tested, and the overall volumetric mass transfer coefficient slightly increased by 10–17%. The presence of a solid phase shortened the homogenization time, especially for lower uSGR and deflector clearance, and reduced the mass transfer coefficient by 15–35%. Compared to the gas–liquid system, the noticeable effect of deflector clearance was found for the kLa coefficient, which was found approx. 20–29% higher for the lowest tested deflector clearance.

Study on the Gas-Liquid Two-Phase Flow Two-Phase Flow Characteristics of Carbon Dioxide Removal by Membrane Method

2011 ◽  
Vol 347-353 ◽  
pp. 1797-1800
Author(s):  
Yan Chao Li ◽  
Zhi Wu Hao ◽  
Xian Ping Zeng ◽  
Fang Qin Li ◽  
Jian Xing Ren
Keyword(s):  
Mass Transfer ◽  
Transfer Coefficient ◽  
Mass Transfer Coefficient ◽  
Flue Gas ◽  
Total Mass ◽  
Hollow Fiber Membrane ◽  
Flue Gases ◽  
Fiber Membrane ◽  
Shell Side ◽  
Two Phase

In this paper, membrane absorption method was introduced. Analyzed and studied flue gases passing in the shell side (hollow fiber membrane) and in the pipe side (membrane lumen) respectively. Total mass transfer coefficient and de CO2 efficiency were calculated. For flue gases passing in the pipe side, total mass transfer coefficient was 1.1191×10-4m/s and de CO2 efficiency was 73.8%; while for flue gases passing in the shell side, total mass transfer coefficient was 3.4701×10-4m/s and de CO2 efficiency was 98.0%. The results showed that the flow of flue gas flowing in the lumen is better than the flow of flue gas flowing out of the hollow fiber membrane from the point of views of removal rate and mass transfer. To build de CO2 experimental devices, flow of flue gas flowing in the pipe side was proposed.

Errors in Measurement of Interfacial Area and Mass Transfer Coefficient in Liquid in Apparatus with Mobile Packing

1993 ◽  
Vol 58 (6) ◽  
pp. 1345-1353
Author(s):  
Zdeněk Palatý
Keyword(s):  
Mass Transfer ◽  
Transfer Coefficient ◽  
Mass Transfer Coefficient ◽  
Interfacial Area ◽  
Solution Temperature ◽  
Adsorption Solution ◽  
Specific Interfacial Area ◽  
Interfacial Areas ◽  
Error Of Measurement

The paper deals with an analysis of errors of measurement of interfacial area and mass transfer coefficient in liquid in an absorber with mobile packing. The system of CO2-NaOH has been used for the testing with recirculation of the adsorption solution. The error of measurement of the absorption solution temperature, CO2 concentration in the gas, the composition of absorption solution, the mass transfer coefficient in gas, and the volume of absorption solution at the beginning and at the end of the measurement have been investigated with regard to their effects upon the resulting values of specific interfacial area and mass transfer coefficient in liquid. From the simulation calculations if follows that the interfacial areas most strongly affected by the error of measurement of CO2 concentration in gas, whereas the mass transfer coefficient in liquid is considerably affected by inaccuracies in measuring the volume of absorption solution at the beginning and at the end of experiment.

Mass Transfer Coefficient behind an Orifice in Two-phase Flow

2016 ◽  
Vol 2016.21 (0) ◽  
pp. D114
Author(s):  
Takayuki YAMAGATA ◽  
Hidefumi TSURUTA ◽  
Yuhei NISHII ◽  
Nobuyuki Fujisawa ◽  
Fumio INADA
Keyword(s):  
Mass Transfer ◽  
Transfer Coefficient ◽  
Mass Transfer Coefficient ◽  
Two Phase Flow ◽  
Phase Flow ◽  
Two Phase

Mass transfer coefficient for two-phase countercurrent flow in a packed column with a novel internal

2004 ◽  
Vol 99 (3) ◽  
pp. 273-277 ◽  
Author(s):  
Yanhui Yuan ◽  
Minghan Han ◽  
Lunwei Wang ◽  
Dezheng Wang ◽  
Yong Jin
Keyword(s):  
Mass Transfer ◽  
Transfer Coefficient ◽  
Mass Transfer Coefficient ◽  
Packed Column ◽  
Countercurrent Flow ◽  
Two Phase

Effect of Vibrating Sparger on Mass Transfer, Gas Holdup, and Bubble Size in a Bubble Column Reactor

2013 ◽  
Vol 11 (1) ◽  
pp. 47-56 ◽  
Author(s):  
Laleh Hadavand ◽  
Ali Fadavi
Keyword(s):  
Mass Transfer ◽  
Transfer Coefficient ◽  
Mass Transfer Coefficient ◽  
Vibration Frequency ◽  
Bubble Size ◽  
Bubble Column ◽  
Gas Holdup ◽  
Bubble Column Reactor ◽  
Gas Velocity ◽  
Superficial Gas Velocity

Abstract Bubble size has a key role in gas holdup and mass transfer in bubble column reactors. In order to have small and uniform bubbles, a new structure was designed; the reactor operates in two modes, with vibrating sparger and conventional bubble column in which sparger is fixed. In vibrating mode, the sparger vibrates gently during gas entering. The vibrating sparger performs like a paddle, resulting in a forced recirculation of gas–liquid inside the reactor; moreover, the bubble detachment is accelerated. The superficial gas velocity was between 0.003 and 0.013 ms− 1, and the vibration frequency was changed between 0 and 10.3 Hz. The bubble size was measured at three various positions of the reactor height by photographic method and using MATLAB 7.0.1 software. The mass transfer coefficient was determined by means of the dynamic gassing-out method. The results show that the bubbles were bigger in vibrating mode than those working without vibration. The bubble size decreases with increase in height from sparger. Gas holdup increased with increase in superficial gas velocity and vibration frequency. The effect of vibration increased the gas holdup with an average of 70% for all superficial gas velocities. Volumetric mass transfer coefficient was almost stable as vibration frequency increased.

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