|Environmental technology & Fluidization technology|
|Development of CO2 Removal Process in Power Plant|
|Recently, high efficient CO2 absorption ceramic particles have been developed at the industry in Japan. When the particles are utilized at the effluent process in power plants, the CO2 emission to atmosphere can be reduced. We design the characteristics of the particles and the suitable process.|
|Sterrization using opt-catalyst particles fluidization|
|For drinking water, sterrized water for hospital and recycle water in hot springs, the technology of water sterrization is very important. In this study, using infra-violet light as well as optcatalyst to sterrize, a novel sterrization reactors are developped.|
|Methane fermentation process utilizing unaerobic active sludge|
|To develop more effective organic efluent waste water treatment process, a novel unaerobic active sludge is utilized.|
|Gas-Solid Fluidization and Pressure Profile in Circulating Fluidized Bed|
|Circulating fluidized beds are often used as boilers and FCC process due
to good combustion efficiency and reactivity. When the circulating fluidized
bed is utilized as a gas-solid catalytic reactor, it is important that
reactant gases react stably enough with solid catalyst because of constant
composition and yield of products.
So, it is necessary to control quantitatively the feed rate of gaseous reactants and catalytic particle in reactor. Although the control of gas flow rate is not so difficult, the solid particle circulation rate cannot be operated quantitatively enough. There are two principal techniques to control particle flow rate in circulating fluidized bed.
When the catalytic reaction can be separated into consumption and regeneration of catalyst activity, the twin-column circulating fluidized bed system can be utilized to recycle catalysts continuously.
In this study, to design a J-shaped pneumatic valves to control solid particle circulation flow rate, the effect of operating parameters on particle flow rate, pressure drop and gas entrainment through the J-valve was investigated experimentally.
|Aerobic Xanthan Production by Xanthomonas campestris|
|Development of Bioreaction Tower for Bioproducts Having Yield Stress|
n food industries, many kinds of thickeners are produced biologically. For xanthan fermentation, which is one of important products, a stirred tank bioreactor is usually used to keep the oxygen transfer rate up to the demand of aerobic bacterium. However, the local stagnant zone in which oxygen transfer is limited was observed in the stirred tank because of the yield stress. On the other hand, the bubble column has good mixing performance under slug flow operation for high concentration of xanthan aqueous solutions, so that the stagnant zone is little.
In this study, the characteristics of the oxygen transfer into highly viscous non-Newtonian liquids having yield stress in bubble columns were investigated to develop an optimum bubble column fermentor for viscous aerobic cultivation.
Due to the yield stress, the small bubbles could not escape from liquid and they were stagnant. On the other hand, the large slug bubbles, which were observed over the almost all operating range in this work, were rising smoothly without coalescence or breakage after they had been accelerated upward just above a gas distributor. The escapable gas holdups increased with increasing superficial gas velocity and decreasing the column diameter. They were estimated well by the modified equation of Nicklin et al. The effect of apparent viscosity of liquids on gas holdup was hardly observed under the operating conditions.
|Development of Soft Material with Multi-Gas Channels|
|Development of Bubble Column with Draft Tube Circulated Forcibly Liquid|
|In the case of mass transfer into highly viscous liquids by using an internal airlift bubble columns, the performance is reduced. Because the friction between the walls in the column and liquids increases with increasing viscosity. In this study, therefore, the screw type propeller was set in the draft tube. By revolving the propeller, the viscous liquid was forced to circulate in the bubble column. The mass transfer coefficient increased with forced circulation rate of liquid.|
|Gas distribution into liquid phase|
|Research on Micro-bubbles for Novel Chemical Processes.|
|Micro-bubbles has a great different characteristics from standard size
bubbles. So we are developing a novel chemical processes.
|Development of Waste Water Treatment Using Micro-bubbles|
|Evaluation of Microbubble Distributors for Industrial Uses.|
|Development of Novel Functional Materials Containing Microbubbles|
|Development of Novel Microbubble Generators|
|Development of Microbubble Removers|
|Simulation of Liquid Velocity Profile around a Single Rising Bubble in Liquid by CFD|
|Bubble Formation from a Nozzle in Shear Liquid Flow|
|To distribute gas phase in liquid phase, an aerated stirred tank reactor
Is usually used in industry, in which the gas phase was crushed by the
Attrition with the blade of impeller. To evaluate the performance of the
reactor, the estimations of bubble size and bubble size distribution are
essential. However, it is very difficult at the present because of too
complicated mechanism of bubble breakage around the impeller.
In this study, therefore, the bubble formation mechanism in simple shear flow conditions was investigated.
The revolving cylindrical rotator was set at the axis on the cylindrical vessel in which the viscous liquid is filled. By revolution of the rotator, the smooth liquid profile was generated in the annual path in the vessel. The bubbles distribute from a horizontal nozzle was deformed strongly by the shear flow. When the uniform bubbles are dispersed in liquid, the bubble volume was measured by the pressure fluctuation in the gas chamber. The bubble size decreased with increasing shear rate. To control the shear rate of the edge of the nozzle, the bubble size can be controlled.
|Downward Bubble Formation in Downstream of Liquid|
|When the termical velocity of a bubble is slower than downward liquid velocity, the bubble flows downward along the liquid flow. In the cases of some gas-liquid operations, gas was downward blown into liquid. In this study, the mechanism of bubble formation at the end of nozzle inserted vertically into the bubble column.|
|Bubble Formation in Viscous non-Newtonian Liquids Having Yield Stress|
|Some foods such as mayonnaise and dressing for salad have strange characteristics,
i.e., YIELD STRESS or zero-shear stress. The yield stress is sometimes
increasing the taste of foods. Some liquidized foods are produced by fermentation.
When the culture liquid has an yield stress, the small bubbles whose buoyant force is smaller than the yield stress cannot rise in the liquid in aerobic fermentors. So, if too small bubbles are distributed in the bubble column, the flooding will be occurred.
In this study, to estimate the bubble size at the gas distributor, the non-spherical bubble formation model was proposed.
|Visualization of Gas Flow in Two-dimensional Bubble|
|To investigate the gas flow in the bubble during bubble formation at the
nozzle, the smoke tracer was used. The smoke was inputted with air into
the bubble growing in a 2D-bubble column so that the image of bubble growth
was photographed using a high-speed video camera with laser beam visualizer.
The smoke tracer was circulated along the gas-liquid interface in the bubble.
|Mechanism of Gas Absorption and Reaction from NH3 Gas Bubble Formation in Water|
|To investigate the mechanism of gas absorption from a bubble containing
soluble and insoluble components, a gaseous mixture of ammonia and nitrogen
was bubbled into water.
The bubble volume decreased with the increasing composition of ammonia in a bubble, decreasing gas chamber volume and decreasing gas flow rate.
The non-spherical bubble formation model combined with the overall mass transfer resistance estimated well experimental bubble shape, bubble volume at its detachment from an orifice, growth rate and mass transfer rate. Moreover, the change of concentration with bubble growth time and the fractional absorption during bubble formation were simulated.
|Measurement of Heat Transfer Coefficient for Direct Contact Condensation|
|When the vapor constant directly coolant and then it condenses with heat transfer, the heat transfer coefficient is much larger than the standard coefficients. The direct-contact heat transfer coefficient is usually neglected. When the very fast phenomena of vapor bubble condensation are simulated, however, those values become very important.|
|Two-phase Bubble Formation from a Nozzle with Condensation|
|When the vapor gas is brown into the immiscible liquid, the bubble is expanding with condensation. If the expansion rate is smaller than condensation rate, the bubble or drop cannot be generated. The phenomena of generation of two-phase bubbles are often observed in the direct-contact heat exchanger. In this study, to produce homogeneous sized liquid droplets, the condensable vapor bubbles are generated constantaneously from a nozzle in a bubble column. at first. Then, by controlling liquid temperature, the size-controlled vapor bubbles are condensed and become droplets. The droplet size is uniform when the specific operating conditions are maintained.
Publiched in News paper, 18 Jul. 2000
|Gas-Liquid Separation from Liquid Phase under Microgravity|
|Left picture: The water flows homogeneously the left side to right side under the ground condition. Bubbles were inputted from three nozzles whose orifice is directed to the downstream. Of course, by the buoyant force, all bubbles rise upward.|
|Left picture: The experimental conditions are same as the upper picture except for the gravity. The equipments were capsuled and dropped into the drop shaft of JAMIC in Hokkaido, Japan, to obtain micro gravity for 10 seconds. The bubbles could not rise in the liquid so that the size of bubbles increased and the bubble shape became spherical.
Published in Newspape, 25 Jul. 2000
|Bubble Formation in Liquid under Microgravity|
|The water is filled in the three neighborhood cells. The gas is blown into water through three downward nozzles. The bubbles rise instantaneously after the detachment from the nozzles under terrestrial gravity.|
|On the other hand, in the case of micro gravity, the bubbles became spherical and never detach from the nozzles.|
|On-line Measurement and Simulation of Shape, Velocity and Interface area of Rising Single Bubble|
|The studies on bubble shape were usually carried out by picture analysis
method using still camera, digital camera and high speed video camera. However,
by those methods, the bubble size, shape and rising velocity could not
measured on real-time so it was difficult to get a lot of data within a
reasonable experimental time. Moreover, if the bubble shape is complicated
three-dimensionally, only the 2-dimensional shape of the bubble is available.
In this study, by using some laser sensors, the 3-dimensional bubble shape, bubble surface area, bubble volume and bubble rising velocity are measured at the real-time. The coordinates of the bubble surface are recorded of the digital file so that those data can input instantaneously to the CFD software.
By this system, it is very useful and convenient to analyze the bubble behavior.
|Simulation of liquid velocity profile around a single rising bubble in liquid by CFD|
|By the combination of experimental work and computational technology, the flow dynamics around a rising bubble were simulated|
|Reactor Design by Non-Spherical Bubble Formation Model and CFD Simulators|
The non-spherical bubble formation model was proposed by Pinczewski at first. Then, Terasaka modified it and developed for various purposed. At the present, the non-spherical bubble formation model can estimate the various non-Newtonian system, constant flow condition, micro gravitational system, reactive gas system, high pressure system, flowing liquid system, vapor condensation system and liquid-liquid system. When the gas distributor will be designed, the estimation by the model is very useful.