Heat transfer performance improvement by fin and groovs is studied for condensation of R-11 on integral-fin tubes. Eight tubes with trapczodially shaped integral-fins having fin density from 748 to 1654fpm(fin per meter) and 10, 30 grooves are tested. A plain tube having the same diameter as the finned tubes is also used for comparison. R-11 condensates at saturation state of 32 ℃ on the outside tube surface coded by inside water flow. All of test data are taken at steady state. The heat transfer loop is used for testing singe long tubes and cooling is pumped from a storage tank through filters and folwmeters to the horizontal test section where it is heated by steam condensing on the outside of the tubes. The pressure drop across the test section is measured by menas pressure gauge and manometer. The results obtained in this study is as follows : 1. Based on inside diameter and nominal inside area, overall heat transfer coefficients of finned tube are enhanced up to 1.6 ~ 3.7 times that of a plain tube at a constant Reynolds number. 2. Friction factors are up to 1.6 ~ 2.1 times those of plain tubes. 3. The constant pumping power ratio for the low integral-fin tubes increase directly with the effective area to the nominal area ratio, and with the effective area diameter ratio. 4. A tube having a fin density of 1299fpm and 30 grooves has the best heat transfer performance.

Flow and heat transfer characteristics of gas, and trajectories and cooling characteristics of droplets/particles in a gas atomizer were investigated by a numerical simulation using FLUENT code. Among several kinds of solution method, the k- turbulent model, power-law scheme, SIMPLE algorithm is adopted in this study. Momentum and heat exchange between a continuous phase(gas) and a dispersed phase(particle) were taken into account. Particle trajectories are simulated using the Lagrangian method, and Rosin-Rammler formula is used for the particle size distribution. Streamlines, velocities and pressures of gas, and trajectories, velocities and cooling rates of particles have been investigated for the various gas inlet conditions. Small but very intensive recirculation is found just below the melt orifice, and this recirculation seems to cause the liquid metal to spread radially. Particle trajectory depends on the particle size, the location of particle formation and the turbulent motion of gas. Small particle cools down rapidly, while large diameter particles solidify slowly, and this is mainly due to the differences in thermal inertia.

The heat transfer performance of R - 11 vapor condensing on integral fin tubes has been studied using fin tubes having the fin density from 748 to 1654 fins per meter. Electric heater supplied heat energy to the boiler to generate R - 11 vapor over the range of 25-60W. Condensation rates of each tubes were tested under the condition of cooling water flow rate from 400l/h to 2500l/h. For the seven fin tubes tested, the best performance has been obtained with a tube having a fin density of 1417fpm and a fin height of 1.3mm. This tube has yielded a maximum value of the heat transfer coefficient of 16500W/m2K, at a vapor to wall temperature difference of 3K. Experimental results of integral fin tubes have been compared with available predictive models such as Beatty - Katz's analysis, Webb's analysis, Sukhatme's analysis and Rudy's empirical relation. The experimental results were shown to be in good agreement with that of the Sukhatme's analysis.

보일러 및 연소로 등에서의 부유체 환경에서 입자와 벽면 사이의 열전달 현상을 규명하기 위한 수치적인 모델링을 행하였다. 본 연구에서는 벽면에 수직 충돌하는 입자에 의한 열전달 현상을 알아보기 위해 2차원 모델을 사용하였다. 입자표면에서 단열된 경계조건과 등온의 경계조건을 사용한 결과를 비교함으로써, 입자가 벽면에 충돌할 때 유체를 매개로한 전도와 입자에 의해 야기된 대류 현상을 비교할 수 있었다. 계산 결과, 입자가 벽면에 충돌하기 직전에는 입자 크기의 반정도의 거리에 도달할 때까지는 입자의 영향이 별로 없고, 충돌하고 난 후에 영향이 많았다. 또한, Pe 수가 작을 때는 유체를 매개로 한 전도가 지배적이며, Pe 수가 증가할수록 야기된 대류의 효과가 점차 증가하였다

3차원 실내공간의 상부에서 일정유속이 유입하여 양측면 하부쪽으로 유출될 경우, 책상형의 가열 장애물 영향에 의한 유동장의 변화와 온도분포를 수치계산 한 결과 다음과 같은 결론을 얻었다. (1)표준 k-ε 2 방정식 모델로 난류유동장을 해석한 결과 장애물을 기준으로 상하부에는 독립적인 큰 재순환 영역이 존재함을 알 수 있었다. (2) 유입류의 속도 변화에 따른 전제적인 유동패턴은 큰 변화없이 상사적인 분포를 하는 것을 알 수 있었다. (3) 유입속도가 감소함에 따라서, 공간에 대한 발열체의 온도영향이 커진다. (4) Re수가 작은 범위 (10 상(4)-10 상(5)에서는 열전달이 급격히 상승하여, Re수가 10 상(5)이상이 도면 열전달이 거의 일정하다.

This work studies for boiling and condensation heat transfer performance of trapezoidally shaped integral-fin tubes having fin densities from 748fpm to 1654fpm. For comparison, tests are made using a plain tube having the same inside and outside diameter as that of the root of fins of finned tubes. Hahne's theoretical model and Webb's theoretical model are used to predict the R-11 boiling heat transfer coefficient and condensing heat transfer coefficient respectively for plain tube and all integral-fin tubes. Experiments are carried out using R-11 as working fluid. This work is limited to film-wise condensation and pool boiling on the outside surface of plain tube and 4 low integral-fin tubes. In case of condensation, the refrigerant condenses at saturation state of 32℃ on the outside tube surface cooled by coolant and in case of boiling. the refrigerant evaporates at saturation state of 1bar on the outside tube surface. The amount of non-con-densable gases in the test loop is reduced to a negligible value by repeated purging. The actual boiling and condensing processes occur on the outside tube surfaces. Hence the nature of this surface geometry affects the heat transfer performances of condenser and evaporator in refrigerating system. The condensation heat transfer coefficient of integral-fin tube is enhanced by both extended tube surface area and surface tension. The ratio of the condensation heat transfer coefficients of finned to plain tubes is greater than that of surface area of finned to plain tubes, while ratio of the boiling heat transfer coefficient of finned to plain tubes shows reverse result. As a result, low integral-fin tube can be used in condenser more effectively than used in evaporator.

Experiments of quenching were made with cylindrical specimens of carbon steel S45C of diameters from 12 to 30mm were performed. The specimens were heated by electric furnace and quenched by immersion method. In order to analyze the temperature profile(cooling curves) of carbon steel including the latent heat of phase transformation, nonlinear heat conduction problem was calculated by the numerical method of inverse heat conduction problem using the apparent heat capacity method. The difference between the calculated and the experimented cooling curves was caused by the latent heat of phase transformation, and the effects of the latent heat were especially manifest at the cooling curves of center of specimens. The temperature and the quantity of the latent heat of phase transformation depend on the cooling speed at A sub(1) transformation point, and the region for cooling speed to become zero was caused by the latent heat of phase transformation.

수평관내 증기분무류의 응축열전달에 관하여 실험을 행하고 상당 Reynolds수를 근거로한 열전달효과와의 비교에서 그 결과를 요약하면 다음과 같다. 1. 관내 응축증기 분무류일 경우의 벽면전단응력의 식은 다음과 같이 쓸 수 있다. root(τ하(0)/τ하(0v))=1+1.46X 하(tt) 상(0.20). 2. 분무류의 응축열전달효과가 상당 Reynolds수에 의한 값보다 대체로 낮게 나타난 이유는 관내 반경 및 길이방향의 불균일한 액막형성에 의한 Reynolds수 측정값의 차이 때문이다. 3. 분무류의 응축열전달효과에 의한 N sub(u)의 값은 다음과 같다. N 하(u)=1.08×[σ 하(l) d/μ 하(l)/δ+(2.5/P 하(rl)) ln(y 하(i)/δ)]×τ 하(0)/ σ 하(l) 상(1/2)