중공사형 정밀여과(MF)와 한외여과(UF)를 포함한 가압식 막여과 시스템은 높은 수준의 병원균 제거 효율로 인해 음용수 처리에 점점 더 많이 사용되고 있다. 그러나 가압식 막여과 시스템에서 분리막의 손상으로 인한 막완결성의 문제가 발생 시 병원체가 유출될 수 있으므로, 효과적인 온라인 또는 오프라인 방식의 막 완결성 모니터링 방법을 통해 수질의 안정성을 보장하여야 한다. 최근 막 완결성 시험 중 하나 인 압력손실시험(pressure decay test, PDT)이 가압식 분리막 모듈을 이용한 음용수 처리 시설에 적용되고 있다. 이 논문에서는 PDT의 기체 주입방법에 따른 세 가지 조건으로 원수 측, 여과수 측, 원수 여과수 양 뱡향 측 세 가지 조건을 선정 후 이에 따른 감지감도를 이론값과 실험값을 적용하여 비교하였다. 실험결과 가압되는 측의 부피와 감도는 반비례함을 확인하였고, 주입부의 반대방향에 부압을 형성 시에도 감도가 증가함을 확인할 수 있다. 즉 막 손상의 감 지감도는 주입되는 부분의 체적이 작아질수록, 분리막을 경계로 유입과 여과 측의 압력차가 클수록 높아짐을 알 수 있었다.

본 연구에서는 지름이 일정한 하나의 직선 관형 막을 가정하여 그 단위구간의 투과속도에 대한 물질수지를 세웠으며 이것을 기초로 하여 파이프의 정상상태 식과 함께 비선형 연립 2차 미분방정식을 이루었다. 이러한 관형 막의 압력손실을 표현한 연립방정식은 비선형이므로 Gauss-Seidel method와 같은 반복법에 의해서 해결될 수 있다. 이러한 수치해를 나타내기 위해 모사 알고리즘을 제시하였다. 또한 투과수는 운전 조건의 변화에 따라 변하므로 각 조건에서의 연립 방정식의 해를 수치적으로 적분하여 해결하였다. 모사의 결과를 검증, 해석하기 위해서 실제 중공사막과 유사한 관형 막을 사용하여 실험을 진행하였다. 본 연구에서는 중공사막을 유체가 흐를 때 발생하는 압력손실, 유량, 그리고 투과수의 관계를 분석적 방법을 이용해 제시하였고 이러한 이론적 기초를 바탕으로 실제 기공을 가진 막에 적용하여 그 정확성을 실험을 통하여 비교하였다.

가스상의 체적분율과 압력강하는 기액이상류에 대한 이해와 예측에 있어서 매우 중요한 인자이다. 또한 그것들은 산업용 대용량의 열교환시스템 및 선박에 설치되는 보일러 및 냉동시스템의 설계에 있어서 필수적인 항목이다. 따라서 본 논문에서는 파이프의 모든 경사각도에서 기액이상류 가스상의 체적분율과 압력손실을 예측할 수 있는 이론적 해석 방법을 제시한다. 여기서의 이론적 해석은 2유체 층상류 모델을 기초로 하고 있다. 또한 이론적 해석결과와 기존의 실험결과와 비교한 결과에 대해서도 제시한다.

본 연구에서는, 혈관 내 폐 보조장치를 설계할 때 혈액의 압력손실에 대한 영향을 받지 않는 최적의 설계조건을 찾기 위하여 압력손실을 예측할 수 있는 관계식을 유도하고자 하였다. 정맥 내경의 직경을 3 cm로 고정하고 삽입되는 중공사 개수의 변화에 따른 압력손실을 측정하였으며 실험에 의하여 얻어진 압력손실과 장치의 전면면적과의 상관관계를 curve fitting을 통하여 유도하였고, 유도되어진 관계식을 이용하여 정맥 내에 삽입되는 중공사 개수의 변화에 따른 압력손실을 예측하였다. 그리고 실험을 통하여 예측되어진 값과 비교 검토하여 유사성을 찾고자 하였다. 실험결과 장치에서 액체 유속의 변화에 따라 압력손실은 2차 함수 형태로 변화됨을 알 수 있었다. 또한 장치의 전면면적이 감소하면 압력손실은 증가하였고 충진율이 증가하면 압력손실도 증가함을 알 수 있었다. 장치 내에서의 압력손실에 대한 관계식을 장치의 전면면적과 충진율의 함수로 유도할 수 있었으며, 관계식에 의하여 압력손실을 예측할 수 있었다. 또한, 실험에 의한 압력손실과 비교하였을 때 유사한 경향성을 보여 줌으로써 압력손실 예측의 신뢰성을 얻을 수 있었다.

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.

With continuous industrial development, the types, and amount of particulate matter (PM) have been increasing. Since 2018, environmental standards regarding PM have become more stringent. Pulse air jet bag filters are suitable for PM under the 20㎛ and, can function regardless of size, concentration and type. Filtration velocity and shape are important factors in the operation and design of the pulse air jet bag filters however, few established studies support this theory. In this research, numerical simulations were conducted based on experimental values and, several methods were employed for minimizing the pressure drop. In the pilot system, as the inlet duct velocity was faster than 19 m/sec, flow was not distributed equally and, re-entrainment occurred due to the hopper directional vortex. The multi-inlet system decelerated the hopper directional vortex by 25 ~ 30% , thereby decreasing total pressure drop by 6.6 ~ 14.7%. The guide vane system blocked the hopper directional vortex, which resulted optimal vane angle of 53°. The total pressure of the guide vane system increased by 0.5 ~ 3% at 1.5 m/min conditions. However, the filtration pressure drop decreased by 4.8 ~ 12.3% in all conditions, thereby reducing the operating cost of filter bags.

In this study, pressure drop was measured in the pulse jet bag filter without venturi on which 16 numbers of filter bags (Ø140 × 850 ℓ) are installed according to operation condition(filtration velocity, inlet dust concentration, pulse pressure, and pulse interval) using coke dust from steel mill. The obtained 180 pressure drop test data were used to predict pressure drop with multiple regression model so that pressure drop data can be used for effective operation condition and as basic data for economical design. The prediction results showed that when filtration velocity was increased by 1%, pressure drop was increased by 2.2% which indicated that filtration velocity among operation condition was attributed on the pressure drop the most. Pressure was dropped by 1.53% when pulse pressure was increased by 1% which also confirmed that pulse pressure was the major factor affecting on the pressure drop next to filtration velocity. Meanwhile, pressure drops were found increased by 0.3% and 0.37%, respectively when inlet dust concentration and pulse interval were increased by 1% implying that the effects of inlet dust concentration and pulse interval were less as compared with those changes of filtration velocity and pulse pressure. Therefore, the larger effect on the pressure drop the pulse jet bag filter was found in the order of filtration velocity(Vf), pulse pressure(Pp), inlet dust concentration(Ci), pulse interval(Pi). Also, the prediction result of filtration velocity, inlet dust concentration, pulse pressure, and pulse interval which showed the largest effect on the pressure drop indicated that stable operation can be executed with filtration velocity less than 1.5 m/min and inlet dust concentration less than 4 g/m3. However, it was regarded that pulse pressure and pulse interval need to be adjusted when inlet dust concentration is higher than 4 g/m3. When filtration velocity and pulse pressure were examined, operation was possible regardless of changes in pulse pressure if filtration velocity was at 1.5 m/min. If filtration velocity was increased to 2 m/min. operation would be possible only when pulse pressure was set at higher than 5.8 kgf/cm2. Also, the prediction result of pressure drop with filtration velocity and pulse interval showed that operation with pulse interval less than 50 sec. should be carried out under filtration velocity at 1.5 m/min. While, pulse interval should be set at lower than 11 sec. if filtration velocity was set at 2 m/min. Under the conditions of filtration velocity lower than 1 m/min and high pulse pressure higher than 7 kgf/cm2, though pressure drop would be less, in this case, economic feasibility would be low due to increased in installation and operation cost since scale of dust collection equipment becomes larger and life of filtration bag becomes shortened due to high pulse pressure.

The new empirical static model was constructed on the basis of dimension analysis to predict the pressure drop according to the operating conditions. The empirical static model consists of the initial pressure drop term (N dust = ω0υf / P pulse t) and the dust mass number term (Δp initial), and two parameters (dust deposit resistance and exponent of dust mass number) have been estimated from experimental data. The optimum injection distance was identified in the 64 experimental data at the fixed filtration velocity and pulse pressure. The dust deposit resistance (K d), one of the empirical static model parameters got the minimum value at , d=0.11m, at which the total pressure drop was minimized. The exponent of dust mass number was interpreted as the elasticity of pressure drop to the dust mass number. The elasticity of the unimodal behavior had also a maximum value at , d=0.11m, at which the pressure drop increased most rapidly with the dust mass number. Additionally, the correlation coefficient for the new empirical static model was 0.914.

The pressure drop through pulse air jet-type bag filter is one of the most important factors on the operating cost of bagfilter houses. In this study, the pilot-scale pulse air jet-type bag filter with about 6 ㎡ filtration area was designed and tested for investigating the effects of the four operating conditions on the total pressure drop, using the coke dust collected from a steel mill factory. When the face velocity is higher than 2 m/min, it is not applicable to on-spot due to the increase of power expenses resulting from a high-pressure drop, and thus, 1.5 m/min is considered to be reasonable. The regression analysis results show that the degree of effects of independent parameters is a order of face velocity > concentration > time > pressure. The results of SPSS answer tree analysis also reveal that the operation time affects the pressure drop greatly in case of 1 m/min of face velocity, while the inlet concentration affects the pressure drop in case of face velocity more than 1.5 m/min.

The change of pressure drop according to the change in the inlet concentration, pulse interval, and injection distance of pulse air jet type bag filters, and the effect of venturi installation are as follows. The pressure drop with the range of 30 to 50mmH2O varies according to the injection distance with 30, 50, 70, 90sec and the inlet concentration of venture built-in fabric filters. For the lower concentration of 0.5g/m3 and 1g/m3, the pressure drop(ΔP) was stable 60 to 90minutes after operation. For the higher concentration of 3g/m3, as ΔP continues to go up, pulse interval should be set shorter than 30 seconds. The pressure drop with the injection distance of 110mm, when inlet dust concentration is 0.5g/m3 or 1g/m3, is 1.3 to 2 lower than with the injection distance of 50, 160, and 220mm, which means that the inflow amount of the secondary air by the instant acceleration is large. The injection distance of 2g/m3 and 3g/m3 has the similar pressure distribution. The higher inlet concentration is, the more important pulse interval is than injection distance. The pressure drop has proved to be larger when inlet concentration is lower and injection distance closer, on condition that the venturi is installed. The change in the pressure drop was smallest when injection distance was 50mm, followed by 220mm, 160mm, and 110mm.