• Transactions of the Korean hydrogen and new energy society
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• v.31 no.6
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• pp.571-577
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• 2020

Thermal analysis was performed for a cold box of a hydrogen liquefaction pilot plant with 0.5 ton/day capacity. The pilot plant has adopted a hydrogen liquefaction process using two-stage helium Brayton cycle with precooling of liquid nitrogen. The cold box for hydrogen liquefaction has generally vacuum insulation but inevitable heat invasion by conduction and radiation exists. The heat loads were calculated for cold box internals according to multilayer insulation emissivity. Total heat load of 181.7 W is estimated for emissivity of 0.03 considered in field condition.

• Progress in Superconductivity and Cryogenics
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• v.22 no.3
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• pp.20-24
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• 2020

The purpose of this analytic study is to design and examine an efficient hydrogen liquefaction cycle by using a pre-cooler. The liquefaction cycle is primarily comprised of a pre-cooler and a refrigerator. The fed hydrogen gas is cooled down from ambient temperature (300 K) to the pre-cooling coolant temperature (either 77 K or 120 K approximately) through the pre-cooler. There are two pre-cooling methods: a single pre-coolant pre-cooler and a cascade pre-cooler which uses two levels of pre-coolants. After heat exchanging with the pre-cooler, the hydrogen gas is further cooled and finally liquefied through the refrigerator. The working fluids of the potential pre-cooling cycle are selected as liquid nitrogen and liquefied natural gas. A commercial software Aspen HYSYS is utilized to perform the numerical simulation of the proposed liquefaction cycle. Efficiency is compared with respect to the various conditions of the heat exchanging part of the pre-cooler. The analysis results show that the cascade method is more efficient, and the heat exchanging part of the pre-coolers should have specific UA ratios to maximize both spatial and energy efficiencies. This paper presents the quantitative performance of the pre-cooler in the hydrogen liquefaction cycle in detail, which shall be useful for designing an energy-efficient liquefaction system.

• Journal of the Korean Society of Food Culture
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• v.14 no.5
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• pp.455-460
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• 1999

In order to establish the processing condition of salt-fermented liquefaction of sardine (Sardinops melanoslicta), effect of temperature, pH value, and concentration of salinity on crude enzyme activity of sardine viscera were investigated. The optimum temperature range of crude enzyme activity in sardine viscera was $45{\sim}50^{\circ}C$ and the optimum pH value of it was 9.8. According to the concentration of salinity increased the crude enzyme activity in sardine viscera decreased. The relationship between concentration of salinity (X) and the crude enzyme activity (Y) in sardine viscera is shown as follows; Y=-0.01363X+0.7676 (r=-0.88). For the purpose of processing conditions of rapid- and low salt-fermented liquefaction of sardine, changes of viable cell count, histamine content, and volatile basic nitrogen (VBN) in the chopped whole sardine with 8% NaCl during preheating process at $40^{\circ},\;45^{\circ}$ and $50^{\circ}C$ for 48 hrs were analyzed. During preheating, initial viable cell counts of chopped whole sardine were $10^{4-7}/g$, but they decreased $10^{1-5}/g$ after 48 hrs. Histamine contents during preheating process at $40^{\circ}\;and\;45^{\circ}C$ were gradually increased, whereas at $50^{\circ}C$ were almost the same level after 48 hrs. VBN contents were continuously increased during preheating, but preheating at $50^{\circ}C$ samples were lower level than that of $40^{\circ}\;and\;45^{\circ}C$ ones. For the purpose to accelerate the fermentation and liquefaction of chopped whole sardine, preheating at optimum temperature of crude enzyme activity for 48 hrs was useful processing method and the contents of viable cell count, histamine, and VBN were safety level for food sanitation.

• Korean Chemical Engineering Research
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• v.62 no.2
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• pp.163-172
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• 2024

In this study, two different scenarios for ammonia liquefaction in the green ammonia manufacturing process were proposed, and the economic-feasibility and environmental impact of each scenario were analyzed. The two liquefaction processes involved gas-liquid separation before cooling at high pressure (high pressure cooling process) or after decompression without the gas-liquid separation (low pressure cooling process). The high-pressure cooling process requires higher capital costs due to the required installation of separation units and heat exchangers, but it offers relatively lower total utility costs of 91.03 $/hr and a reduced duty of 2.81 Gcal/hr. In contrast, although the low-pressure cooling process is simpler and cost-effective, it may encounter operational instability due to rapid pressure drops in the system. Environmental impact assessment revealed that the high-pressure cooling process is more environmentally friendly than the low-pressure cooling process, with an emission factor of 0.83 tCO₂eq less than the low-pressure cooling process, calculated based on power usage. Consequently, the outcomes of this study provide relevant scenario and a database for green ammonia synthesis process adaptable to various process conditions.

• Journal of the Korean Geotechnical Society
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• v.23 no.8
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• pp.47-57
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• 2007

In this study, the analysis of density characteristics of some dredged and reclaimed ground sites, which is necessary for liquefaction evaluation of a dredged and reclaimed ground, was conducted. From analyzing a simplified liquefaction potential evaluation using SPT-N values which have been applied as domestic earthquake-resistant design criterion, improvement scheme is suggested. Based on the analysis result of density characteristics, it was found out that the relative density and the intial N-value ranged respectively $40{\sim}50%\;and\;5{\sim}8$. In the case of applying Liao & Whitman's equation to correct effective overburden pressure, liquefaction resistance of the upper ground that is relatively weaker than that of lower ground is overestimated. So, Skempton's equation is recommended. And the N value with depth which is applied for design process should be estimated by the exponential equation, $N=1.35{\sigma}'^{0.75}$.

• Journal of Advanced Marine Engineering and Technology
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• v.34 no.1
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• pp.46-52
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• 2010

In this study, several types of natural gas liquefaction processes using two staged Inter-cooler are simulated and designed to secure a competitiveness in the industry of natural gas liquefaction plant. These processes are based on basic cascade process, and all of these are improved with two staged compressors type. One of types is applied Inter-cooler to each cycle such as propane, ethylene, methane, the other type is applied Inter-cooler to whole cycle. These processes are compared characteristics of performance with basic process. Cascade process with two staged Inter-cooler in the whole cycle is on the top ranked with increment ratio of COP about 13.7 ~ 20.5%, and yield efficiency of this process are improved comparing with the basic process by 23.8% ~ 35% lower specific power, respectively.

• Journal of Advanced Marine Engineering and Technology
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• v.36 no.5
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• pp.574-579
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• 2012

This paper presents the new cascade liquefaction cycles using $CO_2-C_2H_6-N_2$ and $CO_2-N_2$. The performance and exergy of cascade liquefaction cycles are analyzed using HYSYS software and then confirmed the possibility of these cycles for LNG-FPSO ship. From the comparison of performance and exergy loss of these cycles, the cascade liquefaction cycles using $CO_2-C_2H_6-N_2$ showed higher performance and the cycle using $CO_2-N_2$ presented higher exergy loss. The cascade liquefaction cycle using $CO_2-N_2$ is lower efficiency and higher compressor work compared to the optimized cascade liquefaction cycle using $C_3H_8-C_2H_4-C_1H_4$. But, if the efficiency of $N_2$ cycle in these liquefaction cycles is improved, it is possible to apply the cascade liquefaction cycle using $CO_2-C_2H_6-N_2$ and $CO_2-N_2$ to LNG-FPSO ship due to the simple composition device of these cycles.

• 한국태양에너지학회:학술대회논문집
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• 2012.03a
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• pp.376-381
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• 2012

Natural gas is converted in to LNG by chilling and liquefying the gas to the temperature of $-162^{\circ}C$, when liquefied, the volume of natural gas is reduced to 1/600th of its standard volume. This gives LNG the advantage in transportation. The pressure dorp of the cascade liquefaction cycle was investigated and simulated using HYSYS software. The simulation results showed that the pressure drop in the LNG heat exchanger is set to 50 kPa considering the increase in the compressor work of cryogenic cascade liquefaction cycle.

• KSCE Journal of Civil and Environmental Engineering Research
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• v.11 no.1
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• pp.1-8
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• 1991

Recently, researches for buried lifelines such as pipelines have been carried out to provide for safe design. On of the major causes to the damage of buried pipelines has been soil liquefaction. Analytical models have been presented to compare with the results from recent model experiment under a soil liquefaction environment induced by seismic shaking table. The analytical results were more than two times those those of experimental measurement. Thus the objective of this study is to introduce a rigorous nonlinear analysis of equation of motion with more realistic parameters which are dynamic soil and water pressure, dynamic subgrade reaction coefficient, and damping coefficient for soil liquefaction environment.

• 한국신재생에너지학회:학술대회논문집
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• 2010.06a
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• pp.109.1-109.1
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• 2010

Hybrid형 석탄액화 공정은 직접액화 (Direct Coal Liquefaction, DCL)공정과 간접액화 (Indirect Coal Liquefaction, ICL)공정으로 구성 되며, 공정의 경제성을 분석하기위하여 주요 제품 (디젤, 납사) 생산량이 50,000barrel per day (BPD)의 Hybrid형 석탄액화공정을 선정하고 공정에 적합한 검토기준을 세워 건설비용 및 매출액등을 산정하였다. 또한 석탄액화공정에 대한 중요 변수들의 가격 변동에 따른 민감도 분석을 실시하였다. 생산량을 기준으로 선정된 원료탄(Illinois #6 유연탄)의 사용하였을 때, 총 투자액은 $4,114,730,000 로 나타났으며, 고정비는 $93,610,000, 변동비는 $407,225,000으로 분석되었다. 경제성 분석결과 내부수익률 (internal rate of return, IRR)은 기본조건에서 11.48%로 나타났으며, 순현가(net present value, NPV)는 $526,478,000으로 나타났다. 원금상환 기간은 6.9년으로 나타났으며, 민감도 분석 결과 제품가격, 원료석탄가격, 건설비의 변동률 순서로 수익률에 변화를 주는 것으로 나타났다. 민감도가 가장 높은 제품 가격 25% 상승 시, IRR과 NPV는 각각 17.24%, $2,804,919,000로 나타났다.