• 신재생에너지
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• 제2권2호
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• pp.118-125
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• 2006

The target of this work was the process development of demonstration plant to produce the high quality alternative fuel oil by the pyrolysis of mixed plastic waste. In the first step of research, the bench-scale units of 70 t/y and the pilot plant of 360 t/y had been developed. Main research contents in this step were the process performance test of pilot plant of 360 ton/year and the development of demonstration plant of 3,000 t/y, which was constructed at Korea R & D Company in Kimjae City. The process performance of pilot plant of 360 t/y showed about 80% yield of liquid product, which was obtained by both light gas oil(LGO) and heavy gas oil(HGO), The boiling point range distribution of LO product that was mainly consisting of olefin components in PONA group appeared at between that of commercial gasoline and kerosene. On the other hand, HO product was mainly paraffin and olefin components and also appeared at upper temperature distribution range than commercial diesel. Gas product showed a high fraction of $C_3\;and\;C_4$ product like LPG composition, but also a high fraction of $CO_2$ and CO by probably a little leak of process.

• 한국신재생에너지학회:학술대회논문집
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• 한국신재생에너지학회 2006년도 춘계학술대회
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• pp.523-526
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• 2006

The target of this work was the process development of demonstration plant to produce the high quailty alternative fuel oil by the pyrolysis of mixed plastic waste. In the first step of research, the bench-scale units of 70t/y and the pi lot plant of 360 t/v had been developed. Main research contents in this step were the process performance test of pilot plant ot 360ton/year and the development of demonstration plant of 3 000 t/y which was constructed at Korea R & D Company in Kimjae City. The process performance of pilot plant of 360 t/v showed components in PONA group appeared at between that of commercial gasoline and kerosene. On the other hand, HO product was mainly paraffin and olefin components and also appeared at upper temperature distribution range than commercial diesel. Gas product showed a high fraction of $C_3\;and\;C_4$ product like LPG composition, but also a high fraction of $CO_2$ and CO by probably a little leak of process.

• 한국수소및신에너지학회논문집
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• 제33권3호
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• pp.247-254
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• 2022

Slush hydrogen containing liquid and solid hydrogen is expected to achieve zero boil-off by suppressing boil-off gas because heat of fusion for solid absorbe the heat ingress from atmosphere. In this paper, quantitative analysis on storage cost considering specific energy consumption between 1,000 m³ class liquid hydrogen storage system with re-liquefaction and slush hydrogen storage system during equivalent zero boil off period. Even though approximately 50% of total storage capacity should be converted into solid phase during the initial cargo bunkering, total energy consumption to convert into slush hydrogen is relatively 25% less than re-liquefaction energy for boil off hydrogen during zero boil off period. That's because energy consumption of slush phase change take up only 1.8% of liquefaction energy. moreover, annual revenue requirement including CAPEX, OPEX and electric cost for slush hydrogen storage could be more reduced approximately 32.5% than those of liquid hydrogen storage and specific energy storage cost ($/kg-H₂) could also be lowered by about 41.7% compared with liquid hydrogen storage.

• 한국신재생에너지학회:학술대회논문집
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• 한국신재생에너지학회 2009년도 춘계학술대회 논문집
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• pp.857-860
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• 2009

This report examines the economic feasibility of a commercial 50,000 barrel per day direct/indirect coal liquefaction (DCL/ICL) facility to produce commercial-grade diesel and naphtha liquids from medium-sulfur bituminous coal. The scope of the study includes capital and operating cost estimates, sensitivity analysis and a comparative financial analysis. Based on plant capacity of 50,000BPD, employing Illinois #6 bituminous coal as feed coal the total capital cost appeared $3,994,858,000(DCL) and $4,942,976,000(ICL). Also, the internal rate of return of DCL/ICL appeared 13.27% and 12.68% on the base condition. In this case, coal price and sale price of products were the most influence factors. And ICL's payback period(6.8 years) was longer than DCL's (6.6 years). According to sensitivity analyses, the important factors on DCL/ICL processes were product sale price, feed coal price and the capital cost in order.

• 한국수소및신에너지학회논문집
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• 제34권6호
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• pp.641-649
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• 2023

This study analyzes the cool-down process of liquid hydrogen storage tanks, which have advantages in terms of large-capacity transfer, storage, and utilization as hydrogen demand increases. A hydrogen liquefaction plant is selected for analysis and an efficient tank cooling method is sought by comparing the time required for the cool-down process with the gas consumption in connection with the gassing-up process required for the operation of the liquid hydrogen storage tank. The results of this study can be referred to in the operation process after the initial start-up and maintenance of the hydrogen liquefaction plant.

• Journal of Advanced Marine Engineering and Technology
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• 제39권10호
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• pp.1037-1043
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• 2015

In recent years, Floating Liquefied Natural Gas (FLNG) Unit have attracted considerable attention. Generally, liquefied natural gas (LNG) units are produced in onshore liquefaction terminals from gas supplied from onshore gas fields or large-scale offshore gas fields near the coast. However, the development of these gas fields has approached saturation. Large-scale offshore gas fields far from the coast, as well as undeveloped medium- and small-scale offshore gas fields, have recently attracted attention. Among several proposed concepts, the floating LNG plant in the form of the FLNG system was chosen for further evaluation and development, considering worldwide receiving infrastructure. The design of a 2.5 million tonne per annum FLNG unit has been completed with a capacity corresponding to that of modern onshore liquefaction plants. Various simulation tests were performed to evaluate the performance of the electrical power plant, focusing on the efficiency of the electrical system to secure the aspects of plant safety. This design study analyzes the electrical system for the FLNG unit to improve the safety of operation and maintenance in the field.

• 한국건설관리학회논문집
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• 제15권3호
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• pp.47-57
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• 2014

LNG 플랜트사업은 그 특성상 해외에서 사업을 추진하기 때문에 사업관리도 일반적인 사업관리방식과는 차이점이 있다. LNG 플랜트 사업 프로세스는 가스탐사 및 생산, 물리적인 액화 및 화학적인 전환공정, 수송, 저장 등의 가치사슬로 구성되며, 주로 천연가스를 액체원료나 연료로 전환하는 장치를 중심으로 액화공정(초저온 액화) 및 FEED 패키지, 제어 운영, 건설수행 등 EPC 기술을 대상으로 하고 있다. 이러한 해외에서 수행되고 복잡한 LNG 플랜트공사의 성공은 사업관리 의사결정에 따른 사업의 성패가 달라질 수 있다. 따라서 본 연구는 LNG 플랜트공사의 시공단계 사업관리 의사결정지원 모델을 구축하기 위하여 EPC 단계별로 9개의 사업관리요소 항목을 도출하고, 각 항목별 중요도를 평가하였다. 중요도 평가결과, EPC 단계별로 사업관리와 리스크관리 항목이 공통적으로 중요한 것으로 도출되었다. 특히 본 연구는 사업관리 요소항목과 중요도 평가결과를 기반으로 LNG 플랜트공사의 시공단계의 의사결정지원모델을 개발하였다. 개발된 의사결정지원모델은 향후 시공단계의 사업관리 의사결정지원 시스템 구축의 기반이 될 것이다.

• 시스템엔지니어링학술지
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• 제4권1호
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• pp.19-29
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• 2008

Traditionally gas plant R&D has had a world-wide weak position in terms of high technology. Especially System engineering did not exactly apply to gas plant construction. So, Gas Plant R&D Center is determined to make the establishment of the system engineering for the standard of gas plant. Gas Plant R&D Center has two projects. Firstly, the establishment of the R&D management system. Secondly, the system engineering which is included in the VE concept of EPC parts. But Gas Plant R&D Center exists in the particular conditions for successful development of the new process and core equipments. Now we will describe the establishment of R&D management system and particular conditions(Risk Conditions) for gas plant.

• 플랜트 저널
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• 제15권2호
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• pp.46-55
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• 2019

기존 메탄 & 질소 팽창 사이클의 효율 개선을 위해 2개의 메탄 팽창 공정 (cold composite curve에 변곡점을 하나 더 추가하기 위해 warm & cold 2개 공정으로 나눔)과 1개의 질소 팽창 공정을 사용한 천연가스 액화 사이클을 소개하기 위한 논문이다. 이전 질소 팽창 사이클 및 메탄 & 질소 사이클과 비교했을 때, 13.92 및 13.13에서 12.08 kW/ton/day로 효율이 8~15% 정도 개선되었다. 순 현재가치(NPV) 기준으로 한 수명 주기 비용 분석(LCC analysis) 또한 약간의 CAPEX 증가는 있지만 프로젝트 순 현재가치가 개선된 결과를 보여준다.

• 한국에너지공학회:학술대회논문집
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• 한국에너지공학회 2010년도 춘계학술 발표회
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• pp.162-162
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• 2010