LNG – Based Cogeneration Systems: Evaluation Using Exergy-Based Analyses

Morosuk, Tatiana; Tsatsaronis, George

doi:10.5772/51477

Cited by 13 publications

(14 citation statements)

References 35 publications

Supporting

Mentioning

Contrasting

Order By: Relevance

“…The exergy balance equations provide to define the exergetic performance of the components; then, the obtained results allow for the overall assessment. Since the inlet temperature of LNG vaporizer is smaller than the reference temperature, the physical exergy rates must be divided into the thermal and mechanical exergy components that were well explained by Morosuk and Tsatsaronis and Morosuk et al() Also, the chemical exergy rates must be considered because of the combustion process in the microturbine . General exergy balance equation is presented in Equation .…”

Section: Modelingmentioning

confidence: 99%

See 1 more Smart Citation

Life‐cycle‐integrated thermoeconomic and enviroeconomic assessments of the small‐scale‐liquefied natural gas cold utilization systems

et al. 2019

View full text Add to dashboard Cite

Summary Small‐scale‐liquefied natural gas (LNG) cold‐utilized power generation systems are the sustainable solutions in the rural and inland areas where the large‐scale power generation is infeasible. This study investigates three different small‐scale LNG cold‐utilized power generation systems, which are called as the single, combined, and carbon dioxide (CO2)–reduced combined systems according to their design details. The assessments are done according to the life‐cycle‐based enviroeconomic and life‐cycle‐integrated thermoeconomic assessment (LCiTA) models that are recently developed and new approaches, in order to better monitor their feasibilities in real operations. The life‐cycle‐based enviroeconomic assessment shows that the combined system has the lowest environmental payback period with 7.35 years that is nearly 6 months and 1 year lower than the single and CO2‐reduced combined systems, respectively. The LCiTA study deduces that the combined system has the minimum levelized product cost while the single system has the highest values. The integration of CO2 capture components increases the levelized product cost nearly by 16.0% in the combined design, but the levelized product cost value is still found lower than the single system. Moreover, the sustainability performance of the systems is evaluated according to the improved sustainability index calculated by the life‐cycle‐integrated fuel and destruction costs. The index value of the combined system is twice that of the single system. The multiobjective optimization study is performed in cases of closed operation rooms. The best trade‐off points are found in the close ambient air temperature range between 300.50 and 302.00 K. To observe the dynamic outdoor performance, the finite sum approach is applied for the LCiTA model. The highest fluctuations are seen for the CO2‐reduced combined system while the smallest fluctuations belong to the combined system.

show abstract

Section: Modelingmentioning

confidence: 99%

“…where c water is the unit cost of water as 2.74 Singapore dollar per cubic meter. 53 [54][55][56] Also, the chemical exergy rates must be considered because of the combustion process in the microturbine. 49 General exergy balance equation is presented in Equation 9.…”

Section: Life-cycle-based Enviroeconomic Modelingmentioning

confidence: 99%

Life‐cycle‐integrated thermoeconomic and enviroeconomic assessments of the small‐scale‐liquefied natural gas cold utilization systems

et al. 2019

View full text Add to dashboard Cite

show abstract

“…The annual capital cost is defined as the summation of major equipment investment costs: where C is the cost, M is the number of compression units, N is the number of gas turbines during the plant’s life, and Lf is the life expectancy; the subscripts CP represents the compressor, PP the pump, MSHE the multistream heat exchanger, CL the cooler, j the j th compressor, k the k th cooler, and PT the plant. The total plant life, Lf PT , is assumed as 20 years because the life cycle of a natural gas liquefaction plant is known to be around 20–25 years . The life expectancy of the compression units is approximately 5 years; thus, the compressors are needed four times during the plant’s life .…”

Section: Profit Optimization Modelmentioning

confidence: 99%

“…The total plant life, Lf PT , is assumed as 20 years because the life cycle of a natural gas liquefaction plant is known to be around 20−25 years. 48 The life expectancy of the compression units is approximately 5 years; thus, the compressors are needed four times during the plant's life. 49 The life expectancy of the gas turbine is approximately 11−18 years.…”

Section: Profit Optimization Modelmentioning

confidence: 99%

Strategies for Process and Size Selection of Natural Gas Liquefaction Processes: Specific Profit Portfolio Approach by Economic Based Optimization

Lee

Moon

2017

Ind. Eng. Chem. Res.

View full text Add to dashboard Cite

This study focuses on the strategies for process and size selection of various natural gas liquefaction processes by economic based optimization. As various types of liquefaction processes can be differentiated by their energy efficiency and equipment requirements, the energy requirement and cost of a liquefaction process have to be considered simultaneously to find the optimal process for a given plant size. Herein, we developed two mathematical models, i.e., the thermodynamic model and cost model, based on the unit equipment that were integrated into a profit optimization model that could be applied to various natural gas liquefaction processes and plant sizes. In this study, the profit optimization model was applied to three representative natural gas liquefaction processes: single mixed refrigerant (SMR), dual mixed refrigerant (DMR), and propane precooled mixed refrigerant (C3MR) processes. The capacity of the plants ranged from 1 to 7 million tons per annum (MTPA). As a result of profit optimization, specific profit portfolios were obtained and the economical plant size ranges were figured out: 1–2.2 MTPA for the SMR process, 2.2–4 MTPA for the DMR process, and 4–7 MTPA for the C3MR process.

show abstract

“…An extended review of such technologies as well as novel concepts was reported, for example, in Refs. [9,10].…”

Section: Introductionmentioning

confidence: 99%

Concepts for Regasification of LNG in Industrial Parks

Morosuk¹,

Tesch²,

Tsatsaronis³

2017

Advances in Natural Gas Emerging Technologies

Self Cite

View full text Add to dashboard Cite

The exponentially growing markets of liquefied natural gas (LNG) require efficient processes for LNG regasification within import terminals. Usually, the regasification of LNG is accomplished by direct or indirect heating. However, integrating LNG regasification into different processes within industrial parks (mainly processes involving low temperatures) is an efficient approach because of the utilization of the low-temperature energy. In some LNG import terminals, integration technologies are already being used. Previous publications showed an increase in the thermodynamic efficiency for systems combining air separation (as an example) and LNG regasification. In addition, the variation in the efficiency as well as the capital investment depends on the schematic and operation conditions. This fact creates great potential for improving the systems. In this chapter, different schematics are evaluated using exergy-based methods in order to improve the effectiveness of complex industrial processes that can involve LNG regasification.

show abstract

LNG – Based Cogeneration Systems: Evaluation Using Exergy-Based Analyses

Cited by 13 publications

References 35 publications

Life‐cycle‐integrated thermoeconomic and enviroeconomic assessments of the small‐scale‐liquefied natural gas cold utilization systems

Life‐cycle‐integrated thermoeconomic and enviroeconomic assessments of the small‐scale‐liquefied natural gas cold utilization systems

Strategies for Process and Size Selection of Natural Gas Liquefaction Processes: Specific Profit Portfolio Approach by Economic Based Optimization

Concepts for Regasification of LNG in Industrial Parks

Contact Info

Product

Resources

About