Bibliographic citations
Manrique, H., (2020). Evaluación de la sustitución del etileno por etano en la mezcla refrigerante para el ahorro energético y económico en una planta de licuefacción del gas natural [Tesis, Universidad Nacional de Ingeniería]. http://hdl.handle.net/20.500.14076/21627
Manrique, H., Evaluación de la sustitución del etileno por etano en la mezcla refrigerante para el ahorro energético y económico en una planta de licuefacción del gas natural [Tesis]. PE: Universidad Nacional de Ingeniería; 2020. http://hdl.handle.net/20.500.14076/21627
@misc{renati/266647,
title = "Evaluación de la sustitución del etileno por etano en la mezcla refrigerante para el ahorro energético y económico en una planta de licuefacción del gas natural",
author = "Manrique Olortegui, Herbert Jhordy",
publisher = "Universidad Nacional de Ingeniería",
year = "2020"
}
To develop this research, PERU LNG’s natural gas liquefaction plant located in pampa Melchorita is taken as study case. The Melchorita liquefaction plant uses a mixed refrigerant that has a molar composition of 33% in ethylene and employs the liquefaction process named Propane precooled mixed refrigerant C3MR. PERU LNG imports the ethylene at a price of 2459 USD/t. The ethylene of the mixed refrigerant can be replaced by ethane if there were a plant that separates ethane from the natural gas that comes from Camisea as a part of its operations, maintaining the same operational conditions, the equipment and the liquified natural gas production. The replacement of the imported ethylene with ethane would generate a reduction of operating costs and therefore savings for the liquefaction plant. In addition, this replacement would produce a decrease in the energy used by the compressors and in the propane molar flowrate in the precooling loop. These benefits will be quantified in order to develop an economic analysis having as objective to determine the potential advantages or disadvantages of these modifications. The C3MR process modelling follows a simplified scheme with real operating conditions, three pressure levels in the precooling section and two multi-flow heat exchangers that represent the cryogenic heat exchanger. The mass and energy balances are solved for all the equipment while the Peng-Robinson equation of state is used to calculate the thermodynamic properties of the mixtures in the process.
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