Techno-economic analysis of mechanical vapor recompression for process integration of post-combustion CO2 capture with downstream compression

Jeong, Yeong Su; Jung, Jae Hee; Lee, Ung; Yang, Changryung; Han, Chonghun

doi:10.1016/j.cherd.2015.08.016

Cited by 54 publications

(12 citation statements)

References 20 publications

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“…TCI is calculated by summing the fixed capital cost (FCI), start-up cost (SUC), and working capital investment (WCI) 34,35 : 3.2.2 | Total product cost (TPC) The TPC is the cost related to production and includes labor, raw material, and utilities. The TPC can be calculated by summing fixed charges (FC), direct production cost (DPC), plant overhead cost (OVHD), and general expenses (GE) 36 : First, the fixed charges are calculated as the sum of local taxes (C local tax ) and insurance cost (C insurance ). Local tax and insurance costs were calculated as 4% of the FCI 36 :…”

Section: Equivalent Annual Cost (Eac)mentioning

confidence: 99%

“…Second, the DPC is directly related to production and can be calculated by summing utility costs, such as raw material cost, water, and electricity cost 36 : Third, the overhead cost is the cost related to the operation of the business, including factory rental, advertising, insurance, and repair costs. The overhead cost was calculated as 60% of the sum of the maintenance, labor, and supervision costs 36 : Finally, general expenses (GE) are incurred as part of the operation of a business and can be calculated as the sum of the administrative cost (C admistrative ), marketing cost (C marketing ), and research and development cost (C R&D ) 24 :…”

Section: Equivalent Annual Cost (Eac)mentioning

confidence: 99%

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Techno‐economic comparison of amine regeneration process with heat‐stable amine salt reclaiming units

Lim

Lee

Moon

et al. 2021

Energy Science & Engineering

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Recently, the amount of sulfur compounds such as H 2 S generated in the oil-refining process has increased. 1,2 Removing such compounds from the process is essential because H 2 S is the main cause of air pollution and has a fatal effect on the human body. For example, at 0.0057 ppm in the atmosphere, H 2 S causes eye and nasal symptoms, coughs, and headaches; at 250 ppm, it can damage organs and nervous systems and also deflate cellular metabolism. 3 Therefore, H 2 S should be discarded to avoid environmental pollution and increase process efficiency. Most factories use amine gas sweetening to remove sulfur compounds such as H 2 S generated during the crude-oil refining process. 4 Amines that absorb H 2 S in the amine gas sweetening process are degraded using high temperature in the regenerator and reused; this is called the amine regeneration process. The H 2 S absorption and regeneration mechanism of amines is caused by a difference in pKa; it is absorbed

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Section: Equivalent Annual Cost (Eac)mentioning

confidence: 99%

Section: Equivalent Annual Cost (Eac)mentioning

confidence: 99%

Techno‐economic comparison of amine regeneration process with heat‐stable amine salt reclaiming units

Lim

Lee

Moon

et al. 2021

Energy Science & Engineering

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“…SUC is money required to begin a business till it yields A detailed description of each section is given in Appendix S1. 31,32 Figure 10 shows the analysis of the cost the evaporator, centrifugal compressor, and total equipment cost to calculate the TCI. The prices of the evaporators for the developed models are shown in Figure 10A, and the evaporator cost was analyzed with respect to the presence of MVR and the number of effects.…”

Section: Total Capital Costmentioning

confidence: 99%

“…This study assumed 5% and 30 years, respectively. 31 Tables 5 and 6 show the values for EAC, TPC, and TAC calculated according to the presence of MVR for the developed models, whereas Figure 14 shows TAC for each configuration. When using MVR, TAC was smaller compared to the configurations not using MVR up until the septuple-effect evaporator.…”

Section: Total Annualized Costmentioning

confidence: 99%

Novel mechanical vapor recompression‐assisted evaporation process for improving energy efficiency in pulp and paper industry

Kim

Lim

Cho

et al. 2021

Intl J of Energy Research

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In the pulp and paper industry, black liquor, which is a biomass resource, is burned to produce electricity. Black liquor is concentrated to 21 wt% water through an evaporator before being burned in a boiler. For the evaporator, a multiple-effect evaporator (MEE) is mainly used, but it requires a large amount of energy and cost. Therefore, it is crucial to reduce energy and cost of evaporation process. Hence, this study suggested a novel process model that integrated mechanical vapor recompression (MVR) with MEE to increase the energy efficiency. The suggested MVR-assisted evaporation process was composed of preheating and evaporation processes to effectively concentrate black liquor. In addition, it reduced the steam consumption of MEE by using MVR, which uses relatively inexpensive electric energy in the pre-evaporation process. In the simulation results, the steam, electricity consumption, and the latent heat recovered from the secondary vapor of the suggested process were quantitatively analyzed to verify the energy efficiency. The results indicate that the proposed process increases substantial energy efficiency compared to the conventional process. Then, the appropriateness of the suggested process was evaluated by the techno-economic analysis. The total annualized cost (TAC) is determined for both current and potential future economic benefits. TAC of the MVR-assisted MEE configuration can be reduced by up to 77.54%.

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“…The authors have modeled the compressors assuming fixed isentropic efficiencies and equal compression ratios. Jeong et al (2015) have performed an economic analysis of a monoethanolamine (MEA) capture system including compression. Their compressor model is based on the design data from a CO 2 capture test system.…”

Section: Background and Contributions Of This Workmentioning

confidence: 99%

Design, dynamic modeling, and control of a multistage CO2 compression system

Modekurti

Eslick

Omell

et al. 2017

International Journal of Greenhouse Gas Control

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This paper presents a comprehensive model of a post-combustion CO 2 compression system that uses a multistage centrifugal compressor train to take the CO 2-rich gas from the regenerator of a CO 2 capture system and compress it to the supercritical conditions required for pipeline transport. The compression system model includes inter-stage coolers, flash vessels, glycol tower for water removal, and the CO 2 inventory of the associated system. Both inline and integral gear compressors are designed using dimensionless numbers and appropriate design constraints. The steady-state integral gear compressor model is validated against industrial compressor performance data provided by a commercial CO 2 compressor manufacturer. Its performance is also compared to the performance of an inline compressor model using a typical feed stream from a post-combustion CO 2 capture process. Performance curves using dimensionless exit flow coefficient and isentropic head coefficient are used for simulating off-design performance of the integral gear compressor. To avoid surge during operation, a controller has been designed. Transients of key process variables in response to various disturbances have been studied.

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Techno-economic analysis of mechanical vapor recompression for process integration of post-combustion CO2 capture with downstream compression

Cited by 54 publications

References 20 publications

Techno‐economic comparison of amine regeneration process with heat‐stable amine salt reclaiming units

Techno‐economic comparison of amine regeneration process with heat‐stable amine salt reclaiming units

Novel mechanical vapor recompression‐assisted evaporation process for improving energy efficiency in pulp and paper industry

Design, dynamic modeling, and control of a multistage CO2 compression system

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