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Research Papers: Energy Systems Analysis

Absorption Process in MgCl2–NH3 Thermochemical Batteries With Constant Mass Flow Rate

[+] Author and Article Information
Seyyed Ali Hedayat Mofidi

Sustainable Energy Laboratory,
Department of Mechanical Engineering,
University of Utah,
Salt Lake City, UT 84112
e-mail: Ali.Hedayat@Utah.edu

Kent S. Udell

Professor
Department of Mechanical Engineering,
University of Utah,
Salt Lake City, UT 84112
e-mail: Udell@mech.Utah.edu

1Corresponding author.

Contributed by the Advanced Energy Systems Division of ASME for publication in the JOURNAL OF ENERGY RESOURCES TECHNOLOGY. Manuscript received September 4, 2018; final manuscript received December 25, 2018; published online January 18, 2019. Assoc. Editor: Guangdong Zhu.

J. Energy Resour. Technol 141(6), 062004 (Jan 18, 2019) (10 pages) Paper No: JERT-18-1686; doi: 10.1115/1.4042406 History: Received September 04, 2018; Revised December 25, 2018

In this paper, the performance of a thermochemical battery based on magnesium chloride and ammonia pair with a constant mass flow rate of ammonia gas is studied through a series of experiments using single and multicell configurations. It is shown that a lower mass flow rate lowers the temperature of the reactive complex and increases the duration of the absorption process. However, it was observed that the reaction eventually becomes mass transfer limited which slows the absorption rate to values below those specified by the mass flow controller (MFC). It was shown in the single-cell reactor that a reaction zone starts at the inlet and moves toward the end of the reactor. The mass transfer limited reaction zone movement reduces the absorption rate and temperature in the reaction zone. The overall performance of a multicell thermal battery is also studied to analyze behavior of such reactors as well. It was shown that the controlling the flow rate of ammonia can cause the cells to deviate in absorption rate.

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Figures

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Fig. 1

Van't Hoff diagram for equilibrium lines of magnesium chloride and ammonia reaction (Eq. (1)) and for the liquid–vapor mixture of pure ammonia

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Fig. 2

Schematic of the single cell reactor

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Fig. 3

Schematic of the multicell thermal battery

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Fig. 4

The mass flow rate of ammonia at experiment 1

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Fig. 5

Supply pressure of the hot bed at experiment 1

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Fig. 6

Temperature response of the cells during experiment 1: (a) thermocouples at the inlet location, (b) thermocouples at the middle location, and (c) thermocouples at the end of the cells. Teq is the equilibrium temperature at the inlet pressure.

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Fig. 7

Mass flow rate of ammonia gas at experiment 2

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Fig. 8

Supply pressure of the hot bed at experiment 2

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Fig. 9

Temperature response of the cells during experiment 2: (a) thermocouples at the inlet location, (b) thermocouples at the middle location, and (c) thermocouples at the end of the cells. Teq is the equilibrium temperature at the inlet pressure.

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Fig. 10

Mass flow rate of ammonia gas at experiment 3

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Fig. 11

The pressure at both ends of the reactor

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Fig. 12

Temperature response of the single cell reactor

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Fig. 13

Temperature profiles inside the reactor at different milestones of global reaction rate (Xg)

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Fig. 14

Global reaction progress of experiment 3

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Fig. 15

Mass flow rate of ammonia for tests of experiment 4

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Fig. 16

(a)–(e) Temperature profiles inside the reactor at different milestones of global reaction rate (Xg), and (f) pressure at both ends of the reactor

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