A high performance molten carbonate fuel cell cathode

Franke, Mark; Winnick, Jack

doi:10.1007/bf01039383

Cited by 13 publications

(8 citation statements)

References 11 publications

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“…The greatest improvement found in the present configuration is in the area of polarization. Franke and Winnick (1989b) presented polarization data up to a maximum of 20 A/m2 (0.04 A), with a cathodic overpotential of 2.7 V. The present curves show much higher current densities ( 1 0 -2 0~) for the same or lower overpotential, but still 10-20 times lower than the design goal of 500 A/m2 at 0.5 V (Franke and Winnick, 1989a Offset in calculated rates due to oxidation of SO2 fed to anode. Offset in calculated rates due to oxidation of SO2 fed to anode.…”

Section: Discussionmentioning

confidence: 63%

“…With these values, the activation polarization in a full cell with porous electrodes can be estimated: even with no area enhancement (true area/superficial area = I), the voltage needed at 500 A/m2 is 0.038 V at each electrode, well within the required economic window. However, Franke found, in a full cell experiment, that io was apparently three orders of magnitude lower (Franke and Winnick, 1989b). If the pores in the electrode are flooded, the active area for gas-electrolyte-electrode contact is minimized.…”

Section: Theory and Designmentioning

confidence: 98%

“…Inclusion of 1 wt. Yo of V 2 0 s allowed Franke and Winnick (1989b) to reach greater than 95% removal of SO3 for a flow rate of 100 mL/min (0.3% SO2, 3.0% 02, balance N2) at 100% current efficiency. As currents increase, the rate of electrochemical generation of SO2 (reaction 1) may exceed the rate of SO2 oxidation by V20s in the electrolyte.…”

Section: January 1994mentioning

confidence: 99%

“…Scott (1985) chose a porous perovskite ceramic of Lq,,Sr,,,CoO, and found it to be both conductive and stable in the corrosive cell environment. These electrodes were formed by sintering the proper sized particles at 1,lOO"C in a procedure optimized by Franke and Winnick (1989b). These perovskites were compared with NiO electrodes in the MCFC and were found to have similar overall kinetics.…”

Section: Electrodesmentioning

confidence: 99%

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Electrochemical membrane process for flue gas desulfurization

McHenry

Winnick

1994

AIChE Journal

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A flue gas desulfurization process being developed for coal-fired power plants removes and concentrates sulfur oxides (SO,) IntroductionA large number of flue gas desulfurization processes are presently under development throughout the world to combat the acid rain problem with most using wet or dry sorption to preferentially remove SOz from the flue gas. Most of these processes need expensive reagents, a flue gas reheating step and a landfill for disposal of the captured sulfur. This leads to high operating and capital costs. With the recent 1991 Clean Air Act, these processes will see continued interest as utilities attempt to reduce SO2 emissions by 10 million tons from 1980 levels.Here we present the development of an electrochemical membrane flue gas desulfurization process, which overcomes the problems of most other flue gas desulfurization processes. As a membrane separation process, it has similarities to other membrane processes, with one major difference: the driving force for the separation is an applied electric field instead of a conventional pressure or concentration gradient. This technique has been applied to other separation schemes, such as the production of oxygen from air (Langer and Haldeman, 1964), the removal of carbon dioxide from dilute streams (Kang Walke et al., 1988) and hydrogen sulfide from coal gas (Weaver and Winnick, 1991) or natural gas (Alexander and Winnick, 1990). The key is that the components to be removed must be the strongest electron acceptors (Lewis acids) in the gas mixture. Sulfur oxides are the most acidic of all species present in flue gas and are therefore theoretically separable by this technique.When development is complete, this technique offers several advantages over standard limestone scrubbing. The operation is continuous and totally in situ; no liquid is pumped and no regeneration is required. No reagents are necessary, other than about 1-2070 of the plant electric power production. Furthermore, a salable byproduct, oleum, (anhydrous sulfuric acid) is produced; no waste is emitted. Finally, operation at fluegas temperature eliminates the need for stack-gas-reheat.While the goal of process development is to produce a process for the removal of SO, and NO,, the focus of this article is on the SO, removal capabilities.

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Section: Discussionmentioning

confidence: 63%

Section: Theory and Designmentioning

confidence: 98%

Section: January 1994mentioning

confidence: 99%

Section: Electrodesmentioning

confidence: 99%

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Electrochemical membrane process for flue gas desulfurization

McHenry

Winnick

1994

AIChE Journal

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“…Several ceramic materials with small solubility in the melt have been studied as alternatives to NiO. LiFeO 2 , LiCoO 2 [3] and La 0.2 Sr 0.8 CoO 3 [4] offered initial promise as replacement material for NiO cathodes. LiCoO 2 coated nickel cathodes are reported in literature [5,6].…”

Section: Introductionmentioning

confidence: 99%