42
C. Juhong et al.
that is, the concentration of the reactants is the same whether it is the porous layer
on the surface of the electrode or the internal catalytic layer. This means that the
current distribution of the catalytic layer is uniform. In other words, in the complete
catalytic layer, the utilization of the electron conductor and the ionic conductor can
reach 100%. Conversely, for fast reaction or thick film, the effective mass transfer
coefficient 1 is close to zero, and the internal catalytic layer has almost no reactive
species, resulting in a decrease in the utilization rate of the catalytic layer.
In 1987, Tanaka et al. further expanded the RTLE process and tested the oxygen
reduction performance of high specific surface area catalyst Fe-phthalocyanine. They
applied a slurry of catalyst and Teflon to the disk electrode cavity of a rotating disk
electrode with a thickness of about 100 μm, and called this technique a porous thinlayer coating technique (TPC-RDE). Although the film resistance is large enough to
affect the correctness of the test for the 100 μm film, they only use RTLE to compare
the similarities and differences of several catalytic systems, and do not discuss the
dynamic properties of the system, or the thickness. The effect of the film on mass
transfer. Subsequently, Perez et al. used the same method to study the oxygen reduction performance of carbon-supported platinum catalysts. To explain the effect of the
porous membrane catalytic layer with a thickness of 100 μm on mass transfer, they
cited the PTFE full permeability model to calculate the oxygen reduction kinetic
parameters. However, only about 10–50% of the catalyst solids produced by Perez
et al. can be wetted, resulting in incomplete electron and ion conduction of the catalyst. Similar to the TPC-RDE model, Gloaguen et al. further reduced the thickness of
the film. The thin active disk electrode layer (TAL–RDE) made of the catalyst/Nafion
slurry coated on the platinum carbon rotating disk electrode was about 1–7 μm, and
study the oxygen reduction performance of the Pt/C electrode to verify the effectiveness of the electrode using the full penetration model. In this model, a thin active
layer can be seen as a superposition of an ionic conductor (Nafion) and an electron conductor (catalyst). This means that the solubility and diffusion coefficient of
the reactants in the Nafion membrane and the solubility and diffusion coefficient of
the material in the solution are fully considered. Perez et al. found that the kinetic
parameters can only be obtained directly from the mass transfer correction formula
in catalyst samples with a film thickness of less than 1 μm. The thicker membrane
mass transfer dynamics corrections are related to the applied model and additional
corrections need to be considered. Moreover, the accuracy of these kinetic parameters is affected by the accuracy of the physical property data of the catalyst/Nafion
layer. However, compared to TPC-RDE, TAL-RDE is 100% wetted and all catalyst layers are involved in electron and ion conduction. In 1987, Alonso-Vante and
Tributsch used a rotating thin-layer electrode to study the oxygen reduction performance of Mo4.2Ru1.8Se8 catalyst. They also deposited a mixture of catalyst/Nafion
on the glassy carbon rotating disk electrode, but did not give details. Preparation
information and film thickness data. Similarly, Tamizhmani, Gojkovic, Claude et al.
used a similar method to study the oxygen reduction performance of different catalysts. However, their film is thicker, the ratio of Nafion to catalyst is high, and the
loading of the catalyst is also large, which also leads to an increase in the material
diffusion resistance of the film, which affects the correction of the dynamic current
C. Juhong et al.
that is, the concentration of the reactants is the same whether it is the porous layer
on the surface of the electrode or the internal catalytic layer. This means that the
current distribution of the catalytic layer is uniform. In other words, in the complete
catalytic layer, the utilization of the electron conductor and the ionic conductor can
reach 100%. Conversely, for fast reaction or thick film, the effective mass transfer
coefficient 1 is close to zero, and the internal catalytic layer has almost no reactive
species, resulting in a decrease in the utilization rate of the catalytic layer.
In 1987, Tanaka et al. further expanded the RTLE process and tested the oxygen
reduction performance of high specific surface area catalyst Fe-phthalocyanine. They
applied a slurry of catalyst and Teflon to the disk electrode cavity of a rotating disk
electrode with a thickness of about 100 μm, and called this technique a porous thinlayer coating technique (TPC-RDE). Although the film resistance is large enough to
affect the correctness of the test for the 100 μm film, they only use RTLE to compare
the similarities and differences of several catalytic systems, and do not discuss the
dynamic properties of the system, or the thickness. The effect of the film on mass
transfer. Subsequently, Perez et al. used the same method to study the oxygen reduction performance of carbon-supported platinum catalysts. To explain the effect of the
porous membrane catalytic layer with a thickness of 100 μm on mass transfer, they
cited the PTFE full permeability model to calculate the oxygen reduction kinetic
parameters. However, only about 10–50% of the catalyst solids produced by Perez
et al. can be wetted, resulting in incomplete electron and ion conduction of the catalyst. Similar to the TPC-RDE model, Gloaguen et al. further reduced the thickness of
the film. The thin active disk electrode layer (TAL–RDE) made of the catalyst/Nafion
slurry coated on the platinum carbon rotating disk electrode was about 1–7 μm, and
study the oxygen reduction performance of the Pt/C electrode to verify the effectiveness of the electrode using the full penetration model. In this model, a thin active
layer can be seen as a superposition of an ionic conductor (Nafion) and an electron conductor (catalyst). This means that the solubility and diffusion coefficient of
the reactants in the Nafion membrane and the solubility and diffusion coefficient of
the material in the solution are fully considered. Perez et al. found that the kinetic
parameters can only be obtained directly from the mass transfer correction formula
in catalyst samples with a film thickness of less than 1 μm. The thicker membrane
mass transfer dynamics corrections are related to the applied model and additional
corrections need to be considered. Moreover, the accuracy of these kinetic parameters is affected by the accuracy of the physical property data of the catalyst/Nafion
layer. However, compared to TPC-RDE, TAL-RDE is 100% wetted and all catalyst layers are involved in electron and ion conduction. In 1987, Alonso-Vante and
Tributsch used a rotating thin-layer electrode to study the oxygen reduction performance of Mo4.2Ru1.8Se8 catalyst. They also deposited a mixture of catalyst/Nafion
on the glassy carbon rotating disk electrode, but did not give details. Preparation
information and film thickness data. Similarly, Tamizhmani, Gojkovic, Claude et al.
used a similar method to study the oxygen reduction performance of different catalysts. However, their film is thicker, the ratio of Nafion to catalyst is high, and the
loading of the catalyst is also large, which also leads to an increase in the material
diffusion resistance of the film, which affects the correction of the dynamic current