Progress in Solid Oxide Fuel Cells with Hydrocarbon Fuels

: Solid oxide fuel cells (SOFCs)’ main advantage in fuel ﬂexibility appears to be an interesting subject for further exploration. From the literature survey, direct utilisation of hydrocarbon as fuel for SOFCs has garnered attention with promising results reported. Various approaches, showcasing potential for using methane (CH 4 ) and heavier hydrocarbons in SOFCs, have been described. The direct use of hydrocarbons can occur through either direct internal reforming or gradual internal reforming, with requisite precautionary measures to mitigate carbon formation. While the internal reforming process could proceed via steam reforming, dry reforming or partial oxidation, an exciting development in the direct use of pure hydrocarbons, seems to progress well. Further exploration aims to reﬁne strategies, enhance efﬁciency and ensure the long-term stability and performance of hydrocarbon-fuelled SOFC systems. This review delves into the progress in this ﬁeld, primarily over the past two decades, offering comprehensive insights. Regardless of fuel type, studies have largely concentrated on catalyst compositions, modiﬁcations and reaction conditions to achieve better conversion and selectivity. Finding suitable anode materials exhibiting excellent performance and robustness under demanding operating conditions, remains a hurdle. Alternatively, ongoing efforts are directed towards lowering working temperatures, enabling consideration of a wider range of materials with improved electrochemical performance.


Introduction
In recent years, interest has increased in developing a highly efficient, low-carbon and renewable energy conversion system, as greenhouse gases release from the conventional energy generation methods have become widely known to be harmful to the environment. The most common combustion of fossil fuels has long been used for energy generation, although it suffers from relatively low efficiency and contributes to environmental pollution. Thus, a more efficient and environmentally benign technique to produce energy is required. Fuel cell technology is an encouraging technique to generate energy by directly converting the chemical energy in fuel into electricity through electrochemical reaction. It is a practical application, promising a better, clean alternative source of energy. There are various types of fuel cells that can be characterised according to their particular materials, the charge being transported, their electrolyte and operating temperature. The reader is referred to several review papers for a more thorough description [1][2][3][4][5][6][7][8][9]. Among all types of fuel cell, solid oxide fuel cells (SOFCs) have attracted considerable attention because of two remarkable features related to their high operating temperature. First, it provides fuel flexibility, allowing the use of hydrocarbons, syngas and biofuels. Secondly, SOFCs generate a

Comparison between Oxide-Ion-Conducting SOFCs and Proton-Conducting SOFCs Fuelled by Hydrocarbons
Both oxide-conducting and proton-conducting SOFCs present distinct advantages and challenges when using hydrocarbon fuels. Generally, oxide-conducting SOFCs demonstrate superior efficiency due to their elevated operating temperatures and swift  In this review, we present the progress in hydrocarbon-fuelled SOFCs, particularly those featuring Nickel (Ni)-based anodes and oxide-ion-conducting electrolyte by examining the research output on this subject primarily from the past 20 years. The following section covers inclusive information on different approaches available for direct utilisation of hydrocarbons. Section 1 presents the background of the SOFCs operation with hydrocarbon fuels, while Sections 2 and 3 summarise information on an SOFC system operated by methane (CH 4 ) and heavier hydrocarbons, respectively. As our emphasis is placed on the research with Ni-based anodes operated by hydrocarbons, therefore Sections 2 and 3 largely report different existing strategies and results with respect to the electrochemical performance for works using Ni-based cells. Section 4 analyses the literature and tries to propose next research advances, mainly on the development of anode, stable operating conditions and microstructure tailoring of the cell. Ultimately, a sound understanding of the various approaches to hydrocarbon-fuelled SOFCs is crucial for better improvement and optimisation, aiming at accelerating the commercialisation of an SOFC system for a variety of applications.

Comparison between Oxide-Ion-Conducting SOFCs and Proton-Conducting SOFCs Fuelled by Hydrocarbons
Both oxide-conducting and proton-conducting SOFCs present distinct advantages and challenges when using hydrocarbon fuels. Generally, oxide-conducting SOFCs demonstrate superior efficiency due to their elevated operating temperatures and swift oxide ions transport [14]. This leads to improved energy conversion from hydrocarbon fuels, enhancing overall performance. By contrast, although proton-conducting SOFCs operate at lower temperatures where it provides the advantages in material stability and longevity [15], a trade-off arises in terms of efficiency compared to oxide-conducting SOFCs. In addition, oxide-conducting SOFCs prove more adept at accommodating a broad spectrum of hydrocarbon fuels, affording greater fuel flexibility, courtesy of their high operating temperature that facilitates efficient fuel reforming. On the contrary, proton-conducting SOFCs may necessitate specific reforming conditions to attain optimal performance. Additionally, both types of SOFCs face material selection challenges. Oxide-conducting SOFCs require materials capable of enduring high temperatures, potentially impacting long-term stability. In contrast, proton-conducting SOFCs benefit from lower operating temperatures yet encounter challenges linked to proton conductivity and slower kinetics.
Oxide-conducting SOFCs are typically more resilient against carbon formation when supplied with hydrocarbon fuels. Their higher operating temperatures and thermodynamic conditions enable efficient carbon management, reducing the risk of carbon deposition and ensuring prolonged cell performance. This distinction highlights the importance of considering the type of SOFC electrolyte when utilising hydrocarbon fuel to achieve clean and efficient energy conversion. When considering the use of hydrocarbons, oxide-conducting SOFCs appear as a compelling choice given by their higher efficiency, greater fuel flexibility and resistance to carbon deposition. These attributes align remarkably well with the imperatives of efficient energy conversion and sustainable use of hydrocarbon feedstocks. While proton-conducting SOFCs offer advantages in certain contexts, such as lower operating temperatures, their limitations in terms of efficiency and carbon management underscore the significance of oxide-conducting SOFCs for effectively harnessing the potential of hydrocarbon fuels in clean energy applications [16]. In addition, the materials employed in the fabrication of proton-conducting SOFCs are comparatively more expensive than those used for oxide-conducting SOFCs.
Recent work by Mojaver et al. entailed the simulation of a power generation system that utilizes an integrated CH 4 -fed SOFC and organic Rankine cycle (ORC), with validation carried out using available experimental data [17]. The model underwent thorough validation against the literature data. A comprehensive comparative assessment of the system's performance was then undertaken, comparing the oxide-conducting SOFC with the proton-conducting SOFC. This analysis encompassed evaluations across energy, exergy, Energies 2023, 16, 6404 4 of 36 economic and environmental perspectives. The input variables taken into account were the current density and stack temperature. The findings pointed to the superiority of the oxide-conducting SOFC across various domains, i.e., energy, exergy, economic and environmental, when operating under their respective optimal conditions. It is noteworthy that this deduction is likely to hold consistently within the explored ranges of decision variables.
As the global energy landscape continues to progress, the better performance of oxideconducting SOFCs with hydrocarbon fuels positions them as a frontrunner in the pursuit of a cleaner and more sustainable energy future.

Mode of Operations for Hydrocarbon SOFCs
The use of hydrocarbons from fossil fuel or renewable sources is desirable for energy generation as certain difficulties associated with hydrogen (H 2 ) production, safety, storage and distribution have yet to be resolved [18][19][20]. With escalating demand and limited supply, hydrocarbons will become even more pricey, emphasising the importance of high conversion efficiency of energy generation devices such as SOFCs. While significant progress has been achieved in H 2 -fuelled SOFC studies, investigations continue into the potential use of hydrocarbons. Fuel flexibility is one attractive feature of SOFCs, as they may operate using hydrocarbon fuels, i.e., natural gas, biogas, etc., with less fuel processing compared to other fuel cell types [21].
For hydrocarbon-fuelled oxide ion-conducting SOFCs, there are several modes of operations including external fuel reforming prior entering the cell, internal reforming or directly feeding the pure hydrocarbon into the cell [22]. These approaches are represented in Figure 2, where Figure 2a shows the ideal operation with direct oxidation of the hydrocarbon fuels, and Figure 2b-d illustrate the reforming of hydrocarbon fuels either through external reforming, indirect internal reforming or direct internal reforming, respectively. tion carried out using available experimental data [17]. The model underwent thorough validation against the literature data. A comprehensive comparative assessment of the system's performance was then undertaken, comparing the oxide-conducting SOFC with the proton-conducting SOFC. This analysis encompassed evaluations across energy, exergy, economic and environmental perspectives. The input variables taken into account were the current density and stack temperature. The findings pointed to the superiority of the oxide-conducting SOFC across various domains, i.e., energy, exergy, economic and environmental, when operating under their respective optimal conditions. It is noteworthy that this deduction is likely to hold consistently within the explored ranges of decision variables.
As the global energy landscape continues to progress, the better performance of oxide-conducting SOFCs with hydrocarbon fuels positions them as a frontrunner in the pursuit of a cleaner and more sustainable energy future.

Mode of Operations for Hydrocarbon SOFCs
The use of hydrocarbons from fossil fuel or renewable sources is desirable for energy generation as certain difficulties associated with hydrogen (H2) production, safety, storage and distribution have yet to be resolved [18][19][20]. With escalating demand and limited supply, hydrocarbons will become even more pricey, emphasising the importance of high conversion efficiency of energy generation devices such as SOFCs. While significant progress has been achieved in H2-fuelled SOFC studies, investigations continue into the potential use of hydrocarbons. Fuel flexibility is one attractive feature of SOFCs, as they may operate using hydrocarbon fuels, i.e., natural gas, biogas, etc., with less fuel processing compared to other fuel cell types [21].
For hydrocarbon-fuelled oxide ion-conducting SOFCs, there are several modes of operations including external fuel reforming prior entering the cell, internal reforming or directly feeding the pure hydrocarbon into the cell [22]. These approaches are represented in Figure 2, where Figure 2a shows the ideal operation with direct oxidation of the hydrocarbon fuels, and Figure 2b-d illustrate the reforming of hydrocarbon fuels either through external reforming, indirect internal reforming or direct internal reforming, respectively.  The reforming process transforms the hydrocarbon to simpler fuels, i.e., H 2 and CO, which can then be used directly in a fuel cell. While CO may be considered as a contaminant in most low-temperature fuel, SOFCs can be operated by it. This helps to simplify the fuel process by excluding the purification step. Fuel reforming can be performed externally, using a separate fuel processor known as a reformer, or internally at the anode (Figure 2b). A variant of internal reforming is either to add a separate reforming catalyst within the anode compartment (indirect internal reforming represented by Figure 2c) or directly on the anode (direct internal reforming as shown in Figure 2d) [23]. In a system with indirect internal reforming, reforming catalyst was integrated within the SOFC at the entry point of the hydrocarbons in anodic compartment. However, there could be a significant gradient between the rates of endothermic and exothermic reactions. This would cause a consequential decrease in local temperature at the upstream of anodic compartment that could lead to mechanical failure resulting from thermally induced stresses [24]. Alternatively, direct internal reforming works by the principle of direct feed of SOFCs using a mixture of fuel and reforming agents. This mode in overall offers lower operational cost, reduces the system complexity and necessitates less maintenance thanks to the relinquishment of external reformer, making the system more desirable.
Another considerable interest has been given to a process whereby hydrocarbon-rich fuel is directly fed into the anode compartment (i.e., without the reforming agents). Since external reforming increases complexity and cost to the system, direct feed of hydrocarbonrich fuel offers substantial advantages. This approach is poised to attain higher energy conversion efficiency in addition to the least fuel processing of the system. The direct use of hydrocarbons for SOFCs is, in principle, possible and attractive thanks to the particular prospect of gradual internal reforming of hydrocarbons. Conditionally, the anode material needs to satisfy several ideal criteria, including high catalytic activity for fuel oxidation and excellent ionic and electronic conductivity. At high SOFC working temperatures, either the direct electrochemical oxidation or the internal reforming/partial oxidation of the hydrocarbons becomes kinetically favourable. Nevertheless, these different modes of operation mentioned above have both advantages and disadvantages. Research into each method is still continuing to gain further understanding of the reaction mechanism, better cell performance and eventually helps to accelerate commercialisation. Overall, a different approach when dealing with an SOFC with Ni-based anode when operated with hydrocarbon fuels must be carefully considered with the major aim to avoid carbon formation to ensure stable performance.

Direct Hydrocarbon Utilisation
In theory, the use of hydrocarbons directly may improve the overall efficiency of a system. It is, however, worth mentioning that the understanding of "direct use of hydrocarbon fuels" by electrochemical means is still ambiguous. Compared to the wellunderstood chemical oxidation of hydrocarbons (i.e., hydrogenation and hydrogenolysis, partial oxidation and complete oxidation), the electrochemical oxidation of hydrocarbons is less well understood. In the literature, several terms have been introduced to designate "direct use of hydrocarbon fuels" such as direct utilisation, direct conversion or direct oxidation. This might lead to confusion and misinterpretation of precise definitions.
Mogensen and Kammer defined direct conversion of a hydrocarbon during SOFC operation as the "conversion in the SOFC without pre-mixing the fuel gas with steam or carbon dioxide (CO 2 ) and without processing the fuel before it enters the cell stack" [19]. This implies that the reaction is either through direct electrochemical oxidation or electrochemical oxidation of cracking products with the open circuit voltage (OCV) equals to the Nernst potential. Thus, all steps in the reaction of hydrocarbon conversion must be electrochemical in nature and any reaction pathways that encompass hydrocarbon cracking and electrochemical oxidation of the cracked products are not considered as direct oxidation. In our view, to interpret "direct use of hydrocarbon fuels" to be equivalent to "direct oxidation" is fairly rigid and unfeasible for actual application and, thus, less suitable.
Besides, it has been described that the direct electrochemical oxidation of hydrocarbons is unlikely to occur in one step [25,26]. Gas chromatography (GC) analysis has shown that partial oxidation reactions are dominant for some oxide anodes [27]. For that reason, to define "direct use of hydrocarbons" to be similar to "direct oxidation" seems impractical. McIntosh and Gorte instead suggested a broader definition describing the direct use of hydrocarbon fuels in an SOFC using the term "direct hydrocarbon utilisation" [20]. By this Energies 2023, 16, 6404 6 of 36 meaning, besides a process wherein a dry (i.e., pure) fuel is fed into the system, it also takes in humidified fuels (approximately 3 vol.% H 2 O), regardless of the exact reaction steps [20]. For practical reasons, such a definition is used throughout this review.
It is expected that operations with hydrocarbons as fuel will be much more complex than those using the simpler operating principle of a H 2 -fuelled system. As shown in Figure 3, there is a possibility of different parallel pathways during direct hydrocarbon use in SOFC, each with various individual steps. The ideal reaction for a hydrocarbon-fuelled SOFC is direct oxidation (Figure 2a), in which oxide ions (O 2− ) from the cathode travel through the electrolyte and oxidise the hydrocarbon at the anode triple phase boundary (TPB), a region at which the three components, oxygen ions, electrons and fuels, meet. This ideal and straightforward reaction represented by the following equation releases the most energy since no endothermic processes are involved: However, this requires effective catalysts and careful control of operating conditions. It may also involve multiple steps, along with side reactions such as pyrolysis and oligomerisation. Since side reactions are inherent during the actual operation, the electrochemical reactions for hydrocarbon fuel may proceed either through (1) oxidation of cracked carbon and hydrogen, (2) oxidation of an oxygenated compound or (3) oxidation of the intermediates produced from free radical reactions. this meaning, besides a process wherein a dry (i.e., pure) fuel is fed into the system, it a takes in humidified fuels (approximately 3 vol.% H2O), regardless of the exact react steps [20]. For practical reasons, such a definition is used throughout this review.
It is expected that operations with hydrocarbons as fuel will be much more comp than those using the simpler operating principle of a H2-fuelled system. As shown in F ure 3, there is a possibility of different parallel pathways during direct hydrocarbon in SOFC, each with various individual steps. The ideal reaction for a hydrocarbon-fuel SOFC is direct oxidation (Figure 2a), in which oxide ions (O 2− ) from the cathode tra through the electrolyte and oxidise the hydrocarbon at the anode triple phase bound (TPB), a region at which the three components, oxygen ions, electrons and fuels, m This ideal and straightforward reaction represented by the following equation releases most energy since no endothermic processes are involved: However, this requires effective catalysts and careful control of operating conditio It may also involve multiple steps, along with side reactions such as pyrolysis and oli merisation. Since side reactions are inherent during the actual operation, the electroche ical reactions for hydrocarbon fuel may proceed either through (1) oxidation of crack carbon and hydrogen, (2) oxidation of an oxygenated compound or (3) oxidation of intermediates produced from free radical reactions. Although an SOFC offers the advantage of fuel flexibility, its choice is still limited the affinity of the hydrocarbons to foul the regularly used Ni-cermet anode surface. T fouling which is caused by the carbon formation has become a major impediment t needs to be solved for stable SOFC operation. Unless a suitable catalyst is present to rea direct oxidation of hydrocarbons to minimise this problem, hydrocarbons must be formed prior to the electrochemical reactions. Another concern is catalyst poisoning contaminants such as hydrogen sulphide (H2S), which could poison the catalyst conta ing anodes. There have been several comprehensive reviews about this topic [28, where interested readers can refer to and it is worth mentioning that it is beyond the sco of this review. Although an SOFC offers the advantage of fuel flexibility, its choice is still limited by the affinity of the hydrocarbons to foul the regularly used Ni-cermet anode surface. This fouling which is caused by the carbon formation has become a major impediment that needs to be solved for stable SOFC operation. Unless a suitable catalyst is present to realise direct oxidation of hydrocarbons to minimise this problem, hydrocarbons must be reformed prior to the electrochemical reactions. Another concern is catalyst poisoning by contaminants such as hydrogen sulphide (H 2 S), which could poison the catalyst containing anodes. There have been several comprehensive reviews about this topic [28,29], where interested readers can refer to and it is worth mentioning that it is beyond the scope of this review.

Carbon Formation
An intrinsic problem in SOFC operation when using hydrocarbons as fuel is the formation of carbon through undesired side reactions. It has been reported that the deposition of carbon disrupts the performance of an SOFC, particularly one with Ni-based anodes, as Ni itself is an excellent catalyst for C-C and C-H bond breakage [30]. At high temperatures, hydrocarbon reactions may occur not only on the anode surfaces but also at the interconnect plates and the tubes connecting to the anode compartment. It could also happen in the gas phase via free-radical cracking and polymerisation, forming tar. This deposited carbon can cause pore blockage, obstruct reforming reactions through catalyst particle encapsulation and increase transport resistance to gases trying to reach the TPB, hence lowering the overall system performance.
If this technology is to be practical and economical, understanding the mechanism of carbon formation is indispensable. There are two mechanisms that have been generally reported: first, heterogeneous reaction on catalyst surfaces, producing carbon nanowires or nanofibres, and secondly, homogeneous reaction in the gas phase, forming soot capable of being ubiquitously deposited at the anode. This soot or pyrolytic carbon may cover and deactivate the catalyst. Thorough explanations of these mechanisms have been given by other researchers [19,20,22,31].
There are several factors that affect the degree of carbon formation including reforming agent to carbon (i.e., steam/C or CO 2 /C) ratio, operating conditions and catalyst material. Keeping the fuel within an equilibrium noncoking condition is one way for maintaining stable coke-free operation [20]. This region of stability for hydrocarbon fuels could be mapped based on thermodynamic calculations and would be a useful reference for avoiding severe effects of carbon deposition. Accordingly, selecting appropriate operating conditions (e.g., temperature, pressure and current density) may minimise the severity of the problem, if not totally eliminate it. As can be seen in Figure 4, the composition triangle for C-O-H shows carbon formation limits at 1000 • C, while 800 • C is close to 1:1 for a C/O ratio but displays a considerable discrepancy at a lower temperature. The addition of an ample amount of reforming agent (H 2 O, CO 2 or O 2 ) aids in diminishing the formation of carbon.

Carbon Formation
An intrinsic problem in SOFC operation when using hydrocarbons as fuel is the formation of carbon through undesired side reactions. It has been reported that the deposition of carbon disrupts the performance of an SOFC, particularly one with Ni-based anodes, as Ni itself is an excellent catalyst for C-C and C-H bond breakage [30]. At high temperatures, hydrocarbon reactions may occur not only on the anode surfaces but also at the interconnect plates and the tubes connecting to the anode compartment. It could also happen in the gas phase via free-radical cracking and polymerisation, forming tar. This deposited carbon can cause pore blockage, obstruct reforming reactions through catalyst particle encapsulation and increase transport resistance to gases trying to reach the TPB, hence lowering the overall system performance.
If this technology is to be practical and economical, understanding the mechanism of carbon formation is indispensable. There are two mechanisms that have been generally reported: first, heterogeneous reaction on catalyst surfaces, producing carbon nanowires or nanofibres, and secondly, homogeneous reaction in the gas phase, forming soot capable of being ubiquitously deposited at the anode. This soot or pyrolytic carbon may cover and deactivate the catalyst. Thorough explanations of these mechanisms have been given by other researchers [19,20,22,31].
There are several factors that affect the degree of carbon formation including reforming agent to carbon (i.e., steam/C or CO2/C) ratio, operating conditions and catalyst material. Keeping the fuel within an equilibrium noncoking condition is one way for maintaining stable coke-free operation [20]. This region of stability for hydrocarbon fuels could be mapped based on thermodynamic calculations and would be a useful reference for avoiding severe effects of carbon deposition. Accordingly, selecting appropriate operating conditions (e.g., temperature, pressure and current density) may minimise the severity of the problem, if not totally eliminate it. As can be seen in Figure 4, the composition triangle for C-O-H shows carbon formation limits at 1000 °C, while 800 °C is close to 1:1 for a C/O ratio but displays a considerable discrepancy at a lower temperature. The addition of an ample amount of reforming agent (H2O, CO2 or O2) aids in diminishing the formation of carbon.   Appropriate choice of catalytic material for reforming steps is another important issue to ensure stable system performance. The material has a substantial role as it must be efficient in preventing carbon formation and steady for long-term usage while remaining cost-effective. It is also worth mentioning that several studies reported that the actual ratio of reforming agent to carbon for efficiently suppressing coke formation considerably differs from that expected by thermodynamic calculations. This large discrepancy can be associated with the fact that thermodynamic calculations only provide insight into the predicted equilibrium conditions and do not consider the influence of reaction kinetics [33]. In this light, numerous researchers have examined the reaction kinetics of carbon formation, in search of optimum operating conditions and better materials for the anode [34].
Despite the challenges regarding carbon formation, direct hydrocarbon-fuelled SOFCs are interesting in terms of simplification of fuel processing and the overall energy costs may be substantially reduced. Works on this operation mode have been actively researched for the past two decades, whereby several approaches, including internal reforming or even direct feeding of the fuel into the cell have been studied. There does exist a major difference between the operation with methane (CH 4 ) and other higher molecular weight hydrocarbons (heavier hydrocarbons) as fuel. Theoretically, the molecule of CH 4 is simpler and relatively more stable and thus could be used directly (in undiluted form) with less tendency towards coking. Heavier hydrocarbons (i.e., other than methane), on the contrary, incline to cause a considerable coke or tar deposition on the anode or fuel-compartment surfaces, even when mixed with steam (steam reforming) or carbon dioxide (dry reforming). Therefore, the strategy to deal with heavier hydrocarbons may be differ from that of CH 4fuelled system. These processes are further elaborated upon in subsequent sections.

Methane-Fuelled SOFCs
Methane (CH 4 ), as an abundant resource and the main element of natural gas, is predicted to become the major hydrocarbon feedstock in future [35]. Natural gas is a fossil fuel that is much cleaner than coal and oil due to its higher hydrogen (H) to carbon (C) ratios in its molecular composition and contains a trivial amount of nitrogen (N) and sulphur (S) impurities. Other than that, CH 4 is also the main constituent in biogas with CO as the remainder. The biogas is produced from anaerobic fermentation of various organic matters such as manure, wastewater sludge, municipal solid waste or another decomposable feedstock. Accordingly, CH 4 could be viewed as a promising renewable energy resource which is important for energy generation.
To date, most studies conducted on hydrocarbon utilisation in SOFCs have used CH 4 as fuel (Table 1). This is largely due to a chemical profile throughout its electrochemical process that is simpler than that of heavier hydrocarbons. Ni-cermets continue to be the most frequently applied materials for an SOFC anode. However, as previously described, they are prone to coking, restricting their use in hydrocarbon-fuelled system. As noted earlier, this review emphasis on the research of SOFCs with Ni-based anodes fuelled by hydrocarbons. Further modifications on the Ni-cermets properties are essential along with several other strategies have been proposed in the literature to resolve such issues. Various ways to use CH 4 as fuel are discussed in the following sections which includes internal reforming mode either by steam, CO 2 or partial oxidation, as well as direct utilisation. Table 1 lists the methane-fuelled SOFCs, mainly those with Ni-based anodes and oxide-ionconducting electrolyte.

Internal Reforming
Thermodynamic means are one approach to controlling the formation of carbon during the operation of SOFCs with hydrocarbon fuels. This could be performed by introducing reforming agents such as steam or other oxygen-containing oxidants (CO 2 or O 2 ) together with the fuels into the fuel cell system. The internal reforming is a straightforward process by simply mixing hydrocarbon with reforming agents at a certain ratio to transform into simpler fuels such as hydrogen (H 2 ) and carbon monoxide (CO) in situ. Internal reforming of CH 4 and natural gas in SOFCs have been studied, either with or without partial prereforming [66,67]. However, operation with natural gas is slightly different from using pure CH 4 as some heavier hydrocarbons contained in the natural gas are likely to cause coking. Thus, the additional pre-reforming step is often required. An internal reforming process of pure CH 4 , instead, could be directly performed either through steam reforming, dry (CO 2 ) reforming or partial oxidation. During SOFC operation, one major virtue is that heat is generated in the cell by electrochemical reactions, and this ohmic heating could be directly used for the endothermic reforming reaction [67].
where ∆H 0 298 is the reaction standard enthalpy at 298 K. These different means for internal reforming are summarised in Table 2. Detailed information about these processes is discussed in the following sections. Table 2. Description of different types of reforming process.

Reforming Process Description
Steam reforming (SR) A process in which high-temperature steam is added to hydrocarbons (fuel) that transform into simpler fuels: H 2 and CO.

Dry reforming (DR)
A process in which CO 2 acts as an oxidant in the presence of a suitable catalyst.
Partial oxidation (POx) A chemical reaction between the hydrocarbons and oxygen (O 2 ) typically from the air in a substoichiometric ratio.

Internal Steam Reforming
A study on SOFC operation with hydrocarbons with steam as an input has been conducted as early as in 1962 [69]. Reforming the fuel internally may help to diminish the energy required for water gasification and lead to process simplification as the external reformer can be excluded. It has been reported that the effectiveness of internal reforming to be greater than that of external reforming in the same SOFC system [70]. This process typically applies a steam-to-carbon (S/C) ratio of higher than two to suppress carbon deposition. More interestingly, in the presence of generated water from the electrochemical reaction at the anode, the reforming process could occur even at a lower S/C ratio. Therefore, the supply of CH 4 mixed with a small amount of steam directly to the system inlet is attractive for process simplification.
The operating temperature and S/C ratio have major influences on the degree of coke formation. A CH 4 internal reforming study using electrolyte-supported single cells with different types of anodes, i.e., Ni-YSZ and Ni-GDC (gadolinium-doped ceria), were performed at various S/C ratios, from 0 to 3 [71]. At 950 • C, virtually no discrepancy in the reforming activities of both anodes was observed. However, at a lower temperature of 800 • C, the conversion rate greatly relies on the anode material with a higher CH 4 conversion obtained using a cell with Ni-GDC anode. A similar observation of catalytic activity for the reforming reactions has also been reported elsewhere [72]. It is often thought that a higher S/C ratio would lead to a more efficient reforming process as abundant steam would assist in gasifying deposited carbon and prevent carbon buildup. However, this may not always be the case, as a degradation of a Ni-YSZ anode has been discovered in a system operated with a S/C ratio of 3 [55]. The excess steam was found to oxidise nickel catalyst locally at a vicinity of the interface between electrolyte and anode. More important, excessive steam compromises power generation efficiency by diluting the fuel. Another drawback is that the endothermic nature of steam reforming reaction could cause local cooling where the resultant steep thermal gradient might mechanically damage the cell stack [73]. Although a lower S/C ratio is preferred, carbon may be formed at a ratio of less than one in the equilibrium causing poor electrochemical performance [74]. This is attributable to the deactivation of anode catalysts and the inhibition of fuel diffusion. Therefore, the S/C ratio should be carefully chosen depending on the type of anode materials and the operating conditions.
The improvement on the reforming process could be expected through the addition of catalytic materials into the Ni-based anodes. Incorporation of these catalysts as part of the anode may not only prohibit carbon deposition but also increase the electrochemical performance, as less water for reforming is needed. A noticeable reduction in carbon formation is observed on the modified Ni-YSZ cermets with small quantities (~1 wt%) of molybdenum (Mo) during CH 4 reforming, despite having a slight effect on the reforming activity and cell performance [73]. In contrast, another study employing a cell with copper (Cu)-based anodes reported an opposing outcome [75]. The deposition of MoO x has been believed to some extent to shield the electrocatalytic sites, reducing anode performance and thus being inappropriate in inhibiting coke formation. More research is, therefore, necessary to elucidate such discrepancies.
Takeguchi et al. performed a series of systematic studies on a modified Ni-YSZ anode for a system fuelled by CH 4 with a S/C ratio set at 2 [76,77]. Different alkaline earth oxides, such as calcium oxide (CaO), strontium oxide (SrO), ceria (CeO 2 ) and magnesium oxide (MgO) have been incorporated to the conventional Ni-YSZ anodes [76]. With the first three oxides, carbon deposition was suppressed, while MgO incorporation increased the rate of carbon deposition and reduced the steam reforming activity. A high content of SrO (~2 wt%) in the anode, however, led to poorer CH 4 conversion. Further improvement in the reforming activity could be achieved with the addition of precious metals such as ruthenium (Ru) and platinum (Pt) that helps to increase the anode resistance towards coke formation [77]. In another work, CH 4 steam reforming was conducted on a cell with dual-layer anode, Ni 0.5 Cu 0.5 Fe 2 O 4 and Gd 0.1 Ce 0.9 O 1.95−δ (NCF-GDC) composite, screen printed onto Ni-YSZ [78]. No significant signs of coking were detected during the operation using CH 4 -H 2 O (7 mol%) mixture as fuel at 800 • C and 0.20 A cm −2 . On the contrary, poor electrochemical performance was observed with fuel mixture containing an excessive amount of steam (20 mol% H 2 O) corresponding to fuel dilution.
Aiming at lowering SOFC operating temperature to less than 600 • C, Suzuki and co-workers have introduced a functional layer made of pure ceria, placed on top of the conventional anode surface [52]. Such a layer was beneficial in improving the maximum power density to 0.45 W cm −2 from 0.35 W cm −2 for a cell without such a layer when operated at 554 • C fuelled with CH 4 and steam mixture with nitrogen (CH 4 /H 2 O/ N 2 = 15/60/25 mL min −1 ). This additional layer allows reforming of CH 4 into H 2 and CO, which later being electrochemically oxidised within the anode-electrolyte TPB region.
Notwithstanding their practicality and effectiveness during SOFC operation, there are several concerns with regards to internal steam reforming that must be addressed. The endothermic nature of the process assists in cooling the stack, and it may be difficult to retain a uniform temperature and H 2 content throughout the stack. Severe cooling may take place near the fuel inlet if the reforming reaction is too rapid, causing a very large temperature gradient along the stack [67,79]. This shortcoming may give rise to inhomo-geneous temperature distributions which is detrimental to the mechanical properties of the cermet anode. One potential solution is to ensure an optimal operation wherein the reforming reaction and the electrochemical reactions progress at similar rates [80].

Internal Dry Reforming
Steam can be replaced by carbon dioxide (CO 2 ) as a reforming agent, a process known as dry reforming [81]. Other than being applied for producing synthesis gas (syngas) in the presence of a suitable catalyst, this technique appears to be a potential approach to mitigating greenhouse gases [82]. It is attractive from an industrial standpoint, as the resulting syngas has a low H 2 to CO ratio, suitable for Fischer-Tropsch reactions, a process to yield liquid hydrocarbons. This reforming system is also practical, given that both CH 4 and CO 2 are abundantly available and inexpensive. Despite its benefits, the reaction is very endothermic (∆H 0 298 = 247 kJ mol −1 ), requiring an extensive amount of energy. Moreover, reforming catalysts, which are often Ni-based, are susceptible to deactivation due to coke deposition. Hence, these issues need to be first addressed, and one way of doing it is by developing catalysts that have excellent activity and high resistance against coking [35,83]. In addition to Ni-based catalysts [84,85], other types of catalysts have been explored for this reaction, such as with precious metals, e.g., iridium (Ir), Rh, Ru, Pd, Pt and others [86][87][88]. These materials were reported to have an encouraging catalytic performance with respect to activity and selectivity to syngas formation. Precious metals are renowned for their outstanding coking resistance, yet do not seem to be practical for large-scale uses for economic reasons.
Alternatively, ceria (CeO 2 ) doped with materials such as zirconium (Zr), praseodymium (Pr) and niobium (Nb) were mixed with Ni and have been applied as anodes for an SOFC operated on CH 4 -CO 2 mixture [84]. The anodes were prepared by a hydrothermal method with a Ni content (14 vol.%), much lower than that of typical SOFC anodes (i.e., 30 vol.%). Among these, an anode containing Zr showed the lowest Ni crystallite size leading to a high initial activity on CH 4 dry reforming at 800 • C. Overall, the Ni-CePr catalyst had the least carbon formation associated with the greater oxygen conductivity of CePr support that facilitates carbon removal.
Apart from material selection, the influence of the microstructure of the anode on the catalytic properties under dry reforming has been investigated [89]. Two types of Ni-cermet anodes (i.e., Ni-YSZ and Ni-GDC) with different microstructure upon a sintering process at different temperature were compared. By determining the specific surface area of these anodes and through morphological observations, it was established that anode microstructure has significant impacts on the catalytic properties. The specific surface area of the anode considerably affected the CH 4 conversion rate whereby the cell with a Ni-YSZ anode sintered at 1200 • C which has a larger surface area gave a higher conversion rate. Another simulation study proposed an innovative SOFC configuration based on the coupling of the fuel cell and CH 4 dry reforming method [82]. Using Aspen Plus, the performance between the more common steam-methane-reforming (SMR)-SOFC and dry-methane-reforming (DMR)-SOFC processes was compared, where the efficiency was much better for the latter configuration with an increment of 6.4%. In another work, the prospect of co-generating electricity and CO-concentrated syngas has been demonstrated [90]. A functional layer made of a Ni 0.8 Co 0.2 -La 0.2 Ce 0.8 O 1.9 (NiCo-LDC) composite was added onto the anode support, and the system was fed by a CH 4 -CO 2 stream. Such a layer efficiently catalysed dry reforming in situ with CO 2 conversion reaching 91.5% at 700 • C and remaining stable for 100 h. Moreover, CH 4 was effectively converted through electrochemical oxidation, producing CO-concentrated syngas in the anode effluent. At 700 • C, maximum power density surpassed 0.91 W cm −2 with a low polarisation resistance of 0.121 Ω cm 2 . More interestingly, this system is thermally self-sufficient, as the heat released by the H 2 electrochemical oxidation compensates for the requirements of the endothermic dry reforming reaction.
In addition, the performance and degradation mechanisms of a Ni-based anodesupported SOFC operating at ∼800 • C on the direct internal reforming of dry CH 4 -CO 2 Energies 2023, 16, 6404 13 of 36 mixtures have been studied by Lanzini et al. [91]. Internal reforming with CO 2 has been shown to be effective in reducing carbon formation with a great prospect to cogenerate syngas and concurrently treat greenhouse gases, although, similar to steam reforming, the excessive ratio between CO 2 and CH 4 would dilute the fuel, affecting the H 2 yield and the overall efficiency of the system [92]. Accordingly, optimal operating conditions are of great importance in order to achieve decent performance.

Partial Oxidation
Partial oxidation (POx) involves a chemical reaction between the hydrocarbon fuel and oxygen generally from the air, in a substoichiometric ratio, thus the term "partial oxidation". This alternate approach to fuel reforming allows stable operation, where electricity and valuable chemical products such as syngas are coproduced [93,94]. However, considerable energy loss during oxidation of the hydrocarbon has caused the system with POx to be less energy efficient than with steam reforming even without heat recovery [95]. Nevertheless, the simplicity of the process makes POx attractive, i.e., for auxiliary power unit (APU) application [96].
Asano et al. applied a cell composed of Pt-BaCe 0.8 Y 0.2 O 3−δ -Au operated under POx [97]. Their system did not require a separate supply of fuel and oxidant gases, as the two electrodes (Pt and Au) were exposed to the same mixture of CH 4 and air. Pt functions as a fuel electrode catalysing the partial oxidation of CH 4 to form H 2 and CO, whereas Au acted as an oxygen electrode. Electrochemical reduction of oxygen takes place on discharging the cell. In a uniform atmosphere, the cell produced 0.17 W cm −2 at 950 • C.
An attempt to decrease the reforming temperature has been proposed by using catalytic partial oxidation (CPOx), reducing temperatures from about 1200 • C to between 800 and 900 • C, using Ni as a catalyst. Many articles related to catalysts for POx of CH 4 could be referred [98][99][100]. The state-of-the-art anode is mainly of Ni cermets, as Ni itself acts as a catalyst for the partial oxidation and at the same time functions as an electronic conductor. Nevertheless, similar to the steam and dry reforming, the use of modified Ni catalysts with elements having multiple oxidation states (e.g., Pt and Rh) for a POx process led to a better performance than using pure Ni. Employment of these catalysts led to higher reaction temperature, better fuel conversion and faster O 2 conversion [101]. A microtubular (MT)-SOFC consisting of an anode coated with added catalytic material coupled with a POx process demonstrated stable operation for over 1000 h [102]. Additionally, Majewski and Dhir reported steady power generation through direct feeding of CH 4 using a microtubular cell with a reforming catalyst placed at the cell inlet [103]. The catalyst in a honeycomb structure gave better fuel conversion with a constant rate of H 2 production and trivial coke deposition. They also investigated the temperature distribution along an MT-SOFC [60]. Such studies showed that not only catalyst structure could affect the SOFC performance, but the positioning of the catalyst also plays a major role in ensuring the stable operation.
A system fed with a CH 4 :O 2 ratio of 2 showed negligible carbon formation, and Ni oxidation was inhibited [104]. Cells with different anodes, Ni-YSZ or Ni-GDC, were compared, whereby in all cases, the latter had superior electrochemical performance. The maximum power densities achieved with a Ni-GDC anode were 1.35 W cm −2 and 0.74 W cm −2 at 650 • C and 550 • C, respectively. For Ni-GDC anode, the chemical analyses indicated that oxidation of Ni is inhibited which is due to the oxygen exchange ability of GDC. The use of various reforming agents (H 2 O, CO 2 or O 2 ) to reform CH 4 was systematically studied using a cell with a Ni-ScSZ (scandia stabilised zirconia) anode and a functional layer at 850 • C [105]. It was observed that the maximum power densities of the system operated on all three gas mixtures increased initially as the ratios of CH 4 -to-reforming agents increased but inevitably reduced afterwards. The maximum power densities were acquired at CH 4 : H 2 O/CO 2 /O 2 ratios of 2:1, 4:1 and 8:1, respectively. Too much reforming agents result in large quantities of unconverted H 2 O, CO 2 and O 2 given by the poor catalytic activity of the anode. These unconverted gases diluted the fuels, reducing H 2 /CO concentra-tion. Likewise, a high CH 4 -to-reforming-agent ratio also leads to decreased H 2 and CO concentrations in the fuel gas because of the low amount of these gases are formed.
Another mode of operation which combines POx and reforming either with steam or CO 2 could as well be applied for CH 4 -fuelled SOFCs. This strategy, so-called autothermal reforming (ATR), has the benefits of both processes; it is more flexible than steam reforming on start-up time and has higher efficiency than POx. By carefully controlling the ratio of steam to hydrocarbon fuel and the amount of oxygen supplied, an ATR system can achieve a self-sustaining process. The heat generated by the POx reaction provides the necessary energy for the endothermic steam reforming reaction. The resulting gas mixture, consisting of hydrogen, carbon monoxide and water vapor, is then used as a fuel for the SOFC. The effects of CO 2 and air addition for a system fed by CH 4 have also been studied through modelling [106], in which the stability, which was evaluated by monitoring the fluctuations in voltage at constant current density, was greatly influenced by carbon deposition. At 800 • C, maximum power densities of more than 1 W cm −2 could be achieved with fuel streams of 75% CH 4 -25% CO 2 [106]. Mixing CH 4 with air as the gas inlet has also been found to increase the stability of the system. Another steady operation for 100 h has been demonstrated for a system fuelled with a 1:5 air-to-CH 4 ratio [107].
Some works from the literature indicate that the long-term use of Ni-based cermet anodes (i.e., Ni-YSZ and Ni-GDC) might not be appropriate for SOFCs fuelled by CH 4 even with internal reforming or partial oxidation. Nevertheless, suitable modification of this type of anode is always essential by incorporating suitable catalytic materials that could lower the activity for carbon formation. In addition, the optimum ratio between the reforming agent and CH 4 is crucial to both evade fuel dilution and suppress formation of carbon.

Direct Methane Utilisation
Here, we define "direct utilisation" of methane (CH 4 ) as a process where pure or nearly pure CH 4 (i.e., mix with about 3% of H 2 O, CO 2 or O 2 ) is introduced to the system, analogous to the definition adopted in a previous review [40]. This approach is possible even if the fuel does not undergo the external reforming process. A long-term steady power generation was demonstrated by a system operated with humidified CH 4 (3% H 2 O) at 1000 • C using Ni-ScSZ as anode [108]. It has also been described that during direct utilisation, gradual internal reforming (GIR) may occur by using electrochemically generated H 2 O and CO 2 [109]. This GIR concept is based on a self-sustained operation in which the water produced from the electrochemical oxidation of H 2 reacts in the in situ steam reforming reaction of the hydrocarbon fuel. Provided appropriate conditions are applied, direct SOFC operation with CH 4 using the conventional Ni-YSZ anode has also been shown to be possible [42]. Despite the encouraging performance of this Ni cermet, it is susceptible to coking, as Ni catalyses the hydrocarbon cracking. Several strategies have been proposed to inhibit carbon formation, especially when using Ni-based anodes [110]. These may be categorised into the following: stable operating conditions, modification of a Ni-based anode through surface decoration or incorporation of additional catalyst materials and application of barrier or catalytic layer, placed onto the anode. Alternatively, the use of non-Ni anodes has been actively researched as well.

Stable Operating Conditions
Several studies have reported the feasibility of operating a stable SOFC without coking through direct utilisation of CH 4 under controlled working conditions [42,[111][112][113]. There are two approaches involving either operating at a high current density or applying a low working temperature, typically less than 700 • C. The latter could effectively hinder CH 4 cracking, whereas high current density means there are more reaction products (CO 2 and H 2 O) that could help to facilitate fuel reforming [73]. The noncoking operation can still be achieved even at higher temperatures if appropriate current density is applied [43]. Otherwise, coking is expected to occur, leading to rapid cell failure. During the SOFC operation, the primary electrochemical reaction taking place in anodic compartment involves CH 4 reforming to produce H 2 O (steam) which is subsequently oxidised into H 2 [43]. The resulting steam assists in removing carbon, preventing coking at high applied current densities.
The direct CH 4 operation of Ni-YSZ anode-supported cell resulted in power densities of 0.96 W cm −2 at 800 • C has been reported [42]. By assuming partial oxidation of solid carbon as part of the anodic reactions, the measured OCV value was consistent with theoretical values. A two-step reaction mechanism was proposed involving, firstly, CH 4 cracking followed by the electrochemical oxidation of the resulting solid carbon. A significant buildup of carbon on the anode was suppressed by retaining an appropriate current flowing through the cell. Lin et al. studied the stability of a humidified CH 4 -fuelled cell at different current densities and temperatures [43]. They observed that for operation at 650 and 700 • C, a minimum current density of around 0.1 A cm −2 was necessary to retain stable operation. At higher operating temperatures, larger critical current density is needed, ranging from 0.8 to 1.2 A cm −2 and 1.4 to 1.8 A cm −2 for systems run at 750 and 800 • C, respectively. These results showed that the oxygen ions (O 2− ) flux, conducted through the electrolyte, was in part accountable for hindering carbon formation and allowing steady operation.
Another research explained that a sufficient local oxygen partial pressure originated from the pumping of oxygen ions from the cathode side could as well impede the hydrocarbon cracking [114]. This "self-decoking" phenomenon has been observed in a system with a Ni-CGO anode (3:5 by weight) where the pumped oxygen ions could electrochemically remove carbonaceous deposits. A higher CH 4 utilisation rate was associated with an increase in CO selectivity. Jiao et al. showed the possibility of continuous power output in a system with a Ni-YSZ anode using pure CH 4 . This could be achieved by intermittent supply of CH 4 , whereby fuel supply and consumption play a substantial role in controlling the carbon deposition and its utilisation [115]. This alternative operating mode is feasible in enhancing the stability of direct methane SOFCs; however, prolonged duration of such an operation must be investigated to verify its long-term stability.

Anode Surface Decoration or Incorporation of Additional Materials
Introducing another material with high ionic conductivity and excellent catalytic properties (e.g., metals or oxides) into the Ni cermet anode is another way for system optimisation. This may be realised through Ni alloying with other metals or by surface modification via various techniques including wet impregnation, electrochemical deposition (electroplating) and microwave irradiation processes. Several researchers have ascertained that alloying Ni with another element could give better carbon tolerance. This is due to the reduction in the activity of Ni when it is alloyed with another metal that has lesser catalytic activity for cracking or for activation of C-H bonds. For instance, the alloy of Ni and copper (Cu) is anticipated to improve the stability of the anode during SOFC operation with hydrocarbons by suppressing carbon formation. Copper is known to be catalytically inactive towards hydrocarbon cracking reactions but works excellently as a current collector. A cell with Ni-Cu-YSZ anodes supplied with CH 4 showed the presence of carbon deposited on such alloys surface, whereby the carbon deposition was reduced with the increasing amount of Cu [39]. Similarly, a cell made of Ni-Cu-GDC [116] presented improved performance with minor carbon deposition after long-term operation with dry CH 4 at 750 • C. Furthermore, using Cu-Ni-samaria-doped ceria (SDC) anode-supported cell, the maximum power density of 0.317 W cm −2 was achieved at 600 • C [117]. While losing 60% of power density after 7 h of operation in dry CH 4 with bare Ni, only 7% or 2% losses were measured after 12 h when Cu was doped into the cermet or added as an interlayer, respectively. The poor performance with a pure Ni anode is mainly due to the agglomeration of Ni particles and carbon deposition.
A nanostructured Cu-Ni-CeO 2 -YSZ anode (i.e., Cu-Ni-CeO 2 impregnated into porous YSZ) has been employed which presents higher resistance to carbon deposition than the conventional Ni-based anode [118]. To assess the resilience of the Cu-Ni-CeO 2 -impregnated YSZ anode against coking, different types of anodes were prepared, including a blank porous YSZ matrix, Ni-impregnated YSZ and Cu-Ni-CeO 2 -impregnated YSZ. The loadings of both Ni and Cu-Ni-CeO 2 were controlled at 40%. The results revealed a significant formation of carbon in the Ni-impregnated YSZ sample, while a reduced amount of black carbon was practical in the Cu-Ni-CeO 2 -impregnated YSZ sample, and no noticeable carbon deposition occurred in the porous YSZ sample. The nanostructured anode with a composition of Cu 0.5 Ni 0.5 alloy had the best performance. Hence, the content of added metal, in this case, Cu plays a significant role in suppressing problems with coking. A contradictory outcome was reported, whereby the Cu−Ni alloys were found to be unstable in the presence of hydrocarbons, depending strongly on pre-treatment conditions [119]. Thus, more research should be performed to further investigate the suitability of Cu-Ni alloy as an anode for direct CH 4 utilisation.
Another progress was realised using a Sn-modified Ni-based anode, whereby Sn doped with nanosized Ni and GDC were conjugated on a core GDC nanocomposite anode [120]. Operation with dry CH 4 produced a power density of 0.93 W cm −2 and retained stable operation at 650 • C for over 40 h. Similarly, Yang et al. also used a Sn-modified Ni-based anode SOFC [121], in which a steady operation with humidified CH 4 is achieved in a temperature range of 700-800 • C, using a cell with an Ni-SDC anode containing additional 1 wt% Sn into the porous anode.
Introducing alkaline earth oxide materials to the Ni-cermet anode is another route to reduce carbon accumulation. Theoretically, basic oxides can increase coking resistance through stimulating the reaction of steam or CO 2 with the solid carbon. Asamoto et al. were among the first to study the effects of adding different alkaline earth metal oxides such as MgO, CaO, SrO and BaO to a Ni-SDC anode for direct oxidation of CH 4 [122]. It was found that the addition of these materials leads to lower maximum power densities compared to the bare Ni-SDC. Nevertheless, only Ni-CaO-SDC showed viable stability for 24 h operation, as indicated by minor changes in the terminal voltage.
Using BaO as part of the anode contributed to enhanced carbon tolerance caused by the discrete BaO/Ni interfaces that preferentially adsorbed H 2 O and gasified the carbon deposits [123]. However, there is concern about the diffusion of BaO into YSZ, leading to adverse changes in morphology and volume expansion in the YSZ grains. Hence, a novel fabrication procedure based on microwave irradiation was proposed to selectively deposit BaO solely on Ni [124]. The anode prepared via this technique shows comparable electrochemical performance using dry CH 4 feed to that of conventional and impregnated anodes resulting in lower carbon accumulation when operated at 800 • C. A cell comprising an anode made of Ni 0.75 Fe 0.25 -xMgO-YSZ, where x represents the weight percentage, was operated with humidified CH 4 as fuel at intermediate temperatures [125]. It was found that in the cell with the MgO weight percentage of 5%, a Ni 0.75 Fe 0.25 -5%MgO-YSZ anode gave the best performance, generating~0.65 W cm −2 at 800 • C.
Work by Yang et al. showed that a MgO-modified Ni-cermet anode had better tolerance towards carbon deposition [126]. A Ni-cermet anode was impregnated with a small amount of MgO (1.25 to 3.75 wt% with respect to Ni). The cell with a loading of MgO of 2.5 wt% generated a high-power density of 0.714 W cm −2 and was stable for over 300 h when operated with wet CH 4 at 800 • C. This excellent coking tolerance was associated with the better adsorption properties of H 2 O and CO 2 on MgO as demonstrated experimentally and corroborated by density functional theory (DFT) calculations [126]. MgO is a strong Lewis base, which has a high adsorption capability for CO 2 to help to impede carbon deposition. This indicates that the properties of MgO could yield a paramount effect on the adsorption strength and dissociation characteristic of the involved reactants.
Liu et al. studied the doping of alkali metals (Li or Na) with NiO powder to formulate anode material with enhanced features [59]. Both Li-Ni-SDC and Na-Ni-SDC anodes have been found to increase the capability of adsorbing water vapour and CO 2 under cell operating conditions, enhancing coking tolerance and prevent the deactivation of the anode. The cells with modified anodes demonstrated higher OCVs, improved long-term stability and a maximum power density double that of an unmodified Ni-SDC anode.
Incorporating noble metals which are known for their excellent hydrocarbon reforming activity could as well further improve anode characteristics. A Ru-modified anode showed practical reforming activity of hydrocarbon and excellent resistance towards coking. A single cell with a Ni-GDC-3wt% Ru anode powered by dry CH 4 generated peak power density of 0.75 W cm −2 [41]. Coking of the cell was not observed within 12 min of applied current density of 0.6 A cm −2 and short exposure to the OCV condition. During fuel oxidation reactions, Pd has been described to assist in the adsorption, dissociation and diffusion processes [127,128]. The impregnated Pd transformed the inert Ni-LSC-SDC anodes to be catalytically active towards CH 4 oxidation [127]. In terms of predominant reaction path, the CH 4 activation step appears to be governed by a nonelectrochemical process on the Pd-Ni catalyst, whereas, for the noble Pd catalyst, the activation step only takes place electrochemically on active sites [127].
A cell with an anode composed of three-phase composite powders, NiO, YSZ and Ba x Zr x Y x O (BZY) prepared via spray pyrolysis was tested using dry CH 4 [129]. With the proper amount of BZY (which is a proton conductor), superior anode performance was observed. In addition, the impregnation of other types of proton-conducting perovskites, such as BaCe 0.9 Y 0.1 O 3−δ (BCY) and BaCe 0.9 Yb 0.1 O 3−δ (BCYb) into Ni-GDC has also been reported to lower polarisation and better stability of the system operated with humidified CH 4 by preventing carbon deposition [130].
Overall, improvement of anode properties is desirable mainly for one made from Ni cermets to make them suitable for operation with hydrocarbons. A number of reviews providing a detailed discussion on the selection, progress and the modification techniques are available in the literature for further understanding [131,132].

Anode Catalytic Layer
Barnett's group first demonstrated the idea of using a buffer layer (also termed as a catalytically active layer) applied onto the anode surface to improve system performance [133,134]. There are various terminologies which describe the additional layer, incorporated adjacent to the anode, that have been used in the literature, such as a barrier layer and anode functional layer (AFL). However, it is worth noting that in most SOFCs fuelled by H 2 , the AFL is aimed to reduce the activation and concentration polarisations while enlarging TPB, a region upon which the electrochemical reactions occur [135]. Furthermore, AFL for cells operated with H 2 often has been positioned in between the anode and the electrolyte. Meanwhile, in hydrocarbon-fuelled SOFCs, the additional layer refers to the layer that helps to transform the hydrocarbon to much simpler fuels which are often positioned on top of the anode layer. For example, on the catalyst layer, CH 4 is first converted into CO and H 2 . Next, they diffuse towards the anode on which they participate in electrochemical oxidation to produce H 2 O, CO 2 and electricity. Since CO and H 2 possess higher electrochemical activities than CH 4 , the greater cell performance is anticipated following the application of catalyst layer.
The catalyst layer is typically composed of an oxide material with a minimal tendency for coking, functioning by lowering CH 4 partial pressure and trapping reaction products (H 2 O and CO 2 ) in the anode [133,136,137]. For instance, button cells with a barrier layer made from partially stabilised zirconia (PSZ) and ceria (CeO 2 ) succeeded in sustaining stable and coke-free operation in a system fuelled by humidified CH 4 [136]. A physical model was also used to predict the performance of fuel conversion into energy in tubular cells designed with barrier layers. The model confirmed that this layer facilitates the internal reforming during operation, leading to a free-coking problem.
Murray et al. were among the first to report the direct electrochemical oxidation of CH 4 [36]. They tested a cell with a (Y 2 O 3 ) 0.15 (CeO 2 ) 0.85 (YDC) porous film applied onto the Ni-YSZ anode and achieved power densities of up to 0.37 W cm −2 at 650 • C, and the operation was free of carbon deposition. This performance was matched with the common Ni-YSZ anode, while the YDC layer simultaneously reduced the interfacial resistance by a factor of 6. The capability of CeO 2 to catalyse the oxidation of hydrocarbon has been verified [138]. No carbon deposition could occur at a temperature less than 700 • C based on the theoretical calculation for CH 4 pyrolysis, proposing that such reaction will not take place in that particular operating condition. Beyond 700 • C, the amount of carbon deposited increased with increasing temperatures, while less carbon deposition was detected at a given temperature on Ni-YSZ/YDC anodes than on Ni-YSZ.
A tubular cell-employing double-layer anode consisting of NiO-YSZ as a support layer and CoO-NiO-SDC as an active reforming layer was tested for the direct conversion of CH 4 [44]. At 800 • C, the peak power density was 0.35 W cm −2 . There was no indication of carbon deposition on the surface of the anode when the cell was operated at 0.25 A cm −2 . Due to its high activity, a mesoporous SDC catalyst layer impregnated with Ru showed an excellent activity for CH 4 electrocatalytic oxidation, achieving a maximum power density of about 0.462 W cm −2 in intermediate temperature [139]. Furthermore, a catalyst layer consisting of 0.1 wt% iridium (Ir)-impregnated ceria applied onto a Ni-YSZ anode resulted in stable SOFC operation in dry CH 4 [47,109]. This type of a catalyst layer assisted in ensuring long-term stability for more than 200 h [109].
Depicted in Figure 5 is the principle of a gradual internal reforming (GIR) process using an anode with a catalytic layer. The process was initiated by feeding the system using 15% H 2 in argon. Upon reaching a steady state operation which was an hour after the start, the fuel inlet was abruptly switched to pure CH 4 [140]. The same author also applied a model with the CFD-Ace software (https://www.esi.com.au/software/cfd-ace/) to further investigate the GIR process at the anode. From a thermodynamic perspective, a system with a catalyst layer as reported in their earlier work effectively allows GIR without coking when fuelled with either pure CH 4 or using a mixture with a small quantity of steam [140].
in tubular cells designed with barrier layers. The model confirmed that this layer facilitates the internal reforming during operation, leading to a free-coking problem.
Murray et al. were among the first to report the direct electrochemical oxidation of CH4 [36]. They tested a cell with a (Y2O3)0.15(CeO2)0.85 (YDC) porous film applied onto the Ni-YSZ anode and achieved power densities of up to 0.37 W cm −2 at 650 °C, and the operation was free of carbon deposition. This performance was matched with the common Ni-YSZ anode, while the YDC layer simultaneously reduced the interfacial resistance by a factor of 6. The capability of CeO2 to catalyse the oxidation of hydrocarbon has been verified [138]. No carbon deposition could occur at a temperature less than 700 °C based on the theoretical calculation for CH4 pyrolysis, proposing that such reaction will not take place in that particular operating condition. Beyond 700 °C, the amount of carbon deposited increased with increasing temperatures, while less carbon deposition was detected at a given temperature on Ni-YSZ/YDC anodes than on Ni-YSZ.
A tubular cell-employing double-layer anode consisting of NiO-YSZ as a support layer and CoO-NiO-SDC as an active reforming layer was tested for the direct conversion of CH4 [44]. At 800 °C, the peak power density was 0.35 W cm −2 . There was no indication of carbon deposition on the surface of the anode when the cell was operated at 0.25 A cm −2 . Due to its high activity, a mesoporous SDC catalyst layer impregnated with Ru showed an excellent activity for CH4 electrocatalytic oxidation, achieving a maximum power density of about 0.462 W cm −2 in intermediate temperature [139]. Furthermore, a catalyst layer consisting of 0.1 wt% iridium (Ir)-impregnated ceria applied onto a Ni-YSZ anode resulted in stable SOFC operation in dry CH4 [47,109]. This type of a catalyst layer assisted in ensuring long-term stability for more than 200 h [109].
Depicted in Figure 5 is the principle of a gradual internal reforming (GIR) process using an anode with a catalytic layer. The process was initiated by feeding the system using 15% H2 in argon. Upon reaching a steady state operation which was an hour after the start, the fuel inlet was abruptly switched to pure CH4 [140]. The same author also applied a model with the CFD-Ace software (https://www.esi.com.au/software/cfd-ace/) to further investigate the GIR process at the anode. From a thermodynamic perspective, a system with a catalyst layer as reported in their earlier work effectively allows GIR without coking when fuelled with either pure CH4 or using a mixture with a small quantity of steam [140]. The performance of a single cell with a γ-Al2O3 layer placed onto a Ni-based anode presented a peak power density of 0.382 W cm −2 at 850 °C, more than double that of its The performance of a single cell with a γ-Al 2 O 3 layer placed onto a Ni-based anode presented a peak power density of 0.382 W cm −2 at 850 • C, more than double that of its counterpart without such a layer. This layer also assisted in sustaining stable operation with no carbon formation [141]. A strategy of having catalytic materials used as part of the anode and as a functional layer has been demonstrated [142], where Sn-doped Ni-YSZ was used as both an anode catalyst and a functional layer. This functional layer was sandwiched between the anode and electrolyte, creating a system capable of operating in an intermediate temperature range with a reasonably good power density. The cell achieved 0.41 W cm −2 when operated with humidified CH 4 at 650 • C. A comparison with a cell without Sn indicated that the stability of the operation is much better, as the Sn-doped Ni-YSZ cell worked for 137 h, while the Ni-YSZ cell ceased operation within 27 h. Alloying Ni with Fe is expected to assist in resisting carbon deposition due to lower activities of Fe. It was observed for a cell with a Ni-Fe alloy catalyst layer on top of the Ni-YSZ anode, operated with 97% CH 4 -3% H 2 O as fuel, the additional Ni-Fe layer was effective for CH 4 internal reforming in SOFC systems [143].
Direct internal reforming (DIR), as shown in Figure 2d, involves adding a reforming function to the anode and the reforming agent(s) (e.g., steam or CO 2 ) is supplied together with the hydrocarbon fuel. In this case, an important aspect of the steam-to-carbon ratio must be superior to 1 to prevent coking. As countermeasure to the thermal stress induced within the cell under DIR configuration as described in Section 1.1, new mode of operation has been initiated. Gradual internal reforming (GIR), such as DIR, is based on the synergy between fuel steam reforming taking place on a catalytic layer anode (Ni) and electrochemical oxidation of hydrogen occurring at the electrode's triple-phase. In both the GIR and DIR modes, hydrogen which is required by the electrochemical reaction is continuously generated in situ. They both also suffer from CO 2 production via water-gas shift reaction as depicted in Figure 5. However, unlike DIR which necessitates substantial amount of steam, the GIR process requires small quantity of steam at its fuel inlet, to the point where the steam electrochemically generated within the cell is adequate for the reforming reaction. This approach was the foundation of the works reported by Vernoux et al. [144] and Georges et al. [145] through which they had studied the feasibility of GIR in SOFCs. It has also been reported that an SOFC fuelled by CH 4 for a continuous period of 400 h without adding water, O 2 or CO 2 successfully delivered relatively stable power output [146].

Heavier Hydrocarbon-Fuelled SOFCs
Compared to CH 4 , the use of heavier hydrocarbons as a fuel for SOFCs appears to be more challenging, as it involves even more complex reactions. It has been recognised that carbon formation could damage the Ni-based anodes [147,148]. Particularly at high SOFC operating temperatures, carbon deposition is more likely to occur when using heavier hydrocarbons than CH 4 [149]. Even so, these fuels remain desirable from the perspective of fuel economy [150]; thus, various strategies have been attempted.
There are three ways to utilise heavier hydrocarbons as fuel for SOFCs. First, they may be partially and externally reformed, producing a highly concentrated CH 4 mixture which is then fed and internally reformed [96,151]. This is analogous to CH 4 internal reforming as deliberated in the previous section and is not discussed further below. Second, hydrocarbons can undergo an internal reforming process in which they are first mixed with reforming agents (either H 2 O, CO 2 or air) before being supplied to the system. Third, a pure or nearly pure hydrocarbon (humidified with~3% vol. H 2 O) may be introduced directly into the anode compartment. This mode of operation greatly depends on the properties and the ability of the anode material to suppress the formation of carbon. The following sections discuss the different approaches to the use of heavier hydrocarbons in SOFCs.

Internal Reforming
Internal reforming of heavier hydrocarbons for SOFCs is attractive for a simplified power generation system. A similar approach to a CH 4 -fuelled system could also be applied for the operation with heavier hydrocarbons, in which the fuel could be mixed with different reforming agent, i.e., steam, CO 2 or O 2 , before entering the anode compartment.

Internal Steam and Dry Reforming
The practicality of internal reforming of heavier hydrocarbons has been reported [149][150][151][152], contrary to the earlier report that claimed that only CH 4 could be internally reformed [153]. A study on the direct use of n-dodecane (C 12 H 26 ) has been conducted using cells with a Ni-ScSZ-cermet anode [149]. At a steam-to-carbon (S/C) ratio between 1 and 2, a steady operation at 0.1 A and nearly 45% fuel utilisation are attained with anode potential of approximately 0.77 V. No degradation of both the anode and current collector was observed. Similarly, stable operation is perceived at a lower S/C ratio of 0.5, but the Ni mesh current collector was partially disintegrated due to the metal dusting. The thermal Energies 2023, 16, 6404 20 of 36 decomposition of n-C 12 H 26 formed C 2 H 4 and H 2 as major products with negligible coke deposition. This was followed by steam reforming of hydrocarbons, CO shift reaction and H 2 electrochemical oxidation. The first two reactions turned out to be hostile at a low S/C ratio. Nevertheless, these reactions could be promoted with increasing fuel utilisation, and carbon deposition at the outlet tube is restrained although reforming reactions of hydrocarbons were incomplete.
The influence of steam and discharge conditions onto internal reforming of propane (C 3 H 8 ) was studied using different types of Ni-based anodes [150]. Even at a high S/C ratio, power generation characteristics with a Ni-YSZ anode were declined at 1000 • C due to carbon formation at low current densities. By contrast, stable operation at an S/C ratio of 0.8 was obtained when using either Ni-ScSZ or Ni-samaria-doped ceria (SDC) anode. At low S/C ratio operation, the carbon deposition rate was lower for a cell with a Ni-ScSZ anode than with Ni-YSZ. The overall performance analysis showed that the stability of Ni-based cermet was in the order of Ni-ScSZ > Ni-YSZ > Ni-SDC.
The addition of noble metals is envisioned to promote catalytic properties further during steam reforming [154]. This was demonstrated by the slower deterioration of anodes incorporated with Ru (i.e., Ru-Ni-YSZ and Ru-YSZ anodes) than the unmodified Ni-YSZ anode [150]. In another study, the degree of internal steam reforming activities for Ni-GDC and Ni-YSZ with butane (C 4 H 10 ) at 600 • C was compared, and the former was found to have better output [152]. However, the C 4 H 10 conversion was incomplete, as the gas hourly space velocity was low. To encourage fuel conversion, various dopants such as Cu, Sn and Rh were added to the NiO-GDC anode. Among these, the Rh-modified anode presented a complete conversion of C 4 H 10 without coking during operation with a S/C ratio set at 3 and showed a very low degradation rate when operated in an internal reforming mode.
A survey of the literature described that the presence of a catalyst layer combined with the internal reforming led to a better system performance. For example, two different structures of ceria (mesoporous powders and mesoporous flower-like microspheres), each was used to form a reforming catalyst layer and tested with a fuel mixture of 5% iso-octane, 9% air, 3% H 2 O and 83% CO 2 . In comparison, the cell with a flower-like mesoporous CeO 2 -Ru microsphere catalyst layer demonstrated superior performance, yielding a maximum power density up to 0.654 W cm −2 at 600 • C [155]. It is, however, worth noting that the high fraction of CO 2 added (as part of the agent for reforming processes) could also be responsible for the improved power output.
The direct utilisation of iso-octane (C 8 H 18 ) in an SOFC with a multifunctional anode (made of two layers) without cofeeding O 2 or CO 2 has also been described [156]. Unlike previous works which require a considerable amount of O 2 (typically from the air) or CO 2 to minimise coking and anode deactivation [134,155,157,158], a fuel mixture with a H 2 O-to-C 8 H 18 ratio of ∼0.5 was applied. This ratio is much lower than the ideal value of 8 for steam reforming. These dual-layer anodes have their specific functions, wherein the outer catalyst layer is used to reform the hydrocarbon fuels, while the inner active layer (adjacent to the electrolyte) provides sites for the electrochemical oxidation of the reformed fuels.

Partial Oxidation
SOFCs with an incorporated catalyst layer placed on top of the anode that allows partial oxidation have shown to be advantageous. Partial oxidation (POx) of C 3 H 8 on a Ni-YSZ anode [159] and a Ru-based catalyst layer applied on the anode [160] have been demonstrated. Zhan and Barnett were those who initiated the idea and implemented this approach by utilising a porous PSZ anode supported cell operated by C 3 H 8 [160]. A Ru-CeO 2 catalyst layer applied onto the PSZ surface catalysed the partial oxidation of C 3 H 8 at temperatures higher than 500 • C. The same authors also reported the practicality of using iso-C 8 H 18 , a high-purity compound similar to gasoline, for SOFCs [134,158,161]. The use of a porous PSZ or PSZ/CeO 2 disc positioned in between two Ru/CeO 2 layers was effective in hindering coking attributable to active CO 2 -reforming of iso-C 8 H 18 [134]. A Energies 2023, 16, 6404 21 of 36 similar catalyst layer applied on top of a thick Ni-SDC anode contributed to a stable power density of 0.6 W cm −2 at 590 • C with no sign of carbon formation.
In addition, this synergic method is reported to be effective for in situ reforming of various fuels including natural gas, propane (C 3 H 8 ), butane (C 4 H 10 ) and biomass in a tubular cell system [102]. An SOFC with four-layer internal reforming was found to be efficient in generating high power densities with stable operation. However, for proprietary reasons, the exact composition for the catalytic layer could not be disclosed by the authors.
Overall, the works discussed above show that the integrated catalyst layer is effective in stimulating the reforming process which allows a noncoking operation with steady power output. Although most of the studies reported in the literature were conducted in a small-scale, the obtained information was useful in providing better insight into internal reforming of heavier hydrocarbons during SOFC operation.

Direct Hydrocarbon Utilisation
Extensive efforts have been directed towards the direct use of hydrocarbons for the simplicity of the SOFC system. As larger hydrocarbons impose a greater challenge in direct use, a noncoking anode composition along with a synergistic approach to minimising coking is thus anticipated. Earlier, Park and coworkers demonstrated that operation with dry hydrocarbons including liquid fuels is possible, even without undergoing a reforming process [26]. Different types of hydrocarbons such as CH 4 , C 2 H 6 , 1-butene (C 4 H 8 ), n-C 4 H 10 and toluene (C 7 H 8 ) were tested using cells with a composite anode of Cu and CeO 2 (or Sm-doped CeO 2 ) operated at 700 and 800 • C. Stable operation with no indication of coking on the anode surface is perceived and the final products of the oxidation were CO 2 and water. However, the measured power density of a system fuelled by n-C 4 H 10 was relatively lower than that operated with H 2 .
It has been proposed that the direct oxidation of various hydrocarbons (i.e., CH 4 , C 2 H 6 and C 3 H 8 ) was interrupted by the steam and CO 2 formed as products of the electrochemical reaction [37,41]. Hence, these two components should be removed from the anode surface. This can be achieved by internally reforming unreacted hydrocarbons to further promote the electrochemical oxidation. To verify this assertion, the performance of a Ni-GDC anode modified by different catalysts such as Pt, Pd, Cu, Rh and Ru was studied by directly supply hydrocarbons to the system at 600 • C. These metal-modified anodes facilitate the reforming of the unreacted hydrocarbons using the generated steam and CO 2 , leading to better system efficiency. Interestingly, a system operated with dry CH 4 showed a comparable performance to one using humidified H 2 .
The direct use of 5.3 vol.% C 8 H 18 in N 2 was studied over a temperature range of 600 and 775 • C [162]. Mass spectroscopy analysis indicated the presence of CH 4 and C 2 H 2 ; both were the main products of C 8 H 18 thermal decomposition in the electrochemical reactions. An SOFC with Ni-YSZ anode was proposed to be operated below 750 • C for stable operation without coking. In another study, the influence of C 2 H 6 and C 3 H 8 in a simulated natural gas on the operation of a Ni-YSZ anode-supported SOFC was examined [66]. Incorporating a diffusion barrier layer made of PSZ, which has excellent catalytic properties, should stimulate the reforming reaction of hydrocarbons. This is verified as it was detected that H 2 -rich gases reach the anode surface instead of hydrocarbon fuels. A system fed by natural gas with 5% C 2 H 6 and 2.5% C 3 H 8 and the additional 33% of air at 750 • C demonstrated stable operation, and no noticeable coking was detected.
Another strategy to control carbon formation is by creating nanostructured BaO/Ni interfaces on the anode through a vapour deposition method, where the promotion of water-mediated carbon removal in a system fuelled with dry C 3 H 8 at 750 • C was demonstrated [163]. The system produced a constant peak power density of 0.88 W cm −2 . A main benefit of this BaO vapour deposition is that it can be readily integrated into existing processes for preparing SOFCs, as it does not require extra processing steps.
It has also been reported that composite oxide anodes, doped CeO 2 -LaFeO 3 (Ce(Mn, Fe)O 2 -La(Sr)Fe(Mn)O 3 ), displayed promising results in a system fed by either dry C 3 H 8 or dry C 4 H 10 [27]. After a long-term test, the system generated consistent power densities of approximately 1 W cm −2 at 800 • C with no observable carbon deposit. In another work, the same authors achieved even better performance using a similar composite anode, but with the addition of RuO 2 as a catalyst [164]. An anode consisting of 10 wt% RuO 2 contributed to a power density of 1.5 W cm −2 when fuelled with dry C 3 H 8 at 800 • C and operated stably for 50 h without noticeable carbon deposition.
In contradiction of the renowned deleterious impact of coking on cell performance, the formation of carbonaceous residues within the Cu-CeO 2 -YSZ anode upon exposure to n-C 4 H 10 at 700 • C was found to offer better energy output [147]. During operation with n-C 4 H 10 , polyaromatic compounds (tars) formed from the vapour phase and free radical reactions are deposited on the anode surface. Although the formation rate is insignificant at and below 700 • C, it becomes more apparent beyond this temperature. At 700 • C, the sufficient amounts of tar formed over a short period help to improve performance by allowing supplementary electronic conductivity [147,148,165]. However, with extended operation, the increased amount of tar deposit became more stable and damaging to the anode functionality. In addition, tar deposition will gradually block the active sites compromising the electrochemical performance. Thus, avoiding carbon formation is necessary to ensure long-term stability of the SOFC system fuelled by the heavy hydrocarbons.
Analysis of the carbon removal could be performed using a mass spectrometer by referring to the amount of CO 2 produced (represented by m/e = 44) [147]. As shown in Figure 6, exposure to oxidising gas (20% O 2 in a He carrier) at a range of operating temperatures could eliminate the deposits. The amount of CO 2 increases with the applied temperature. In contrast, it was reported that the removal of these deposits using steam requires much higher temperatures (>900 • C) [147]. These findings show that such an SOFC would have to be regenerated periodically by a redox cycle, particularly when fuelled with hydrocarbons for long-term use. These cells, unfortunately, have yet to be able to generate power densities comparable to those with Ni-based anodes. This is partly because the operating temperature must be kept at 700 • C to curtail carbon deposition. Lower temperatures may affect the reactions kinetic and the conductivity of the electrolyte depending on the material used for making the cell. The use of heavier hydrocarbons is intriguing as they originate from a variety of sources with reasonable prices. Those in liquid form may help to resolve transportation difficulties. However, the chemistry behind the electrochemical reactions of these hydrocarbons during SOFC operation is still not fully understood. Ongoing research on the reaction mechanism, control, impurities issues as well as the requirement for a robust cata- Figure 6. Temperature-programme oxidation (TPO) curves in oxidising gas with porous YSZ-CeO 2 exposed to n-butane at 973 K for different periods. Figure is adapted from [147]. The use of heavier hydrocarbons is intriguing as they originate from a variety of sources with reasonable prices. Those in liquid form may help to resolve transportation difficulties. However, the chemistry behind the electrochemical reactions of these hydrocarbons during SOFC operation is still not fully understood. Ongoing research on the reaction mechanism, control, impurities issues as well as the requirement for a robust catalyst with adequate lifespan is necessary if this technology is to be applied commercially. Table 3 lists the electrochemical performance parameters of heavier hydrocarbon-fuelled SOFCs, showing some cells with decent power densities reported.

Current and Future Trends of Research on Hydrocarbon-Fuelled SOFCs
A fuel cell is an environmentally friendly alternative to the conventional combustion technology for energy generation. Especially with SOFCs, high working temperatures allow such systems to use a wide variety of fuel intake including hydrocarbons. The possibility of utilising hydrocarbons presents a substantial benefit against other low-temperature fuel cell counterparts. For decades, SOFCs technology has been continuously, if not rapidly, progressing. Numerous aspects are constantly being explored and improved [173]. While many improvements have been achieved, the issues of cost, durability, stability and sustainable electrochemical performance remain as major challenges. Until now, Ni-based anodes for hydrocarbon-fuelled SOFCs have garnered the most extensive global research attention. Nevertheless, recent attempt to implement the LiNi 0.8 Co 0.15 Al 0.05 O 2 anode under CH 4 -fuelled conditions have demonstrated instability, manifesting through its decomposition [174]. While endeavours to enhance and modify Ni-based anodes persist, the pursuit of alternatives of Ni-based cermets as anode materials for a hydrocarbon-fuelled system is required to resolve coking issues and ensure long-term stability [175]. Direct utilisation of hydrocarbons has become a key feature that may allow SOFCs to be commercialised as current impediments include the high cost of H 2 production along with its safety and environmental concerns. In addition, with regards to sustainable development, the fuel flexibility of this technology also presents a promising transition from fossil to renewable fuels.

Use of Non-Ni Anode Materials
As a fuel electrode, an anode must not only be able to catalyse the electrochemical oxidation of the hydrocarbon fuel but also have the ability to withstand SOFC operating conditions. In recent years, there has been a proposition to apply nickel-free anodes such as other types of cermet (i.e., Cu-CeO 2 ) [176] or perovskite-based for operation with hydrocarbons [177]. Numerous lab-scale studies with these anodes have described consistent cell performance with possible noncoking operation. For instance, Cu-CeO 2 and perovskites such as La 0.75 Sr 0.25 Cr 0.5 Mn 0.5 O 3−δ (LSCM) [177] have been reported to present stable SOFC operation with wet methane. For the former, researchers from the University of Pennsylvania have developed SOFCs with copper (Cu)-based anodes with ceria (CeO 2 ) as catalyst and tested them with various hydrocarbons, where good cell performance and noncoking condition have been demonstrated [20,40,166,178]. Their cell was developed by forming the porous YSZ matrix using dual-tape-casting technique then followed by the impregnation of Cu and CeO 2 using nitrate-based solutions. Following that was the decomposition and reduction processes to form Cu-CeO 2 -YSZ composites [20]. Copper and ceria have their own functionalities as a current collector and catalyst for the fuel electrochemical reactions, respectively. Copper is a poor catalyst for breaking C-H bonds, and its ability to form C-C bonds is restricted, and these may be the causes of noncoking operation. The OCV acquired, however, remains much lower than that estimated by thermodynamics. This alludes that the conversion of hydrocarbon involves a route other than direct oxidation, viz., through hydrocarbon cracking and subsequently the electrochemical oxidation of cracked products.
During operation at 700 • C with Cu-CeO 2 -YSZ cermet anodes for the oxidation of various types of hydrocarbons such as methane, propane, butane, decane and toluene, cells containing less than 20 wt% Cu in the cermet anode structure demonstrated improved cell performance that further enhanced over time. This was attributed to enhanced electrical connectivity owing to the formation of carbonaceous deposits within the pores of the cermet anode that link the Cu particles together for better percolation [148,165]. This observation is in agreement with other works on enhanced cell performance caused by the carbon deposits during CH 4 oxidation on Cu-based anodes.
Alternatively, the use of oxide materials as anode materials allows the prospect that all cell components to be derived from ceramic materials, making the fabrication and processing of the cell simple and easier. More interesting, they do not form carbon under most conditions and could solve issues of redox stability. These oxide materials can be categorised according to their crystalline structures: fluorite (e.g., zirconia-and ceria-based), rutile, tungsten bronze, pyrochlore, perovskites (e.g., chromite, titanate and vanadate) and double perovskites [179]. Remarkable progress has been reported in recent years, as most perovskite and perovskite-related structures that are often applied as a cathode are now being tested for making anode. With this development, the anode may be made of a single component contrasted with cermets, resolving disputes such as thermal expansion mismatches and solid-state reactions between the cell components. Ge et al. [110] indicated that SOFC's oxide anode materials could be assessed qualitatively using a "performance tetrahedron" whose four vertices are electrical conductivity, electrocatalytic activity, redox stability and fuel flexibility.
Among various oxide types, the most common are those of perovskite and double perovskite structures. Several potential candidates include La 0. 8 [110]. As detailed discussion on these possible anode materials are beyond the scope of this review, interested readers are directed to several excellent reviews for more information [12,18,110,[179][180][181]. Indeed, issues concerning the electrical conductivity of LSCM, LSTMG and SMMO, the thermal stability of SMMO and SMFO and redox stability of LSV and SMMO remain as great challenges, but further improvement of such issues is continuing. Oxide materials have shown encouraging power output and exceptional redox stability at high temperatures, typically beyond 700 • C. Catalytic activity, however, declines promptly with temperature, and these materials cannot at the moment work well in the intermediate temperature range. Despite this encouraging progress, these materials are, at this point, more costly than the regularly applied Ni cermets. In addition, the use of these oxides as anodes yielded relatively lower power density (between 0.2 and 0.44 W cm −2 ) at 800-900 • C compared to the Ni-based anode.
It is noteworthy that there is a trade-off between deficiency in carbon deposition and sufficient electrochemical activity. Anodes that do not catalyse carbon formation incline to be less reactive for the electrochemical oxidation or vice versa. Nevertheless, the use of redox stable metal oxides as anodes appears to be exciting. This field of research may see major advances in the future, but until these materials have been properly developed and their characteristics in harsh SOFC operating atmospheres are well-understood, cermets will remain the material of choice for making anode.

Strategies for Stable SOFC Operation
Apprehension about the system's durability and stability should also be taken into thoughtful consideration. For a success in the marketplace, SOFCs must be economical and present a decent lifespan. Long-term stability is necessary to be competitive means for energy generation against the conventional combustion technology. Essentially, materials applied for an SOFC should be robust and able to function properly for continuous operation in harsh conditions. Latest emergence of perovskite-based material has been intriguing, but before being considered practical, issues surrounding the cost and fabrication process must be resolved to allow large-scale production with economic benefits [9].
It has been commonly accepted that the activity of SOFC anodes is dependent not only on materials of electrode but also on its morphology as well as operating environments [182]. It has been recognised that the reliability, durability and stability of the SOFCs could be markedly improved by decreasing their working temperature. There are concerns with regards to high-temperature operation (≥750 • C) including the strictly limited selection of material, electrode sintering and the interfacial diffusion between cell components. Hence, it is of great interest to operate the system in an intermediate range of temperatures, i.e., 550 to 750 • C [183,184]. Lowering the working temperature could certainly allow more choice of SOFC materials. Studies have demonstrated that the operation at lower temperatures (<800 • C) for cells with Ni-based anodes are likely with thin YSZ electrolytes [185] or using highly conducting electrolytes such as GDC and doped LaGaO 3 [186]. In addition, applying SOFCs at a low-temperature range (≤650 • C) has received lots of attention to directly use hydrocarbons as fuels. For instance, performance degradation caused by carbon formation during the direct use of CH 4 could be avoided through the addition of an internal reforming layer composed of Ni supported on proton-conducting La-doped ceria (i.e., La 2 Ce 2 O 7 (LDC) and La 1.95 Sm 0.05 Ce 2 O 7 (LSDC)) which was applied over Ni-Ce 0.8 Sm 0.2 O 2−x (SDC) anodes. Such a proton-conducting layer can adsorb water for internal reforming and therefore considerably improve the performance of the direct methane SOFCs.
Another emerging proton-conducting material for making an SOFC is BaZr 0.1 Ce 0.7 Y 0.1 Yb 0.1 O 3−δ (BZCYYb). Using a NiO-BZCYYb anode with an additional LaNi 0.6 Co 0.4 O 3 anode functional layer and a thin BZCYYb electrolyte, stable operation for 200 h has been demonstrated when operated under wet CH 4 at 550 • C [61]. Review by Su and Hu summarises the most recent advances in hydrocarbon-fuelled SOFCs operating at 650 • C, with a particular emphasis on the challenges and strategies associated with the cells components [8]. It has been highlighted on the requirement for highly active and carbon/sulphur resistant anodes, as well as highly ionic conductive electrolytes, in order to achieve superior fuel cell performance at lower temperature range.

Cell Geometry and Microstructure Optimisation
The present-day materials for constructing SOFCs remains virtually the same for the past years as only few numbers of suitable materials could be applied due to high operating temperatures. Having been aware of this constraint, an approach to realising high-performance SOFCs is by refining cell geometry, associated with microstructural design and optimisation. An appropriate microstructure design could be beneficial to improve the stability of Ni-based anodes with regard to the carbon formation so as to come up with a reliable fuel cell that offers stable conversion performance. The microstructure of a cell plays an important role, particularly during the transport of gases to and from the TPB region which influences the concentration polarisation. Most common geometries for an SOFC are flat and tubular, wherein similar preparation techniques to those described in the literature are still being used, including screen printing and tape casting. A newer design, microtubular cell has been introduced in the 1990s [187] which presents extra benefits which include smaller and portable size for easy transportation, rapid start-up and shutdown, better thermal shock resistance and improved volumetric power density.
There are basically two ways to produce microtubes: plastic mass ram extrusion and the phase inversion-assisted extrusion method (also known as a spinning process) [188]. Contrary to ram-extrusion-based methods, the latter could form microtubes having distinctive microstructure due to the controllability and flexibility of the process. The microtubes derived from the phase-inversion method typically has a plurality of self-organised microchannels in the cross section of the microtube walls and sponge-like structure. The presence of the former has been described to facilitate gas transport, whereas the latter provides mechanical robustness.
The main advantage of the phase inversion method is better microstructural designing, which could be tailored by adjusting the spinning parameters and the sintering step. More interestingly, such technique also allows the fabrication of multichannel microtube [189][190][191] and multilayer microtubes, up to three layers in a single step [135,182,192,193]. The unique structure of the microtubular SOFCs developed from such technique have demonstrated excellent electrochemical performance [192,194]. Ni-based anode-supported microtubes derived from the phase-inversion process has a common asymmetric structure, whereby such microtubular cells developed using this method have presented outstanding electrochemical performance for operation with H 2 [135,[195][196][197].
A proof-of-concept study by Lee et al. showed that various ceramic microtube designs could be derived using a phase inversion method [198]. This includes microtubes having microchannels with open entrances that could act as a substrate for catalyst deposition, which could later be developed as SOFCs with enhanced properties. If such tubes are derived using electrolyte materials, they can act as an appropriate scaffold for anode material addition, which require less amount to be added compared to the conventional anode-suspension mixture. For instance, YSZ microtube with open entrances which suitable functioned as a scaffold for Cu-CeO 2 impregnation has been successfully developed and presented good performance under direct methane-fuel cell mode [176]. More interestingly, the success in producing microtubes with multichannel design or so-called micromonolithic could help to address issues regarding the mechanical stability of the microtubes which appears to be a major impediment from commercialisation. Recent development of multichannel microtubular SOFCs, otherwise known as micromonolithic cells has shown excellent fuel cell performance under H 2 -fuelled system [190,191,199,200] and low-calorific CH 4 -fuelled operation, respectively [64]. Nevertheless, more work can be conducted to further improve not only the microstructure of the microtubular cell but also to bundle the microtubes together to obtain larger power output.

Key Factors Influencing the Efficiency of Hydrocarbon-Fuelled SOFCs
Despite the promising prospects of applying hydrocarbons as fuel for SOFCs, it remains crucial to identify the various factors that impact the efficiency of the system. This recognition is vital for advancing the technology, optimising its performance and ensuring its successful integration into the energy landscape. Among the key factors that affect cell efficiency is the fuel composition and quality. While numerous studies to date are conducted at a laboratory scale using pure hydrocarbons, the actual composition and quality of hydrocarbon fuels (i.e., natural gas or biogas) to be applied in SOFCs will exert a considerable impact on cell efficiency. Impurities present in the fuel, such as sulphur and heavy metals, can poison the catalysts used in the fuel cell's anodes. This poisoning effect can degrade the performance of the anodes, leading to poor electrochemical reactions and reduced overall efficiency. In addition, impurities can also lead to carbon deposition, where unconverted hydrocarbons form solid carbon deposits on the anodes. These deposits can block active anode sites, increase overpotentials (i.e., energy losses) and reduce the cell's efficiency. Variations in the hydrocarbon mixture alter the kinetics of the reforming reactions, which are responsible for converting hydrocarbons into H 2 -rich gases. These as well will negatively impact the fuel conversion, thereby reducing the overall effectiveness of the cell.
In addition, the efficiency of hydrocarbon conversion within SOFCs relies on the kinetics of reforming reactions, which transform hydrocarbons into H 2 -rich gases. The choice of catalysts and their properties (i.e., activity and stability) significantly influence the extent of hydrocarbon conversion. Catalysts have a critical role in accelerating these reactions and facilitating the production of H 2 , a vital reactant in the electrochemical reactions taking place within the cell. Efficient reforming reactions are crucial as they ensure a continuous supply of H 2 for the electrochemical processes, thus enhancing the overall efficiency of the fuel cell. Catalyst degradation over time can lead to reduced reforming effectiveness and, subsequently, a decline in the cell's performance.
Operating temperature is another factor affecting SOFCs efficiency. Higher temperatures can improve the kinetics of both electrochemical reactions and fuel reforming. Elevated temperatures increase the speed upon which reactions occur, hence promoting more efficient energy conversion. Better reforming kinetics led to improved H 2 production, while faster electrochemical reactions result in higher power output. However, maintaining high temperatures poses challenges such as thermal management and material compatibility. Excessive heat can lead to material degradation, impacting the longevity and stability of the cell. Therefore, balancing the benefits of improved kinetics with the challenges of high-temperature operation is decisive for achieving optimum efficiency.
Overall, understanding and optimising the critical factors influencing hydrocarbonfuelled SOFCs is pivotal. This knowledge allows researchers and engineers to continuously improve the cell and system design, addressing challenges in fuel composition, operating temperature and materials selection for better efficiency and performance. Effective management of fuel impurities, proper material selection and precise temperature control contribute to SOFC durability, while enhanced efficiency leads to reduced fuel consumption, lower emissions and potential economic benefits. An SOFC is thus holds promise for a cleaner energy future and increased competitiveness in energy systems.

Conclusions
A major societal goal is clean and efficient energy generation technology using renewable sources, combined with the minimisation of the emission of both atmospheric pollutants and greenhouse gases. SOFC technology emerges as a promising way to produce clean energy to replace conventional combustion techniques in high efficiency. This relatively new technology is typically operated with hydrogen (H 2 ). However, a major drawback of the H 2 -fuelled system is that H 2 is expensive, with most of it being produced from natural gas steam reforming processes. In addition, energy requirements are not satisfactorily effective to generate H 2 in a cost-efficient way. Therefore, with SOFCs, the direct use of hydrocarbons as fuel without first externally reforming them to H 2 will significantly decrease the complexity and cost of a fuel cell system. There are various approaches to direct hydrocarbon utilisation described in this review highlighting the internal reforming process and the direct feeding of pure fuel to the system. This allows the exclusion of an external reformer and circumvents the requirement for the complicated water and heat exchange system necessary to reform hydrocarbons before entering the anode compartment.
The literature shows that the direct use of hydrocarbon fuel for SOFCs is promising if certain precautions and strategies are to be applied. In comparison, CH 4 -fuelled SOFCs are well-studied as it poses lesser challenges compared to heavier hydrocarbons. Regardless of the fuel types, the target of most studies largely focused on the effects of catalyst compositions, modifications and reaction conditions toward achieving high conversion and selectivity. Finding the appropriate anode materials with excellent performance and sufficient robustness is difficult due to challenging operating conditions. Thus, continuous efforts have been made to reduce working temperatures to allow more materials to be considered with better electrochemical performance.
The SOFC technology has been developed with research aiming at utilising fuel directly both with and without internal reforming and preferably at lower operating temperatures. This includes the development of alternative anode materials (i.e., non-Ni-based anodes) that can tolerate, if not completely eliminate, carbon formation while remaining stable upon exposure to other contaminants (such as H 2 S). Use of perovskites as the cell materials could lead to the reduced operating temperature, but challenges persist with hydrocarbon as fuels due to high anode polarisation resistance. Lowering the anodic activation overpotentials along with optimising and maintaining the microstructure remains as critical aspects to be addressed for success in this field. While more investigation is needed, the future looks promising for the commercialisation of direct hydrocarbon SOFCs.