Continuous Catalytic Deoxygenation of Waste Free Fatty Acid-Based Feeds to Fuel-Like Hydrocarbons Over a Supported Ni-Cu Catalyst

While commercial hydrodeoxygenation (HDO) processes convert fats, oils, and grease (FOG) to fuel-like hydrocarbons, alternative processes based on decarboxylation/decarbonylation (deCOx) continue to attract interest. In this contribution, the activity of 20% Ni-5% Cu/Al2O3 in the deCOx of waste free fatty acid (FFA)-based feeds—including brown grease (BG) and an FFA feed obtained by steam stripping a biodiesel feedstock—was investigated, along with the structure-activity relationships responsible for Ni promotion by Cu and the structural evolution of catalysts during use and regeneration. In eight-hour experiments, near quantitative conversion of the aforementioned feeds to diesel-like hydrocarbons was achieved. Moreover, yields of diesel-like hydrocarbons in excess of 80% were obtained at all reaction times during a BG upgrading experiment lasting 100 h, after which the catalyst was successfully regenerated in situ and found to display improved performance during a second 100 h cycle. Insights into this improved performance were obtained through characterization of the fresh and spent catalyst, which indicated that metal particle sintering, alloying of Ni with Cu, and particle enrichment with Cu occur during reaction and/or catalyst regeneration.


Introduction
Due to the interest in renewable fuels resulting from environmental and sustainability concerns and the high fuel demand of the transportation sector, biofuel production requires multiple feed sources. Currently, edible feeds are used in considerable amounts to achieve lower greenhouse gas emissions relative to liquid fossil fuels [1,2]. However, these feeds are needed to meet the food demand of a growing population, food prices rising when edible crops are used for fuel production [3]. Inedible oleaginous plants that thrive in arid soil avoid disrupting the food supply [1,4], but their current scale of cultivation is insufficient. Microalgae produce more oil than terrestrial crops, but energy and cost challenges associated with their cultivation remain to be overcome [5,6]. Thus, additional inedible feeds are required to meet fuel demand, fats, oils, and grease (FOG) waste streams showing great promise due to their low cost and widespread availability.
Noteworthy oleaginous waste streams include yellow grease (waste cooking oil) and brown grease (FOG collected from grease traps, i.e., devices engineered to separate insoluble oils from commercial kitchen wastewater streams [7]). Although a significant fraction of yellow grease (YG) is currently At 275 °C the yield of diesel-like hydrocarbons (C10-C20) decreased from 88.8% at 1 h to 71.3% at 8 h on stream, while the selectivity to heavier products (C21-C35) progressively increased over the same time period. The heavy products, listed in Table A2, are mainly long chain esters that are formed when alcohol intermediates undergo esterification with fatty acids on the catalyst surface [21]. These side reaction products are less prominent at high reaction temperatures, as evinced by the lack of any oxygenates (heavy or otherwise) at 375 °C, albeit the small amount of heavier (C21-C35) hydrocarbons formed at this temperature likely stems from the direct decarboxylation of long chain ester intermediates [21]. Alternatively, these esters can undergo hydrogenolysis to form alcohols and aldehydes, while the former can also be dehydrogenated to the latter as these two products have been shown to exist in equilibrium under hydrogen-rich conditions [21]. In turn, aldehydes can undergo decarbonylation to form diesel-like hydrocarbons. At 325 °C the yield of diesel-like hydrocarbons is ≥95% irrespective of time on stream. Notably, near complete deoxygenation occurs at this temperature, with the highest amount of oxygenates (accumulated during the last hour of the experiment) totaling only 0.2% of the liquid products. Heavy products are still formed, but in significantly lower quantities than at 275 °C. Complete deoxygenation occurs at all reaction times sampled when the reaction temperature is increased to 375 °C, the selectivity to diesel-like hydrocarbons being ≥98% irrespective of time on stream. The increase in selectivity to diesel-like hydrocarbons as the reaction temperature increases is most likely due to: 1) the cracking of the long chain hydrocarbons (≥C20) observed at lower reaction temperatures; and 2) direct deoxygenation of the fatty acids without formation of long chain ester intermediates.

Catalytic Deoxygenation of Brown Grease at Different Temperatures
The GC-MS analysis of the lipids extracted from the BG feed is also displayed in Appendix A within Table A1. The composition is similar to the industrial FFA waste stream above, the extracted lipids being mainly fatty acids (97.3%) the most abundant of which are oleic, palmitic, and stearic acids (ca. 64. 5, 20.4, and 8.7%, respectively). In addition, the BG contains 2.66% glycerides (mostly At 275 • C the yield of diesel-like hydrocarbons (C10-C20) decreased from 88.8% at 1 h to 71.3% at 8 h on stream, while the selectivity to heavier products (C21-C35) progressively increased over the same time period. The heavy products, listed in Table A2, are mainly long chain esters that are formed when alcohol intermediates undergo esterification with fatty acids on the catalyst surface [21]. These side reaction products are less prominent at high reaction temperatures, as evinced by the lack of any oxygenates (heavy or otherwise) at 375 • C, albeit the small amount of heavier (C21-C35) hydrocarbons formed at this temperature likely stems from the direct decarboxylation of long chain ester intermediates [21]. Alternatively, these esters can undergo hydrogenolysis to form alcohols and aldehydes, while the former can also be dehydrogenated to the latter as these two products have been shown to exist in equilibrium under hydrogen-rich conditions [21]. In turn, aldehydes can undergo decarbonylation to form diesel-like hydrocarbons. At 325 • C the yield of diesel-like hydrocarbons is ≥95% irrespective of time on stream. Notably, near complete deoxygenation occurs at this temperature, with the highest amount of oxygenates (accumulated during the last hour of the experiment) totaling only 0.2% of the liquid products. Heavy products are still formed, but in significantly lower quantities than at 275 • C. Complete deoxygenation occurs at all reaction times sampled when the reaction temperature is increased to 375 • C, the selectivity to diesel-like hydrocarbons being ≥98% irrespective of time on stream. The increase in selectivity to diesel-like hydrocarbons as the reaction temperature increases is most likely due to: 1) the cracking of the long chain hydrocarbons (≥C20) observed at lower reaction temperatures; and 2) direct deoxygenation of the fatty acids without formation of long chain ester intermediates.

Catalytic Deoxygenation of Brown Grease at Different Temperatures
The GC-MS analysis of the lipids extracted from the BG feed is also displayed in Appendix A within Table A1. The composition is similar to the industrial FFA waste stream above, the extracted lipids being mainly fatty acids (97.3%) the most abundant of which are oleic, palmitic, and stearic acids (ca. 64. 5, 20.4, and 8.7%, respectively). In addition, the BG contains 2.66% glycerides (mostly diolein), signifying that the feed predominately consists of unsaturated lipids. Notably, this composition is comparable to other BG samples described in the literature [14,22,23], which confirms that the simple extraction method employed (see Section 3.3) was effective in affording lipids representative of those contained in BG. The lipid concentration for these experiments was increased from that used in the FFA upgrading runs discussed in Section 2.1 above to 50 wt% lipids in dodecane, while the WHSV was kept at 1 h −1 . This allowed an evaluation of the effect of feed concentration on the deoxygenation of free fatty acid-based feeds. In turn, the most promising reaction temperatures identified through the FFA upgrading runs-namely, 325 and 375 • C-were investigated to assess the effect of temperature on the deoxygenation of BG lipids. The simulated distillation GC-MS analyses of the liquid products obtained during each hour are summarized in Figure 2 and in Appendix A (Tables A5 and A6), while the incondensable gaseous products are provided as Supplementary Material ( Figure S1). diolein), signifying that the feed predominately consists of unsaturated lipids. Notably, this composition is comparable to other BG samples described in the literature [14,22,23], which confirms that the simple extraction method employed (see Section 4.3) was effective in affording lipids representative of those contained in BG. The lipid concentration for these experiments was increased from that used in the FFA upgrading runs discussed in Section 2.1 above to 50 wt% lipids in dodecane, while the WHSV was kept at 1 h -1 . This allowed an evaluation of the effect of feed concentration on the deoxygenation of free fatty acid-based feeds. In turn, the most promising reaction temperatures identified through the FFA upgrading runs-namely, 325 and 375 °C-were investigated to assess the effect of temperature on the deoxygenation of BG lipids. The simulated distillation GC-MS analyses of the liquid products obtained during each hour are summarized in Figure 2 and in Appendix A (Tables A5 and A6), while the incondensable gaseous products are provided as Supplementary Material ( Figure S1). Quantitative conversion of the BG lipids was achieved regardless of the reaction temperature employed. However, the deoxygenation of the BG lipids at 325 °C yields more than double the amount of heavy products that was obtained in the free fatty acid experiments at the same temperature, reaching 11% of the total liquid products at 8 h on stream. Other authors have seen an increase in heavy products as the feed concentration increases and suggested that this stems from an increase in the amount of fatty acids present on the catalyst surface [14]. The rise in fatty acid concentration increases the possibility of esterification reactions with the alcohol intermediates, forming long chain esters that can undergo direct decarboxylation to yield heavy hydrocarbons. However, the esters observed in the FFA upgrading experiments were not detected in the BG upgrading experiments, suggesting that rapid decarboxylation occurs upon formation of the ester intermediates. Remarkably, >94% of the liquid products obtained during the deoxygenation of the BG lipids at 375 °C are diesel-like hydrocarbons at all reaction times sampled. Parenthetically, at 375 °C there were a number of liquid products-from 9.74% at t = 1 h to 7.62% at t = 8 h (see Appendix A Table A6)-deemed to be hydrocarbons by the GC-MS, although their specific identity could not be determined. Nevertheless, according to the simulated distillation GC of these unidentifiable products, they all boil within the diesel range (180-350 °C). The heavy product formation also decreased at the higher reaction temperature, the total amount obtained being <6% of the liquid products irrespective of time on stream. This is consistent with higher temperatures favoring the occurrence of cracking reactions, which is also indicated by the higher amount of gaseous C1-C4 products obtained at 375 °C (see Supplementary Material). Nevertheless, only a relatively small amount of the carbon in the feed becomes C1-C4 gaseous products. Indeed, at 325°C only 3.5 mol% Quantitative conversion of the BG lipids was achieved regardless of the reaction temperature employed. However, the deoxygenation of the BG lipids at 325 • C yields more than double the amount of heavy products that was obtained in the free fatty acid experiments at the same temperature, reaching 11% of the total liquid products at 8 h on stream. Other authors have seen an increase in heavy products as the feed concentration increases and suggested that this stems from an increase in the amount of fatty acids present on the catalyst surface [14]. The rise in fatty acid concentration increases the possibility of esterification reactions with the alcohol intermediates, forming long chain esters that can undergo direct decarboxylation to yield heavy hydrocarbons. However, the esters observed in the FFA upgrading experiments were not detected in the BG upgrading experiments, suggesting that rapid decarboxylation occurs upon formation of the ester intermediates. Remarkably, >94% of the liquid products obtained during the deoxygenation of the BG lipids at 375 • C are diesel-like hydrocarbons at all reaction times sampled. Parenthetically, at 375 • C there were a number of liquid products-from 9.74% at t = 1 h to 7.62% at t = 8 h (see Appendix A Table A6)-deemed to be hydrocarbons by the GC-MS, although their specific identity could not be determined. Nevertheless, according to the simulated distillation GC of these unidentifiable products, they all boil within the diesel range (180-350 • C). The heavy product formation also decreased at the higher reaction temperature, the total amount obtained being <6% of the liquid products irrespective of time on stream. This is consistent with higher temperatures favoring the occurrence of cracking reactions, which is also indicated by the higher amount of gaseous C1-C4 products obtained at 375 • C (see Supplementary Material). Nevertheless, only a relatively small amount of the carbon in the feed becomes C1-C4 gaseous products. Indeed, at 325 • C only 3.5 mol% of the carbon in the BG feed is converted to these gaseous products, this value reaching 6.1 mol% when the reaction temperature is increased to 375 • C.

Catalytic Deoxygenation of Brown Grease at Different H 2 Partial Pressures
The presence of H 2 in the reaction atmosphere has been shown to improve catalyst performance during the deCO x of lipids even if H 2 is not directly involved in the deoxygenation reaction [24][25][26]. Interestingly, some authors have also shown that supported Pd catalysts perform better under lower H 2 partial pressure conditions than under pure H 2 atmospheres [27], and the same effect has been reported for some Ni catalysts [26]. Therefore, it is instructive to investigate the effect of H 2 partial pressure on the deoxygenation of waste fatty acid-based feeds. To this end, the deoxygenation of BG was conducted under a reaction atmosphere of 20% H 2 /Ar at 375 • C, the GC-MS analysis of the liquid products being shown in Figure 3 and in Appendix A (Table A7), while the incondensable gaseous products are also shown in Figure 3. Note that the part of the y-axis not shown in Figures 3 and 5 consists entirely of the reaction atmosphere, i.e., either H 2 or a mixture of H 2 and Ar. of the carbon in the BG feed is converted to these gaseous products, this value reaching 6.1 mol% when the reaction temperature is increased to 375 °C.

Catalytic Deoxygenation of Brown Grease at Different H2 Partial Pressures
The presence of H2 in the reaction atmosphere has been shown to improve catalyst performance during the deCOx of lipids even if H2 is not directly involved in the deoxygenation reaction [24][25][26]. Interestingly, some authors have also shown that supported Pd catalysts perform better under lower H2 partial pressure conditions than under pure H2 atmospheres [27], and the same effect has been reported for some Ni catalysts [26]. Therefore, it is instructive to investigate the effect of H2 partial pressure on the deoxygenation of waste fatty acid-based feeds. To this end, the deoxygenation of BG was conducted under a reaction atmosphere of 20% H2/Ar at 375 °C, the GC-MS analysis of the liquid products being shown in Figure 3 and in Appendix A (Table A7), while the incondensable gaseous products are also shown in Figure 3. Note that the part of the y-axis not shown in Figures 3 and 5 consists entirely of the reaction atmosphere, i.e., either H2 or a mixture of H2 and Ar. Under 20% H2, the 20% Ni-5% Cu/Al2O3 catalyst quantitatively converts the BG feed, no trace of starting material being observed at any reaction time sampled (see Figure 3c). However, the amount of diesel-like hydrocarbons in the reaction products decreases to 86-89% of the total liquid products relative to the 94-98% values observed when the reaction is performed under pure H2 (see Figure 3a). Additionally, the amount of heavy products increases when the reaction is performed under reduced H2 partial pressure, albeit it is worth noting that only a relatively small amount (an average of 14.8%) of the total heavy products collected are long chain esters. The increase in the amount of long chain hydrocarbons suggests that after the formation of esters, the lower H2 partial pressure favors their direct decarboxylation, as opposed to their hydrogenolysis to afford alcohols and aldehydes [21]. Interestingly, while there is only a small decrease in the yield of diesel-like products, the gaseous products show a noticeable decrease in methane formation when the reaction is performed under reduced H2 partial pressure (see Figures 3b,d). Indeed, while the amount of CO or CO2 present in the gaseous products obtained using pure H2 is negligible and methane represents the vast majority of the gaseous products, the gas products contain considerably more CO2 and less methane when the Under 20% H 2 , the 20% Ni-5% Cu/Al 2 O 3 catalyst quantitatively converts the BG feed, no trace of starting material being observed at any reaction time sampled (see Figure 3c). However, the amount of diesel-like hydrocarbons in the reaction products decreases to 86-89% of the total liquid products relative to the 94-98% values observed when the reaction is performed under pure H 2 (see Figure 3a). Additionally, the amount of heavy products increases when the reaction is performed under reduced H 2 partial pressure, albeit it is worth noting that only a relatively small amount (an average of 14.8%) of the total heavy products collected are long chain esters. The increase in the amount of long chain hydrocarbons suggests that after the formation of esters, the lower H 2 partial pressure favors their direct decarboxylation, as opposed to their hydrogenolysis to afford alcohols and aldehydes [21]. Interestingly, while there is only a small decrease in the yield of diesel-like products, the gaseous products show a noticeable decrease in methane formation when the reaction is performed under reduced H 2 partial pressure (see Figure 3b,d). Indeed, while the amount of CO or CO 2 present in the gaseous products obtained using pure H 2 is negligible and methane represents the vast majority of the gaseous products, the gas products contain considerably more CO 2 and less methane when the reaction is run under 20% H 2 . Therefore, under reduced H 2 partial pressures, methanation of CO x is disfavored and does not proceed to completion. Instead, the methane formed at lower H 2 partial pressures is likely formed from the fatty acids alkyl chains via the end-chain cracking mechanism described in a recent contribution [13]. As with other experiments, only a relatively small amount of the carbon in the BG feed becomes C1-C4 gaseous products, this value being 5.8 mol% for the experiment performed under reduced H 2 partial pressure.

Catalyst Deactivation and Online Regeneration
Tellingly, the composition of the gas products is still changing not only at the end of the reactions discussed in Section 2.3, but also at the end of previously reported YG and hemp seed oil upgrading experiments [13], all of which lasted eight hours. Therefore, it appears that eight hours do not constitute sufficient time for the attainment of steady state. Obviously, this also hinders an assessment of whether significant catalyst deactivation occurs when upgrading a realistic feed under these conditions. Therefore, the most promising conditions evaluated in this study, i.e., 375 • C and a pure H 2 atmosphere, were employed in a run in which the deoxygenation reaction time was extended to 100 h on stream. After this (first) 100 h cycle, the catalyst was regenerated in situ by washing, drying, calcining (in air), and re-reducing the catalyst (under flowing H 2 ). Catalyst calcination was performed for 5 h at 450 • C, which is both the top temperature rating of the furnace employed and a temperature at which the majority of the carbonaceous deposits can be eliminated according to the results of thermogravimetric analysis (see Section 2.5 and Figure 7). Results from the analysis of representative liquid samples (recovered at 24 h intervals) are shown in Figure 4 and in Appendix A (Tables A8 and A9), the analysis of the gaseous products being shown in Figure 5. It should be noted that the results shown correspond to products recovered in a single hour and not to products accumulated over a 24 h period, such that the catalyst performance can be assessed at the specified time intervals with a "time resolution" equal to one hour. reaction is run under 20% H2. Therefore, under reduced H2 partial pressures, methanation of COx is disfavored and does not proceed to completion. Instead, the methane formed at lower H2 partial pressures is likely formed from the fatty acids alkyl chains via the end-chain cracking mechanism described in a recent contribution [13]. As with other experiments, only a relatively small amount of the carbon in the BG feed becomes C1-C4 gaseous products, this value being 5.8 mol% for the experiment performed under reduced H2 partial pressure.

Catalyst Deactivation and Online Regeneration
Tellingly, the composition of the gas products is still changing not only at the end of the reactions discussed in Section 2.3, but also at the end of previously reported YG and hemp seed oil upgrading experiments [13], all of which lasted eight hours. Therefore, it appears that eight hours do not constitute sufficient time for the attainment of steady state. Obviously, this also hinders an assessment of whether significant catalyst deactivation occurs when upgrading a realistic feed under these conditions. Therefore, the most promising conditions evaluated in this study, i.e., 375 °C and a pure H2 atmosphere, were employed in a run in which the deoxygenation reaction time was extended to 100 h on stream. After this (first) 100 h cycle, the catalyst was regenerated in situ by washing, drying, calcining (in air), and re-reducing the catalyst (under flowing H2). Catalyst calcination was performed for 5 h at 450 °C, which is both the top temperature rating of the furnace employed and a temperature at which the majority of the carbonaceous deposits can be eliminated according to the results of thermogravimetric analysis (see Section 2.5 and Figure 7). Results from the analysis of representative liquid samples (recovered at 24 h intervals) are shown in Figure 4 and in Appendix A (Tables A8 and A9), the analysis of the gaseous products being shown in Figure 5. It should be noted that the results shown correspond to products recovered in a single hour and not to products accumulated over a 24 h period, such that the catalyst performance can be assessed at the specified time intervals with a "time resolution" equal to one hour. During the first 100 h run, quantitative conversion of the BG lipids is achieved during the initial 48 h. After that, the amount of fatty acids in the products begins to increase, reaching a total of 8.1% of the total liquid products collected at the end of the first 100 h cycle. The yield of diesel-like hydrocarbons is >92% of the liquid products for the first 48 h on stream, this value decreasing to During the first 100 h run, quantitative conversion of the BG lipids is achieved during the initial 48 h. After that, the amount of fatty acids in the products begins to increase, reaching a total of 8.1% of the total liquid products collected at the end of the first 100 h cycle. The yield of diesel-like hydrocarbons is >92% of the liquid products for the first 48 h on stream, this value decreasing to 82.8% after 96 h on stream. Notably, catalyst performance improves after the catalyst is regenerated in situ, the yield of diesel-like hydrocarbons being~90% or greater for 72 h on stream during the second 100 h cycle. Interestingly, improvements in performance following catalyst regeneration have been reported for other Ni-based formulations, which was attributed to an increase in the number of strong basic sites during the treatment of the spent catalyst in hot air [26]. A closer look at the individual components of the liquid products (listed in Tables A8 and A9) provides valuable information vis-à-vis changes in selectivity that take place as the reaction progresses and/or after catalyst regeneration. Indeed, while the vast majority of the feed (93.6%) comprised C18 and C16 fatty acids-73.2 and 20.4% of the feedstock, respectively-the most abundant products are C17 and C15 hydrocarbons, suggesting that the reaction proceeds mainly via deCO x as opposed to HDO. Nevertheless, C18 and C16 hydrocarbons are also produced in significant amounts, which indicates that HDO also occurs to some extent. Additionally, of note is the trend followed by lighter diesel-like hydrocarbons (C10-C14), whose abundance in the product mixtures tends to decrease with time on stream and after regeneration (see Tables A8 and A9). This indicates that cracking reactions progressively become less prevalent and implies that surface sites responsible for cracking deactivate gradually and irreversibly. This is in line with the evolution of the incondensable gas products with time on stream, which also provides valuable insights regarding the changes in selectivity observed as the reaction advances and after catalyst regeneration (see Figure 5). 82.8% after 96 h on stream. Notably, catalyst performance improves after the catalyst is regenerated in situ, the yield of diesel-like hydrocarbons being ~90% or greater for 72 h on stream during the second 100 h cycle. Interestingly, improvements in performance following catalyst regeneration have been reported for other Ni-based formulations, which was attributed to an increase in the number of strong basic sites during the treatment of the spent catalyst in hot air [26]. A closer look at the individual components of the liquid products (listed in Tables A8 and A9) provides valuable information vis-à-vis changes in selectivity that take place as the reaction progresses and/or after catalyst regeneration. Indeed, while the vast majority of the feed (93.6%) comprised C18 and C16 fatty acids-73.2 and 20.4% of the feedstock, respectively-the most abundant products are C17 and C15 hydrocarbons, suggesting that the reaction proceeds mainly via deCOx as opposed to HDO. Nevertheless, C18 and C16 hydrocarbons are also produced in significant amounts, which indicates that HDO also occurs to some extent. Additionally, of note is the trend followed by lighter diesel-like hydrocarbons (C10-C14), whose abundance in the product mixtures tends to decrease with time on stream and after regeneration (see Tables A8 and A9). This indicates that cracking reactions progressively become less prevalent and implies that surface sites responsible for cracking deactivate gradually and irreversibly. This is in line with the evolution of the incondensable gas products with time on stream, which also provides valuable insights regarding the changes in selectivity observed as the reaction advances and after catalyst regeneration (see Figure 5). First, the difference in the amount of light (C1-C4 alkanes) observed before and after regeneration confirms the irreversible deactivation of cracking sites. Indeed, these gases result from the shortening of alkyl chains via terminal carbon loss (-C1) and internal chain cracking (-C2, -C3, and -C4), both of which also lead to the formation of C10-C14 fuel-like hydrocarbons [13]. However, the fact that both light (C10-C14) fuel-like hydrocarbons and methane tend to decrease with time on stream prior to remaining fairly constant-while C2-C4 hydrocarbons follow the opposite trendsuggests that chain shortening occurs mainly through the removal of terminal carbons, which is in line with the conclusions of a recent contribution [13]. Moreover, changes in the amounts of COx and methane-which progressively increase and decrease, respectively ( Figure 5, left)-may also suggest that sites responsible for methanation are gradually and irreversibly poisoned as the reaction First, the difference in the amount of light (C1-C4 alkanes) observed before and after regeneration confirms the irreversible deactivation of cracking sites. Indeed, these gases result from the shortening of alkyl chains via terminal carbon loss (-C1) and internal chain cracking (-C2, -C3, and -C4), both of which also lead to the formation of C10-C14 fuel-like hydrocarbons [13]. However, the fact that both light (C10-C14) fuel-like hydrocarbons and methane tend to decrease with time on stream prior to remaining fairly constant-while C2-C4 hydrocarbons follow the opposite trend-suggests that chain shortening occurs mainly through the removal of terminal carbons, which is in line with the conclusions of a recent contribution [13]. Moreover, changes in the amounts of CO x and methane-which progressively increase and decrease, respectively ( Figure 5, left)-may also suggest that sites responsible for methanation are gradually and irreversibly poisoned as the reaction progresses. This represents a noteworthy result, since hydrogen consumption should correspondingly decrease with time on stream without sacrificing significant deoxygenation activity. Lastly, it is worth noting the induction period (observed at the beginning of both cycles in Figure 5 but also in Figure 3d) in which the concentration of CO x gradually increases with time on stream prior to becoming relatively constant at steady state. Given that methane formation is negligible during the second 100 h cycle (right of Figure 5), the low concentration of CO x during this induction period cannot be assigned to CO x methanation. Instead, this can be attributed to the accumulation of CO x on the catalyst surface, which has to become saturated before CO 2 and CO can break through. Indeed, a previous contribution has shown that CO 2 accumulates on the surface of 20% Ni-5% Cu/Al 2 O 3 as alumina-bound carbonates [13]. Based on the results in Figure 5-and ignoring the effects of potentially confounding reactions (including methanation, water gas shift and the Boudouard reaction)-it seems that deoxygenation proceeds fairly equally via decarboxylation (-CO 2 ) and decarbonylation (-CO) once the system reaches steady state. Although-as with other experiments-only a relatively small amount of the carbon in the feed becomes C1-C4 gaseous products, the values obtained for this experiment are particularly informative, since this is the only experiment in which steady state was attained before and after catalyst regeneration. Tellingly, in the first 100 h cycle, the fraction of carbon in the feed converted to C1-C4 gaseous products starts at~2 mol% before reaching a maximum of~7 mol% at 11 h on stream, an increase that can be ascribed to the initial accumulation of CO 2 on the catalyst surface mentioned above. Subsequently, this value stabilizes between~2.5 and~4.9 mol% for the remainder of the first 100 h cycle. During the second 100 h cycle (after catalyst regeneration), the fraction of carbon in the feed converted to C1-C4 gaseous products starts at~0.4 mol% before stabilizing (at around 24 h on stream and for the remainder of the experiment) between~2.6 and~3.6 mol%. This is consistent with both the initial accumulation of CO 2 on the regenerated catalyst surface and the lower cracking activity observed after catalyst regeneration.

Catalyst Characterization
Although the characterization of the 20% Ni-5% Cu/Al 2 O 3 catalyst used in this contribution has been described previously [18], additional characterization work was performed in this study, including an investigation of room temperature CO adsorption on the fresh and spent catalyst via diffuse reflectance infrared Fourier transform spectroscopy (DRIFTS), the resulting spectra being shown in Figure 6. progresses. This represents a noteworthy result, since hydrogen consumption should correspondingly decrease with time on stream without sacrificing significant deoxygenation activity. Lastly, it is worth noting the induction period (observed at the beginning of both cycles in Figure 5 but also in Figure 3d) in which the concentration of COx gradually increases with time on stream prior to becoming relatively constant at steady state. Given that methane formation is negligible during the second 100 h cycle (right of Figure 5), the low concentration of COx during this induction period cannot be assigned to COx methanation. Instead, this can be attributed to the accumulation of COx on the catalyst surface, which has to become saturated before CO2 and CO can break through. Indeed, a previous contribution has shown that CO2 accumulates on the surface of 20% Ni-5% Cu/Al2O3 as alumina-bound carbonates [13]. Based on the results in Figure 5-and ignoring the effects of potentially confounding reactions (including methanation, water gas shift and the Boudouard reaction)-it seems that deoxygenation proceeds fairly equally via decarboxylation (-CO2) and decarbonylation (-CO) once the system reaches steady state. Although-as with other experimentsonly a relatively small amount of the carbon in the feed becomes C1-C4 gaseous products, the values obtained for this experiment are particularly informative, since this is the only experiment in which steady state was attained before and after catalyst regeneration. Tellingly, in the first 100 h cycle, the fraction of carbon in the feed converted to C1-C4 gaseous products starts at ~2 mol% before reaching a maximum of ~7 mol% at 11 h on stream, an increase that can be ascribed to the initial accumulation of CO2 on the catalyst surface mentioned above. Subsequently, this value stabilizes between ~2.5 and ~4.9 mol% for the remainder of the first 100 h cycle. During the second 100 h cycle (after catalyst regeneration), the fraction of carbon in the feed converted to C1-C4 gaseous products starts at ~0.4 mol% before stabilizing (at around 24 h on stream and for the remainder of the experiment) between ~2.6 and ~3.6 mol%. This is consistent with both the initial accumulation of CO2 on the regenerated catalyst surface and the lower cracking activity observed after catalyst regeneration.

Catalyst Characterization
Although the characterization of the 20% Ni-5% Cu/Al2O3 catalyst used in this contribution has been described previously [18], additional characterization work was performed in this study, including an investigation of room temperature CO adsorption on the fresh and spent catalyst via diffuse reflectance infrared Fourier transform spectroscopy (DRIFTS), the resulting spectra being shown in Figure 6. CO adsorption on the reduced fresh catalyst produced a strong absorbance peak at 2100 cm -1 . Since CO adsorption on the spent catalyst did not afford this peak, the spent catalyst was reduced in situ (i.e., inside the DRIFTS cell) to counter any oxidation that may have occurred when the catalyst Figure 6. DRIFTS spectra of the fresh catalyst after reduction, the spent catalyst, and the spent catalyst after reduction. CO adsorption on the reduced fresh catalyst produced a strong absorbance peak at 2100 cm −1 . Since CO adsorption on the spent catalyst did not afford this peak, the spent catalyst was reduced in situ (i.e., inside the DRIFTS cell) to counter any oxidation that may have occurred when the catalyst was exposed to air while being transferred from the reactor to the DRIFTS cell. The reduced spent catalyst also lacked the CO adsorption peak, which indicates that the surface active sites that readily adsorb CO on the reduced fresh catalysts are irreversibly poisoned-or otherwise eliminated-under the reaction conditions employed. This could explain the reduced methane formation observed during the second 100 h cycle, as less CO adsorbs on the catalyst surface. In fact, the C1 gaseous products observed during the second 100 h cycle are almost entirely CO and CO 2 , which is consistent with decreased methanation. Given than in previous work on 20% Ni-5% Cu/Al 2 O 3 and 4.7% Cu/Al 2 O 3 CO DRIFTS bands at 2121 and 2115 cm −1 were assigned to CO adsorbed on Cu sites [18,28], it is possible that during reaction these sites are made inaccessible by the deposition of carbonaceous material on the surface of metal particles (vide infra and see Figure A1 in Appendix B). However, another possibility is that in the course of the reaction these sites tend to disappear via sintering and/or alloying with Ni (see Figure 8 and Figure A2 in Appendix B). Since previous CO DRIFTS measurements on 20% Ni-5% Cu/Al 2 O 3 have also confirmed an electronic interaction between Cu and Ni [18], it can be argued that these changes would also have an electronic effect on surface Ni, which offers one potential explanation for the absence of a band at 2050 cm −1 attributable to CO adsorbed on Ni sites [29]. Interestingly, other authors have observed improved catalytic performance when the CO binding energy to Ni is lowered, as this causes active sites to be freed up more readily during deCO x thereby resulting in enhanced activity [30]. In fact, the CO produced via decarbonylation is a known catalyst poison-as well as a coke precursor (vide infra)-and, thus, a lower amount and/or a reduced residency time of CO on the catalyst surface should benefit deCO x activity [31].
The conclusions garnered from DRIFTS measurements are reinforced by the results of x-ray photoelectron spectroscopy (XPS) analyses performed on both the fresh and spent catalysts (see Figure A3 in Appendix B). Indeed, while the spent catalyst displays features indicative of deactivation via coking and fouling-i.e., increased intensity of carbon peaks (not shown) and lower intensity of peaks associated with metals-a shift in both Ni and Cu peak maxima consistent with surface reduction to form metallic phases and a Ni-Cu alloy [32,33] is also observed. While the extent of alloying is difficult to determine quantitatively in the absence of density of state measurements, qualitative examination of the peak positions indicate a shift of the Cu 2p 3/2 binding energy tõ 0.2 eV higher than that expected for copper metal, consistent with significant Ni-Cu alloying [34,35]. Integrating the respective Ni and Cu peaks after correcting for background and elemental sensitivity also shows evidence of Cu enrichment on the surface of the spent catalyst, with the surface Ni/Cu atomic ratio decreasing from 5.55 Ni atoms per Cu atom to 4.14 Ni atoms per Cu atom after 200 h on stream [36]. Taken together, the CO-DRIFTS and the XPS data provide compelling evidence that both surface enrichment of copper and alloying of Ni with Cu have occurred, with other authors reporting depth profiling of similar species evincing near total coverage of metal particles by Cu despite XPS integrals consistent with the bulk composition [36].
The thermogravimetric analysis (TGA) results in Figure 7 show that the total mass loss displayed by the spent catalyst is 9.5 and 5.1% after the first and second 100 h cycle, respectively. This indicates that less coke forms during the second 100 h cycle, i.e., after the catalyst regeneration step. Catalytic cracking of the feed is known to exacerbate catalyst deactivation via coking and to be particularly problematic for Ni-based catalysts [37]. As mentioned above, light hydrocarbons such as ethane, propane and butane are observed in greater abundance in the gaseous products evolved during the first 100 h cycle relative to the amount observed during the second 100 h cycle. This is consistent with the notion that the increased coking observed during the first 100 h stems from a higher cracking activity. Thus, sites responsible for cracking reactions appear to become irreversibly deactivated during the first 100 h cycle. Additionally, since adsorbed CO can also contribute to coking via the Boudouard reaction, the lower CO adsorption discussed above could also explain the decrease in carbonaceous deposits formed on the catalyst surface during the second 100 h cycle. Important insights were also gained through the analysis of the fresh and spent (after the second 100 h on stream) catalyst via transmission electron microscopy-energy dispersive X-ray spectroscopy (TEM-EDS). First, TEM results show that while the metal particle size distribution in the fresh catalysts is narrow and centers around 4 nm particles, the spent catalyst has a wider particle size distribution with a considerable number of particles larger than 10 nm and as large as 40 nm (see Figure 8a and Figure B2 in Appendix B). The fact that large particles arise at the expense of smaller particles (see Figure 8a) suggests that sintering occurs via Ostwald ripening. TEM-EDS results show that the composition of metal particles in the fresh catalyst is very consistent and close to the composition of the bulk catalyst (particles of 80% Ni-20% Cu are expected for a 20% Ni-5% Cu/Al2O3 formulation, atomic and weight percent being very close due to the similar atomic weight of Ni and Cu), albeit a significant number of Ni-rich (85-95% Ni) particles is also observed (see Figure 8b). However, the composition of metal particles in the spent catalyst is considerably different, as Cu-rich particles-from slightly enriched (75% Ni-25% Cu) to greatly enriched (35% Ni-65% Cu)-arise at the expense of the Ni-rich particles in the fresh catalyst. In short, the TEM and TEM-EDS results in Figure  8 suggest that in the course of the experiment metal particles tend to both grow and become Cu-rich. The latter is consistent with the results of elemental mapping included in Figure B2 in Appendix B, which also show that Ni and Cu are closely associated irrespective of the catalyst state (fresh or spent). Nevertheless, more detailed studies-which fall outside the scope of this contribution-are needed to more thoroughly ascertain the relationship between particle size and both surface and bulk composition. Important insights were also gained through the analysis of the fresh and spent (after the second 100 h on stream) catalyst via transmission electron microscopy-energy dispersive X-ray spectroscopy (TEM-EDS). First, TEM results show that while the metal particle size distribution in the fresh catalysts is narrow and centers around 4 nm particles, the spent catalyst has a wider particle size distribution with a considerable number of particles larger than 10 nm and as large as 40 nm (see Figures 8a and A2 in Appendix B). The fact that large particles arise at the expense of smaller particles (see Figure 8a) suggests that sintering occurs via Ostwald ripening. TEM-EDS results show that the composition of metal particles in the fresh catalyst is very consistent and close to the composition of the bulk catalyst (particles of 80% Ni-20% Cu are expected for a 20% Ni-5% Cu/Al 2 O 3 formulation, atomic and weight percent being very close due to the similar atomic weight of Ni and Cu), albeit a significant number of Ni-rich (85-95% Ni) particles is also observed (see Figure 8b). However, the composition of metal particles in the spent catalyst is considerably different, as Cu-rich particles-from slightly enriched (75% Ni-25% Cu) to greatly enriched (35% Ni-65% Cu)-arise at the expense of the Ni-rich particles in the fresh catalyst. In short, the TEM and TEM-EDS results in Figure 8 suggest that in the course of the experiment metal particles tend to both grow and become Cu-rich. The latter is consistent with the results of elemental mapping included in Figure A2 in Appendix B, which also show that Ni and Cu are closely associated irrespective of the catalyst state (fresh or spent). Nevertheless, more detailed studies-which fall outside the scope of this contribution-are needed to more thoroughly ascertain the relationship between particle size and both surface and bulk composition. Finally, since it could be argued that the Cu enrichment of the catalyst can be attributed to the reaction between CO and Ni resulting in the formation of volatile Ni carbonyl and the concomitant loss of Ni, the fresh and spent (after the second 100 h cycle) catalyst was analyzed by inductivelycoupled plasma-atomic emission spectroscopy (ICP-AES). Tellingly, while the material loaded into the reactor (a 1:1 mixture of catalyst and SiC diluent) had a Ni and Cu content of 8.87 and 1.98%, respectively, the corresponding values for the material recovered from the reactor (which also included 9.5% of coke deposits) were 7.39 and 1.62% (or 8.16 and 1.79% when corrected for coke). This corresponds to a Ni/Cu ratio of ~4.48 and ~4.56 for the fresh and spent catalysts, respectively, which clearly indicates that the catalyst experiences no loss of Ni. This is consistent with a report on the kinetics of nickel carbonyl formation [38]. Indeed, the authors of this report concluded that the highly exothermic reaction that forms nickel carbonyl reaches a maximum rate at ~75 °C, after which nickel carbonyl formation decreases to reach negligible levels by 150 °C irrespective of the pressures (partial CO, H2, or total pressure) employed. In deoxygenation experiments, the catalyst would only be exposed to CO at the reaction temperature of 375 °C, i.e., well above the range in which nickel carbonyl would form to an appreciable degree per the reference above. These results further confirm both the robustness of the catalyst under reaction conditions and its industrial applicability.

Catalyst Preparation
Catalysts were prepared by excess wetness impregnation using Ni(NO3)2·6H2O (Alfa Aesar, Haverhill, MA, USA) and Cu(NO3)2·3H2O (Sigma Aldrich, St. Louis, MO, USA) as the metal precursors. Beads of γ-Al2O3 (Sasol, Johannesburg, South Africa; surface area of 216 m 2 /g) were used as the support and were crushed to a particle size of <150 µm before the impregnation. The target metal loadings for the catalyst were 20 wt% Ni and 5 wt% Cu. The impregnated catalyst was dried overnight at 60 °C under vacuum prior to calcination for 3 h at 500 °C in static air. The catalyst and SiC catalyst diluent (Kramer Industries, Piscataway Township, NJ, USA) were sieved separately to a particle size between 150 and 300 µm and stored in a vacuum oven at 60 °C until use.  Finally, since it could be argued that the Cu enrichment of the catalyst can be attributed to the reaction between CO and Ni resulting in the formation of volatile Ni carbonyl and the concomitant loss of Ni, the fresh and spent (after the second 100 h cycle) catalyst was analyzed by inductively-coupled plasma-atomic emission spectroscopy (ICP-AES). Tellingly, while the material loaded into the reactor (a 1:1 mixture of catalyst and SiC diluent) had a Ni and Cu content of 8.87 and 1.98%, respectively, the corresponding values for the material recovered from the reactor (which also included 9.5% of coke deposits) were 7.39 and 1.62% (or 8.16 and 1.79% when corrected for coke). This corresponds to a Ni/Cu ratio of~4.48 and~4.56 for the fresh and spent catalysts, respectively, which clearly indicates that the catalyst experiences no loss of Ni. This is consistent with a report on the kinetics of nickel carbonyl formation [38]. Indeed, the authors of this report concluded that the highly exothermic reaction that forms nickel carbonyl reaches a maximum rate at~75 • C, after which nickel carbonyl formation decreases to reach negligible levels by 150 • C irrespective of the pressures (partial CO, H 2 , or total pressure) employed. In deoxygenation experiments, the catalyst would only be exposed to CO at the reaction temperature of 375 • C, i.e., well above the range in which nickel carbonyl would form to an appreciable degree per the reference above. These results further confirm both the robustness of the catalyst under reaction conditions and its industrial applicability.

Catalyst Preparation
Catalysts were prepared by excess wetness impregnation using Ni(NO 3 ) 2 ·6H 2 O (Alfa Aesar, Haverhill, MA, USA) and Cu(NO 3 ) 2 ·3H 2 O (Sigma Aldrich, St. Louis, MO, USA) as the metal precursors. Beads of γ-Al 2 O 3 (Sasol, Johannesburg, South Africa; surface area of 216 m 2 /g) were used as the support and were crushed to a particle size of <150 µm before the impregnation. The target metal loadings for the catalyst were 20 wt% Ni and 5 wt% Cu. The impregnated catalyst was dried overnight at 60 • C under vacuum prior to calcination for 3 h at 500 • C in static air. The catalyst and SiC catalyst diluent (Kramer Industries, Piscataway Township, NJ, USA) were sieved separately to a particle size between 150 and 300 µm and stored in a vacuum oven at 60 • C until use.

Catalyst Characterization
A small sample of the catalyst after the first 100 h on stream (in an experiment involving two 100 h cycles and an intermediate catalyst regeneration step) was subjected to TGA under flowing air (50 mL/min) on a TA instruments (New Castle, DE, USA) Discovery Series thermogravimetric analyzer. The temperature was ramped from room temperature to 800 • C at a rate of 10 • C/min. The same TGA procedure was used on the spent catalyst after the second 100 h cycle. DRIFTS was performed on the fresh and the spent catalyst after CO adsorption using a Thermo Scientific (Waltham, MA, USA) Nicolette 6700 FTIR instrument equipped with a Harrick Scientific (Pleasantville, NY, USA) praying mantis DRIFTS cell. The catalysts were dried under flowing Ar (50 mL/min) at 200 • C for 2 h and allowed to cool to 25 • C. The catalyst sample was then subjected to flowing 1% CO/Ar (50 mL/min) at 25 • C for 1 h, followed by Ar purging to remove gas phase CO and weakly absorbed CO before the spectrum was collected. The sample was then heated to 200 • C under flowing Ar (50 ml/min) and complete CO desorption was monitored by a return of the DRIFTS signal to a previously established baseline. The gas flow was then switched to 10% H 2 /N 2 (50 mL/min) as the temperature was increased to 400 • C and held for 1 h. The catalyst was then cooled to 25 • C under flowing Ar (50 mL/min) to remove excess H 2 . The catalyst was again subjected to flowing 1% CO/Ar (50 mL/min) at 25 • C for 1 h, followed by Ar purging to remove gas phase CO and weakly absorbed CO before spectra were collected. XPS measurements were performed on a Thermo Scientific (Waltham, MA, USA) K-Alpha system utilizing Al K-α radiation and a spot size of 100 µm. A minimum of 15 scans were collected for the full range spectra as well as for individual element scans, each spectrum produced being the average of two sample points. A linear background correction was used for sample integration and an elemental effectiveness factor of 1.1 was applied to copper to compensate for signal intensity variation. TEM observations were conducted on the fresh and spent (after 2 nd 100 h on stream) Ni-Cu catalyst. The catalyst powders were loaded on lacey carbon 400 mesh gold (C/Au) grids via a sonication-assisted method. This required a sample of the catalyst powder to be sonicated in 1 mL of ethanol for 20 min before placing one drop of the resulting suspension solution onto a blank C/Au grid that was subsequently allowed to dry in air. Samples thus prepared were then introduced into a Thermo Scientific (Waltham, MA, USA) Talos F200X analytical electron microscope, operated at 200 keV and equipped with four silicon drift detector (SDD)-based EDS systems for quantitative chemical composition analysis and elemental distribution mapping.

Feed Preparation
A waste FFA feedstock was obtained from the steam stripping of triglyceride-based feeds used for biodiesel synthesis. BG from waste water grease traps was supplied by Pincelli and Associates (Chattanooga, TN, USA). The BG was mixed vigorously with 25 wt% chloroform (HPLC grade, supplied by J.T. Baker, Radnor, PA, USA) for 2 h at 30 • C. The resulting solution was filtered with occasional heating to counter the solidification of fats. The water layer from the resulting filtrate was then decanted and the remaining organic mixture was dried using Na 2 SO 4 . The chloroform was removed by rotatory evaporation and the remaining lipids were diluted to the desired concentration with n-dodecane (99+%, Alfa Aesar, Haverhill, MA, USA).

Continuous Fixed-Bed Deoxygenation Experiments
Experiments were operated in continuous mode using a fixed bed stainless steel tubular reactor (1/2 in o.d., Parr, Moline, IL, USA) with a stainless steel porous frit to hold the catalyst bed in place. A mixture of equal parts catalyst and SiC diluent (by weight, 1 g total) was used for all experiments. The catalyst was reduced in situ at 400 • C for 3 h under flowing H 2 (60 mL/min). Temperature was monitored using two K-type thermocouples, one introduced from above and made to contact the catalyst bed and one introduced from below and made to contact the aforementioned porous frit under the catalyst bed. For experiments in which the reaction atmosphere was not pure H 2 , the reactor was purged after the reduction with Ar and pressurized with the reaction gas to 40 bar. The pressure was monitored both upstream and downstream of the catalyst bed by Omega (Norwalk, CT, USA) digital pressure gauges. After the system was pressurized, the catalyst bed was heated to the desired reaction temperature (275-375 • C). The liquid feed solution was introduced to the reactor using a Harvard Apparatus (Holliston, MA, USA) syringe pump equipped with an 8 mL syringe, either at 0.043 mL/min for the FFA feed (25 wt% in C12) or at 0.021 mL/min for BG (50 wt% in C12) to achieve a weight hour space velocity (WHSV) of 1 h −1 . The flow of the reaction gas was held at 60 mL/min for the duration of the experiment. Liquid products were sampled from a liquid-gas separator (kept at 0 • C) placed downstream from the catalyst bed. Incondensable gases were directed to a dry test meter before being collected in Tedlar ® gas sample bags. Gas sample bags were changed every time a liquid sample was taken to ensure that the gas samples analyzed and the liquid samples collected could be correlated. Representative experiments were performed in duplicate to ensure reproducibility. The average standard deviation of diesel-like hydrocarbons and heavy products formed was 2.77% and 1.47% in duplicate FFA and BG upgrading experiments, respectively.

Liquid and Gaseous Product Analysis
The liquid products were analyzed using a combined simulated-distillation-GC and GC-MS method specifically devised to identify and quantify the products obtained in the upgrading of FOG to hydrocarbons. Detailed information about the development and application of this method is available elsewhere [39]. Briefly, the analyses were performed using an Agilent (Santa Clara, CA, USA) 7890B GC system equipped with an Agilent (Santa Clara, CA, USA) 5977A extractor MSD and flame ionization detector (FID). The multimode inlet, which contained a helix liner, was run in a split mode (15:1; split flow, 48 mL/min) with an initial temperature of 100 • C. Helium was used as the carrier gas and a 1 µL injection was employed. Upon injection, the inlet temperature was immediately increased to 380 • C at a rate of 8 • C/min, and the temperature was maintained for the course of the analysis. The oven temperature was increased upon injection from 40 • C to 325 • C at a rate of 4 • C/min, followed by a ramp of 10 • C/min to 400 • C, which was maintained for 12.5 min. The total analysis run time was 91.25 min. An Agilent (Santa Clara, CA, USA) J and W VF-5ht column (30 m × 250 µm × 0.1 µm) rated to 450 • C was used. Column eluents were directed to a Siltek MXT™ connector that split the flow into two streams, one leading to the MSD (J and W Ultimetal Plus Tubing, 11 m × 0.25 mm i.d.) and one leading to the FID (J and W Ultimetal Plus Tubing, 5 m × 0.25 mm i.d.). The MS zone temperatures (MS source at 230 • C and quadrupole at 150 • C) were held constant for the duration of the analysis. A 1.75 min solvent delay was implemented and the MSD scanned from 10 to 700 Da. The FID was set to 390 • C with the following gas flow rates: H 2 at 40 mL/min; air at 400 mL/min; He makeup at 25 mL/min. Quantification was performed using cyclohexanone as an internal standard. Agilent (Santa Clara, CA, USA) MassHunter Acquisition and SimDis Expert 9-purchased from Separation Systems Inc. (Gulf Breeze, FL, USA)-software were respectively used to perform chromatographic programming and to process the GC-FID data acquired. Solvents (i.e., chloroform and dodecane) were quenched and/or subtracted prior to processing the data.
Gaseous samples were analyzed using an Agilent (Santa Clara, CA, USA) 3000 Micro-GC equipped with 5 Å molecular sieve, PoraPLOT U, alumina, and OV-1 columns. The GC was calibrated for all of the gaseous products obtained, including CO x , as well as straight chain C1-C6 alkanes and alkenes.

Conclusions
20% Ni-5% Cu/Al 2 O 3 was found to be an effective catalyst in the deoxygenation of fatty acid waste streams to fuel-like hydrocarbons. Near quantitative conversion of a free fatty acid feed obtained by steam stripping a biodiesel feedstock (25 wt% in dodecane) was achieved at all the reaction temperatures employed, i.e., 275, 325, and 375 • C. Notably, upon increasing the lipid concentration-from the 25 wt% used in experiments involving the feed obtained by steam stripping to the 50 wt% used in experiments involving BG-quantitative conversion of the BG lipids to hydrocarbons was obtained in experiments performed at 325 and 375 • C. While the 20% Ni-5% Cu/Al 2 O 3 catalyst yielded a larger amount of heavy chain hydrocarbons during the upgrading of BG under reduced H 2 partial pressure, CO x methanation (and the associated H 2 consumption) was significantly reduced. Saliently, the 20% Ni-5% Cu/Al 2 O 3 catalyst gave yields of diesel-like hydrocarbons in excess of 80% at all reaction times during a BG upgrading experiment lasting 100 h. Moreover, the catalyst was successfully regenerated in situ and displayed improved deoxygenation and decreased cracking and methanation activity during a second 100 h cycle, which is ascribed to irreversible poisoning of cracking and CO adsorption sites and/or to the decrease in the CO binding energy to Ni sites. Indeed, the lower concentration of CO on the catalyst surface decreases catalyst poisoning from CO-resulting in the superior activity and stability observed by the regenerated catalyst-as well as the likelihood of methane and coke formation. This conclusion is supported by data pertaining to the characterization of the fresh and spent (after the second 100 h on stream) catalyst via TEM-EDS, CO-DRIFTS, and XPS, analytical results showing that metal particle sintering, alloying of Ni with Cu, as well as both surface and bulk particle enrichment with copper all occur in the course of reaction and/or catalyst regeneration. Taken together, these results explain the superior properties of the regenerated catalyst in lipid deoxygenation relative to its fresh counterpart. Overall, these results confirm that 20% Ni-5% Cu/Al 2 O 3 is a robust and effective catalyst for the conversion of waste lipid streams to diesel-range hydrocarbons. Acknowledgments: Brad Davis of ESC Energy is thanked for providing the sample of waste FFAs used in this study. Beth Hamilton of Pincelli and Associates is thanked for providing the sample of brown grease used in this study. Maria Wright is thanked for her assistance with feed preparation.

Conflicts of Interest:
The authors declare no conflict of interest. The funders had no role in the design of the study; in the collection, analyses, or interpretation of data; in the writing of the manuscript; or in the decision to publish the results.   Appendix B Figure A1. TEM micrographs of the fresh (left) and spent (right) catalyst. Distinct layers of carbonaceous deposits can be seen surrounding a metal particle in the spent catalyst outlined in red.