Hydroprocessing (HT) followed by oxidative desulfurization (ODS) and denitrogenation (ODN) of gas oils has been reported by Badoga et al. The mechanism of methanol synthesis from CO2 hydrogenation using Cu-ZnO based catalysts was investigated by Gao et al. 2019) using a combination of strong electronic adsorption (SEA) and atomic layer deposition (ALD) techniques.
Influence of Bio-Oil Phospholipid on the Hydrodeoxygenation Activity
Introduction
A marked effect on HDO activity and selectivity was observed in the presence of phosphatidylcholine (PC) (Figure 2). However, the broadening of the phosphate peak area confirms the increasing deposition of P on the catalyst with increasing phospholipid (PC) in the feed.
Materials and Methods 1. Catalyst Preparation
They were then placed on the manipulator forks of the pretreatment chamber under a nitrogen atmosphere. Coke deposition on each of the spent catalyst samples was calculated based on calibration for CO, CO2 and H2O in the carrier gas.
Conclusions
Study of the hydrodeoxygenation of carbonyl, carboyl and guaiacyl groups over sulfided CoMo/γ-Al2O3 and NiMo/γ-Al2O3 catalysts.Appl. Insight into sulfur species in the hydrodeoxygenation of aliphatic esters over sulfided NiMo/γ-Al2O3 catalyst.Appl.
Hydrotreatment Followed by Oxidative
Desulfurization and Denitrogenation to Attain Low Sulphur and Nitrogen Bitumen Derived Gas Oils
Results and Discussion 1. Material Characterization
The synthesized catalysts were tested for the oxidation of sulfur- and nitrogen-containing aromatic compounds present in hydrotreated HGO and LGO. Results shown in Table 2 suggest the effectiveness of activated carbon as an adsorbent for the removal of oxygenated sulfur and nitrogen compounds.
Experimental 1. Materials
Synthesis and characterization of a new Co-Mo/γ-Al2O3 catalyst for oxidative desulfurization (ODS) of model diesel fuel. Oxidative desulfurization and denitrogenation of light gas oil by an oxidation/adsorptive continuous flow process.Appl.
Hydrotreated Vegetable Oil as a Fuel from Waste Materials
- Results
- Discussion
- Materials and Methods
- Conclusions
Hydrotreated vegetable oils are one of the possible ways of using the increased biofuel content in diesel. The cold filter plugging point (CFPP) practically corresponds to the cloud point value, therefore the cloud point value is important in the case of hydrotreated oils. However, in the case of a flash point value, these values do not affect the performance of the diesel engine.
Figure 11 shows the increasing trend lines of cetane number and cetane index with increasing HVO content. Water-treated oil is a suitable additive for increasing the cetane number due to the nature of the fuel, where its effect is greater than the use of conventional additives. The calculation of the cetane index is suitable for standard diesel fuels (with FAME) and its use for hydrotreated oils is not suitable.
In Figure 12, we can see the composition of the analyzed diesel fuel with labeled n-alkanes, which represent the main components of the sample. The measured high values of the cetane number and the calculated values of the cetane index increase with the HVO content in the mineral oil mixture.
The Promoting Effect of Ni on Glycerol
Hydrogenolysis to 1,2-Propanediol with In Situ Hydrogen from Methanol Steam Reforming Using a
Results and Discussion 1. Catalyst Characterization
The NH3TPD data for Ni-added Cu/ZnO/Al2O3-OA catalysts are listed in Table 1 and Figure 2. The effect of Ni loading on the acidity of the Cu/ZnO/Al2O3-OA catalyst is shown in Figure 2. Cu/ZnO/Al2O3-OA and Cu/ZnO/Al2O3-Na completely decomposed at 325 and 630 ◦C, respectively.
Figure 6 shows the TGA results for Cu/ZnO/Al2O3-OA and Ni/Cu/ZnO/Al2O3-OA oxalates. Figure 8 shows the XRD patterns for CuO/ZnO/Al2O3-OA catalysts with different Ni loadings. Therefore, the Cu/ZnO/Al2O3-OA catalyst is believed to be feasible for this reaction system.
Product distribution of glycerol hydrogenolysis with in situ H2 from steam reforming methanol over Cu/ZnO/Al2O3-OA catalysts with different Ni1 loadings. Therefore, the selectivity of 1,2-PD using the Ni/Cu/ZnO/Al2O3-OA catalyst is higher in the reaction time as shown in Figure 11b.
Materials and Methods
Promoting the effect of rhenium on the catalytic performance of Ru catalysts in the hydrogenolysis of glycerol to propanediol.Catal. Aqueous phase reforming of glycerol to 1,2-propanediol over Pt nanoparticles on hydrotalcite in the absence of hydrogen. Green Chem. Selective transfer hydrogenolysis of glycerol promoted by palladium catalysts in the absence of hydrogen. Green Chem.
Physiochemical study of glycerol hydrogenolysis over a Ni-Cu/Al2O3 catalyst using formic acid as the hydrogen source.Bo. Catalytic hydrogenolysis of glycerol to propylene glycol over mixed oxides derived from a hydrotalcite-type precursor.Ind. Selective hydrogenolysis of glycerol to propylene glycol on Cu–ZnO composite catalysts: Structural requirements and reaction mechanism.Chem.
Aqueous Hydrogenolysis of Glycerol over Ni-Ce/AC Catalyst: Inducing Effect of Ce on Catalytic Performance.Appl. Synthesis and performance of highly dispersed Cu/SiO2 catalysts for the hydrogenolysis of glycerol.Appl.
Influence of Chemical Surface Characteristics of Ammonium-Modified Chilean Zeolite on Oak
Results and Discussion
A semiquantitative gas chromatography/mass spectrophotometry (GC/MS) analysis of fractionated bio-oil samples was performed (see Materials and Methods) to identify primary chemical compounds from representative families to evaluate the influence of chemical surface characteristics of natural and modified zeolite samples on the chemical composition of obtained bio-oil samples. The highest composition of furfural in obtained bio-oil samples was obtained when 2NHZ zeolite sample was used. Table 5 shows a qualitative compositional analysis of obtained bio-oil samples, using natural and modified zeolite samples on the catalytic slow pyrolysis of oak investigated in this study.
As Table 5 shows, a lower percentage of oxygenated compounds was recorded in the bio-oil samples from catalytic assays using the 2NHZ sample. Bio-oil samples were diluted (1:1 ratio) with ultrapure water and centrifuged at 3300 rpm for 5 minutes in a LW SCIENTIFIC (Santiago, Chile) ULTRA 8V apparatus. The Brønsted acid sites on ammonium-modified zeolite samples are responsible for the upgraded bio-oil and value-added chemicals obtained in this study.
Catalytic pyrolysis of Chilean oak: Influence of Brønsted acid sites of Chilean natural zeolite. Catalysts. Catalytic fast pyrolysis of biomass over zeolites for high quality bio-oil – a review.Fuel process.
Enhancement of Light Olefins Selectivity Over N-Doped Fischer-Tropsch Synthesis Catalyst
The ID/IG ratios of Fe-10MnK-AC and FeN-10MnK-AC are lower than those of Fe-AC and FeN-AC catalysts. In particular, based on the XRD spectrum analysis result, another type of iron nitride (ζ-Fe2N, JCPDS No. 50-0958) is obtained on FeN-10MnK-AC catalyst. Only a small fraction of iron nitrides was obtained on FeN-AC and FeN-10MnK-AC catalysts according to the lower intensity of the peaks attributed to ε-Fe3N and ζ-Fe2N.
Strongly interacting spinel (Fe, Mn)Oxwuth mixed oxides lead to extensive reduction peaks of Fe-10MnK-AC and FeN-10MnK-AC catalysts, which inhibits iron oxide reduction to some extent. Fe-10MnK-AC and FeN-10MnK-AC also show a similar trend in CO2 selectivity. The hydrogen-competitive adsorption of manganese and the electron-donating effect of nitrogen enhance the FTO performance on the FeN-10MnK-AC catalyst.
Finally, samples were calcined under static N2 at 300◦C for 3 h (heating rate: 2◦C/min) and Fe-AC and Fe-10MnK-AC catalysts were received. A higher light olefins selectivity (44.7%) than Fe-AC, FeN-AC and Fe-10MnK-AC catalysts was achieved over FeN-10MnK-AC catalyst.
Application of Microwave in Hydrogen Production from Methane Dry Reforming: Comparison Between
Experimental
In addition, the crystal patterns of the catalysts were determined by X-ray diffraction (XRD) using a Bruker D8 Advance spectrometer. The temperature of the catalyst bed was measured with a thermal gun (Milwakee M12 model) through an open window in front of the catalyst. The system was at atmospheric pressure and the applied microwave power was adjusted to change the temperature of the catalyst.
Operating conditions similar to those of the microwave catalytic reaction were applied, and the effects of temperature and metal content were investigated and compared with the results of the microwave setup. The addition of Mg as a promoter was found to increase the activity of the catalyst by increasing the nickel dispersion. Compared to conventional heating, applying microwave heating at the same catalyst bed temperature for both heating systems resulted in a significant improvement in methane conversion.
However, for high flow rates (GHSV of 33,000 mL/g cat.h), the conversions were below the equilibrium value. Investigation of mechanistic aspects of the catalytic CO2 reforming of methane in a dielectric-barrier discharge using optical emission spectroscopy and kinetic modeling.Phys.
The Effects of Catalyst Support and Temperature on the Hydrotreating of Waste Cooking Oil (WCO) over
Reaction Route Discussion
The reaction routes of the hydrotreated WCO over the unsupported CoMoS were investigated in a previous study [14]. Focus is placed on the deoxygenation, cracking/polymerization, and hydrogenation/dehydrogenation reactions of the supported and unsupported CoMoS catalyst. This indicates that the presence of the catalyst support caused an enhancement of the deoxygenation reactions.
It was found that the C18/C17 ratios of the products obtained on supported CoMoS were much higher than those on unsupported CoMoS, as shown in Figure 5. This suggests that HDO was the main reaction pathway of the supported CoMoS catalyst (oxygen was removed mainly as H2O). On the other hand, this result also suggests that HDCO was the main reaction pathway of unsupported CoMoS (oxygen was mainly removed in the form of CO or CO2).
Therefore, at the reaction temperature of 300 to 375 °C, the main active sites of the supported catalyst were the sulfur site, while the unsupported catalyst was dominated by saturated sites. The cracking and polymerization selectivities of unsupported and supported CoMoS products at different temperatures were evaluated, and the experimental results are shown in Figure 6.
Experimental
This research investigated the role of catalyst support and reaction temperature in the WCO hydrotreating process by evaluating the deoxygenation, cracking/polymerization, and hydrogenation/dehydrogenation efficiencies of an unsupported CoMoS catalyst and an Al2O3-TiO2-SiO2 supported CoMoS catalyst. HDO was the main reaction pathway of the supported CoMoS catalyst, and HDCO was the main reaction pathway of the unsupported CoMoS. Increasing the reaction temperature did not affect the main reaction pathways, but slightly increased the capacity of HDCO. In the hydrocracking and polymerization process, the unsupported catalyst was associated with higher polymerization rates compared to the supported catalyst due to the lack of acidic support.
In the hydrogenation and dehydrogenation process, the dehydrogenation reaction occurred when the reaction temperature was above 375◦C. Compared to unsupported CoMoS, supported CoMoS exhibited higher hydrogenation abilities at 300–375◦C. During the hydrotreatment process of WCO, the presence of CoMoS catalyst support increased the HDO, decreased the degree of polymerization, and decreased the reaction temperature. A stands for active catalyst metal, B stands for catalyst support. For example, CoMoS/SiO2 means that the active catalyst metal is sulfided cobalt and molybdenum, and the catalyst support is silica.
Effect of Alumina Support on Active Phase Formation of Co-Mo/Al2O3 Selective Hydrodesulfurization Catalysts.Chin. Effect of CoMo sulfide catalyst support and addition of potassium and platinum on catalytic properties for hydrodeoxygenation of carbonyl, carboxyl and guaiacol molecules.J.
