The Experts below are selected from a list of 360 Experts worldwide ranked by ideXlab platform
Jorge Ancheyta - One of the best experts on this subject based on the ideXlab platform.
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experimental methods for developing kinetic models for Hydrocracking reactions with slurry phase catalyst using batch reactors
Energy & Fuels, 2016Co-Authors: Alexander Quitian, Jorge AncheytaAbstract:Experimental methods for studying the chemical kinetics of Hydrocracking reactions with disperse catalysts in batch operation are reviewed. Batch operating conditions and description of modes of operation of the reactors are discussed. The experimental procedures used to produce, analyze, and interpret the experimental data required for determining the chemical kinetics of Hydrocracking reactions with catalyst in dispersed phase are also reviewed. Two possible batch operation modes used for the study of such reactions are described: isothermal and temperature scanning operation. The typical kinetic models for Hydrocracking are discussed in detail and step-by-step procedures to calculate the stoichiometric coefficients, mass transfer coefficients, rate constants, and activation energies from experimental data are provided.
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Hydrocracking of maya crude oil in a slurry phase batch reactor ii effect of catalyst load
Fuel, 2014Co-Authors: Hugo Ortizmoreno, Jorge Ramirez, Felipe Sanchezminero, Rogelio Cuevas, Jorge AncheytaAbstract:Abstract The effect of the catalyst load in slurry Hydrocracking of heavy Maya crude oil was investigated at mild conditions (390 °C and 1400 H2 psi). The catalyst load and operating time were varied in the intervals 0–1000 ppm Mo and 0–11 h respectively. The results allowed to establish the transformation routes of the different fractions under thermal or catalytic conditions. Under thermal conditions, the contributors to gas formation were found to be: Asphaltenes ≫ resins > vacuum gas–oil and the use of catalyst inhibited the contributions of resins and vacuum gas–oil. It was found that catalytic slurry Hydrocracking evolves in two general reaction stages: the first, dominated by the catalyst-induced reactions, from zero to 50% VR conversion, and the second, above 50% VR conversion, dominated by thermal reactions leading to high production of coke. During the first stage the naturally occurring asphaltenes of Maya crude were effectively transformed to liquid fractions and the formation of coke and new asphaltene-like components were catalytically inhibited. Moreover, the production of middle distillates was enhanced. The second reaction stage in catalytic Hydrocracking approaches thermal behavior likely because part of the catalyst is lost when the crude mixture above 50% VR conversion departs from physical equilibrium and forms asphaltenic aggregates that precipitate entrapping some catalyst. During the second reaction stage, middle distillates are transformed to light ends, which are end products because no declination was observed in its production. The use of catalyst improves API gravity and viscosity of the liquid product. In all cases the API gravity increased with naphtha production. The hydrodesulfurization results indicate that most of the eliminated sulfur was of asphaltenic nature, presumably associated to the aliphatic lateral chains of asphaltenes. A qualitative estimation of the importance of the different reaction routes is proposed on the basis of the results of this work.
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a review of experimental procedures for heavy oil Hydrocracking with dispersed catalyst
Catalysis Today, 2014Co-Authors: M J Angeles, Jorge Ancheyta, Carolina Leyva, Sergio RamirezAbstract:Abstract This paper summarizes the technical knowledge necessary to study the Hydrocracking of heavy oil with dispersed catalysts. Chemical kinetics aspects of the Hydrocracking of heavy oil reaction are reviewed. The discussion also includes a description of the experimental setups, operation modes and suitable reactors for conducting heavy oil Hydrocracking experiments. Reactors and their hydrodynamics are described in order to establish the more appropriate operating conditions to perform the experiments. The most common catalyst precursors used in the reaction are listed as well as the analytical techniques employed in characterizing and quantifying gas, liquid and solid samples. Procedures for pretreatment of feed, catalyst dispersion and sulfurization of catalyst precursors are also presented
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kinetic model for Hydrocracking of heavy oil in a cstr involving short term catalyst deactivation
Fuel, 2012Co-Authors: Jeremias Martinez, Jorge AncheytaAbstract:Abstract A five-lump model previously reported in the literature was used for the kinetic modeling of an atmospheric residue (312 °C+) Hydrocracking. The model has ten reaction rate coefficients, makes a distinction of different hydrocarbon groups based on boiling ranges, and includes the following lumps: unconverted vacuum residue (538 °C+), vacuum gas oil (VGO; 343–538 °C), middle distillates (204–343 °C), naphtha (IBP-204 °C), and gases. The kinetic study was carried out in a CSTBR at the following operating conditions: 380–420 °C, 100 kg f /cm 2 , 5000 std ft 3 H 2 /bbl of oil, and 0.5–1.25 ml feed /(ml cat h). Experiments were performed with a commercial size tetra lobular catalyst. The model also incorporates the effectiveness factor, and a time-dependant deactivation function for obtaining the intrinsic kinetic parameters. The Hydrocracking of vacuum residue, VGO and middle distillates exhibited a higher selectivity toward the heavier lumps as temperature is increased. The predicted product composition is in good agreement with experimental values with an average absolute error less than 5%.
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hydrodesulfurization and Hydrocracking of maya crude with p modified nimo al2o3 catalysts
Fuel, 2012Co-Authors: P Rayo, S K Maity, Jorge Ramirez, Pablo Torresmancera, Gustavo Marroquin, Jorge AncheytaAbstract:Abstract In the present work we analyze the changes in Hydrocracking, hydrodesulfurization, hydrodeasphaltenization, and hydrodesmetallization, during the hydrotreating of Maya crude, when 3.4 wt.% of P 2 O 5 is incorporated by two different routes to a NiMo/Al 2 O 3 catalyst. The catalysts were characterized by nitrogen physisorption, XRD, HRTEM, SEM, and CO adsorption analyzed by FTIR. Additionally, to obtain deeper knowledge on the reaction system, the catalysts were also tested in the HDS of 4,6-DMDBT, and Hydrocracking of cumene. NiMo/PAl 2 O 3 shows the highest HDS activity for 4,6-DMDBT, the better hydrogenating properties, and the best performance in all the reactions during hydrotreating of Maya crude. The acidity and porosity of the catalyst are determinant factor for the conversion of atmospheric residue. At similar acidity, the porosity defines the best catalyst and conversely, at similar porosity, acidity will define the activity of the catalyst. However, an excess of acidity in the catalyst can lead to rapid deactivation. NiMo/PAl 2 O 3 displays superior performance compared to NiMo/Al 2 O 3 and NiMoP/Al 2 O 3 because it presents the best combination of acidity, porosity and distribution of the sulfided Ni and Mo phases, which provide the hydrodesulfurization and hydrogenating functions.
Jose E.a. Graciano - One of the best experts on this subject based on the ideXlab platform.
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conversion of co2 rich natural gas to liquid transportation fuels via trireforming and fischer tropsch synthesis model based assessment
Industrial & Engineering Chemistry Research, 2018Co-Authors: Jose E.a. Graciano, Benoît Chachuat, Rita M.b. AlvesAbstract:This paper presents a model-based analysis of a process coupling trireforming and Fischer–Tropsch technologies for the production of liquid fuels from CO2-rich natural gas. The process also includes an upgrading section based on Hydrocracking, a separation section, a water gas shift unit, and a Rankine cycle unit for recovering the excess thermal energy produced by the Fischer–Tropsch reactor. Simulations are carried out in the process simulator Aspen Plus using standard unit operation models where applicable, while modeling the nonconventional units, such as the Fischer–Tropsch and Hydrocracking reactors, using Aspen Custom Modeler. The proposed process could achieve a carbon conversion efficiency upward of 50% in the analyzed scenario, despite a natural gas feedstock with 30 mol % CO2. The analysis also reveals that the plant-wide electricity consumption could be covered nearly entirely by the Rankine cycle unit, enabling significant cost savings alongside a reduction of the overall global warming poten...
Aggeliki Kalogianni - One of the best experts on this subject based on the ideXlab platform.
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Hydrocracking of used cooking oil for biofuels production
Bioresource Technology, 2009Co-Authors: Stella Bezergianni, Aggeliki KalogianniAbstract:Hydrocracking of used cooking oil is studied as a potential process for biofuels production. In this work several parameters are considered for evaluating the effectiveness of this technology, including Hydrocracking temperature, liquid hourly space velocity (LHSV) and days on stream (DOS). Conversion and total biofuels production is favored by increasing temperature and decreasing LHSV. However moderate reaction temperatures and LHSVs are more attractive for diesel production, whereas higher temperatures and smaller LHSVs are more suitable for gasoline production. Furthermore heteroatom (S, N and O) removal increases as Hydrocracking temperature increases, with de-oxygenation being particularly favorable. Saturation, however, is not favored with temperature indicating the necessity of a pre-treatment step prior to Hydrocracking to enable saturation of the double bonds and heteroatom removal. Finally the impact of extended operation (catalyst life) on product yields and qualities indicates that all reactions are affected yet at different rates.
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catalytic Hydrocracking of fresh and used cooking oil
Industrial & Engineering Chemistry Research, 2009Co-Authors: Stella Bezergianni, Spyros Voutetakis, Aggeliki KalogianniAbstract:Hydrocracking of vegetable oils is a prominent technology for the production of biofuels. This work compares the product yields and quality of Hydrocracking fresh and used cooking oil under nominal operating conditions. Cracking, heteroatom removal and saturation reaction mechanisms are evaluated for both feedstock types and for three typical Hydrocracking temperatures. The assessment of both feedstocks indicates that they are both suitable for high diesel yields with smaller kerosene/jet and gasoline/naphtha yields. As temperature increases, diesel selectivity increases for both feedstock types. However, the used oil feedstock exhibits higher kerosene/jet and naphtha selectivity at low temperatures (350 °C) and lower at the highest Hydrocracking temperature (390 °C).
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Hydrocracking of vacuum gas oil vegetable oil mixtures for biofuels production
Bioresource Technology, 2009Co-Authors: Stella Bezergianni, Aggeliki Kalogianni, I A VasalosAbstract:Hydrocracking of vacuum gas oil (VGO) - vegetable oil mixtures is a prominent process for the production of biofuels. In this work both pre-hydrotreated and non-hydrotreated VGO are assessed whether they are suitable fossil components in a VGO-vegetable oil mixture as feed-stocks to a Hydrocracking process. This assessment indicates the necessity of a VGO pre-hydrotreated step prior to Hydrocracking the VGO-vegetable oil mixture. Moreover, the comparison of two different mixing ratios suggests that higher vegetable oil content favors Hydrocracking product yields and qualities. Three commercial catalysts of different activity are utilized in order to identify a range of products that can be produced via a Hydrocracking route. Finally, the effect of temperature on Hydrocracking VGO-vegetable oil mixtures is studied in terms of conversion and selectivity to diesel, jet/kerosene and naphtha.
Stella Bezergianni - One of the best experts on this subject based on the ideXlab platform.
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Hydrocracking of used cooking oil for biofuels production
Bioresource Technology, 2009Co-Authors: Stella Bezergianni, Aggeliki KalogianniAbstract:Hydrocracking of used cooking oil is studied as a potential process for biofuels production. In this work several parameters are considered for evaluating the effectiveness of this technology, including Hydrocracking temperature, liquid hourly space velocity (LHSV) and days on stream (DOS). Conversion and total biofuels production is favored by increasing temperature and decreasing LHSV. However moderate reaction temperatures and LHSVs are more attractive for diesel production, whereas higher temperatures and smaller LHSVs are more suitable for gasoline production. Furthermore heteroatom (S, N and O) removal increases as Hydrocracking temperature increases, with de-oxygenation being particularly favorable. Saturation, however, is not favored with temperature indicating the necessity of a pre-treatment step prior to Hydrocracking to enable saturation of the double bonds and heteroatom removal. Finally the impact of extended operation (catalyst life) on product yields and qualities indicates that all reactions are affected yet at different rates.
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catalytic Hydrocracking of fresh and used cooking oil
Industrial & Engineering Chemistry Research, 2009Co-Authors: Stella Bezergianni, Spyros Voutetakis, Aggeliki KalogianniAbstract:Hydrocracking of vegetable oils is a prominent technology for the production of biofuels. This work compares the product yields and quality of Hydrocracking fresh and used cooking oil under nominal operating conditions. Cracking, heteroatom removal and saturation reaction mechanisms are evaluated for both feedstock types and for three typical Hydrocracking temperatures. The assessment of both feedstocks indicates that they are both suitable for high diesel yields with smaller kerosene/jet and gasoline/naphtha yields. As temperature increases, diesel selectivity increases for both feedstock types. However, the used oil feedstock exhibits higher kerosene/jet and naphtha selectivity at low temperatures (350 °C) and lower at the highest Hydrocracking temperature (390 °C).
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Hydrocracking of vacuum gas oil vegetable oil mixtures for biofuels production
Bioresource Technology, 2009Co-Authors: Stella Bezergianni, Aggeliki Kalogianni, I A VasalosAbstract:Hydrocracking of vacuum gas oil (VGO) - vegetable oil mixtures is a prominent process for the production of biofuels. In this work both pre-hydrotreated and non-hydrotreated VGO are assessed whether they are suitable fossil components in a VGO-vegetable oil mixture as feed-stocks to a Hydrocracking process. This assessment indicates the necessity of a VGO pre-hydrotreated step prior to Hydrocracking the VGO-vegetable oil mixture. Moreover, the comparison of two different mixing ratios suggests that higher vegetable oil content favors Hydrocracking product yields and qualities. Three commercial catalysts of different activity are utilized in order to identify a range of products that can be produced via a Hydrocracking route. Finally, the effect of temperature on Hydrocracking VGO-vegetable oil mixtures is studied in terms of conversion and selectivity to diesel, jet/kerosene and naphtha.
Rita M.b. Alves - One of the best experts on this subject based on the ideXlab platform.
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conversion of co2 rich natural gas to liquid transportation fuels via trireforming and fischer tropsch synthesis model based assessment
Industrial & Engineering Chemistry Research, 2018Co-Authors: Jose E.a. Graciano, Benoît Chachuat, Rita M.b. AlvesAbstract:This paper presents a model-based analysis of a process coupling trireforming and Fischer–Tropsch technologies for the production of liquid fuels from CO2-rich natural gas. The process also includes an upgrading section based on Hydrocracking, a separation section, a water gas shift unit, and a Rankine cycle unit for recovering the excess thermal energy produced by the Fischer–Tropsch reactor. Simulations are carried out in the process simulator Aspen Plus using standard unit operation models where applicable, while modeling the nonconventional units, such as the Fischer–Tropsch and Hydrocracking reactors, using Aspen Custom Modeler. The proposed process could achieve a carbon conversion efficiency upward of 50% in the analyzed scenario, despite a natural gas feedstock with 30 mol % CO2. The analysis also reveals that the plant-wide electricity consumption could be covered nearly entirely by the Rankine cycle unit, enabling significant cost savings alongside a reduction of the overall global warming poten...