Hydrocracking of Athabasca Bitumen Using Submicronic Multimetallic Catalysts at Near In-Reservoir Conditions

Galarraga, C.; Pereira‐Almao, Pedro

doi:10.1021/ef9013407

Cited by 98 publications

(110 citation statements)

References 24 publications

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“…However, most of these techniques do not exceed 20 %-25 % oil recovery or 50 % for the steam-assisted gravity drainage (SAGD) process (Butler 1998;Nasr et al 2003;Hashemi et al 2013). Nanoparticle technology has emerged as an alternative with a great potential to improve the previously mentioned techniques and increase oil recovery (Hashemi et al 2014a, b, c;Galarraga and Pereira-Almao 2010;Hashemi et al 2012;Franco et al 2013aFranco et al , b, 2014Hosseinpour et al 2014). …”

Section: Introductionmentioning

confidence: 99%

Kinetics and mechanisms of the catalytic thermal cracking of asphaltenes adsorbed on supported nanoparticles

et al. 2016

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The production of heavy and extra-heavy oil is challenging because of the rheological properties that crude oil presents due to its high asphaltene content. The upgrading and recovery processes of these unconventional oils are typically water and energy intensive, which makes such processes costly and environmentally unfriendly. Nanoparticle catalysts could be used to enhance the upgrading and recovery of heavy oil under both in situ and ex situ conditions. In this study, the effect of the Ni-Pd nanocatalysts supported on fumed silica nanoparticles on post-adsorption catalytic thermal cracking of n-C 7 asphaltenes was investigated using a thermogravimetric analyzer coupled with FTIR. The performance of catalytic thermal cracking of n-C 7 asphaltenes in the presence of NiO and PdO supported on fumed silica nanoparticles was better than on the fumed silica support alone. For a fixed amount of adsorbed n-C 7 asphaltenes (0.2 mg/m 2 ), bimetallic nanoparticles showed better catalytic behavior than monometallic nanoparticles, confirming their synergistic effects. The corrected OzawaFlynn-Wall equation (OFW) was used to estimate the effective activation energies of the catalytic process. The mechanism function, kinetic parameters, and transition state thermodynamic functions for the thermal cracking process of n-C 7 asphaltenes in the presence and absence of nanoparticles are investigated.

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Section: Introductionmentioning

confidence: 99%

Kinetics and mechanisms of the catalytic thermal cracking of asphaltenes adsorbed on supported nanoparticles

et al. 2016

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“…The challenges of packing the horizontal production well with pelleted catalyst and deactivation caused by coke and metal deposition could potentially be decreased by using ultradispersed, once-through nano-sized catalyst. Galarraga and Pereira-Almao [9] reported the use of a trimetallic (Ni-W-Mo) submicronic catalyst for dispersed upgrading at 380°C in a batch reactor, using a stirrer speed of 500 rpm, and a reaction time of 3-70 h. They found that the produced oil API gravity increased by 6.5°API and the extent of viscosity reduction was 99% relative to the Athabasca bitumen (API gravity 9.5 and viscosity 7680 mPa·s).…”

Section: Introductionmentioning

confidence: 99%

“…Moreover nano-sized catalysts have a high surface to volume ratio, low intraparticle mass transfer resistance and thus may be more resistant to deactivation than pelleted catalysts [9,11]. Ultrafine (micron) scale particles may also offer some of these advantages whilst being cheaper to produce, not requiring specialist preparation and easier to handle, for example not being absorbed easily through the skin.…”

Section: Introductionmentioning

confidence: 99%

Effect of cyclohexane as hydrogen-donor in ultradispersed catalytic upgrading of heavy oil

Hart

Lewis

White

et al. 2015

Fuel Processing Technology

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The incorporation of catalysts to enhance downhole upgrading in the Toe-to-Heel Air Injection (THAI) process is limited by deactivation due to coking arising from the cracking of heavy oil. This study aims to reduce the catalyst deactivation problems that can occur with upgrading of heavy oils. Ultradispersed catalyst particles could potentially replace pelleted catalysts which may be difficult to regenerate once deactivated during the THAI operation. The dispersed particles could potentially be applied once through, down-hole for in situ upgrading of heavy oil. The catalyst studied was finely crushed pelleted Ni-Mo/Al 2 O 3 catalyst (2.4 μm). The product distribution of liquid, coke and gas may be influenced by the presence of a suitable hydrogen source which promotes hydroconversion reactions rather than simple cracking. In order to improve liquid yield whilst suppressing coke formation, the effect of cyclohexane as hydrogen-donor solvent was studied in a stirred batch reactor (100 mL) at temperature 425°C, initial pressure 17.5 bar, agitation 500 rpm, and a short reaction time of 10 min. The use of cyclohexane was evaluated against that of hydrogen gas. The reaction under hydrogen atmosphere significantly reduced coke yield by 41.3% compared with a nitrogen environment under the same conditions. Also, the coke decreased by 6.2-45.4% as the cyclohexane:oil ratio increased from 0.01 to 0.08 (g·g −1 ) relative to 4.67 wt.% of coke observed without added cyclohexane in ultradispersed catalytic upgrading under nitrogen environment. As the cyclohexane:oil ratio increases, the produced oil API gravity and middle distillate fractions (200-343°C) increase whilst the viscosity decreases. An estimated 0.073 CH:oil ratio was found to suppress coke formation in a similar manner to upgrading under hydrogen atmosphere at the same conditions.

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“…Up to now, many homogeneously dispersed catalysts have been studied and developed, which could be formulated as water-soluble catalysts [13][14][15][16] and oil-soluble catalysts [17][18][19][20][21]. Homogeneously dispersed catalysts are metal compounds, and the metal is selected from elements of group IV B-VIII among which the molybdenum, nickel, cobalt and chromium are commonly used [22][23][24][25]. The homogeneously dispersed catalyst and feedstock oil were added into the reactor simultaneously, the catalyst was actually a precursor which could be converted to the active metal sulfides through a sulfuration reaction.…”

Section: Introductionmentioning

confidence: 99%

Slurry-phase hydrocracking of heavy oil and model reactant: effect of dispersed Mo catalyst

Ren

et al. 2015

Appl Petrochem Res

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Thermal hydrocracking and catalytic hydrocracking of heavy oil and model reactant have been carried out to investigate the effect of dispersed Mo catalyst on slurry-phase hydrocracking. The XRD and XPS patterns suggested that the major existence form of dispersed Mo catalyst in slurry-phase hydrocracking was MoS 2 . Experimental data revealed that the conversion of feedstock oils and model reactant increased with the presence of catalyst, while the yields of light products (gas, naphtha) and heavy products (vacuum residue, coke) decreased, the yields of diesel and vacuum gas oil increased in the meantime. Besides, the yields of aromatic hydrocarbon and naphthenic hydrocarbon in naphtha fraction decreased. Effect parameters R G (the ratio of i-C 4 H 10 yield to n-C 4 H 10 yield) and isoparaffin/n-paraffin ratio were proposed to study the reaction mechanism of slurry-phase hydrocracking, the smaller effect parameters showed that there was no carbonium ion mechanism in slurry-phase hydrocracking, which still followed the free radical mechanism, and that the isomerization ratio of products decreased with the presence of Mo catalyst.

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Hydrocracking of Athabasca Bitumen Using Submicronic Multimetallic Catalysts at Near In-Reservoir Conditions

Cited by 98 publications

References 24 publications

Kinetics and mechanisms of the catalytic thermal cracking of asphaltenes adsorbed on supported nanoparticles

Kinetics and mechanisms of the catalytic thermal cracking of asphaltenes adsorbed on supported nanoparticles

Effect of cyclohexane as hydrogen-donor in ultradispersed catalytic upgrading of heavy oil

Slurry-phase hydrocracking of heavy oil and model reactant: effect of dispersed Mo catalyst

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