A review of recent advances in catalytic hydrocracking of heavy residues

Sahu, Rabindra Kumar; Song, Byung Jin; Im, Ji Sun; Jeon, Young Pyo; Lee, Chul Wee

doi:10.1016/j.jiec.2015.01.011

Cited by 235 publications

(230 citation statements)

References 88 publications

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“…Stirred tank reactors have been widely used for the purpose of investigating the effect of dispersed nanocatalysts on hydroconversion of heavy oil 31,32 . The stirring speed used was in line with the guidelines reported in the literature to ensure suspension and adequate dispersion of the particles in the oil during reaction [33][34][35] . Table 1 shows the effect of particle size on the extent of upgrading for experiments carried out with unsupported Fe 2 O 3 particles.…”

Section: Effect Of Catalyst Size On Heavy Oil Upgradingmentioning

confidence: 99%

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Effectiveness of Different Transition Metal Dispersed Catalysts for In Situ Heavy Oil Upgrading

Al-Marshed

Hart

Leeke

et al. 2015

Ind. Eng. Chem. Res.

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Ultradispersed particles of size less than 100 nm for in situ catalytic upgrading have been reported to outperform the augmented catalytic upgrading achieved by incorporating pelleted refinery catalyst to the horizontal production well of the THAI process. Hydroconversion of heavy oil was carried out in a stirred batch reactor at 425˚C, 50 bar (initial H 2 pressure), 900 rpm and 60 min reaction time using a range of unsupported transition metal (Mo, Ni and Fe) catalysts. The effect of metal nanoparticles (NPs) was evaluated in terms of product distribution, physical properties and product quality. The produced coke and recovered catalysts were also studied. The levels of API gravity and viscosity of the upgraded oils observed with the NPs was approximately 21˚API and 108 cP compared with thermal cracking alone (24˚API and 53.5 cP), this moderate upgrade with NPs is due to the lack of cracking functionality offered by supports such as zeolite, alumina or silica. However, it was found that the presence of dispersed NPs significantly suppressed coke formation 4.4 wt% (MoS 2 ), 5.7 wt% (NiO) and 6.8 wt% (Fe 2 O 3 ) compared to 12 wt% obtained with thermal cracking alone. The results also showed that with dispersed unsupported metal NPs in sulfide form the middle distillate (177-343 ˚C) of the upgraded oil was improved particularly MoS 2 which gave 50 wt% relative to 43 wt% (thermal cracking) and 28 wt% (feed oil). The middle distillate yields for Fe 2 O 3 and NiO are 47 wt% and 49 wt%, respectively. Hence, iron and nickel-based unsupported NPs showed similar activity when compared to MoS 2 . The cost and availability of iron-based catalysts compared to Ni and Mo counterpart for heavy oil upgrading are advantages that may justify its preference.Furthermore, the X-ray diffraction (XRD) and scanning electron microscopy (SEM) analysis showed that introducing dispersed catalysts to the upgrading helped to produce sponge-type coke which could be used as industrial fuel compared to shot-type obtained upon thermal cracking.

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Section: Effect Of Catalyst Size On Heavy Oil Upgradingmentioning

confidence: 99%

“…The HDS and HDM obtained was 35.1% and 65.4% respectively for NiO in comparison to 43.9% and 85.7 % for thermal upgrading. It has been reported that the breaking of the C-heteroatoms bond is mainly controlled by temperature 35,81 .…”

Section: Nickel-based Catalystsmentioning

confidence: 99%

Effectiveness of Different Transition Metal Dispersed Catalysts for In Situ Heavy Oil Upgrading

Al-Marshed

Hart

Leeke

et al. 2015

Ind. Eng. Chem. Res.

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“…Subsequently, emitted SO x reacts with water vapor and causes formation of acid rain, which is harmful to mammals and other living organisms [31][32][33]. Removal of H 2 S from a gas stream could be done by several methods, namely, adsorption onto a solid adsorbent, absorption using a liquid solution, and catalytic oxidation [34][35][36][37][38]. Adsorption by metal oxide sorbents is recognized as an energy-e cient technology for H 2 S removal.…”

Section: Introductionmentioning

confidence: 99%

H2S Removal Using ZnO/SBA-3: New Synthesis Route and Optimization of Process Parameters

2017

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Abstract. H 2 S is a major toxic compound that could be found in air, water, and fossil fuels and causes some bad e ects such as acidic rain and corrosion. In the present work, SBA-3 (Santa Barbara University no. 3) with three di erent weight percentages of ZnO, namely, 5%, 10%, and 15%, was synthesized via an in situ approach. All synthesized samples were characterized using atomic absorption spectrometry, X-Ray Di raction (XRD), nitrogen adsorption, and Transmission Electron Microscopy (TEM). The obtained results from XRD and nitrogen adsorption con rmed that all the samples almost retained their ordered structure after incorporation of ZnO nanoparticles within the mesopores of SBA-3. TEM images showed that ZnO nanoparticles were arranged along the direction of mesopores of SBA-3. Then, adsorption of H2S from a model gas was investigated. A three-factor Box-Behnken design with ve center points and one response was performed for the evaluation of e ect of three process parameters, namely, ZnO wt%, space velocity, and temperature, on the adsorption of H 2 S and a quadratic model (r 2 : 0.9185) was developed to navigate the design space. Temperature had the largest and space velocity had the lowest e ect on the breakthrough of H 2 S. The optimum breakthrough time (t bp ) was 588 min.

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“…However, due to rapid population growth, the consumption of fuels, energy, and petrochemical products has been increasing tremendously. Thus, new challenges for the petroleum refineries to upgrade heavy oils and residues are (1) to produce more middle distillate products [1][2][3], (2) high-quality transportation fuels, and (3) depletion of crude oil sources [4]. During the past three decades, hydrocracking has gained prominence in light petroleum refining processes [5].…”

Section: Introductionmentioning

confidence: 99%

Modification of USY zeolites with malic–nitric acid for hydrocracking

Qiao

Yang

et al. 2016

Appl Petrochem Res

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The modification of commercial ultra-stable Y zeolite using malic acid (MA) and nitric acid (NA) was investigated. A series of factors including the amount of MA and NA solutions, the pH of the solutions, the treatment time, and the reaction temperature were investigated and optimized. The pore structure, acid properties, and crystal structure of modified USY zeolite were characterized by N 2 -adsorption, temperature-programmed desorption of ammonia (NH 3 -TPD), pyridine adsorbed Fourier transform infrared spectroscopy, and X-ray diffraction techniques. The as-obtained sample under the optimum conditions presents an increased secondary pore volume up to 0.202 cm 3 g -1 , which accounts for 45.3 % of the total pore volume, and appropriate acid properties as well as good crystallinity. Furthermore, the USY zeolite modified with different methods was also investigated, indicating that malic-nitric combined acid is an effective modifier for USY zeolite. The modified USY zeolite was used as support to prepare hydrocracking catalysts. The 140-370°C middle distillate yield of the catalyst is 68.59 %, and middle distillate selectivity can reach up to 81.52 %. Compared with commercial catalyst, the yield and selectivity increased by 8.17 and 5.14 %, respectively.

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A review of recent advances in catalytic hydrocracking of heavy residues

Cited by 235 publications

References 88 publications

Effectiveness of Different Transition Metal Dispersed Catalysts for In Situ Heavy Oil Upgrading

Effectiveness of Different Transition Metal Dispersed Catalysts for In Situ Heavy Oil Upgrading

H2S Removal Using ZnO/SBA-3: New Synthesis Route and Optimization of Process Parameters

Modification of USY zeolites with malic–nitric acid for hydrocracking

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