Catalytic Cracking of Light Crude Oil: Effect of Feed Mixing with Liquid Hydrocarbon Fractions

Usman, Abdulhafiz; Aitani, Abdullah M.

doi:10.1021/acs.energyfuels.7b02324

Cited by 24 publications

(17 citation statements)

References 30 publications

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“…It increased with the increase in temperature, reaching a maximum of 4.9 wt % at 650 °C, which agrees with literature reports. 15,16,31,32,33 M-cat showed a lower coke yield than E-cat (1.7 wt % at 650 °C). Thermal cracking resulted in the lowest coke yield.…”

Section: Methodsmentioning

confidence: 95%

Conversion of Arabian Light Crude Oil to Light Olefins via Catalytic and Thermal Cracking

Al-Absi

Al-Khattaf

2018

Energy Fuels

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The thermal and catalytic cracking of Arabian Light crude oil, which has a density of 34° API, were evaluated in a fixed-bed microactivity test (MAT) unit between 550 and 650 °C. For the catalytic cracking, two catalysts were used, a steamed commercial MFI catalyst (M-cat) and an equilibrium FCC catalyst (E-cat). Thermal and catalytic cracking were compared at the same conversion, 34%, at 650 °C. For both, as the temperature increased, the yields of light olefins, LPG, dry gas, and coke increased, associated with a consistent decrease in heavy ends (LCO and HCO). The naphtha yield for catalytic cracking decreased as temperature increased; however, for thermal cracking, it was nearly constant. The superiority of catalytic cracking over thermal cracking for the propylene yield was interpreted in terms of mechanisms of free radicals and carbenium ions. Thermal cracking gave a higher yield of ethylene. At high temperature (650 °C) and catalyst to oil (C/O) ratio of 4, the olefins yield decreased in the order of M-cat (32.7 wt %) > E-cat (30.3 wt %) > thermal cracking (22.8 wt %). The highest yields of ethylene and propylene (10.9 and 15.7 wt %), achieved over M-cat at 650 °C, are attributed to shape selectivity and higher acidity. The naphtha yield for E-cat was much higher than for M-cat; for instance, at 550 °C it was 48.3 wt % for E-cat and 24.4 wt % for M-cat. This was attributed to diffusion limitations for M-cat. The effect of the C/O ratio on conversion and yields was also inspected, and the analysis showed that after a C/O ratio of 4, further increases had only a minor effect. Lastly, the effect of mixing E-cat and M-cat at different percentages was evaluated, and the investigation showed an optimum point at 58% M-cat, with the corresponding yields of ethylene and propylene at 10.7 and 19.2 wt %, respectively.

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Section: Methodsmentioning

confidence: 95%

Conversion of Arabian Light Crude Oil to Light Olefins via Catalytic and Thermal Cracking

Al-Absi

Al-Khattaf

2018

Energy Fuels

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“…The catalytic cracking performance of LCO was investigated by Abdulhafiz, who found a poor cracking performance of LCO with an approximately 20 wt % yield of gasoline product. 17 Obviously, the cracking activity of LCO is lower than the conventional feed. LCO has abundant aromatic hydrocarbons with the high adsorptive ability, which are difficult to convert but tend to condense to form coke.…”

Section: Introductionmentioning

confidence: 99%

“…In order to adapt to the changes in market needs, processing LCO into gasoline products is considered a better choice. The catalytic cracking performance of LCO was investigated by Abdulhafiz, who found a poor cracking performance of LCO with an approximately 20 wt % yield of gasoline product . Obviously, the cracking activity of LCO is lower than the conventional feed.…”

Section: Introductionmentioning

confidence: 99%

Efficient Conversion of Light Cycle Oil into Gasoline with a Combined Hydrogenation and Catalytic Cracking Process: Effect of Pre-distillation

Miao

Guo

et al. 2020

Energy Fuels

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The combined hydrogenation and catalytic cracking (HCC) process is reported to be able to convert inferior light cycle oil (LCO) into high-quality gasoline efficiently. However, when the LCO rich in tricyclic aromatic hydrocarbons (TAHs) is used as feedstock, a high hydrogenation severity is required to saturate the aromatic rings and abundant gaseous hydrocarbons are generated during the following catalytic cracking process, thereby reducing the gasoline yield and its quality. In this work, the LCO was distilled into light, middle, and heavy fractions, which were rich in mononuclear aromatic hydrocarbons (MAHs), bicyclic aromatic hydrocarbons (BAHs), and TAHs, respectively. Based on the systematic analysis of compositions of hydrogenated LCO fractions and their catalytic cracking products, the optimal hydrogenation severities for each fraction to achieve the maximum gasoline production were determined. A novel combined process of selective hydrogenation and catalytic cracking based on predistillation (SHCC-PD) was further proposed. In the SHCC-PD process, LCO was primarily distilled and selectively hydrogenated, thereby delivering an improved catalytic cracking performance with an LCO conversion of ∼66 wt % and selectivity of high-quality gasoline of ∼72 wt %.

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“…FCC is a key operation for converting heavy oil to light products in refineries, and vacuum gas oil (VGO) is the conventional feedstock of FCC units. However, many researchers have attempted to process crude oil by a catalytic cracking method to obtain light products (e.g., light olefins, naphtha). − In addition, FCC has been successfully employed to process high-acid crude oils in China. , Tian et al proposed a new FCC technology to process high-acid crude oil. The high-acid crude oil is injected into a riser at 200 °C to react over a regenerated catalyst at a high temperature.…”

Section: Introductionmentioning

confidence: 99%

Conceptual Coupled Process for Catalytic Cracking of High-Acid Crude Oil

Liu

Chen

et al. 2019

Ind. Eng. Chem. Res.

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To process high-acid crude oil by catalytic cracking technology, a coupled process (FCD–FCC) involving fluid catalytic deacidification (FCD) of high-acid crude oil over a spent catalyst and fluid catalytic cracking (FCC) of heavy oil over a regenerated catalyst was proposed. Experiments were carried out in a confined fluidized bed reactor to test the feasibility of this process. The results indicate that the spent catalyst can be used for deacidification of high-acid crude oil to restrain the overcracking of light fractions. The optimal reaction conditions for the catalytic deacidification of Dar acidic crude oil are a temperature of 460 °C, a catalyst-to-oil ratio of 5, and a spent catalyst with a coke content of 1.26 wt %. Compared with the direct catalytic cracking of Dar crude oil over a regenerated catalyst, the yields of light oil and desired product increased by 6.10 and 6.78 wt % in the FCD–FCC process, respectively, and the olefin content of naphtha decreased by approximately 16 wt %, although the naphtha yield was lowered by 2.9 wt %. This strategy sheds new light on the processing of high-acid crude oil.

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Catalytic Cracking of Light Crude Oil: Effect of Feed Mixing with Liquid Hydrocarbon Fractions

Cited by 24 publications

References 30 publications

Conversion of Arabian Light Crude Oil to Light Olefins via Catalytic and Thermal Cracking

Conversion of Arabian Light Crude Oil to Light Olefins via Catalytic and Thermal Cracking

Efficient Conversion of Light Cycle Oil into Gasoline with a Combined Hydrogenation and Catalytic Cracking Process: Effect of Pre-distillation

Conceptual Coupled Process for Catalytic Cracking of High-Acid Crude Oil

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