Reactivity of naphtha fractions for light olefins production

Akah, Aaron; Al-Ghrami, Musaed; Saeed, M.R.; Siddiqui, M. Abdul Bari

doi:10.1007/s40090-016-0106-8

Cited by 32 publications

(14 citation statements)

References 23 publications

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“…The optimized gas oil mass flow rate is 34.86 kg/s, which is a 32.7% decrease on the 51.8 kg/s of the base case simulation and corresponds to C/O of 5.48, an increase of C/O ratio of 0.04 compared with the C/O ratio of optimization case 1. This result, as in case 1, is consistent with the riser hydrodynamics where increase in C/O results in increase in the reaction temperature and yield of intermediate products [7,56]. There is 3.90 and 3.95% increase in the temperatures of the gas phase and catalyst, respectively.…”

Section: Model Validation and Parameter Estimation Resultssupporting

confidence: 86%

“…The optimized catalyst mass flow rate is 282.0 kg/s; it is a 47.72% increase on the 190.9 kg/s base case simulation. This increase produced results consistent with the riser hydrodynamics where increase in mass flow rate of catalyst can result in an increase in the reaction temperature and consequent yield of intermediate products [9,19,56]. There is 3.81 and 3.89% increase in the temperatures of the gas phase and catalyst, respectively, which in turn causes the increase in the yield of a difference of 5.26 wt% of dry gas from 1.55 wt% at C/O ratio of 3.69-6.81 wt% at C/O ratio of 5.44.…”

Section: Model Validation and Parameter Estimation Resultssupporting

confidence: 73%

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Maximization of propylene in an industrial FCC unit

2018

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The FCC riser cracks gas oil into useful fuels such as gasoline, diesel and some lighter products such as ethylene and propylene, which are major building blocks for the polyethylene and polypropylene production. The production objective of the riser is usually the maximization of gasoline and diesel, but it can also be to maximize propylene. The optimization and parameter estimation of a six-lumped catalytic cracking reaction of gas oil in FCC is carried out to maximize the yield of propylene using an optimisation framework developed in gPROMS software 5.0 by optimizing mass flow rates and temperatures of catalyst and gas oil. The optimal values of 290.8 kg/s mass flow rate of catalyst and 53.4 kg/s mass flow rate of gas oil were obtained as propylene yield is maximized to give 8.95 wt%. When compared with the base case simulation value of 4.59 wt% propylene yield, the maximized propylene yield is increased by 95%.

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Section: Model Validation and Parameter Estimation Resultssupporting

confidence: 86%

Section: Model Validation and Parameter Estimation Resultssupporting

confidence: 73%

Maximization of propylene in an industrial FCC unit

2018

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“…The low conversion of LP (1.2 wt %) can be attributed to the dilution of the feed by its high naphtha content (59.6 wt %), which is highly aromatic and has a low reactivity. 23 The highest product yield from LP cracking was naphtha at 40.0 wt %, followed by LCO (25.4 wt %) and HCO (14.5 wt %). It is worth mentioning that naphtha molecules in the LP fraction convert easier than LCO and HCO molecules, because of the ease of diffusion in the zeolite pores.…”

Section: Methodsmentioning

confidence: 92%

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

Usman

Aitani

2017

Energy Fuels

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The direct catalytic cracking of Arab Extra Light (AXL) crude oil was conducted in a microactivity test (MAT) unit at 550 °C, where product recycling was simulated by mixing feed and liquid products in varying proportions. The effect of AXL mixing with total liquid product (LP) or a mixture of light cycle oil (LCO) and heavy cycle oil (HCO) was investigated at various ratios to determine the dependence of light olefins yield on feed composition. It was observed that mixing the least amount of LP with AXL yielded ∼20.3 wt % light olefins and 39.6 wt % naphtha. The cracking of AXL and LCO+HCO yielded similar results as the case of cracking LP. A configuration of 100% recycle of liquid product without blending with AXL feed showed an increase in the yield of light olefins from 20 wt % to 29 wt % associated with a decrease in naphtha yield from 40 wt % to 27 wt %. A second configuration of 100% recycle of LCO+HCO without blending with AXL feed showed that the yield of light olefins increased from 20 wt % to 26 wt % associated with an increase in naphtha yield from 40 wt % to 50 wt %. The study has shown that the recycling of low-value heavy fraction (LCO+HCO) is a cost-effective means to supplement the AXL feed without loss in the yield of desired light olefins and naphtha.

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“…Figure 3 illustrates the significant variation of these quantities, dependent upon the catalyst support. CMR is defined by equation (4.1) and indicates whether the reaction is dominated by protolytic cracking or β-scission, facilitated by acid sites within the zeolite support [ 45 ]. When CMR > 1, this indicates that protolytic cracking is dominant in the final product selectivity.…”

Section: Discussionmentioning

confidence: 99%

Transition metal chalcogenide bifunctional catalysts for chemical recycling by plastic hydrocracking: a single-source precursor approach

et al. 2022

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Sulfided nickel, an established hydrocracking and hydrotreating catalyst for hydrocarbon refining, was synthesized on porous aluminosilicate supports for the hydrocracking of mixed polyolefin waste. Zeolite beta, zeolite 13X, MCM41 and an amorphous silica-alumina catalyst support were impregnated with the single-source precursor (SSP) nickel (II) ethylxanthate for catalyst support screening. Application of this synthesis method to beta-supported nickel (Ni@Beta), as an alternative to wet impregnation using aqueous nickel (II) nitrate, provided catalytic materials with higher conversion to fluid products at the same mild batch reaction conditions of 330°C with appropriate agitation and 20 bar H 2 pressure. Mass balance quantification demonstrated that SSP-derived 5wt%Ni@Beta yielded a greater than 95 wt% conversion of a mixed polyolefin feed to fluid products, compared with 39.8 wt% conversion in the case of 5wt%Ni@Beta prepared by wet impregnation. Liquid and gas products were quantitatively analysed by gas chromatography–flame ionization detection (GC-FID) and gas chromatography–mass spectrometry (GC-MS), revealing a strong selectivity to saturated C 4 (37.3 wt%), C 5 (21.6 wt%) and C 6 (12.8 wt%) hydrocarbons in the case of the SSP-derived catalyst.

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Reactivity of naphtha fractions for light olefins production

Cited by 32 publications

References 23 publications

Maximization of propylene in an industrial FCC unit

Maximization of propylene in an industrial FCC unit

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

Transition metal chalcogenide bifunctional catalysts for chemical recycling by plastic hydrocracking: a single-source precursor approach

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