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Frontiers of Chemical Science and Engineering

ISSN 2095-0179

ISSN 2095-0187(Online)

CN 11-5981/TQ

Postal Subscription Code 80-969

2018 Impact Factor: 2.809

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Front. Chem. Sci. Eng.    2015, Vol. 9 Issue (1) : 64-76    https://doi.org/10.1007/s11705-015-1504-8
RESEARCH ARTICLE
Co-hydrotreating light cycle oil-canola oil blends
Huali WANG,Hena FAROOQI,Jinwen CHEN()
Natural Resources Canada, CanmetENERGY-Devon, One Oil Patch Drive, Devon, AB T9G1A8, Canada
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Abstract

Canola oil and light cycle oil (LCO) blends were co-hydrotreated over a commercial hydrotreating catalyst (NiMo/Al2O3) to produce diesel fuel with a green diesel component. High hydrodeoxygenation, hydrodesulphurization and hydrodenitrogenation catalytic activities were achieved for all three feedstocks tested in the temperature range of 350–380 °C with a hydrogen pressure of 7 MPa and a gas/oil ratio of 800 nL/L. The hydrocracking conversion of the 360 °C+ materials in the feedstocks increased by 5% and 15% when 5 and 7.5 wt-% canola oil was added to the LCO, respectively. Compared to the pure LCO, the cetane index of the diesel product formed from hydrotreating the two canola oil-LCO blends increased by 2.5 and 4, respectively. Due to the higher hydrogen requirement to crack and deoxygenate the triglycerides contained in the canola oil, a higher hydrogen consumption was needed to hydrotreat the canola oil-LCO blends.
Keywords hydrotreating      co-hydrotreating      co-processing      canola oil      light cycle oil (LCO)     
Corresponding Author(s): Jinwen CHEN   
Issue Date: 07 April 2015
 Cite this article:   
Huali WANG,Hena FAROOQI,Jinwen CHEN. Co-hydrotreating light cycle oil-canola oil blends[J]. Front. Chem. Sci. Eng., 2015, 9(1): 64-76.
 URL:  
https://academic.hep.com.cn/fcse/EN/10.1007/s11705-015-1504-8
https://academic.hep.com.cn/fcse/EN/Y2015/V9/I1/64
Fig.1  Schematic diagram of the hydroprocessing pilot plant
Units Light cycle oil 5 wt-% Canola oil 7.5 wt-% Canola oil Canola oil
Density g/mL 0.9071 0.9082 0.9097 0.9237
Carbon wt-% 88.22 88.16 86.97 77.41
Hydrogen wt-% 11.43 11.44 11.46 11.76
Sulfur wt-% 0.782 0.721 0.633 0.021
Nitrogen wppm 326.9 320.2 316.8 192.7
Oxygen wt-% 0 0.26 0.48 8.31
Saturates wt-% 35.8 39.7 38.6 0.15
Aromatics wt-% 58.4 54.1 52.9 0.0
Polarsa) wt-% 0 6.2 8.5 99.75
Olefinsb) wt-% 5.8 - - -
SimDis
IBP °C 130.8 128.2 134.6 360.0
10 wt-% °C 221.0 222.4 223.0 541.2
30 wt-% °C 250.2 251.2 252.4 609.8
?50 wt-% °C 276.0 279.0 280.8 614.2
?70 wt-% °C 305.0 310.0 313.4 617.2
?90 wt-% °C 353.2 372.0 389.8 619.8
?FBP °C 478.2 608.0 611.6 715.6
Tab.1  Properties of the feedstocks
Fig.2  Hydrocracking conversion of 360 °C+ materials at different temperatures with different feedstocks
Fig.3  Gasoline yield at different temperatures with different feedstocks
Fig.4  Diesel yield at different temperatures with different feedstocks
Fig.5  Simulated distillation curves of the three feedstocks
Fig.6  Gasoline product quality at different temperatures with different feedstocks. (a) Olefin content in the gasoline product, (b) Aromatic content in the gasoline product, (c) Iso/normal paraffin ratio in the gasoline product, (d) Research octane number of the gasoline product, (e) Motor octane number of the gasoline product
Fig.7  Diesel product quality at different temperature with different feedstocks. (a) Saturates content in the diesel product, (b) Aromatic content in the diesel product, (c) Cetane index of the diesel product
Fig.8  Hydrogen (H2) consumption at different temperatures with different feedstocks. P= 880 psig, LHSV= 1.5 h-1 and H2/oil= 800 nL/L
Fig.9  HDS and HDN conversion at different temperatures with different feedstocks. (a) HDS conversion, (b) HDN conversion
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