Efficient One-Stage Bio-Oil Upgrading over Sulfided Catalysts

Abstract

Efficient upgrading of fast pyrolysis bio-oils into products that can be easily integrated into existing refinery complexes remains to be a challenge particularly from the stability of a catalyst performance point of view. Several NiMo catalysts, mainly alumina-supported, were either prepared or acquired and used in hydrotreating of bio-oil from ablative fast pyrolysis of straw. The experiments were carried out in a fixed-bed reactor at 340 °C and 4 MPa and lasted for 80 h. Detailed monitoring of the key physicochemical properties allowed comparing the performance of the catalysts and assessing its changes with the time-on-stream (TOS). The quality of all products deteriorated with the increasing TOS evidencing gradual loss of performance. Nonetheless, the product quality over the best catalysts remained suitable for further refinery upgrading by coprocessing during the 80-h TOS. Distillation of a hydrotreated bio-oil into naphtha, gas oil, and atmospheric residue allowed obtaining further insights into oxygenates present and their distribution.

Upgrading of Hydrothermal Liquefaction Biocrudes from Mono- and Co-Liquefaction of Cow Manure and Wheat Straw Through Hydrotreating and Distillation

“…Cobalt-Molybdenum (CoMo) and Nickel-Molybdenum (NiMo) sulfided catalysts supported on alumina were identified as promising approaches for deoxygenation of these types of oil, and given their classic use in fossil refining processes for denitrogenation [12], these catalysts are until today the preferred choice for bio-oil upgrading via hydrotreatment. Since then, several reports have used similar catalysts for upgrading of HTL biocrudes in batch and continuous processing from algae [13][14][15][16][17][18], lignocellulosic materials [18,19], sewage sludge [18,20] and pyrolysis bio-oils [21][22][23][24][25]. While fast pyrolysis bio-oils have been reported to deactivate NiMo catalysts when processed via hydrotreating [23], recently, HTL biocrude hydrotreating using a two-stage catalyst bed of CoMo and NiMo with temperature gradient over the reactor was shown to have an extended lifetime for upgrading of wet waste biocrude up to 1500 h of steady-state operation [26].…”

Recent Advances in the Value Addition of Biomass‐Derived Levulinic Acid: A Review Focusing on its Chemical Reactivity Patterns

“…[18] However, the energy-intensive processes produce a rather complicated concoction of liquid or gaseous products that must be stabilized before using as fuel or segregated into individual components for further value addition as chemical intermediates. [19,20] The biotechnological route is very selective, works under ambient conditions, and scalable. However, these processes are relatively slow and require enzymes or live organisms; hence they mandate specific reaction conditions and must conform to strict regulatory guidelines.…”

“…Thermochemical processes such as pyrolysis and gasification of biomass are fast, biomass independent, and are relatively well‐documented technologies [18] . However, the energy‐intensive processes produce a rather complicated concoction of liquid or gaseous products that must be stabilized before using as fuel or segregated into individual components for further value addition as chemical intermediates [19,20] . The biotechnological route is very selective, works under ambient conditions, and scalable.…”

Hydrodeoxygenation of fatty acid methyl esters and simultaneous products isomerization over bimetallic Ni‐Co / SAPO ‐11 catalysts

“…[8][9][10][11] Therefore, hydrodeoxygenation (HDO) of FAMEs, involving hydrogenation and deoxygenation of FAMEs with hydrogen over catalysts to generate C 15-18 dieselrange hydrocarbons, has received a great attention in recent years, since the properties of the obtained hydrocarbons are similar to those of petro-diesel. 12,13 Conventional hydrodesulphurization (HDS) catalysts [14][15][16][17] (supported sulfided metal catalysts) and hydrogenation catalysts [18][19][20][21][22][23] (supported noble metal catalysts) have been commonly applied in the HDO process, and exhibit high activity for obtaining long-chain alkanes from FAMEs. Nevertheless, the sulfided metal catalysts undergo deactivation by oxidation of active sulfided phase during the HDO reaction and thus necessitate addition of sulfiding agent to maintain their catalytic activity, which will contaminate the final products by sulfur and increase the operation costs.…”