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Luận án tiến sĩ Kỹ thuật hóa học: Catalytic hydrodeoxygenation of guaiacol and its application in bio-oil upgrading

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Cấu trúc

  • CHAPTER 1 INTRODUCTION (26)
    • 1.1 Back ground of study (26)
    • 1.2 Problem statement (28)
    • 1.3 Objective (30)
    • 1.4 Scope of Research (30)
    • 1.5 Thesis outline (32)
  • CHAPTER 2 LITERATURE REVIEW (34)
    • 2.1 Overview (34)
    • 2.2 Pyrolysis oil (35)
      • 2.2.1 Bio-oil production (35)
      • 2.2.2 Bio-oil properties (38)
    • 2.3 Upgrading of bio-oil (42)
      • 2.3.1 Zeolite cracking (43)
      • 2.3.2 Catalytic hydrodeoxygenation (HDO) (43)
        • 2.3.2.1 Catalyst in HDO (46)
        • 2.3.2.2 Reaction condition (47)
        • 2.3.2.3 HDO of actual oil in batch reactor (48)
        • 2.3.2.4 HDO of actual bio-oil in continuous flow reactor (49)
        • 2.3.2.5 HDO of guaiacol in continuous flow reactor (50)
    • 2.4 Catalyst deactivation and regeneration (54)
    • 2.5 HDO reactions pathway and mechanism (56)
    • 2.6 Research Gap (60)
  • CHAPTER 3 METHODOLOGY (63)
    • 3.1 Overall Research Project’s Methodology (63)
    • 3.2 Materials (64)
    • 3.3 Catalyst preparation (66)
      • 3.3.1 Monometallic Ni and Co catalysts (66)
      • 3.3.2 Bimetallic Pd-Me catalysts (Me = Co or Fe) (67)
    • 3.4 Characterization of catalyst (67)
    • 3.5 Products analysis (70)
    • 3.6 Catalytic HDO of model compound (71)
      • 3.6.1 Fixed-bed reactor (72)
      • 3.6.2 Catalytic HDO on Al-MCM-41 supported Ni and Co catalysts (73)
      • 3.6.3 Catalytic HDO on Al-MCM-41 supported Pd, Fe and Co catalysts (74)
    • 3.7 Kinetic study (76)
      • 3.7.1 Reaction rate equations (76)
      • 3.7.2 MATLAB modeling and optimization (78)
    • 3.8 Catalytic upgrading of lignin-derived bio-oil (79)
  • CHAPTER 4 RESULTS AND DISCUSSION (82)
    • 4.1 Catalyst characterization (82)
      • 4.1.1 Al-MCM-41 supported Ni and Co catalysts (82)
      • 4.1.2 Al-MCM-41 supported Pd-Co and Pd-Fe catalysts (89)
    • 4.2 Catalytic HDO of guaiacol (95)
      • 4.2.1 GC-FID calibration (95)
      • 4.2.2 Blank test for hydrotreatment of guaiacol (97)
      • 4.2.3 HDO of guaiacol over Ni and Co catalysts (98)
        • 4.2.3.1 Effect of metal sites (98)
        • 4.2.3.2 Effect of reaction conditions (99)
        • 4.2.3.3 Reaction pathway of HDO of guaiacol on Al-MCM-41 (105)
        • 4.2.3.4 Catalyst deactivation and regeneration (106)
      • 4.2.4 HDO of guaiacol over bimetallic Pd-Co and Pd-Fe catalysts (112)
        • 4.2.4.1 The synergistic effect of bimetallic in catalytic HDO (112)
        • 4.2.4.2 Catalyst regeneration (116)
    • 4.3 Kinetic and reaction pathway of catalytic HDO of guaiacol (124)
      • 4.3.1 Study on HDO of different feedstock (124)
      • 4.3.2 Kinetic study of HDO of guaiacol (128)
        • 4.3.2.1 Reaction networks (128)
        • 4.3.2.2 Kinetic model for bimetallic catalysts (130)
    • 4.4 Catalytic upgrading of lignin-derived bio-oil (137)
      • 4.4.1 Successive of pyrolysis and upgrading process (137)
      • 4.4.2 Bio-oil composition (140)
  • CHAPTER 5 CONCLUSION (144)
    • 5.1 Conclusions (144)
    • 5.2 Recommendations (146)
  • or 12 months storage while LP-280T and LP-330T keep one phase after 12 months (0)
    • C) Ni-Co/Al-MCM-41 (84)
      • 3.0 g. Upgrading conditions: T = 400 ºC, P = 1 bar, m Catalyst = 1.5 g, and H 2 flow = 90 mL/min (138)

Nội dung

INTRODUCTION

Back ground of study

Malaysia has tremendous biomass resources from agricultural sector such as oil palm, paddy, sugarcane and rubber trees [1, 2] Among them, biomass from oil palm plantation and mill has the main contribution, and this solid biomass is predicted to reach 85-110 million tons by 2020 [2] Nowadays, the biomass residues are utilized for steam and power generation at mills, fiber material, pellets and fertilizer [3, 4] However, a certain big portion of biomass residues is not fully utilized, raising waste treatment and environmental pollution issues [5, 6]

The lignocellulose biomass resource can be used not only as direct energy in combustion, but also as a more valuable fuel after conversion and upgrading process [7] Thermal conversion of biomass is one of the prominent technologies to produce bio-char, bio-oil and bio-gas [7] In comparison with torrefaction or gasification, pyrolysis is conducted at moderate temperature (400600 ºC) and in the absence of oxygen [8] The pyrolysis oil (bio-oil) product has significant advantages in storage, transport and ability to utilize as useful petrochemical and fuel [9] In Malaysia, pyrolysis oil can be produced from different biomass feedstock such as palm kernel shell (PKS) [10, 11], empty fruit bunch (EFB) [12, 13], rice husk [14, 15] and wood sawdust [16] Interestingly, BTG (the coordinator of the EMPYRO project) has already constructed a 2 t/h pyrolysis plan using EFB as the feedstock [17]

Bio-oil is considered a promising second-generation biofuel and has been used to generate heat and electricity, e.g in combustors or turbines or as a co-feed in heat and power production plants However, it is very difficult to directly utilize the pyrolysis

2 oil because of its higher water (1634 wt%) and oxygen contents (3257 wt%) than heavy fuel oil (0.1 wt% and

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