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3.1.5 Preparation of sand for the reactor Fine river sand was used for the experiments. The sand, obtained from a local merchant, was a slight shade of pink. The colour of the sand indicated the presence of potassium felspar. It was not expected that this would influence the experiments as no differentiation is recorded in the literature between sodium, potassium and calcium felspars on pyrolytic reactions. Approximately 1.5kg of sand was sieved through a 500 μm stainless steel mesh to remove particles that were too large. In order to destroy any organic material, the fine fraction was placed in a cylindrical stainless steel vessel and placed in the furnace for 2 hours at 600 o C. Upon cooling, the sand was manually sieved into the desired fractions. 3.2 Description of the bench scale pyrolysis unit hardware A series of fast pyrolysis experiments were conducted on a bench scale apparatus. The apparatus was based on the fluidised bed method of heat transfer. Heating rates of greater than 500 o C/second have been claimed for this method 31 . The objective of the experiments was to determine the effect of certain operational parameters and feedstock properties on the pyrolysis of lignocellulose, primarily with respect to the yield of monomeric phenolic compounds and furfuryls. 3.2.1 Major components of the fast pyrolysis unit Reactor and furnace The reactor was manufactured by RTI Ltd, a Canadian company that specialises in the production of small-scale pyrolysis apparatus. The reactor was manufactured from 316 grade stainless steel and was equipped with a type K thermocouple that enabled the temperature of the sand bed to be continuously monitored. At normal operating conditions (450-600 o C), the reactor can process up to 100g of feed material per hour. A cyclone was permanently attached to the outlet of the reactor in order to separate entrained char from the product gases. The char was collected in a vessel attached to the base of the cyclone. A diagram of the reactor is displayed in Figure 3.2.1.1. A 3.6 kW furnace, manufactured by Ceramic Engineering, was used to heat the reactor to the reaction temperatures. The furnace chamber was cylindrical in shape and was approximately 600mm in length and 100mm in diameter. The temperature of the furnace was controlled by a Eurotherm controller. A separate Eurotherm controller was used to monitor the reactor temperature. If the reactor temperature exceeded, or approached too rapidly, a preset value, the furnace elements were either switched off or the power was reduced. Feeder system A feeder was manufactured by RTI limited and was capable of delivering a steady stream of entrained feedstock particles into the reactor sand bed. The feeder consisted of a cylindrical Perspex vessel, approximately 200mm in length and 60mm in diameter, which served as a hopper. A 2mm I.D stainless steel tube, referred to as the entrainment tube, is positioned diametrically through the feeder and close to the base. A stream of gas, referred to as the feeder gas, is passed through this tube. A small hole, the size and orientation of which is dependent on the particle size and type of feedstock to be processed, is positioned midway between the inlet end and centre of the tube. For the present study, a hole of 1mm diameter was employed and was orientated downwards. A downward orientation permits a lower feed rate compared with an upward or sideways orientation. 16
Feedstock inlet line Attach to Stirrer Cooling gas outlet Cooling gas inlet Top section Temperature probe To Quench system Feeder Gas Inlets Stirring Mechanism Bottom section Aperture for Sample Cyclone Reactor To Reactor Char pot B. Feeder system Base plate Carrier gas inlet A. Fluidised bed reactor To electrostatic precipitator C. Solid residue collector Solids trap Quench fluid Inlet from reactor D. Quench system Mesh Desiccant Inlet nozzle Cotton wool F. Moisture trap E. Electrostatic precipitator Figure 3.2.1.1. Main components of the bench scale fast pyrolysis system 17
Page 1: Thermochemical Processing of Agrofo
Page 4 and 5: © 2006 Rural Industries Research a
Page 6 and 7: Table of contents 1 2 3 4 5 6 7 8 9
Page 8 and 9: 5.4.2.2 5.4.2.3 5.5.1 5.5.2 5.6.1 5
Page 10 and 11: 4.4.4.1 5.1.1 5.2.1 5.3.1 5.4.1.1 5
Page 12 and 13: Executive summary What the report i
Page 14 and 15: Under the conditions that resulted
Page 16 and 17: net increase of 28% compared to sim
Page 18 and 19: Due to the sensitivity of the pyrol
Page 20 and 21: It has been found that the composit
Page 22 and 23: carbon dioxide, carbon monoxide 9,1
Page 24 and 25: TGA studies have revealed that hemi
Page 26 and 27: There is a large project in Western
Page 28 and 29: The 1,8-cineole content of Eucalypt
Page 30 and 31: Chapter 2: Objectives The overall a
Page 34 and 35: A mechanical stirrer, the purpose o
Page 36 and 37: A separate needle valve was employe
Page 38 and 39: Product collection train assembly T
Page 40 and 41: In the current study, a DB-1701 col
Page 42 and 43: to the chromatographic method (cons
Page 44 and 45: The ethylenediamine to cupric ion r
Page 46 and 47: Table 3.6.2. Experimental design fo
Page 48 and 49: Modification 2: recovery of Eucalyp
Page 50 and 51: 4.1.2 Identification by comparison
Page 52 and 53: Table 4.1.4.1. Summary of lignin de
Page 54 and 55: The retention times of the compound
Page 56 and 57: treatment. The balance of the water
Page 58 and 59: 4.4.2 Holocellulose determination b
Page 60 and 61: 4.4.4 Analysis of the properties of
Page 62 and 63: 1. Survey the influence of various
Page 64 and 65: of the material converted to volati
Page 66 and 67: The selectivity of the process towa
Page 68 and 69: The effect of fluid bed mass on the
Page 70 and 71: Table 5.4.2.1. Comparison of cellul
Page 72 and 73: 1.2. The parameter values employed
Page 74 and 75: Chapter 6: Influence of selected op
Page 76 and 77: Yield (%m/m) 6 5 4 3 2 1 0 Figure 6
Page 78 and 79: The proportion of feed converted to
Page 80 and 81: Chapter 7: Optimisation of essentia
Page 82 and 83:
The very large improvement in cineo
Page 84 and 85:
A schematic diagram of each of the
Page 86 and 87:
14 17 19 11 12 9 13 15 16 10 1. Gla
Page 88 and 89:
8.2 Evaluation of the fast pyrolysi
Page 90 and 91:
Table 8.2.1.3. Yield of solid resid
Page 92 and 93:
Table 8.2.2.3. Yield of solid resid
Page 94 and 95:
The influence of carrier gas flow r
Page 96 and 97:
Chapter 9. Assessment of any health
Page 98 and 99:
Table 9.1.2. Toxicity information o
Page 100 and 101:
3.0 Synonyms Bio-oil, pyrolysis liq
Page 102 and 103:
• Vapour is irritating to the eye
Page 104 and 105:
1-tridecene 2,6,10,14-tetramethylpe
Page 106 and 107:
Chapter 11: Market analysis This ch
Page 108 and 109:
Table 11.1.2.1. World production of
Page 110 and 111:
11.2.3 World consumption of furfury
Page 112 and 113:
11.3.2 Guaiacol There is relatively
Page 114 and 115:
Current applications of isoeugenol
Page 116 and 117:
will involve passivation by a proce
Page 118 and 119:
produces around 14 billion litres/a
Page 120 and 121:
Appendix 1. Mass balances associate
Page 122 and 123:
Appendix 2. Mass balances associate
Page 124 and 125:
Appendix 3: Quantification data for
Page 126 and 127:
Phenol Trial 1.1 Trial 1.2A Trial 1
Page 128 and 129:
Isoeugenol Trial 1.1 Trial 1.2A Tri
Page 130 and 131:
Syringol Trial 1.1 Trial 1.2A Trial
Page 132 and 133:
Furfural Trial 1.1 Trial 1.2A Trial
Page 134 and 135:
Furfural methyl acetal Trial 1.1 Tr
Page 136 and 137:
Retention Time 15.177 15.667 18.246
Page 138 and 139:
Retention Time 15.177 15.667 18.246
Page 140 and 141:
Retention Time 15.177 15.667 18.246
Page 142 and 143:
Retention Time 15.177 15.667 18.246
Page 144 and 145:
Retention Time 15.177 15.667 18.246
Page 146 and 147:
130 Standardised Peak Area Retentio
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Retention Time 3.205 3.268 3.989 4.
Page 150 and 151:
Retention Time 3.205 3.268 3.989 4.
Page 152 and 153:
Retention Time 3.205 3.268 3.989 4.
Page 154 and 155:
Retention Time 3.205 3.268 3.989 4.
Page 156 and 157:
Page 158 and 159:
Page 160 and 161:
Sample Steam Extract 1 Ethanol Extr
Page 162 and 163:
Sample Steam Extract 1 Ethanol Extr
Page 164 and 165:
15. Klein, M.T. and P. Virk. 1981.
Page 166 and 167:
45. Vuori, A. 1986. Pyrolysis Studi
Page 168 and 169:
78. Faix. O., I. Fortmann, J. Breme
Page 170 and 171:
112. Kurth, E.F., and G.J. Ritter.
Page 172:
Thermochemical Processing of Agrofo
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