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ZSM5 catalysts
02 Liquid fuels (derived liquid fuels) differences and particle size distributions. It was confirmed by the simulation that removing a small amount of solids from the bottom of the first reactor was effective to achieve a long-term continuous operation without accumulation of coarse solid particles. 02/00208 About the impact of olefin reactions of FischerTropsch product distributions for high diesel yield Schulz, H., Claeys, M. Prepr. - Am. chemical Sot., Div. Per. chemical, 2000, 45, (2), 206-209.
Olefin secondary reactions strongly contribute to the final FischerTropsch product distribution. Particularly, high gas oil and wax yields, which are essential for high diesel fuel yields in an integrated process, are possible through I-olefin readsorption. 02lOO209 Acetone-butanol and water gas from the methanol-producing process starting from the bagasse left from ethanol and sugar production Audi, R. Braz. Pedido PI BR 97 06,136 (Cl. C12P7/28), 20 Jul 1999, Appl. 1997/6,136, 15 Dee 1997. 11. (In Portugese) The title process is carried out by diverting part of the xylose syrup used for the production of MeOH to a tank where it undergoes anaerobic fermentation by a microorganism such as Closrridium acetobulylicum to produce acetone (68%), BuOH (30%), and EtOH (2%), and by passing steam through an incandescent charcoal bed in which the C is partially oxidized to form water gas (CO + Hz), which is injected into the same reactor receiving synthesis gas from another fermentation. and reacted to form EtOH. yu;/i210
Activation
and recycling
of waste edible oils as
Toyama, K. Jpn. Kokai Tokkyo Koho JP 2000 119,685 (Cl. CllB13/00), 25 Apr 2000, Appl. 1998/297,855, 20 Ott 1998. 3. (In Japanese) Title process for recycling waste edible oils, which are mixed with light or lamp oil at a ratio of 220 wt% as fuels, comprises: (1) filtration to remove impurities, (2) mixing with water to dissolve and separate water-soluble substances, and (3) activation using ozone, oxygen, or air. 02/00211 Alkanol production reactor Maeda, T., Morita, H. Jpn. Kokai Tokkyo Koho JP 2000 166,584 (Cl. C12P7/04), 20 Jun 2000, Appl. 1998/349,157, 8 Dee 1998. 6. (In Japanese) Alkanol, especially methanol, is manufactured with alkane-utilizing bacteria or with enzyme preparation of the bacteria in a reactor which is supplied with methane. The methanol concentration is kept at 210 mM of that of the unit bacterial biomass in the reactor. Methanol is useful for manufacturing di-Me ether and liquefied petroleum gas. 02/00212 An apparatus and method for preparation of dimethyl ether from natural gas Okada, T., Mashiko, Y. Jpn. Kokai Tokkyo Koho JP 2000 169,411 (Cl. CO7C41/01), 20 Jun 2000, Appl. 1998/348,772, 8 Dee 1998. 5. (In Japanese) Di-Me ether is prepared by conversion of natural gas into synthesis gas (CO and H) and preparation of di-Me ether from the synthesis gas. This process is eqiipied with two means for recovering C6, instead of one in prior art method and suppresses release of CO* into the environment, excessive formation of hydrogen, and consumption of natural gas (raw material). An apparatus for preparation of di-Me ether comprises: (a) a means for removing sulphur components from natural gas which is later used as reforming raw material, (b) a steam reformer for reforming desulphurized natural gas (reforming raw material) to obtain reformed gas (synthesis gas) by burning it after mixing it with CO1 and steam, (c) a first means for recovering CO2 from the reformed gas, (d) a second means for recovering COz from the exhaust gas of the reformer which is missing in prior art method, and (e) feeding COz recovered from both the means to the reforming raw material. 02lOO213 Apparatus and method for use in the liquefaction of biomass containing polysaccharides Shiraishi, N. ef al. Jpn. Kokai Tokkyo Koho JP 2000 103,864 (Cl. CO8H5/00), 11 Apr 2000, JP Appl. 1998/212,806, 28 Jul 1998. 23. (In Japanese) The method uses a tandem-type apparatus comprising a first twinescrew extruder having means for carrying out the reaction, kneading and devolatilizing, and a second extruder having means for devolatilizing and cooling where the crushed biomass materials prepared in a crushing and transporting part are mixed with a solvent which has been forcedly injected into the first extruder with an acid catalyst. The mixture in the first extruder is then neutralized, and devolatilized in vacua to remove excess solvent while the resulting liquefied products is forwarded to the second extruder where it is devolatilized and cooled to give a liquid.
22
Fuel and Energy
Abstracts
January 2002
02lOO214 Co-coking of coal and petroleum resid mixtures for production of coal-based jet fuel Fickinger, A.E. et al. Prepr. Symp. -Am. Chem. Sot.. Div. Fuel Chem., 2000, 45, (2), 299-303.
Coal was incorporated into a simulated delayed coking process. The intent of the co-coking process was to obtain liquid products of coalderived structures which would produce a product with higher thermal stability than petroleum-based fuels. The work presented here focuses on the effects of different feed ratios and reaction length effects for various co-coking reactions. 02lOO215 Co-liquefaction of coal and biomass in supercritical water using a batch reactor Yokura, H., Matsumura, Y. Sekitan Kagaku Kaigi Happy0 Ronbunshu, 1998, 35th, 63-66. (In Japanese) Co-liquefaction of coal and biomass in supercritical water using a batch reactor was conducted at 400”, 25 MPa. The result shows larger amount of generation of volatile liquefied products compared with the semibatch operation. Effective recovery and utilization of these water soluble products are wanted. 02/00218 Coal liquefaction at early stage through a single reactor operation of the NED01 process. A 1 t/d process supporting unit (PSU) Ikeda, K. et al. Sekiran Kagaku Kaigi Happy0 Ronbunshu, 1998, 35th, 221-224. (In Japanese) A single reactor operation test of the PSU has been conducted using only one of the three reactors in series to investigate the behaviour of coal liquefaction at early stage of the process. At this stage, the oil yield was already more than 50 wt% with the residue yield as small as 20 wt% on daf coal basis. 02lOO217 Compact reformers in gas conversion Linthwaite, M., Gamlin, T. Hydrocarbon Eng., 2000, 5, (5), 67-69. The future for the compact reformer is very positive, with the impending requirement for gas conversion to liquid fuels, particularly in the areas of: methanol, gas to liquids (FT), hydrogen. The areas of initial implementation include methanol based fuel cell vehicles and the need for associated gas processing offshore. 02/00218 Comparison of the thermal stability of coalderived jet fuels in the autoxidative and pyrolytic regimes under batch and flow conditions Andresen, J.M. et al. Prepr. Symp. - Am. Chem. Sot., Div. Fuel Chem., 2000, 45, (2), 304-308.
The thermal stability of coal- and petroleum-derived jet fuels and the associated model compounds decahydronaphthalene and n-tetradecane, as they go through the autoxidative and pyrolytic regime both under batch and flow conditions, was studied. Under batch reactor conditions, the decahydronaphthalene showed excellent thermal stability up to 5Oo”C, whereas the n-tetradecane started its cracking process at around 450°C. Flow reactor studies mirrored the thermal decomposition of the model compounds, although the cracking appeared at higher bulk fuel temperatures. The thermal behaviour of the experimental. jet fuels also confirmed that the paraffinic proportion of the fuels is the main reason for thermal fuel degradation. 02/00219 Composition and quality of the gasoline obtained from syngas on Cr203-ZnO/ZSM5 catalysts Arandes, J.M. et al. Chem. Eng. Commun., 1999, 174, l-19. The kinetic equations for the formation of the lumps of the gasoline produced (C, fraction), paraffins (C,-C,), xylenes (o-xylene, m-xylene and p-xylene) and aromatics (benzene, toluene, C9-Cl,) in the transformation of syngas on Crz03-ZnO/ZSMS bifunctional catalyst have been established as a function of the concentration of both reactants (CO and Hz) and COz byproduct. The effect of the operating conditions on the RON and on the molecular weight of the gasoline has been studied by experimentation in an integral fixed bed reactor in the range between 10 and 50 atm and between 300 and 425°C. The octane index increases with Cr/Zn atomic ratio of the Crz03-ZnO metallic function, with Si/Al ratio of the HZSM5 zeolite, with space time and with the CO/Hz molar ratio in the feed, in that order, whereas it passes through a maximum with pressure (at 20 atm) and with temperature (at 375°C). On the other hand, the molecular weight of the gasoline increases with the Cr/Zn atomic ratio, pressure, CO2 molar ratio and space time, and decreases with the Si/AI ratio and temperature. 02lOO220 Conversion of organic wastes via biogas to methanol Fechner, W., Kotowski, W. Gospod. Paliwami Energy., 1998, 46, (6), 19-2 1. (In Polish)
Olefin secondary reactions strongly contribute to the final FischerTropsch product distribution. Particularly, high gas oil and wax yields, which are essential for high diesel fuel yields in an integrated process, are possible through I-olefin readsorption. 02lOO209 Acetone-butanol and water gas from the methanol-producing process starting from the bagasse left from ethanol and sugar production Audi, R. Braz. Pedido PI BR 97 06,136 (Cl. C12P7/28), 20 Jul 1999, Appl. 1997/6,136, 15 Dee 1997. 11. (In Portugese) The title process is carried out by diverting part of the xylose syrup used for the production of MeOH to a tank where it undergoes anaerobic fermentation by a microorganism such as Closrridium acetobulylicum to produce acetone (68%), BuOH (30%), and EtOH (2%), and by passing steam through an incandescent charcoal bed in which the C is partially oxidized to form water gas (CO + Hz), which is injected into the same reactor receiving synthesis gas from another fermentation. and reacted to form EtOH. yu;/i210
Activation
and recycling
of waste edible oils as
Toyama, K. Jpn. Kokai Tokkyo Koho JP 2000 119,685 (Cl. CllB13/00), 25 Apr 2000, Appl. 1998/297,855, 20 Ott 1998. 3. (In Japanese) Title process for recycling waste edible oils, which are mixed with light or lamp oil at a ratio of 220 wt% as fuels, comprises: (1) filtration to remove impurities, (2) mixing with water to dissolve and separate water-soluble substances, and (3) activation using ozone, oxygen, or air. 02/00211 Alkanol production reactor Maeda, T., Morita, H. Jpn. Kokai Tokkyo Koho JP 2000 166,584 (Cl. C12P7/04), 20 Jun 2000, Appl. 1998/349,157, 8 Dee 1998. 6. (In Japanese) Alkanol, especially methanol, is manufactured with alkane-utilizing bacteria or with enzyme preparation of the bacteria in a reactor which is supplied with methane. The methanol concentration is kept at 210 mM of that of the unit bacterial biomass in the reactor. Methanol is useful for manufacturing di-Me ether and liquefied petroleum gas. 02/00212 An apparatus and method for preparation of dimethyl ether from natural gas Okada, T., Mashiko, Y. Jpn. Kokai Tokkyo Koho JP 2000 169,411 (Cl. CO7C41/01), 20 Jun 2000, Appl. 1998/348,772, 8 Dee 1998. 5. (In Japanese) Di-Me ether is prepared by conversion of natural gas into synthesis gas (CO and H) and preparation of di-Me ether from the synthesis gas. This process is eqiipied with two means for recovering C6, instead of one in prior art method and suppresses release of CO* into the environment, excessive formation of hydrogen, and consumption of natural gas (raw material). An apparatus for preparation of di-Me ether comprises: (a) a means for removing sulphur components from natural gas which is later used as reforming raw material, (b) a steam reformer for reforming desulphurized natural gas (reforming raw material) to obtain reformed gas (synthesis gas) by burning it after mixing it with CO1 and steam, (c) a first means for recovering CO2 from the reformed gas, (d) a second means for recovering COz from the exhaust gas of the reformer which is missing in prior art method, and (e) feeding COz recovered from both the means to the reforming raw material. 02lOO213 Apparatus and method for use in the liquefaction of biomass containing polysaccharides Shiraishi, N. ef al. Jpn. Kokai Tokkyo Koho JP 2000 103,864 (Cl. CO8H5/00), 11 Apr 2000, JP Appl. 1998/212,806, 28 Jul 1998. 23. (In Japanese) The method uses a tandem-type apparatus comprising a first twinescrew extruder having means for carrying out the reaction, kneading and devolatilizing, and a second extruder having means for devolatilizing and cooling where the crushed biomass materials prepared in a crushing and transporting part are mixed with a solvent which has been forcedly injected into the first extruder with an acid catalyst. The mixture in the first extruder is then neutralized, and devolatilized in vacua to remove excess solvent while the resulting liquefied products is forwarded to the second extruder where it is devolatilized and cooled to give a liquid.
22
Fuel and Energy
Abstracts
January 2002
02lOO214 Co-coking of coal and petroleum resid mixtures for production of coal-based jet fuel Fickinger, A.E. et al. Prepr. Symp. -Am. Chem. Sot.. Div. Fuel Chem., 2000, 45, (2), 299-303.
Coal was incorporated into a simulated delayed coking process. The intent of the co-coking process was to obtain liquid products of coalderived structures which would produce a product with higher thermal stability than petroleum-based fuels. The work presented here focuses on the effects of different feed ratios and reaction length effects for various co-coking reactions. 02lOO215 Co-liquefaction of coal and biomass in supercritical water using a batch reactor Yokura, H., Matsumura, Y. Sekitan Kagaku Kaigi Happy0 Ronbunshu, 1998, 35th, 63-66. (In Japanese) Co-liquefaction of coal and biomass in supercritical water using a batch reactor was conducted at 400”, 25 MPa. The result shows larger amount of generation of volatile liquefied products compared with the semibatch operation. Effective recovery and utilization of these water soluble products are wanted. 02/00218 Coal liquefaction at early stage through a single reactor operation of the NED01 process. A 1 t/d process supporting unit (PSU) Ikeda, K. et al. Sekiran Kagaku Kaigi Happy0 Ronbunshu, 1998, 35th, 221-224. (In Japanese) A single reactor operation test of the PSU has been conducted using only one of the three reactors in series to investigate the behaviour of coal liquefaction at early stage of the process. At this stage, the oil yield was already more than 50 wt% with the residue yield as small as 20 wt% on daf coal basis. 02lOO217 Compact reformers in gas conversion Linthwaite, M., Gamlin, T. Hydrocarbon Eng., 2000, 5, (5), 67-69. The future for the compact reformer is very positive, with the impending requirement for gas conversion to liquid fuels, particularly in the areas of: methanol, gas to liquids (FT), hydrogen. The areas of initial implementation include methanol based fuel cell vehicles and the need for associated gas processing offshore. 02/00218 Comparison of the thermal stability of coalderived jet fuels in the autoxidative and pyrolytic regimes under batch and flow conditions Andresen, J.M. et al. Prepr. Symp. - Am. Chem. Sot., Div. Fuel Chem., 2000, 45, (2), 304-308.
The thermal stability of coal- and petroleum-derived jet fuels and the associated model compounds decahydronaphthalene and n-tetradecane, as they go through the autoxidative and pyrolytic regime both under batch and flow conditions, was studied. Under batch reactor conditions, the decahydronaphthalene showed excellent thermal stability up to 5Oo”C, whereas the n-tetradecane started its cracking process at around 450°C. Flow reactor studies mirrored the thermal decomposition of the model compounds, although the cracking appeared at higher bulk fuel temperatures. The thermal behaviour of the experimental. jet fuels also confirmed that the paraffinic proportion of the fuels is the main reason for thermal fuel degradation. 02/00219 Composition and quality of the gasoline obtained from syngas on Cr203-ZnO/ZSM5 catalysts Arandes, J.M. et al. Chem. Eng. Commun., 1999, 174, l-19. The kinetic equations for the formation of the lumps of the gasoline produced (C, fraction), paraffins (C,-C,), xylenes (o-xylene, m-xylene and p-xylene) and aromatics (benzene, toluene, C9-Cl,) in the transformation of syngas on Crz03-ZnO/ZSMS bifunctional catalyst have been established as a function of the concentration of both reactants (CO and Hz) and COz byproduct. The effect of the operating conditions on the RON and on the molecular weight of the gasoline has been studied by experimentation in an integral fixed bed reactor in the range between 10 and 50 atm and between 300 and 425°C. The octane index increases with Cr/Zn atomic ratio of the Crz03-ZnO metallic function, with Si/Al ratio of the HZSM5 zeolite, with space time and with the CO/Hz molar ratio in the feed, in that order, whereas it passes through a maximum with pressure (at 20 atm) and with temperature (at 375°C). On the other hand, the molecular weight of the gasoline increases with the Cr/Zn atomic ratio, pressure, CO2 molar ratio and space time, and decreases with the Si/AI ratio and temperature. 02lOO220 Conversion of organic wastes via biogas to methanol Fechner, W., Kotowski, W. Gospod. Paliwami Energy., 1998, 46, (6), 19-2 1. (In Polish)