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Fuel additive composition for heavy oils
02 Liquid fuels (transport, refining, quality, storage)
Transport,
refining,
quality,
storage
02/00176 Catalytic upgrading of pyrolytic oils over HZSM-5 zeolite: behaviour of the catalyst when used in repeated upgrading-regenerating cycles Vitolo, S. et al. Fuel, 2001, 80, (I), 17-26. The behaviour of HZSM-5 zeolite in the upgrading of a wood pyrolysis oil produced in the ENEL fast-pyrolysis plant located in Bastardo, Italy, was studied in repeated upgrading-regenerating cycles. The HZSM-5 zeolite performs a catalytic activity by its acidic sites that, through a carbonium ion mechanism, promote deoxygenation, decarboxylation and decarbonylation of the oil constituents, as well as cracking, oligomerization, alkylation, isomerization, cyclization and aromatization. As a consequence of the catalytic process, coke and tar were also obtained as undesirable by-products. The continued regeneration of the zeolite, consisting of removal of the coke deposits by air at 5OO”C, reduced the effectivenes,s of the catalyst in converting biomass pyrolysis oils to an aromatic product, until an irreversible deactivation was observed. By the analysis conducted on the catalyst it was possible to assess that the loss of activity is mainly connected to the disappearance of a significant amount of acidic sites, mainly the stronger ones, due to the thermal cycling to which the catalyst was submitted. Even if the regeneration was conducted at 5Oo”C, localized raisings of temperature above 500°C due to the combustion of coke may have caused dehydroxylation of the Bronsted acid sites that predominate in zeolites activated at 500°C with formation of Lewis acid sites. Thus, the active acid sites in the upgrading reactions are presumed to be preferentially Bronsted acid sites, which were gradually deactivated by the repeated regeneration treatments. 02/00177 Composite heavy oil combustion improvers and their preparation Wang, J. Faming Zhuanli Shenqing Gongkai Shuomingshu CN 1,222,561 (Cl. ClOL1/22), 14 Jul 1999, Appl. 98,100,111, 8 Jan 1998. 9. (In Chinese) A composite combustion improver for heavy oil is composed of rare earth nitrate or carbonate 5-20, Mg naphthenate 5-15, Fe naphthenate 4-10, Ca naphthenate 3-8, oil solvent 1-5, Mg stearate 1-5, Ba stearate 0.8-4.5, Ca stearate l-5, polyisobutenylsuccinimide 0.08-0.2, and solvent 50-70 wt. parts, preferably rare earth nitrate or carbonate 10.5, Mg naphthenate 7.2, Fe naphthenate 7.2, Ca naphthenate 6, oil solvent 3.2, Mg stearate 1.31, Ba stearate 1.5, Ca stearate 1, polyisobutenylsuccinimide 0.1, and solvent 61.99 wt. parts. The addition of the combustion improver in heavy oil is 0.2-0.5 wt.%. 02lOOl76 Conversion of hydrocarbon resources into hydrogen, gas oil, and water-soluble oil Chikazawa, T., Miyashita, Y. Jpn. Kokai Tokkyo Koho JP 2000 192,055 (Cl. ClOJ3/46), 11 Jul 2000, Appl. 1998/369,405, 25 Dee 1998. 5. (In Japanese) Hydrocarbon resources are treated in a first reactor at 380-500” and 25-40 MPa for primary decomposition of the resources into waterinsoluble oil and aqueous solution of water-soluble oil and then the primary decomposition residue and water is treated in the second reactor at 500-900” and 25-40 MPa for their conversion into H-based gas. The resources may be fossil fuel and organic waste, e.g. municipal waste, sludge. Hydrocarbon resources are converted into energy sources at high rate by a simple process. W2/;;;9
Desulfurization
of engine fuel on board a motor
Holder, E. er al. PCT Int. Appl. WO 00 20,531 (Cl. ClOG25/00), 13 Apr 2000, DE Appl. 19,845,397, 2 Ott 1998. 18. (In German) The invention relates to a method for desulphurizing engine fuel on board a motor vehicle by separating the constituents of the engine fuel containing S by using selective liquid-phase adsorption with the aid of an adsorbing material. 02/00160 Diesel oil emulsifying agent and method for preparation of emulsified diesel oil Liu, X. Faming Zhuanli Shenqing Gongkai Shuomingshu CN 1,215,747 (Cl. ClOG31/08), 5 May 1999, Appl. 97,119,930, 28 Ott 1997. 5. (In Chinese) The diesel oil emulsifying agent is composed of water 15-20, NaOH l3, kerosene 5-9, rosin 5-9, Tween-60 5-9, Span-80 40-49, Tween-20 48.and antirust agent (petroleum sodium suiphonate) IO-15 wt.%. The preparing method for the emulsifying agent comprises: mixing water, NaOH, kerosene, rosin at 90-100”; cooling to 40-50” and adding Tween-60, Span-SO, Tween-20 and antirust agent; and cooling to room temperature. The emulsified diesel oil is prepared by mixing diesel oil 60-90, water 10-40 and the emulsifying agent 0.05-2 wt.%.
02lOO161 Effect of the composition of synthesis gas on the preparation of hydrocarbons on a Co catalyst Krylova, A.Y. et al. Khim. Tverd. Topl. (Moscow), 2000, 1, 3-7. (In Russian) Fischer-Tropsch synthesis from non-stoichiometric Hz-CO gas mixtures in a three-stage-reactor, common-scale plant was studied. The increase in the H&O ratio from 4 to 10 resulted in a decrease in the production of liquid hydrocarbons at I and II stages, changing at the same time the fractional composition of the broad heavy fraction. The content of the fraction boiling 225-335°C increased from 35% to 48%.
02/00162 Experimental study on hydraulic characteristics with slurrv flowina in horizontal oinelines Xu, J.L. et il. Int. Co;f. Proc. Radioact: k’aste Manage. Environ. Rem., 7th. 1999. 1302-I 307. A flow loop, which contains a mixing tank, pump, horizontal pipeline, and corresponding measurement transducers, has been constructed at Florida International University’s Hemispheric Center for Environmental Technology (FIU-HCET). Six typical slurry simulants, of interest to DOE (Department of Energy) sites, were tested. New data were provided on the pressure gradient and volume concentrations across the vertical cross-section. Much attention was paid to the particle settling at lower flow velocity. An apparent transition point exists in the curve of pressure drop versus flow velocity. The velocity at which the limit transition point occurs is identified as the limit deposition velocity. At velocities greater than the limit deposition velocity, there is heterogeneous flow in the pipeline. Lower velocity than the limit deposition velocity will result in stationary bed flow. The present flow shows distinct characteristics with the classical sample slurries, such as coal-water or a sand-water system. A correlation is recommended to calculate the pressure drop.
02/00163 Fuel additive composition for heavy oils Kim, Y. er al. Faming Zhuanli Shenqing Gongkai Shuomingshu CN 1,207,404 (Cl. ClOL1/30), 10 Feb 1999, KR Appl. 9,731,528, 8 Jul 1997. 16. (In Chinese) The additive composition comprises a kerosene 260, a lower Cl-s alcohol 5-15, polybutylene 5-15, a polypropylene glycol for butylated hydroxytoluene) 2-10, and an organic Fe compound 0.5-5 wt.%. The organic Fe compound may be ferrocene or its derivatives such as acetylferrocene, benzoylferrocene, and ferrocene carboxy aldehyde.
02/00164 Kinetics of the thermal decomposition of oil shale from Puertollano (Spain) Torrente, M.C., Galan, M.A. Fuel, 2001, 80, (3) 327-334. The kinetics of the thermal decomposition of Spanish oil shale was studied using isothermal and non-isothermal thermogravimetric analyses (TGA). The isothermal TG data were studied at different particles sizes (0.250 x 10m3, 0.505 x lo-’ and 0.925 x 10-s m) and three temperature plateaux (703, 688 and 673 K). For the kinetic analysis, the Integral Method was used. The non-isothermal weight-loss data was analysed at different heating rates (5, 10, 15,20 and 50 K/min) up to 1173 K and for a particle size of 0.250 x lo-’ m. Three methods were applied for the determination of the kinetic parameters: the Direct Arrhenius Plot Method, the Integral Method and the Differential Method. From an engineering point of view, the rate of the thermal decomposition of Spanish oil shale can be suitably described by overall first-order kinetics. We also found that transport effect problems affected the observed rate when the heating rates were higher than 10 Wmin; additionally, no mass and heat transfer resistance was observed for the different particle sizes studied. The results obtained from the isothermal method give an apparent activation energy of 150 kJ/mol and a frequency factor of 2.11 x 10’ s-t, while for the non-isothermal method these results were: E = 167 kJ/mol and A = 2.16 x IO9 s-‘. The pyrolysis rates of Spanish shale are compared with those of Anvil Points, Clear Creek and Moroccan shale.
02/00165 Lipid vesicle-based fuel additives and liquid energy sources containing same Mathur, R. U.S. US 6,080,211 (Cl. 44-301; ClOL1/14), 27 Jun 2000, Appl. 252,546, 19 Feb 1999. 8. Liquid energy sources, e.g. liquid fuels comprising lipid vesicles having fuel additives such as water are disclosed herein. The liquid energy sources, methods for preparation, and methods of enhancing engine performance disclosed herein employing the lipid vesicles result in enhanced fuel efficiency and/or lowered engine emissions. The invention further relates to liquid energy sources containing such additives which further comprise a polymeric dispersion assistant, which reduces the interfacial tension and coalescence of vesicles during dispersion process and storage, and thereby provide transparent looks to the liquid energy source. Fuel and Energy Abstracts
January 2002
19
Transport,
refining,
quality,
storage
02/00176 Catalytic upgrading of pyrolytic oils over HZSM-5 zeolite: behaviour of the catalyst when used in repeated upgrading-regenerating cycles Vitolo, S. et al. Fuel, 2001, 80, (I), 17-26. The behaviour of HZSM-5 zeolite in the upgrading of a wood pyrolysis oil produced in the ENEL fast-pyrolysis plant located in Bastardo, Italy, was studied in repeated upgrading-regenerating cycles. The HZSM-5 zeolite performs a catalytic activity by its acidic sites that, through a carbonium ion mechanism, promote deoxygenation, decarboxylation and decarbonylation of the oil constituents, as well as cracking, oligomerization, alkylation, isomerization, cyclization and aromatization. As a consequence of the catalytic process, coke and tar were also obtained as undesirable by-products. The continued regeneration of the zeolite, consisting of removal of the coke deposits by air at 5OO”C, reduced the effectivenes,s of the catalyst in converting biomass pyrolysis oils to an aromatic product, until an irreversible deactivation was observed. By the analysis conducted on the catalyst it was possible to assess that the loss of activity is mainly connected to the disappearance of a significant amount of acidic sites, mainly the stronger ones, due to the thermal cycling to which the catalyst was submitted. Even if the regeneration was conducted at 5Oo”C, localized raisings of temperature above 500°C due to the combustion of coke may have caused dehydroxylation of the Bronsted acid sites that predominate in zeolites activated at 500°C with formation of Lewis acid sites. Thus, the active acid sites in the upgrading reactions are presumed to be preferentially Bronsted acid sites, which were gradually deactivated by the repeated regeneration treatments. 02/00177 Composite heavy oil combustion improvers and their preparation Wang, J. Faming Zhuanli Shenqing Gongkai Shuomingshu CN 1,222,561 (Cl. ClOL1/22), 14 Jul 1999, Appl. 98,100,111, 8 Jan 1998. 9. (In Chinese) A composite combustion improver for heavy oil is composed of rare earth nitrate or carbonate 5-20, Mg naphthenate 5-15, Fe naphthenate 4-10, Ca naphthenate 3-8, oil solvent 1-5, Mg stearate 1-5, Ba stearate 0.8-4.5, Ca stearate l-5, polyisobutenylsuccinimide 0.08-0.2, and solvent 50-70 wt. parts, preferably rare earth nitrate or carbonate 10.5, Mg naphthenate 7.2, Fe naphthenate 7.2, Ca naphthenate 6, oil solvent 3.2, Mg stearate 1.31, Ba stearate 1.5, Ca stearate 1, polyisobutenylsuccinimide 0.1, and solvent 61.99 wt. parts. The addition of the combustion improver in heavy oil is 0.2-0.5 wt.%. 02lOOl76 Conversion of hydrocarbon resources into hydrogen, gas oil, and water-soluble oil Chikazawa, T., Miyashita, Y. Jpn. Kokai Tokkyo Koho JP 2000 192,055 (Cl. ClOJ3/46), 11 Jul 2000, Appl. 1998/369,405, 25 Dee 1998. 5. (In Japanese) Hydrocarbon resources are treated in a first reactor at 380-500” and 25-40 MPa for primary decomposition of the resources into waterinsoluble oil and aqueous solution of water-soluble oil and then the primary decomposition residue and water is treated in the second reactor at 500-900” and 25-40 MPa for their conversion into H-based gas. The resources may be fossil fuel and organic waste, e.g. municipal waste, sludge. Hydrocarbon resources are converted into energy sources at high rate by a simple process. W2/;;;9
Desulfurization
of engine fuel on board a motor
Holder, E. er al. PCT Int. Appl. WO 00 20,531 (Cl. ClOG25/00), 13 Apr 2000, DE Appl. 19,845,397, 2 Ott 1998. 18. (In German) The invention relates to a method for desulphurizing engine fuel on board a motor vehicle by separating the constituents of the engine fuel containing S by using selective liquid-phase adsorption with the aid of an adsorbing material. 02/00160 Diesel oil emulsifying agent and method for preparation of emulsified diesel oil Liu, X. Faming Zhuanli Shenqing Gongkai Shuomingshu CN 1,215,747 (Cl. ClOG31/08), 5 May 1999, Appl. 97,119,930, 28 Ott 1997. 5. (In Chinese) The diesel oil emulsifying agent is composed of water 15-20, NaOH l3, kerosene 5-9, rosin 5-9, Tween-60 5-9, Span-80 40-49, Tween-20 48.and antirust agent (petroleum sodium suiphonate) IO-15 wt.%. The preparing method for the emulsifying agent comprises: mixing water, NaOH, kerosene, rosin at 90-100”; cooling to 40-50” and adding Tween-60, Span-SO, Tween-20 and antirust agent; and cooling to room temperature. The emulsified diesel oil is prepared by mixing diesel oil 60-90, water 10-40 and the emulsifying agent 0.05-2 wt.%.
02lOO161 Effect of the composition of synthesis gas on the preparation of hydrocarbons on a Co catalyst Krylova, A.Y. et al. Khim. Tverd. Topl. (Moscow), 2000, 1, 3-7. (In Russian) Fischer-Tropsch synthesis from non-stoichiometric Hz-CO gas mixtures in a three-stage-reactor, common-scale plant was studied. The increase in the H&O ratio from 4 to 10 resulted in a decrease in the production of liquid hydrocarbons at I and II stages, changing at the same time the fractional composition of the broad heavy fraction. The content of the fraction boiling 225-335°C increased from 35% to 48%.
02/00162 Experimental study on hydraulic characteristics with slurrv flowina in horizontal oinelines Xu, J.L. et il. Int. Co;f. Proc. Radioact: k’aste Manage. Environ. Rem., 7th. 1999. 1302-I 307. A flow loop, which contains a mixing tank, pump, horizontal pipeline, and corresponding measurement transducers, has been constructed at Florida International University’s Hemispheric Center for Environmental Technology (FIU-HCET). Six typical slurry simulants, of interest to DOE (Department of Energy) sites, were tested. New data were provided on the pressure gradient and volume concentrations across the vertical cross-section. Much attention was paid to the particle settling at lower flow velocity. An apparent transition point exists in the curve of pressure drop versus flow velocity. The velocity at which the limit transition point occurs is identified as the limit deposition velocity. At velocities greater than the limit deposition velocity, there is heterogeneous flow in the pipeline. Lower velocity than the limit deposition velocity will result in stationary bed flow. The present flow shows distinct characteristics with the classical sample slurries, such as coal-water or a sand-water system. A correlation is recommended to calculate the pressure drop.
02/00163 Fuel additive composition for heavy oils Kim, Y. er al. Faming Zhuanli Shenqing Gongkai Shuomingshu CN 1,207,404 (Cl. ClOL1/30), 10 Feb 1999, KR Appl. 9,731,528, 8 Jul 1997. 16. (In Chinese) The additive composition comprises a kerosene 260, a lower Cl-s alcohol 5-15, polybutylene 5-15, a polypropylene glycol for butylated hydroxytoluene) 2-10, and an organic Fe compound 0.5-5 wt.%. The organic Fe compound may be ferrocene or its derivatives such as acetylferrocene, benzoylferrocene, and ferrocene carboxy aldehyde.
02/00164 Kinetics of the thermal decomposition of oil shale from Puertollano (Spain) Torrente, M.C., Galan, M.A. Fuel, 2001, 80, (3) 327-334. The kinetics of the thermal decomposition of Spanish oil shale was studied using isothermal and non-isothermal thermogravimetric analyses (TGA). The isothermal TG data were studied at different particles sizes (0.250 x 10m3, 0.505 x lo-’ and 0.925 x 10-s m) and three temperature plateaux (703, 688 and 673 K). For the kinetic analysis, the Integral Method was used. The non-isothermal weight-loss data was analysed at different heating rates (5, 10, 15,20 and 50 K/min) up to 1173 K and for a particle size of 0.250 x lo-’ m. Three methods were applied for the determination of the kinetic parameters: the Direct Arrhenius Plot Method, the Integral Method and the Differential Method. From an engineering point of view, the rate of the thermal decomposition of Spanish oil shale can be suitably described by overall first-order kinetics. We also found that transport effect problems affected the observed rate when the heating rates were higher than 10 Wmin; additionally, no mass and heat transfer resistance was observed for the different particle sizes studied. The results obtained from the isothermal method give an apparent activation energy of 150 kJ/mol and a frequency factor of 2.11 x 10’ s-t, while for the non-isothermal method these results were: E = 167 kJ/mol and A = 2.16 x IO9 s-‘. The pyrolysis rates of Spanish shale are compared with those of Anvil Points, Clear Creek and Moroccan shale.
02/00165 Lipid vesicle-based fuel additives and liquid energy sources containing same Mathur, R. U.S. US 6,080,211 (Cl. 44-301; ClOL1/14), 27 Jun 2000, Appl. 252,546, 19 Feb 1999. 8. Liquid energy sources, e.g. liquid fuels comprising lipid vesicles having fuel additives such as water are disclosed herein. The liquid energy sources, methods for preparation, and methods of enhancing engine performance disclosed herein employing the lipid vesicles result in enhanced fuel efficiency and/or lowered engine emissions. The invention further relates to liquid energy sources containing such additives which further comprise a polymeric dispersion assistant, which reduces the interfacial tension and coalescence of vesicles during dispersion process and storage, and thereby provide transparent looks to the liquid energy source. Fuel and Energy Abstracts
January 2002
19