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03596 Hydrorefining activity and acid-base properties of nickel-molybdenum catalysts incorporated on sodium and magnesium ions-modified alumina
02
Catalytic upgrading of the crude gasification pro98103590 duct gas Myren, C. et al. Dev. Thermochem. Biomass Cowers., 1997, 2, 1170-1178. Edited by Bridgwater, A. V. and Boocock, D. G. B., Blackie, London, UK. The ultimate goal of this work is to gain knowledge of the conditions necessary for sufficient removal of tars from gasification gas. A tar-rich gas is produced through pyrolysis at 700°C and alter steam addition, the produced gas is cracked thermally and catalytically between 700 and 900°C using short contact times to allow tar decomposition to be studied. Chromatography is used to analyse the remaining tar. Tars obtained from Miscanthus and straw have been cracked using dolomite and nickel as catalysts. Analyses of tars from Miscanthus and straw are also compared with those of tars from hardwood. The origin of the tars and their composition are found to be reflected in their origin. Coprocessing of oil shales and petroleum residues 98103591 Bibartseva, E. R. et al. Khim. Tekhnol. To@. Masel, 1997, (6). 16-17. (In Russian) Under autoclave conditions of 425°C for 1 h in the presence of 5-15 wt% oil shale, a petroleum vacuum residue is thermally cracked. The presence of the oil shale increases the gasoline and diesel fuel cuts yields to reach a maximum of 8-11 wt%. Determination of thermodynamic data for simula9alo3592 tion of vegetable oil refining: estimation of thermodynamic properties of fats and oils Chakroun, I. er al. Entropic, 1997, 33, (206). 55-60. (In French) Based on group contributions and structure-property relationships, the authors’ method for estimating the thermodynamic properties of vegetable oils is reported. Physical properties considered include boiling point and critical point co-ordinates. The example of linolenic acid and tristearin is used to illustrate the methodology. The evaluation of a biomass-derived liquid product 98163593 as a fuel for boiler applications Whaley, H. et al. FACT (Am. Sot. Mechanical Eng.), 1996, 21, (Proceedings of the International Joint Power Generation Conference, Volume 1: Environmental Control/Fuels and Combustion Technologies, 1996) 463471. The paper investigates the handling properties and the combustion, flame and heat transfer characteristics of a fuel produced from wood and cellulosic products by a rapid thermal process. The resulting pyrolysis liquid fuel products were supplied from a small 50 kg/h pilot plant for comparison with commercially available No. 2 and No. 6 fuel oil at the CANMET Energy Technology Center (CETC). In all, four projects were undertaken with different goals. The combustion tests were conducted in the CETC pilot-scale calorimetric flame tunnel furnace, rated at 0.7 MW,h. The raw unscreened product could not be handled in CETC’s air-atomizing burner without further screening of large char particles. The fuel developer then produced a product which was screened to pass 150 pm size, which burned satisfactorily, with significantly lower carbon monoxide levels in the flue gas. These fuels were then used to complete the four projects. Fischer-Tropsch, hydrotreating and Superclaus 9ai63594 catalysts Van Der Kraan, A. M. Hyper-fine Interact., 1998 (Pub. 1997) 111, (l-4, Industrial Applications of the Moessbauer Effect, Pt. l), 23-34. A gel-forming composition and its use in gelling 96l93595 hydrocarbon liquids Dimitrieva, Z. T. PCT Int. Appl. WO 98 10,038 (Cl. ClOL7/02), 12 Mar 1998, Appl. 96/1B907, 9 Sep 1996, 21 pp. Crude oil and other flammable and toxic liquids are quickly converted into a non-flowing state to prevent spills during their production, transport, storage and processing. The invention may also be used in the technologies for the production of crude oil and the repair of wells. The gel-forming composition is distinguished by the fact that the following can be used as structure-forming components: a mixture of trialkyl borates of the formula B(OR)s or a mixture of dialkyl borates of the formula HOB(OR)z (R = CzHs-C3,,Hhl with normal and isometric structure) in any make-up and any mass ratio of alkyl borates, and a mixture of lithium alkoxides of the formula LiOR’ (R’ = CHs-C3aHhl with a normal and isometric structure) in any make-up and in any mass ratio of lithium alkoxides. The method for the production of the gel-forming composition is characterized by the fact that the alkyl borate mixture and the lithium alkoxide mixture are introduced into the hydrocarbon liquids, crude oil, oil products, halohydrocarbons, fused paraffin, waxes, liquid gases with a mass ratio of structure-forming components from 6:l to 1:6 correspondingly, with a total concentration of components from 0.1 to 17% and at from -70 to 150°C. While mixing the alkyl borate and lithium alkoxide mixtures into the liquid, a solvation compound is also added. Hydrorefining activity and acid-base properties of 98/03596 nickel-molybdenum catalysts incorporated on sodium and magnesium ions-modified alumina Lewandowski, M. and Sarbak, Z. Appl. Catal., A, 1998, 168, (l), 179-185. The decomposition of iso-Pr or diacetone alcohol and ethylbenzene were used as model reactions in the study of a series of NiMo catalysts incorporated on alumina modified with sodium and magnesium ions. Coal
Liquid fuels (transport, refining, quality, storage)
liquid hydrorefining was performed at the pressure of 9.0 MPa and at 400°C. Modification of alumina with sodium and magnesium ions leads to a decrease in the acidity of nickel-molybdenum catalysts, and by the same token increases their basicity. Another effect of modification with sodium and magnesium ions is dehydrogenation of catalysts. Introduction of sodium ions results in a distinct decrease of hydrodenitrogenation and hydrodesulfurization activity. Magnesium ions, on the other hand, decrease the hydrodenitrogenation activity and an insignificant decrease is also seen in the hydrodesulfurization activity of catalysts. 98/03597 Initial activity and selectivity for Fischer-Tropsch synthesis with modified cobalt and nickel catalysts Nie, Z. Fortschr. Ber. VDI, Reihe 3, 1997, 492, 1-176. (In German) Discusses both historical and current literature. 9ai63598 Kinetics of hydrorefining of coal distillates in preparation of furnace fuel Yulin, M. K. er al. Khim. Tverd. Topl., 1997, (5), 86-95. (In Russian) A set of first order equations for the overall reactions of sulfur, nitrogen, and oxygen compound removal and hydrogenation of unsaturated compounds describes the kinetics of hydrorefining brown coal liquid cuts at 34&4Oo”C, 4-10 MPa and space velocity l-3 hh’ over a Ni-Mo/AlzO, catalyst. 98163599 Method and equipment for fractionation of crude oil Leontievsky, V. G. and Korolkov, A. G. PCT Int. Appl. WO 97 43,355 (Cl. ClOG7/00), 20 Nov 1997, RU Appl. 96,109,533, 12 May 1996, 18 pp. (In Russian) A method and equipment for separating crude oil or gaseous condensates into fuel oil, diesel fuel, light and heavy kerosene, light and medium gasoline, as well as liquefied and dry gas, is reported. 9ai03600 Method of refining waste oils (petroleum products) Dimitrieva, Z. T. PCT Int. Appl. WO 98 10,045 (Cl. ClOM175/00), 12 Mar 1998, Appl. 9611B906, 9 Sep 1996, 28 pp. The ecology of the environment and conservation of energy-containing mineral hydrocarbon raw material are addressed in this process, due to secondary use after treatment of the refined oils and cutting oils in the metal-working industry and in machine engineering. The method involves intensive treatment, without heating, of the raw material by extractantabsorbents as aqueous solutions of phosphoric, hydrochloric and sulfuric acids, caustic soda at concentrations from 2 up to 88% by mass with a volumetric ratio for the extractant:raw material from 1:l up to 1:60, without drying or subsequent drying and neutralization over oxides, hydroxides, salts of alkali and alkali-earth metals. The method includes treatment of the raw material with the adsorbent where the raw material is filtered through charcoal or hard coal or coke cut with sand in a mass ratio from 1:0.5 to 1:45 and particle dispersion of 160-400 /Irn. 98/03601 New processes for LCO upgrading from deep catalytic cracking Peng, P. et al. Shiyou Lianzhi Yu Huagong, 1998, 29, (2) 13-16. (In Chinese) In order to upgrade the light cycle oil (LCO) from deep catalytic cracking, two processes were developed. The medium hydrotreatment upgrading process produced low aromatic content diesel oil and high octane number gasoline from the LCO. The LCO was converted to sulfonate fraction and oil fraction by partial sulfonation and redistillation process. The sulfonate fraction was condensed with formaldehyde to form polymeric electrolyte which can be used as super plasticizer, coal-water slurry emulsifier and clay dispersant. The oil fraction was further fractionated into low aromatic light diesel oil and painting solvent. No pollution problem is found with either of these two processes, however, the latter offers low investment and high economic benefit, making it more attractive. 9ai63602 New rapid method to pre-screen catalysts for pyrolysis oil’s vapor phase upgrading Leppamaki, E. A. et al. Biomass Gasif. Pyrolysis, [Conf.], 1997, 407-410. Edited by Kaltschmitt, M. and Bridgwater, A. V., CPL Press, Newbury, UK. It is necessary to improve the storage stability of biomass-based pyrolysis oils and one possible route is catalytic vapour phase upgrading. The Technical Research Centre of Finland and the Helsinki University of Technology have developed new rapid concept to pro-screen catalysts for this purpose. 98lO3603 Process development and scale-up. IV. Case history of the development of a Fischer-Tropsch synthesis process Sie, S. T. Rev. Chem. Eng., 1998, 14, (2) 109-157. Presents a history of the Fischer-Tropsch reaction. Particular attention is given to the development of the Shell middle distillate synthesis process, which uses a multi-tubular trickle-bed reactor in a process configuration for heavy paraffin synthesis using synthesis gas manufactured from natural gas. The heavy paraffin product from the Fischer-Tropsch synthesis is then cracked to produce high-quality middle distillate and diesel fuel. The reactor was selected after an evaluation was made of several reactor designs for heavy paraffin synthesis. A commercial unit was constructed at Bintulu, Malaysia.
Fuel and Energy Abstracts
September
1998
339
Catalytic upgrading of the crude gasification pro98103590 duct gas Myren, C. et al. Dev. Thermochem. Biomass Cowers., 1997, 2, 1170-1178. Edited by Bridgwater, A. V. and Boocock, D. G. B., Blackie, London, UK. The ultimate goal of this work is to gain knowledge of the conditions necessary for sufficient removal of tars from gasification gas. A tar-rich gas is produced through pyrolysis at 700°C and alter steam addition, the produced gas is cracked thermally and catalytically between 700 and 900°C using short contact times to allow tar decomposition to be studied. Chromatography is used to analyse the remaining tar. Tars obtained from Miscanthus and straw have been cracked using dolomite and nickel as catalysts. Analyses of tars from Miscanthus and straw are also compared with those of tars from hardwood. The origin of the tars and their composition are found to be reflected in their origin. Coprocessing of oil shales and petroleum residues 98103591 Bibartseva, E. R. et al. Khim. Tekhnol. To@. Masel, 1997, (6). 16-17. (In Russian) Under autoclave conditions of 425°C for 1 h in the presence of 5-15 wt% oil shale, a petroleum vacuum residue is thermally cracked. The presence of the oil shale increases the gasoline and diesel fuel cuts yields to reach a maximum of 8-11 wt%. Determination of thermodynamic data for simula9alo3592 tion of vegetable oil refining: estimation of thermodynamic properties of fats and oils Chakroun, I. er al. Entropic, 1997, 33, (206). 55-60. (In French) Based on group contributions and structure-property relationships, the authors’ method for estimating the thermodynamic properties of vegetable oils is reported. Physical properties considered include boiling point and critical point co-ordinates. The example of linolenic acid and tristearin is used to illustrate the methodology. The evaluation of a biomass-derived liquid product 98163593 as a fuel for boiler applications Whaley, H. et al. FACT (Am. Sot. Mechanical Eng.), 1996, 21, (Proceedings of the International Joint Power Generation Conference, Volume 1: Environmental Control/Fuels and Combustion Technologies, 1996) 463471. The paper investigates the handling properties and the combustion, flame and heat transfer characteristics of a fuel produced from wood and cellulosic products by a rapid thermal process. The resulting pyrolysis liquid fuel products were supplied from a small 50 kg/h pilot plant for comparison with commercially available No. 2 and No. 6 fuel oil at the CANMET Energy Technology Center (CETC). In all, four projects were undertaken with different goals. The combustion tests were conducted in the CETC pilot-scale calorimetric flame tunnel furnace, rated at 0.7 MW,h. The raw unscreened product could not be handled in CETC’s air-atomizing burner without further screening of large char particles. The fuel developer then produced a product which was screened to pass 150 pm size, which burned satisfactorily, with significantly lower carbon monoxide levels in the flue gas. These fuels were then used to complete the four projects. Fischer-Tropsch, hydrotreating and Superclaus 9ai63594 catalysts Van Der Kraan, A. M. Hyper-fine Interact., 1998 (Pub. 1997) 111, (l-4, Industrial Applications of the Moessbauer Effect, Pt. l), 23-34. A gel-forming composition and its use in gelling 96l93595 hydrocarbon liquids Dimitrieva, Z. T. PCT Int. Appl. WO 98 10,038 (Cl. ClOL7/02), 12 Mar 1998, Appl. 96/1B907, 9 Sep 1996, 21 pp. Crude oil and other flammable and toxic liquids are quickly converted into a non-flowing state to prevent spills during their production, transport, storage and processing. The invention may also be used in the technologies for the production of crude oil and the repair of wells. The gel-forming composition is distinguished by the fact that the following can be used as structure-forming components: a mixture of trialkyl borates of the formula B(OR)s or a mixture of dialkyl borates of the formula HOB(OR)z (R = CzHs-C3,,Hhl with normal and isometric structure) in any make-up and any mass ratio of alkyl borates, and a mixture of lithium alkoxides of the formula LiOR’ (R’ = CHs-C3aHhl with a normal and isometric structure) in any make-up and in any mass ratio of lithium alkoxides. The method for the production of the gel-forming composition is characterized by the fact that the alkyl borate mixture and the lithium alkoxide mixture are introduced into the hydrocarbon liquids, crude oil, oil products, halohydrocarbons, fused paraffin, waxes, liquid gases with a mass ratio of structure-forming components from 6:l to 1:6 correspondingly, with a total concentration of components from 0.1 to 17% and at from -70 to 150°C. While mixing the alkyl borate and lithium alkoxide mixtures into the liquid, a solvation compound is also added. Hydrorefining activity and acid-base properties of 98/03596 nickel-molybdenum catalysts incorporated on sodium and magnesium ions-modified alumina Lewandowski, M. and Sarbak, Z. Appl. Catal., A, 1998, 168, (l), 179-185. The decomposition of iso-Pr or diacetone alcohol and ethylbenzene were used as model reactions in the study of a series of NiMo catalysts incorporated on alumina modified with sodium and magnesium ions. Coal
Liquid fuels (transport, refining, quality, storage)
liquid hydrorefining was performed at the pressure of 9.0 MPa and at 400°C. Modification of alumina with sodium and magnesium ions leads to a decrease in the acidity of nickel-molybdenum catalysts, and by the same token increases their basicity. Another effect of modification with sodium and magnesium ions is dehydrogenation of catalysts. Introduction of sodium ions results in a distinct decrease of hydrodenitrogenation and hydrodesulfurization activity. Magnesium ions, on the other hand, decrease the hydrodenitrogenation activity and an insignificant decrease is also seen in the hydrodesulfurization activity of catalysts. 98/03597 Initial activity and selectivity for Fischer-Tropsch synthesis with modified cobalt and nickel catalysts Nie, Z. Fortschr. Ber. VDI, Reihe 3, 1997, 492, 1-176. (In German) Discusses both historical and current literature. 9ai63598 Kinetics of hydrorefining of coal distillates in preparation of furnace fuel Yulin, M. K. er al. Khim. Tverd. Topl., 1997, (5), 86-95. (In Russian) A set of first order equations for the overall reactions of sulfur, nitrogen, and oxygen compound removal and hydrogenation of unsaturated compounds describes the kinetics of hydrorefining brown coal liquid cuts at 34&4Oo”C, 4-10 MPa and space velocity l-3 hh’ over a Ni-Mo/AlzO, catalyst. 98163599 Method and equipment for fractionation of crude oil Leontievsky, V. G. and Korolkov, A. G. PCT Int. Appl. WO 97 43,355 (Cl. ClOG7/00), 20 Nov 1997, RU Appl. 96,109,533, 12 May 1996, 18 pp. (In Russian) A method and equipment for separating crude oil or gaseous condensates into fuel oil, diesel fuel, light and heavy kerosene, light and medium gasoline, as well as liquefied and dry gas, is reported. 9ai03600 Method of refining waste oils (petroleum products) Dimitrieva, Z. T. PCT Int. Appl. WO 98 10,045 (Cl. ClOM175/00), 12 Mar 1998, Appl. 9611B906, 9 Sep 1996, 28 pp. The ecology of the environment and conservation of energy-containing mineral hydrocarbon raw material are addressed in this process, due to secondary use after treatment of the refined oils and cutting oils in the metal-working industry and in machine engineering. The method involves intensive treatment, without heating, of the raw material by extractantabsorbents as aqueous solutions of phosphoric, hydrochloric and sulfuric acids, caustic soda at concentrations from 2 up to 88% by mass with a volumetric ratio for the extractant:raw material from 1:l up to 1:60, without drying or subsequent drying and neutralization over oxides, hydroxides, salts of alkali and alkali-earth metals. The method includes treatment of the raw material with the adsorbent where the raw material is filtered through charcoal or hard coal or coke cut with sand in a mass ratio from 1:0.5 to 1:45 and particle dispersion of 160-400 /Irn. 98/03601 New processes for LCO upgrading from deep catalytic cracking Peng, P. et al. Shiyou Lianzhi Yu Huagong, 1998, 29, (2) 13-16. (In Chinese) In order to upgrade the light cycle oil (LCO) from deep catalytic cracking, two processes were developed. The medium hydrotreatment upgrading process produced low aromatic content diesel oil and high octane number gasoline from the LCO. The LCO was converted to sulfonate fraction and oil fraction by partial sulfonation and redistillation process. The sulfonate fraction was condensed with formaldehyde to form polymeric electrolyte which can be used as super plasticizer, coal-water slurry emulsifier and clay dispersant. The oil fraction was further fractionated into low aromatic light diesel oil and painting solvent. No pollution problem is found with either of these two processes, however, the latter offers low investment and high economic benefit, making it more attractive. 9ai63602 New rapid method to pre-screen catalysts for pyrolysis oil’s vapor phase upgrading Leppamaki, E. A. et al. Biomass Gasif. Pyrolysis, [Conf.], 1997, 407-410. Edited by Kaltschmitt, M. and Bridgwater, A. V., CPL Press, Newbury, UK. It is necessary to improve the storage stability of biomass-based pyrolysis oils and one possible route is catalytic vapour phase upgrading. The Technical Research Centre of Finland and the Helsinki University of Technology have developed new rapid concept to pro-screen catalysts for this purpose. 98lO3603 Process development and scale-up. IV. Case history of the development of a Fischer-Tropsch synthesis process Sie, S. T. Rev. Chem. Eng., 1998, 14, (2) 109-157. Presents a history of the Fischer-Tropsch reaction. Particular attention is given to the development of the Shell middle distillate synthesis process, which uses a multi-tubular trickle-bed reactor in a process configuration for heavy paraffin synthesis using synthesis gas manufactured from natural gas. The heavy paraffin product from the Fischer-Tropsch synthesis is then cracked to produce high-quality middle distillate and diesel fuel. The reactor was selected after an evaluation was made of several reactor designs for heavy paraffin synthesis. A commercial unit was constructed at Bintulu, Malaysia.
Fuel and Energy Abstracts
September
1998
339