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00829 Chemical conversion of natural gas
02
Carbon-13 solid-state NMR investigation on spent catalysts used in coal liquefaction Netzel, D. A. ef crl. I;&. 1996. 75, (12), 1397-1405.
97/00921 deposits
of coke
CoMo type catalysts were prepared on four different surface-modified alumina supports. These catalysts were used in a catalytic coal liquefaction microreactor. The coke deposits on the spent catalysts were investigated. CP-MAS “C spectral data of the coke dyposits were used to quantify the C DD spectral data of the same aromatic and aliphatic carbon types. and samples to quantify the aromatic quaternary carbon types, from which the aromatic cluster size of the coke deposits was determined. Catalysts which promoted the most coke deposition performed poorly in terms of coal liquefaction conversion. The aromatic cluster size of the coke deposited on the spent catalysts depends on the initial pore volume of the fresh catalyst and on the percentage of surface coating of the alumina support.
97100822 methanol
The Carnol production
process
system for COP mitigation
and
Steinberg, M. Enew. FebiMarch 1997. 22, (213). 143-149. Investigates the feasibility of an alternative COz mitigation system and a methanol production proces\. The Carnol system has three components: (i) ;I coal-fired power plant supplying flue gas CO?, (ii) a process which converts the CO? in the presence of He from natural gas to methanol. (iii) use of methanol as a fuel component in the automotive sector. The Carnol system i\ technically feasible and economically competitive with alternative CO:-disposal system\ for coal-fired power plants.
97iooa23
Catalysis
of pyrite for coal liquefaction
The catalyst CNJ 502 with wide temperature range 97tooa24 and high activity for preparing methanol from synthesis gas Luo, H. et ~1. Tiarrranqi Huagong. 1996. 21, (I). 26-29. (In Chinese) Presents the results of a study into the catalytic reaction from synthesis gas to methanol in a fixed bed reactor with catalyst CNJ 502. Effects of the reaction temperature. pressure and space-velocity on the catalyst activity and space-time yield were observed. CNJ SO2 was stable with wide temperature range and had high activity. The catalyst is suitable for methanol synthesis process at low or medium pressure and in methanolmethanation procedure.
Catalytic
hydrocracking
of an asphaltic
coal resi-
Benito, A. and Martinez, M. T. &rew Frrels, 1996. IO, (6), 1235-1240. The study described involved the catalytic hydrocracking of a residue from deasphalting a syncrude obtained by direct coal liquefaction of a suhhituminous Spanish coal at different temperatures and reaction times. The viscosity, coke content, boiling point distribution, elemental analysis, and aromaticity of the reaction products have heen determined.
97looa2a and coal.
Catalytic
two stage coprocessing
of waste plastics
Luo. M. and Curtis, C. W. Prcpr. Pap. Am. Chem. Sot.. Div. Fuel Chem., l9YfI. 41, (3). 1032-1036. In the first stage of the study conducted, waste plastics represented by a mixture of HDPE. poly(ethylene terephthalate), and polystyrene were subjected to hydrocracking to provide a solvent for the second stage of coal liquefaction. The reaction conditions and catalysts for each stage were optimized.
97tooa27
Chain mechanisms
in catalytic
fuels (derived liquid fuels)
selectivity data to yield newly-defined fundamental quantities describing the detarls of the cracking reaction: the reaction path probabilities or RPPs. The RPPs are of fundamental importance in understanding the effects of catalyst formulation, feed composition, reaction conditions. and so on. The contribution of this new methodology to the understanding of previouslystudied catalytic cracking systems IS illustrated using some published examples. The concept of chain mechanisms in catalytic cracking in put into context by comparison with other types of chain mechanism: those previously encountered in gas phase pyrolysis. polymerisation. and the Fischer-Tropsch process.
Characterization and activity of ferric-sulfide-based 97/00828 catalyst in model reactions of direct coal liquefaction: effect of preparation conditions Chadha. A. rr ol. Inn. Eng. C/rem. Rey.. 19Y7, 36. (2) 2X4-295. Presents the results of a study into the activity of various ferric-sulfidcand cracking reactions under based catalysts in model hydrogenation conditions typical of direct coal liquefaction.
97100829
Chemical
conversion
of natural
gas
Chaumette, P. Rw. Inct. Fr. Pet.. 1996. 51, (5). 71 l-727. (In French). Reviews research and development work and current processes for the chemical conversion of natural gas, especially to petrochemicals. fuels, and chemical Intermediates. Two general methods are discussed: (I) direct conversion of methane, and (2) indirect conversion via synthesis gas.
reaction
Hirano. K. el crl. h’i[r/rofr Errenrgi Grrlika;.rlti, 1996. 75. (I I). 977-986 (In Japanese). Details the findings of an investigation into the catalytic activity of pyrite on coal liquefaction. The report states a number of conclusions. (1) Pulverized pyrite exhihits high catalytic activity for asphaltene hydrogenating reaction so that high oil yield and high grade solvent having high hydrogen donatability are obtained in the coal liquefaction system. (2) It is inferred that oxidation of pulverized pyrite slows down the transformation rate to pyrrhotite which exhibits high catalytic activity on coal liquefaction reaction. (3) S addition to pulverized and oxidized pyrite increases the catalytic activity for asphaltene cracking reaction but it is not effective for asphaltem hydrogenating reaction. S addition is supposed to have a different effect to pulverization on the catalytic activity of pyrite.
97100825 due
Liquid
cracking
Wojciechowski, B. W., Arahian J. Sci. Eng., 1996, 21, (2). 165-179. Discusses how the kinetics and selectivity of catalytic cracking can be described by a set of elementary processes which constitute the single-step components of an overall chain mechanism. This mechanism is responsible for most. if not all, of the variety of phenomena encountered in catalytic cracking The products resulting from each of the elementary reactions can he related by a linear equation to the observed selectivity for each product found in the initial stages of the reaction. A reaction-specific set of such equations describes the details of the cracking process of that reaction. A solution of this set of equations reveals the probability of each elementary step in the mechanism resulting in the conversion of a feed molecule, as calculated from the experimental data on the initial selectivities of the reaction products. This approach elaborates and shows how the pertinent chemical concepts are quantified in the form of the elementary reactions and the consequent selectivity equations-for any catalytic cracking system one may wish to study. The selectivity equations, in turn, are solved using matrix algebra. and in this way are made to interpret experimental
The chemical 97iooa30 Fischer-Tropsch wax
oxidation
and
refinement
of
raw
Zhu. J. er al. Proc. Annu. Int. Pmhurgh Cot11 Conf.. lYY5, 12, 681-684. In this study raw Fischer-Tropsch wax (FT wax), produced in a pilot plant and a demonstration plant for coal-based synthetic gasoline, was refined by oxidation. The properties of the refined FT wax were greatly improved.
COP fixation and ethanol production with micro97iooa3i algal photosynthesis and intracellular anaerobic fermentation Hirano, A. ef ul. Energy. FebiMarch lY97. 22. (2/3), 137-142. Microalgae strains were tested to examine ethanol productivity. The characteristics of intracellular ethanol productron were examined with the Chlamydomorzus. The results indicate that rntracellular ethanol production is simpler and less energy intensive than the conventional ethanolfermentation process.
97100832 chloride
Coal
liquefaction
in the
presence
of aluminum
Polubentseva. M. F. PI ul. Khinr. Twr~l. Top/ (Mowm), IYYfr, (3). I IX124. (In Russian) The authors undertook a study of the mechanism of the liquefaction of coal in the presence of AIC17 catalyst and Tetralin-‘?. The effect of the catalyst and solvent on the conversion of organic components of coal and composition of products was examined.
97iooa33
Coal liquefaction
kinetics
Wang, S. et al. Pwpr. Pap. Am. Chem. kc.. DIV. Fuel Chcm., 1996. 41, (3), 935-940. Two stages are distinguished in the liquefaction of two coals (bituminous and subbituminous) at reaction time 10 s to 60 min, i.e. an extraction stage and multiple slower stages representing the breakdown of various components of the coal structure. These hacome apparent only when conversions can be accurately be distinguished at reaction time as low as 10 s. The kinetics of each stage of the process can he adequately described. The extraction stages are two orders of magnitude faster than the breakdown stages.
97iooa34
Coal liquefaction
method
Mochizuki, M.-E. et al. Kokai Tokkyo Koho JP OX, 143, 870 [96, 143, 8701 (Cl. CIOGilOS), 4 Jun 1996, Appl. 941308, 381. I8 Nov 1994, 14 pp (In Japanese). The work details a coal liquefaction method comprising four processes of slurry formulation, coal liquefaction, liquefied oil distillation and solvent hydrogenation The method discussed prevents the fluctuation of the fraction of aromatics of the recycle solvent and recycle solvent with highhydrogen donor ability can he stably manufactured in a short time.
97iooa35 Coal liquefaction: bon Technologies Inc
PDU-scale
testing
at Hydrocar-
Stalzer, R. H. et al. Proc.Annu. Int. Pitfsburgh Cm/ Conf., 199.5. 12. IIN1046. Liquefaction of Illinois No. 6 bituminous and Wyoming Black Thunder subbituminous coal was successfully demonstrated in two test runs at a processing rate of 3 TPD using HRl’s catalytic two-stage liquefaction (CTSL) technology. In the CTSL process, the first-stage reactor operates at lower temperature (385-415”) to hydrogenate the coal and recycle oil, at which the second-stage operates at a higher temperature (425-440”) to convert the coal and heavy oils to clean distillate products.
Fuel and Energy Abstracts
March 1997
73
Carbon-13 solid-state NMR investigation on spent catalysts used in coal liquefaction Netzel, D. A. ef crl. I;&. 1996. 75, (12), 1397-1405.
97/00921 deposits
of coke
CoMo type catalysts were prepared on four different surface-modified alumina supports. These catalysts were used in a catalytic coal liquefaction microreactor. The coke deposits on the spent catalysts were investigated. CP-MAS “C spectral data of the coke dyposits were used to quantify the C DD spectral data of the same aromatic and aliphatic carbon types. and samples to quantify the aromatic quaternary carbon types, from which the aromatic cluster size of the coke deposits was determined. Catalysts which promoted the most coke deposition performed poorly in terms of coal liquefaction conversion. The aromatic cluster size of the coke deposited on the spent catalysts depends on the initial pore volume of the fresh catalyst and on the percentage of surface coating of the alumina support.
97100822 methanol
The Carnol production
process
system for COP mitigation
and
Steinberg, M. Enew. FebiMarch 1997. 22, (213). 143-149. Investigates the feasibility of an alternative COz mitigation system and a methanol production proces\. The Carnol system has three components: (i) ;I coal-fired power plant supplying flue gas CO?, (ii) a process which converts the CO? in the presence of He from natural gas to methanol. (iii) use of methanol as a fuel component in the automotive sector. The Carnol system i\ technically feasible and economically competitive with alternative CO:-disposal system\ for coal-fired power plants.
97iooa23
Catalysis
of pyrite for coal liquefaction
The catalyst CNJ 502 with wide temperature range 97tooa24 and high activity for preparing methanol from synthesis gas Luo, H. et ~1. Tiarrranqi Huagong. 1996. 21, (I). 26-29. (In Chinese) Presents the results of a study into the catalytic reaction from synthesis gas to methanol in a fixed bed reactor with catalyst CNJ 502. Effects of the reaction temperature. pressure and space-velocity on the catalyst activity and space-time yield were observed. CNJ SO2 was stable with wide temperature range and had high activity. The catalyst is suitable for methanol synthesis process at low or medium pressure and in methanolmethanation procedure.
Catalytic
hydrocracking
of an asphaltic
coal resi-
Benito, A. and Martinez, M. T. &rew Frrels, 1996. IO, (6), 1235-1240. The study described involved the catalytic hydrocracking of a residue from deasphalting a syncrude obtained by direct coal liquefaction of a suhhituminous Spanish coal at different temperatures and reaction times. The viscosity, coke content, boiling point distribution, elemental analysis, and aromaticity of the reaction products have heen determined.
97looa2a and coal.
Catalytic
two stage coprocessing
of waste plastics
Luo. M. and Curtis, C. W. Prcpr. Pap. Am. Chem. Sot.. Div. Fuel Chem., l9YfI. 41, (3). 1032-1036. In the first stage of the study conducted, waste plastics represented by a mixture of HDPE. poly(ethylene terephthalate), and polystyrene were subjected to hydrocracking to provide a solvent for the second stage of coal liquefaction. The reaction conditions and catalysts for each stage were optimized.
97tooa27
Chain mechanisms
in catalytic
fuels (derived liquid fuels)
selectivity data to yield newly-defined fundamental quantities describing the detarls of the cracking reaction: the reaction path probabilities or RPPs. The RPPs are of fundamental importance in understanding the effects of catalyst formulation, feed composition, reaction conditions. and so on. The contribution of this new methodology to the understanding of previouslystudied catalytic cracking systems IS illustrated using some published examples. The concept of chain mechanisms in catalytic cracking in put into context by comparison with other types of chain mechanism: those previously encountered in gas phase pyrolysis. polymerisation. and the Fischer-Tropsch process.
Characterization and activity of ferric-sulfide-based 97/00828 catalyst in model reactions of direct coal liquefaction: effect of preparation conditions Chadha. A. rr ol. Inn. Eng. C/rem. Rey.. 19Y7, 36. (2) 2X4-295. Presents the results of a study into the activity of various ferric-sulfidcand cracking reactions under based catalysts in model hydrogenation conditions typical of direct coal liquefaction.
97100829
Chemical
conversion
of natural
gas
Chaumette, P. Rw. Inct. Fr. Pet.. 1996. 51, (5). 71 l-727. (In French). Reviews research and development work and current processes for the chemical conversion of natural gas, especially to petrochemicals. fuels, and chemical Intermediates. Two general methods are discussed: (I) direct conversion of methane, and (2) indirect conversion via synthesis gas.
reaction
Hirano. K. el crl. h’i[r/rofr Errenrgi Grrlika;.rlti, 1996. 75. (I I). 977-986 (In Japanese). Details the findings of an investigation into the catalytic activity of pyrite on coal liquefaction. The report states a number of conclusions. (1) Pulverized pyrite exhihits high catalytic activity for asphaltene hydrogenating reaction so that high oil yield and high grade solvent having high hydrogen donatability are obtained in the coal liquefaction system. (2) It is inferred that oxidation of pulverized pyrite slows down the transformation rate to pyrrhotite which exhibits high catalytic activity on coal liquefaction reaction. (3) S addition to pulverized and oxidized pyrite increases the catalytic activity for asphaltene cracking reaction but it is not effective for asphaltem hydrogenating reaction. S addition is supposed to have a different effect to pulverization on the catalytic activity of pyrite.
97100825 due
Liquid
cracking
Wojciechowski, B. W., Arahian J. Sci. Eng., 1996, 21, (2). 165-179. Discusses how the kinetics and selectivity of catalytic cracking can be described by a set of elementary processes which constitute the single-step components of an overall chain mechanism. This mechanism is responsible for most. if not all, of the variety of phenomena encountered in catalytic cracking The products resulting from each of the elementary reactions can he related by a linear equation to the observed selectivity for each product found in the initial stages of the reaction. A reaction-specific set of such equations describes the details of the cracking process of that reaction. A solution of this set of equations reveals the probability of each elementary step in the mechanism resulting in the conversion of a feed molecule, as calculated from the experimental data on the initial selectivities of the reaction products. This approach elaborates and shows how the pertinent chemical concepts are quantified in the form of the elementary reactions and the consequent selectivity equations-for any catalytic cracking system one may wish to study. The selectivity equations, in turn, are solved using matrix algebra. and in this way are made to interpret experimental
The chemical 97iooa30 Fischer-Tropsch wax
oxidation
and
refinement
of
raw
Zhu. J. er al. Proc. Annu. Int. Pmhurgh Cot11 Conf.. lYY5, 12, 681-684. In this study raw Fischer-Tropsch wax (FT wax), produced in a pilot plant and a demonstration plant for coal-based synthetic gasoline, was refined by oxidation. The properties of the refined FT wax were greatly improved.
COP fixation and ethanol production with micro97iooa3i algal photosynthesis and intracellular anaerobic fermentation Hirano, A. ef ul. Energy. FebiMarch lY97. 22. (2/3), 137-142. Microalgae strains were tested to examine ethanol productivity. The characteristics of intracellular ethanol productron were examined with the Chlamydomorzus. The results indicate that rntracellular ethanol production is simpler and less energy intensive than the conventional ethanolfermentation process.
97100832 chloride
Coal
liquefaction
in the
presence
of aluminum
Polubentseva. M. F. PI ul. Khinr. Twr~l. Top/ (Mowm), IYYfr, (3). I IX124. (In Russian) The authors undertook a study of the mechanism of the liquefaction of coal in the presence of AIC17 catalyst and Tetralin-‘?. The effect of the catalyst and solvent on the conversion of organic components of coal and composition of products was examined.
97iooa33
Coal liquefaction
kinetics
Wang, S. et al. Pwpr. Pap. Am. Chem. kc.. DIV. Fuel Chcm., 1996. 41, (3), 935-940. Two stages are distinguished in the liquefaction of two coals (bituminous and subbituminous) at reaction time 10 s to 60 min, i.e. an extraction stage and multiple slower stages representing the breakdown of various components of the coal structure. These hacome apparent only when conversions can be accurately be distinguished at reaction time as low as 10 s. The kinetics of each stage of the process can he adequately described. The extraction stages are two orders of magnitude faster than the breakdown stages.
97iooa34
Coal liquefaction
method
Mochizuki, M.-E. et al. Kokai Tokkyo Koho JP OX, 143, 870 [96, 143, 8701 (Cl. CIOGilOS), 4 Jun 1996, Appl. 941308, 381. I8 Nov 1994, 14 pp (In Japanese). The work details a coal liquefaction method comprising four processes of slurry formulation, coal liquefaction, liquefied oil distillation and solvent hydrogenation The method discussed prevents the fluctuation of the fraction of aromatics of the recycle solvent and recycle solvent with highhydrogen donor ability can he stably manufactured in a short time.
97iooa35 Coal liquefaction: bon Technologies Inc
PDU-scale
testing
at Hydrocar-
Stalzer, R. H. et al. Proc.Annu. Int. Pitfsburgh Cm/ Conf., 199.5. 12. IIN1046. Liquefaction of Illinois No. 6 bituminous and Wyoming Black Thunder subbituminous coal was successfully demonstrated in two test runs at a processing rate of 3 TPD using HRl’s catalytic two-stage liquefaction (CTSL) technology. In the CTSL process, the first-stage reactor operates at lower temperature (385-415”) to hydrogenate the coal and recycle oil, at which the second-stage operates at a higher temperature (425-440”) to convert the coal and heavy oils to clean distillate products.
Fuel and Energy Abstracts
March 1997
73