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00170 System for power generation in a process producing hydrocarbons by catalytic conversion of synthesis gas
04 the maximum selectivity of the objective oxygenate. The highest selectivity of acetic acid was 5.2% achieved at CH4 and CO2 conversions of 64.3% and 43.1%, respectively. 04100164 Process for the gasification of heavy oil using 4-stream nozzle for fuel injection and recycled quench water Stellaccio, R. J. et al. U.S. Pat. Appl. Publ. US 2003 85,385 (Cl. 252373; COlB3/24), 8 May 2003, Appl. 2,510. The present invention provides a process whereby a high viscosity hydrocarbonaceous material is fed to a gasifier for conversion to synthesis gas. The feedstock, steam, oxygen, and recycled gasification system water are all fed into the gasifier through a four-stream feed injector. The feedstock in this design is sandwiched between two oxygen streams so as to provide better conversion for the exceptionally heavy feed. The fourth stream down the central bayonet of the feed injector provides the flow path for the recycled water. 04/00165 Production of synthesis gas from Hz0 and COP with nonthermal plasma Futamura, S. and Kabashima, H. Preprints of Symposia - American Chemical Society, Division of Fuel Chemistry, 2003, 48, (1), 266261. A ferroelectric packed bed reactor bed reactor (FPR) and a silent discharge reactor were used to produce synthesis gas from a HZO/COZ at room temperature and an atmospheric pressure. It was demonstrated that synthesis gas production from HzOICOz with non-thermal plasma was possible. Good C balances were obtained, and the molar ratio of Hz and CO produced, could be controlled by the adjustment of the initial ratios of Ha0 and COZ. A continuous operation of the FPR for 5 h resulted in constant yields of Hz and CO. 04/00166 Recent developments in autothermal reforming and pre-reforming for synthesis gas production in GTL applications Aasberg-Petersen, K. et al. Fuel Processing Technology, 2003, 83, (l-3), 253-261. The synthesis gas unit consumes a considerable part of the capital cost in a plant for production of synthetic (Fischer-Tropsch) fuels. Oxygenblown autothermal reforming has been identified as the preferred option for large-scale synthesis gas production. This paper describes recent developments in pre-reforming and autothermal reforming including results of pilot plant demonstrations at low steam-to-carbon ratios. 04/00167 Studies of the release rule of NO, precursors during gasification of coal and its char Feng, J. et al. Fuel Processing Technology, 2003, 84, (l-3), 2433254. This investigation involved the formation and release of precursors of NO,, which were HCN and NHa, during gasification of coal and its char. Gasification was carried out in a fixed bed reactor at atmospheric pressure. The reactor allowed coal particles to be heated up rapidly and held for a pre-specified period of time at peak temperature. The influence of coal rank and coal particle size on the release of Ncontaining compounds during coal gasification with CO, is discussed. Gasification agents and coal gasification temperature were two key factors on the amount of nitrogenous compounds released. Results showed that with an increase of reaction temperature a great amount of NH3 was formed during gasification with steam: the yield of NH3 was highest at 800°C during gasification with COz. The volatiles in coal played the key role in the formation of HCN and NH3 during coal gasification under steam atmosphere. Volatiles were the main source of the formation of HCN and NH,, mainly from the nascent char thermal cracking, whose procedure could be promoted by H,O(g). The yield of HCN during coal gasification had no strong relation with gasification agents and increased with an increase in gasification temperature. A reasonable mechanism for the formation of nitrogenous compounds during coal gasification was suggested in this study, which could explain some results in the literature on pyrolysis and gasification of coal. 04100166 Synergistic effect of pyrite and water on conversion of dibenzyl ether under coal hydrogenation conditions Yoneyama, Y. et al. Energy & Fuels, 2003, 17, (2), 5044505. The conversion of dibenzyl ether under coal hydrogenation conditions with pyrite as catalyst under addition of steam was investigated in laboratory scale. Typical products of this conversion were benzene, toluene, benzaldehyde, benzyl alcohol and dibenzyl. Without addition of pyrite and/or water the conversion was relatively low, and using pyrite catalyst without steam addition resulted in large amounts of a polymeric residue. The results indicated a synergetic effect between pyrite and water under coal hydrogenation conditions.
By-products
reiated
to fuels
04/00169 Synthesis of higher carbon ethers from olefins and alcohols I. Reactions with methanol Snelling, J. et al. Fuel Processing Technology, 2003, 83, (l-3), 2199234. Higher carbon ether compounds (HME; hexyl methyl ether and OME; octyl methyl ether) are produced from olefins (C, olefins: 23DMlB; 2,3-dimethyl-1-butene and 23DM2B; 2,3-dimethyl-2-butene and Cs oiefins: 244TMlP; 2,4,4-trimethyl-1-pentene and 244TM2P; 2,4,4trimethyl-2-pentene) and methanol in the presence of commercially available Amberlyst 15 ion exchange catalyst. Stainless steel batch reactors are used and the experiments are conducted from 333 to 373 K. It appeared that o-olefins are much more reactive to produce the corresponding ether compounds than 8-olefins are. Probably due to steric hindrance, the reactivity of Ca olefins seems to be less than that of C6 olefins. Analysis of variance shows that the amount of catalyst and reaction medium is significant at 2.5% and 1% levels for the production of octyl methyl ether and at 25% and 10% levels for the production of hexyl methyl ether, respectively. The implications of the current results to the design of a continuous process for the preparation of higher carbon ethers from olefins and synthesis gas in a single-step etherification reactor are discussed. 04/00170 System for power generation in a process producing hydrocarbons by catalytic conversion of synthesis gas Geijsel, J. I. etal. PCT Int. Appl. WO 03 31,327 (Cl. ClOB3/36), 17 Apr 2003, EP Appl. 2001/308,527. A system for power generation in a process producing hydrocarbons by catalytic conversion of synthesis gas consisting of an oxidation unit for producing synthesis gas by partial oxidation of a hydrocarbonaceous feed and a conversion unit for producing hydrocarbons from the synthesis gas. The syngas produced is cooled from about llOO-1400°C to about 200-500°C and this cooling generates oxidation unit steam. The super heated steam can be used for power generation, 04/00171 Tubular Inorganic catalytic membrane reactors: advantages and performance in multiphase hydrogenation reactions Centi, G. et al. Catalysis Today; 2003, 79-80. 1399149. The tubular inorganic catalytic membrane (TICM) reactor is a novel multiphase solution for advanced chemical or environmental technologies. The advantages of the use of this technology are discussed with reference to two types of applications: (i) water remediation technologies by catalytic hydrogenation (nitrate removal and chlorinated hydrocarbon dehalogenation) and (ii) HzOz synthesis by H2 + 02 reaction, both occurring over Pd-type catalysts supported over porous inorganic membranes. Some examples of the behaviour of these catalytic membranes are given in long-term tests in nitrate reduction, in chloroform dehalogenation and in Hz02 synthesis.
04 BY-PRODUCTS RELATED TO FUELS 04/00172 Catalytic dry reforming of natural gas for the production of chemicals and hydrogen Verykios, X. E. International Journal of Hydrogen Energy. 2003, 28, (lo), 1045-1063. Carbon dioxide reforming of methane to synthesis gas was studied over Ni-based catalysts. It is shown that, in contrast to other Ni-based catalysts which exhibit continuous deactivation with time-on-stream, the rate over the Ni/LazOa catalyst increases during the initial 2-3 h of reaction and then tends to be essentially invariable, displaying very good stability. X-ray diffraction, hydrogen and CO uptake studies, as well as high-resolution TEM indicate that, under reaction conditions, the Ni particles are partially covered by LaZ02C03 species which are formed by interaction of LaaOa with COZ. Catalytic activity occurs at the Ni-LazOsCOa interface, while the oxy-carbonate species participate directly by reacting with deposited carbon, thus restoring the activity of the Ni sites at the interface. XPS and FTIR studies provide evidence in support of this mechanistic scheme. It was also found that methane cracking on Ni sites and surface reaction between deposited carbon and oxy-carbonate species are the rate determining steps in the reaction sequence. A kinetic model is developed based on this mechanistic scheme, which is found to predict satisfactorily the kinetic measurements. 04100173 Coal ash processing apparatus measurement of unburnt carbon content Kuromi, Y. et al. Jpn. Kokai Tokkyo Koho BO9BSjOO): 7 May 2003, JP Appl. 2001/243,243.
Fuel and Energy Abstracts
and device for in coal ash JP 2003 126;832 (Cl. (In Japanese) January
2004
21
By-products
reiated
to fuels
04/00169 Synthesis of higher carbon ethers from olefins and alcohols I. Reactions with methanol Snelling, J. et al. Fuel Processing Technology, 2003, 83, (l-3), 2199234. Higher carbon ether compounds (HME; hexyl methyl ether and OME; octyl methyl ether) are produced from olefins (C, olefins: 23DMlB; 2,3-dimethyl-1-butene and 23DM2B; 2,3-dimethyl-2-butene and Cs oiefins: 244TMlP; 2,4,4-trimethyl-1-pentene and 244TM2P; 2,4,4trimethyl-2-pentene) and methanol in the presence of commercially available Amberlyst 15 ion exchange catalyst. Stainless steel batch reactors are used and the experiments are conducted from 333 to 373 K. It appeared that o-olefins are much more reactive to produce the corresponding ether compounds than 8-olefins are. Probably due to steric hindrance, the reactivity of Ca olefins seems to be less than that of C6 olefins. Analysis of variance shows that the amount of catalyst and reaction medium is significant at 2.5% and 1% levels for the production of octyl methyl ether and at 25% and 10% levels for the production of hexyl methyl ether, respectively. The implications of the current results to the design of a continuous process for the preparation of higher carbon ethers from olefins and synthesis gas in a single-step etherification reactor are discussed. 04/00170 System for power generation in a process producing hydrocarbons by catalytic conversion of synthesis gas Geijsel, J. I. etal. PCT Int. Appl. WO 03 31,327 (Cl. ClOB3/36), 17 Apr 2003, EP Appl. 2001/308,527. A system for power generation in a process producing hydrocarbons by catalytic conversion of synthesis gas consisting of an oxidation unit for producing synthesis gas by partial oxidation of a hydrocarbonaceous feed and a conversion unit for producing hydrocarbons from the synthesis gas. The syngas produced is cooled from about llOO-1400°C to about 200-500°C and this cooling generates oxidation unit steam. The super heated steam can be used for power generation, 04/00171 Tubular Inorganic catalytic membrane reactors: advantages and performance in multiphase hydrogenation reactions Centi, G. et al. Catalysis Today; 2003, 79-80. 1399149. The tubular inorganic catalytic membrane (TICM) reactor is a novel multiphase solution for advanced chemical or environmental technologies. The advantages of the use of this technology are discussed with reference to two types of applications: (i) water remediation technologies by catalytic hydrogenation (nitrate removal and chlorinated hydrocarbon dehalogenation) and (ii) HzOz synthesis by H2 + 02 reaction, both occurring over Pd-type catalysts supported over porous inorganic membranes. Some examples of the behaviour of these catalytic membranes are given in long-term tests in nitrate reduction, in chloroform dehalogenation and in Hz02 synthesis.
04 BY-PRODUCTS RELATED TO FUELS 04/00172 Catalytic dry reforming of natural gas for the production of chemicals and hydrogen Verykios, X. E. International Journal of Hydrogen Energy. 2003, 28, (lo), 1045-1063. Carbon dioxide reforming of methane to synthesis gas was studied over Ni-based catalysts. It is shown that, in contrast to other Ni-based catalysts which exhibit continuous deactivation with time-on-stream, the rate over the Ni/LazOa catalyst increases during the initial 2-3 h of reaction and then tends to be essentially invariable, displaying very good stability. X-ray diffraction, hydrogen and CO uptake studies, as well as high-resolution TEM indicate that, under reaction conditions, the Ni particles are partially covered by LaZ02C03 species which are formed by interaction of LaaOa with COZ. Catalytic activity occurs at the Ni-LazOsCOa interface, while the oxy-carbonate species participate directly by reacting with deposited carbon, thus restoring the activity of the Ni sites at the interface. XPS and FTIR studies provide evidence in support of this mechanistic scheme. It was also found that methane cracking on Ni sites and surface reaction between deposited carbon and oxy-carbonate species are the rate determining steps in the reaction sequence. A kinetic model is developed based on this mechanistic scheme, which is found to predict satisfactorily the kinetic measurements. 04100173 Coal ash processing apparatus measurement of unburnt carbon content Kuromi, Y. et al. Jpn. Kokai Tokkyo Koho BO9BSjOO): 7 May 2003, JP Appl. 2001/243,243.
Fuel and Energy Abstracts
and device for in coal ash JP 2003 126;832 (Cl. (In Japanese) January
2004
21