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Gasification combined-cycle power generation equipment
03 Gaseous fuels (derived gaseous fuels) and CO-rich gas is used as fuel or for syntheses. Post-treatment or appropriate reaction conditions are used to solve the problems caused by Cl-, N-, or S-containing input materials. 00/00171 Estimation method of coke strength Kato, K. and Matsuura, S. Jpn. Kokai Tokkyo Koho JP 11 349,957 [99 349,957] (Cl. ClOB57/00), 21 Dee 1999, Appl. 1998/159,013,8 Jun 1998. 6. (In Japanese) A method for estimating the strength of coke composed of 30-100 wt% non-sliehtlv cakine coal and the remainder of cakine coal. involves measu&g’swellini rate of raw coal by swelling tr:atment with a solvent, predetermining the relationship of the swelling rate with the coke strength after coking the raw coal in a coke oven. Finally, the coke strength can be estimated from the swelling rate and Gieseler maximum fluidity of the raw coal.
Experimental research on partial oxidation of methane to syngas in tubular perovskite-type membrane reactor
00/00172
Huang, P. et al. Nanjing Huagong Daxue Xuebao, 1999, 21, (2), 2630. (In Chinese) Partial oxidation of methane to svnthesis eas was uerformed on a tubular La~.~Sro.4CO~.~Fe~.sO~.~ membrane &actor packed with a Ni/ ~A1203 catalyst. An investigation was carried out into the reaction temperature on the syngas reaction and methane concentration in the feed. A discussion is also included on the stability of the membrane under reaction conditions.
Experimental study of nonfuel hydrocarbons and soot in coflowing partially premixed ethylene/air flames
OOlOO173
McEnally, C. S. and Pfefferle, L. D. Combusfion and Flame, 2000, 121, (4), 575-592. Centreline profiles of gas temperature, Cl to Cl2 nonfuel hydrocarbon concentrations, polycyclic aromatic hydrocarbon (PAH) laser-induced fluorescence (LIF), and soot volume fraction are reported for coflowing ethylene nonpremixed and partially premixed flames with primary equivalence ratios ranging from 24 to 3. Concentrations of acetylene and C4 hydrocarbons were lower in nearly all of the partially premixed flames than in the nonpremixed flame, whereas concentrations of methane and CxH4 were larger in all of the partially premixed flames than in the nonpremixed flame. These results indicate that the primary effect of partial premixing is not to uniformly increase the concentrations of pyrolysis products, but to shift the pyrolysis mechanism towards odd-carbon species. The concentration of benzene was larger in several of the richer partially premixed flames than in the nonpremixed flame, probably because the shift in pyrolysis mechanism enhances self-reaction of CsH3 radicals. Increases in soot volume fraction and other aromatics were observed that matched the increases in benzene. Profiles of PAH fluorescence agreed closely with those for specific gas-phase PAH such as naphthalene, and the maximum PAH signals were a good predictor of the eventual maximum soot volume fractions. Concentrations of oxygenated hydrocarbons such as formaldehyde and ketene were dramatically increased in the partially premixed flames; for formaldehyde this trend was confirmed with in situ LIF measurements.
Experimental study on cogasification of biomass and coal promoted reactivity of char due to synergetic effect 00/00174
Chen, G. et al. Surv. Combusr. Res. Swed., Proc. List Participants, 1999, ( 94-97. Edited by Olsson E. A pressurized fluidized bed gasifier was used to perform an experimental study on co-gasification of biomass and coal in an oxygen-containing atmosphere. Two biomass materials, birch and miscanthus and Daw Mill coal (UK) were used in the study. The operation temperature was 900°C; and the pressure was 0.4 MPa. The studv was focused on svnereism in the thermochemical treatment of the blends of biomass and co;. The blends of the fuels and their in situ formed char demonstrated unexpectedly high reaction rate of gasification. The formation of tar and nitrogen compounds seems also to exhibit synergism in the co-gasification. However, the tar and ammonia yields were much lower than predicted.
Fluidized-bed co-gasification of residual biomass/poor coal blends for fuel gas production
00100175
Pan, Y.G. er al. Fuel, 2000, 79, (ll), 1317-1326. Experiments involving the co-gasification of residual biomass/poor coal blends and gasification of individual feedstocks used in the blends were performed in a bench scale, continuous fluidized-bed working at atmospheric pressure. Two type of blends were prepared, mixing pine chips (from Valcabadillo, Spain) with black coal, a low-grade coal from Escatr6n. Spain, and Saber0 coal, a refuse coal from Sabero, Spain, in the ratio range of O/100-100/O). Experimental tests were carried out using as a gasification agent mixtures of air and steam with dew points of 74-85°C at gasification temperatures of 840-910°C and superficial fluidized gas velocities of 0.7-1.4 m/s. Feasibility studies were very
16
Fuel and Energy Abstracts
January 2001
positive, showing that blending effectively improved the performance of fluidized-bed co-gasification of the low-grade coal, and the possibility of converting the refuse coal to a low-btu fuel gas. This study indicates that a blend ratio with no less than 20% pine chips for the low-grade coal and 40% pine chips for the refuse coal are the most appropriate. The dry product gas low heating value augments with increasing blend ratio from 3700 to 4560 kJ/N m3 for pine chips/lowgrade coal, and from 4000 to 4750 kJ/N m3 for pine chips/refuse coal. Dry product gas yield rises with the increase of the blend ratio from 1.80 to 3.20 N m3/kg (pine chips/low-grade coal), and from 0.75 to 1.75 N m3/kg (pine chips/refuse coal), respectively. About 50% cogasification process overall thermal efficiency can be achieved for the two types of blend.
Fuel gas from residues. Innovative plant concepts based on circulating fluidized bed gasification
00100176
Greil, C. Hirschfelder, H. Enfsorgungs Praxis, 1999, 17, (4), 28-30. (In German) The principles of nasification in circulating fluidized beds (CFB1. operitionai experience, application possibilityes and the develdpmeii of Lurgi CFB gasification process is reviewed. The suitability of CFB technology has been commercialized worldwide and it has been demons&ted to be suitable for electric power and steam generation and the manufacture of fuel gas from biomass, coal and all types of residues.
00100177 Furnace structure of the gasification furnace in coal gasification equipment Egashira, T. et al. Jpn. Kokai Tokkyo Koho JP 11 279,569 [99 279,569] (Cl. ClOJ3/46), 12 Ott 1999, Appl. 1998/80,771, 27 Mar 1998. 4. (In Jaoanesel A gasificstion furnace equipped with gasification burners for gasification of coal and coal materials is described. It has a furnace well of water-cooling structure below the position of the burners and in the upper part of the furnace there is an insulation structure.
Gas conversion using synthesis gas-produced hydrogen for catalyst rejuvenation and hydrocarbon conversion
00100176
Degeorge, C. W. and Denton, R. D. PCT Int. Appl. WO 99 41,217 (Cl. CO7C1/04), 19 Aug 1999, US Appl. 23,581, 13 Feb 1998. 27. A gas cotiversion-process is p&sented. During the procedure, both hydrocarbons and hydrogen are produced from a hydrogen and carbon monoxide synthesis gas feed which uses hydrogen from a portion of the feed for both hydrocarbon synthesis catalyst rejuvenation and hydroconversion upgrading of a portion of the synthesized hydrocarbons. Hydrogen is produced from a slipstream of the synthesis gas fed into the hydrocarbon synthesis reactor by either a physical separation means, such as pressure-swing adsorption and chemical means, like a water-gas shift reactor. If a shift reactor is used due to insufficient capacity of the synthesis gas generator, physical separation means such as pressure-swing adsorption will still be used to separate a pure stream of hydrogen from the shift reactor gas effluent. The paper also provides process flow diagrams.
00100179 Gasification and combustion reactivity of coals in combined cycle processes
Paterson, N. Eur. Comm., [Rep.] EUR, 1999, 1-128. Five coals of varying rank are studied in terms of their gasification and combustion behaviour. They are tested in a fluidized-bed reactor, highpressure wire mesh reactor and a hot-rod reactor. In order to simulate the main process conditions in a fluidized-bed gasifier, a range of conditions were established.
00/00160
Gasification apparatus for waste plastics
Shinva, K. ef al. Jpn. Kokai Tokkyo Koho JP 11 293.260 199 293.2601 (Cl. ?lOGI/lO), i6 Ott 1999, Appl. 1998/95,984, 8 Apr 1’997. 8.. (Id Japanese) An entrained-bed gasifying apparatus for heat-resistant waste plastic gasification, consists of an embers-fired combustor that uses the fly ash residues discharged from the apparatus, with a mixed gas of combustion waste gas from other system or steam and a gasification gas. It is essential that the temperature is maintained greater than the dioxin formation temperature.
00/00161 Gasification combined-cycle power generation equipment Hashimoto, K. Jpn. Kokai Tokkyo Koho JP 11246,875 (99 246,875] (Cl. ClOJ3/20), 14 Sep 1999, Appl. 1998/51,633, 4 Mar 1998. 5. (In Japanese) The gasification combined-cycle power-generation equipment comprises (1) a gasification-cooling equipment for generating crude gasification gas, (2) a dry-type desulfurization apparatus to produce a refined gas, (3) gas-turbine combined-cycle power-generation equip-
03 Gaseous fuels (derived gaseous fuels) ment for generating power by combustion of the refined gas, and (4) a deashing refining apparatus positioned between the (1) and (2) equipment for removal of dust, heavy metals and alkali components, where the (4) apparatus is composed of a scrubber apparatus for water washing the crude gas and a heater for heating the dedusted crude gas by high-temperature steam. The waste-heat recovery boiler supplies the high-temperature steam and is set at a higher temperature than that of the dedusted gas.
00100182 Gasification of biomass and model compounds in hot compressed water
Kruse, A. er al. Wiss. Ber. - Forschungszent. Karlsruhe, 1999, I1 I-114. Presented are the experimental results of the gasification of biomass such as wood, straw and sewage sludge, plus model compounds in supercritical water. The tests were performed in three batch and two tubular reactors over a temperature range of 300-600” and pressures up to 70 MPa. For the cellulose, sucrose and glucose were chosen as model compounds. Vanillin and pyrocatechol as aromatic compounds are model compounds for lignin. An investigation was also carried out into the influence of slat addition and solid catalysts on the process of gasification.
00100183 Gasification power generation equipment with ammonium sulfate manufacture Akiyama, T. et al. Jpn. Kokai Tokkyo Koho JP 11 349,964 [99 349,964] (Cl. ClOKl/IO), 21 Dee 1999, Appl. 1998/164,681, 12 Jun 1998. 5. (In Japanese) Gasification power-generation equipment is described. The technology is comprised of a gasifier for gasification of coal and/or heavy oils containing C, H, S, and N with an oxidizing agent to form a combustible gas, an apparatus for removing dust particles from the combustible gas, a NH3 removal apparatus and a Hz removal apparatus, plus an ammonium sulfate manufacturing apparatus.
for the reaction C(a)+ O(a) = CO(a) is the highest among all the elementary reactions, the rate-determining step of the partial oxidation of methane could possibly be the above mentioned reaction.
00100188 Method and apparatus for control of pressure of carbonization chamber of coke oven Ozawa, T. et al. Jpn. Kokai Tokkyo Koho JP 11 349,955 [99 349,955] (Cl. ClOB41/00), 21 Dee 1999, Appl. 1998/163,236, 11 Jun 1998.6. (In Japanese) The method and apparatus for control of pressure of carbonization chamber of coke oven is presented. The method involves connecting a plurality of pressurized fluid supply pipeline systems with the supply nozzle equipped on the bend part of the coke oven riser tube, adjusting the pressure of pressurized fluid at the supply nozzle inlet in 21 of pipeline systems, and then based on the measurement of internal gas pressure of the dry main, the pressure of the pressurized fluid is adjusted.
00100189 Method and apparatus for manufacture of combustible gas and power generation equipment using the gas Hanzawa, M. and Hasegawa, S. Jpn. Kokai Tokkyo Koho JP 11 246,876 [99 246,876) (Cl. ClOJ3/46), 14 Sep 1999, Appl. 1998/50,781, 3 Mar 1998. 7. (In Japanese) The method for manufacture of combustible gas used for combinedcycle power generation consists of four steps: (1) the decomposition of coal slurry and heavy oil emulsion under supercritical or subcritical conditions; (2) the separation stage, which involves the oil fraction and residues being separated from each other under subcritical or supercritical conditions; (3) active hydrogen is formed by adding a source of oxygen to the residues separated in a partial oxidation stage, the hydrogen formed is supplied to the decomposition reaction stage; and (4) the oil fraction is gasified at reduced pressure and/or decreased temperature conditions to produce combustible gases with high temperature and high pressure.
00100184 High temperature gasification of solid fuels Yoshikawa, K. Proc. Intersor. Energy Comers. Eng. Conf., 1999, 34th, 584-588. This report proposes a new energy extraction and utilization system for low grade solid fuels, including wastes and coals. The procedure involves the fuels being gasified with high temperatures and air The syngas is first cooled in a waste heat recovery boiler to extract its sensible thermal energy followed by conventional low temperature gas cleaning. A part of this cleaned-up syngas is used for high temperature air preheating while the rest is used for various energy utilization and conversion systems such as industrial furnaces, boilers and gas turbines. In addition, this paper also reports on the systems two main components, namely, the gasifier and high temperature preheater.
Investigation of the deactivation of a circulating ash catalyst due to coke formation from tar cracking
00100185
Lu, J. and Yue, G. Gongcheng Rewuli Xuebao, 1999, 20, (5), 637-641. (In Chinese) With the object of two main tar components: benzene and toluene, the deactivation of a kind of circulating ash of circulating fluidized bed boiler (CFBB) for coking is investigated in a fixed bed reactor. The deactivation mechanism and the measured deactivation parameters of this circulating ash are discussed. The experimental results demonstrate that increasing the coke content of ash results in the tar cracking more slowly.
00100186 Kerosene space heater and heat-resistant coating for use in its gasification chamber Muraoka. Y. and Morita, K. Jnn. Kokai Tokkvo Koho JP 11279.436 199 279,436] (Cl. C09Dl/OO); 12 dct 1999, Appl. i998/84,616,30 Mar 19’98. 4. (In Japanese) The heat resistant coating comprises of (i) 100 parts silica, alumina or/ and silica-alumina composite oxides and optionally tar-removing oxide fillers, (ii) 20-100 parts binders primarily containing Al phosphate and (iii) 2-50 parts hydroxide compounds as curing agents. Thus, a coating contained 40%-solids Al phosphate 100, silica particles 130, hydrocarbon-oxidizing catalyst containing mainly Mn oxide 115, Al hydroxide curing agent 5, a black pigment 43 and 70 g of water.
00/00187 Mechanistic studies of methane partial oxidation to syngas over LiNiLaOx/Alz03 catalyst
Miao, Q. et al. React. Kinet. Catal. Let!., 1999, 66, (2), 273-279. Temperature-programmed reduction of the LiNiLaOJAlzOs catalyst was characterized before and after the partial oxidation of methane and a series of Oz., CH4 and CHJOz pulse reaction experiments over the catalyst under different pre-treatments. It was found that CH., dissociatively adsorbs on active centre nickel producing Hz and surface carbon, C(a). The surface carbon reacts with surface lattice oxygen or surface adsorbed oxygen to produce CO. Because the activation barrier
00100190 Method and device for power generation with gasification of hydrocarbon fuels Akiyama, T. ef al. Jpn. Kokai Tokkyo Koho JP 11263,987 [99 263,987] (Cl. ClOKl/lO), 28 Sep 1999, Appl. 1998/68,110, 18 Mar 1998. 5. (In Japanese) A method for generating power through the gasification of hydrocarbons such as coal and heavy oil is described. The process is performed in a gasifier, combustible gases containing hazardous gas and solids are generated. The generated gas is cooled in a waterwashing tower at <60”, ammonia and solids are removed from the gas, then the gas is introduced into a catalytic converter for converting COS to HzS, this is followed by the removal of a sulfur-containing compound from the gas in an absorbing tower for removing HzS from the combustible gas to have a clean gas. The clean gas is returned to the washing tower where it undergoes indirect heat-exchange with hot gas, then the heated clean gas is used in a gas turbine for generating power to improve heat efficiency.
00100191 Method for manufacture of synthetic fuel gas by aas bubblina fiuang, C. Flming Zhuanli Shenqing Gongkai Shuomingshu CN 1,127,289 (CLClOL3/00), 24 Jul 1996, Appl. 95,100,082, 17 Jan 1995. 7. (In Chinese) A method for the manufacture of svnthetic fuel eas is nresented. The process of fuel gas manufacturing i&olves mixingsolvent oil CsHts (or benzene) 60-80, hexane 8-12, industrial alcohols (or n-BuOH) 5-10, and MeOH (or acetone, EtOAc, toluene, or BuOAc) 5-20% in a sealed container at atmospheric pressure at room temperature. Oz-contgaining gas (pressure > 1 atm) is introduced into the container from the bottom and fuel gas is collected from a gas outlet at the top of the container. The Oz-containing gas is either air, a mixture of Or and Nr or purely Oz.
00/00192 Microwave effect on partial oxidation of methane to syngas over NflZrOz
Bi, X. J. et al. Chin. Chem. Left., 1998, 9, (8) 775-777. The partial oxidation of methane to syngas over Ni/ZrOz catalyst irradiated by microwave has been studied. Compared with a conventional heating mode, the temperature of the catalytic bed is much lower and there is a higher selectivity of CO and Hz with microwave irradiation.
00100193 Microwave effect on partial oxidation of methane to syngas
Bi, X-J. ef al. Read. Kinet. Catal. Letf., 1999, 66, (2), 381-386. Reported in this paper are the results of the partial oxidation of methane over Ni-based and Co-based catalysts activated by two different heating modes, namely, conventional and microwaves. The Fuel and Energy Abstracts
January 2001
19
Experimental research on partial oxidation of methane to syngas in tubular perovskite-type membrane reactor
00/00172
Huang, P. et al. Nanjing Huagong Daxue Xuebao, 1999, 21, (2), 2630. (In Chinese) Partial oxidation of methane to svnthesis eas was uerformed on a tubular La~.~Sro.4CO~.~Fe~.sO~.~ membrane &actor packed with a Ni/ ~A1203 catalyst. An investigation was carried out into the reaction temperature on the syngas reaction and methane concentration in the feed. A discussion is also included on the stability of the membrane under reaction conditions.
Experimental study of nonfuel hydrocarbons and soot in coflowing partially premixed ethylene/air flames
OOlOO173
McEnally, C. S. and Pfefferle, L. D. Combusfion and Flame, 2000, 121, (4), 575-592. Centreline profiles of gas temperature, Cl to Cl2 nonfuel hydrocarbon concentrations, polycyclic aromatic hydrocarbon (PAH) laser-induced fluorescence (LIF), and soot volume fraction are reported for coflowing ethylene nonpremixed and partially premixed flames with primary equivalence ratios ranging from 24 to 3. Concentrations of acetylene and C4 hydrocarbons were lower in nearly all of the partially premixed flames than in the nonpremixed flame, whereas concentrations of methane and CxH4 were larger in all of the partially premixed flames than in the nonpremixed flame. These results indicate that the primary effect of partial premixing is not to uniformly increase the concentrations of pyrolysis products, but to shift the pyrolysis mechanism towards odd-carbon species. The concentration of benzene was larger in several of the richer partially premixed flames than in the nonpremixed flame, probably because the shift in pyrolysis mechanism enhances self-reaction of CsH3 radicals. Increases in soot volume fraction and other aromatics were observed that matched the increases in benzene. Profiles of PAH fluorescence agreed closely with those for specific gas-phase PAH such as naphthalene, and the maximum PAH signals were a good predictor of the eventual maximum soot volume fractions. Concentrations of oxygenated hydrocarbons such as formaldehyde and ketene were dramatically increased in the partially premixed flames; for formaldehyde this trend was confirmed with in situ LIF measurements.
Experimental study on cogasification of biomass and coal promoted reactivity of char due to synergetic effect 00/00174
Chen, G. et al. Surv. Combusr. Res. Swed., Proc. List Participants, 1999, ( 94-97. Edited by Olsson E. A pressurized fluidized bed gasifier was used to perform an experimental study on co-gasification of biomass and coal in an oxygen-containing atmosphere. Two biomass materials, birch and miscanthus and Daw Mill coal (UK) were used in the study. The operation temperature was 900°C; and the pressure was 0.4 MPa. The studv was focused on svnereism in the thermochemical treatment of the blends of biomass and co;. The blends of the fuels and their in situ formed char demonstrated unexpectedly high reaction rate of gasification. The formation of tar and nitrogen compounds seems also to exhibit synergism in the co-gasification. However, the tar and ammonia yields were much lower than predicted.
Fluidized-bed co-gasification of residual biomass/poor coal blends for fuel gas production
00100175
Pan, Y.G. er al. Fuel, 2000, 79, (ll), 1317-1326. Experiments involving the co-gasification of residual biomass/poor coal blends and gasification of individual feedstocks used in the blends were performed in a bench scale, continuous fluidized-bed working at atmospheric pressure. Two type of blends were prepared, mixing pine chips (from Valcabadillo, Spain) with black coal, a low-grade coal from Escatr6n. Spain, and Saber0 coal, a refuse coal from Sabero, Spain, in the ratio range of O/100-100/O). Experimental tests were carried out using as a gasification agent mixtures of air and steam with dew points of 74-85°C at gasification temperatures of 840-910°C and superficial fluidized gas velocities of 0.7-1.4 m/s. Feasibility studies were very
16
Fuel and Energy Abstracts
January 2001
positive, showing that blending effectively improved the performance of fluidized-bed co-gasification of the low-grade coal, and the possibility of converting the refuse coal to a low-btu fuel gas. This study indicates that a blend ratio with no less than 20% pine chips for the low-grade coal and 40% pine chips for the refuse coal are the most appropriate. The dry product gas low heating value augments with increasing blend ratio from 3700 to 4560 kJ/N m3 for pine chips/lowgrade coal, and from 4000 to 4750 kJ/N m3 for pine chips/refuse coal. Dry product gas yield rises with the increase of the blend ratio from 1.80 to 3.20 N m3/kg (pine chips/low-grade coal), and from 0.75 to 1.75 N m3/kg (pine chips/refuse coal), respectively. About 50% cogasification process overall thermal efficiency can be achieved for the two types of blend.
Fuel gas from residues. Innovative plant concepts based on circulating fluidized bed gasification
00100176
Greil, C. Hirschfelder, H. Enfsorgungs Praxis, 1999, 17, (4), 28-30. (In German) The principles of nasification in circulating fluidized beds (CFB1. operitionai experience, application possibilityes and the develdpmeii of Lurgi CFB gasification process is reviewed. The suitability of CFB technology has been commercialized worldwide and it has been demons&ted to be suitable for electric power and steam generation and the manufacture of fuel gas from biomass, coal and all types of residues.
00100177 Furnace structure of the gasification furnace in coal gasification equipment Egashira, T. et al. Jpn. Kokai Tokkyo Koho JP 11 279,569 [99 279,569] (Cl. ClOJ3/46), 12 Ott 1999, Appl. 1998/80,771, 27 Mar 1998. 4. (In Jaoanesel A gasificstion furnace equipped with gasification burners for gasification of coal and coal materials is described. It has a furnace well of water-cooling structure below the position of the burners and in the upper part of the furnace there is an insulation structure.
Gas conversion using synthesis gas-produced hydrogen for catalyst rejuvenation and hydrocarbon conversion
00100176
Degeorge, C. W. and Denton, R. D. PCT Int. Appl. WO 99 41,217 (Cl. CO7C1/04), 19 Aug 1999, US Appl. 23,581, 13 Feb 1998. 27. A gas cotiversion-process is p&sented. During the procedure, both hydrocarbons and hydrogen are produced from a hydrogen and carbon monoxide synthesis gas feed which uses hydrogen from a portion of the feed for both hydrocarbon synthesis catalyst rejuvenation and hydroconversion upgrading of a portion of the synthesized hydrocarbons. Hydrogen is produced from a slipstream of the synthesis gas fed into the hydrocarbon synthesis reactor by either a physical separation means, such as pressure-swing adsorption and chemical means, like a water-gas shift reactor. If a shift reactor is used due to insufficient capacity of the synthesis gas generator, physical separation means such as pressure-swing adsorption will still be used to separate a pure stream of hydrogen from the shift reactor gas effluent. The paper also provides process flow diagrams.
00100179 Gasification and combustion reactivity of coals in combined cycle processes
Paterson, N. Eur. Comm., [Rep.] EUR, 1999, 1-128. Five coals of varying rank are studied in terms of their gasification and combustion behaviour. They are tested in a fluidized-bed reactor, highpressure wire mesh reactor and a hot-rod reactor. In order to simulate the main process conditions in a fluidized-bed gasifier, a range of conditions were established.
00/00160
Gasification apparatus for waste plastics
Shinva, K. ef al. Jpn. Kokai Tokkyo Koho JP 11 293.260 199 293.2601 (Cl. ?lOGI/lO), i6 Ott 1999, Appl. 1998/95,984, 8 Apr 1’997. 8.. (Id Japanese) An entrained-bed gasifying apparatus for heat-resistant waste plastic gasification, consists of an embers-fired combustor that uses the fly ash residues discharged from the apparatus, with a mixed gas of combustion waste gas from other system or steam and a gasification gas. It is essential that the temperature is maintained greater than the dioxin formation temperature.
00/00161 Gasification combined-cycle power generation equipment Hashimoto, K. Jpn. Kokai Tokkyo Koho JP 11246,875 (99 246,875] (Cl. ClOJ3/20), 14 Sep 1999, Appl. 1998/51,633, 4 Mar 1998. 5. (In Japanese) The gasification combined-cycle power-generation equipment comprises (1) a gasification-cooling equipment for generating crude gasification gas, (2) a dry-type desulfurization apparatus to produce a refined gas, (3) gas-turbine combined-cycle power-generation equip-
03 Gaseous fuels (derived gaseous fuels) ment for generating power by combustion of the refined gas, and (4) a deashing refining apparatus positioned between the (1) and (2) equipment for removal of dust, heavy metals and alkali components, where the (4) apparatus is composed of a scrubber apparatus for water washing the crude gas and a heater for heating the dedusted crude gas by high-temperature steam. The waste-heat recovery boiler supplies the high-temperature steam and is set at a higher temperature than that of the dedusted gas.
00100182 Gasification of biomass and model compounds in hot compressed water
Kruse, A. er al. Wiss. Ber. - Forschungszent. Karlsruhe, 1999, I1 I-114. Presented are the experimental results of the gasification of biomass such as wood, straw and sewage sludge, plus model compounds in supercritical water. The tests were performed in three batch and two tubular reactors over a temperature range of 300-600” and pressures up to 70 MPa. For the cellulose, sucrose and glucose were chosen as model compounds. Vanillin and pyrocatechol as aromatic compounds are model compounds for lignin. An investigation was also carried out into the influence of slat addition and solid catalysts on the process of gasification.
00100183 Gasification power generation equipment with ammonium sulfate manufacture Akiyama, T. et al. Jpn. Kokai Tokkyo Koho JP 11 349,964 [99 349,964] (Cl. ClOKl/IO), 21 Dee 1999, Appl. 1998/164,681, 12 Jun 1998. 5. (In Japanese) Gasification power-generation equipment is described. The technology is comprised of a gasifier for gasification of coal and/or heavy oils containing C, H, S, and N with an oxidizing agent to form a combustible gas, an apparatus for removing dust particles from the combustible gas, a NH3 removal apparatus and a Hz removal apparatus, plus an ammonium sulfate manufacturing apparatus.
for the reaction C(a)+ O(a) = CO(a) is the highest among all the elementary reactions, the rate-determining step of the partial oxidation of methane could possibly be the above mentioned reaction.
00100188 Method and apparatus for control of pressure of carbonization chamber of coke oven Ozawa, T. et al. Jpn. Kokai Tokkyo Koho JP 11 349,955 [99 349,955] (Cl. ClOB41/00), 21 Dee 1999, Appl. 1998/163,236, 11 Jun 1998.6. (In Japanese) The method and apparatus for control of pressure of carbonization chamber of coke oven is presented. The method involves connecting a plurality of pressurized fluid supply pipeline systems with the supply nozzle equipped on the bend part of the coke oven riser tube, adjusting the pressure of pressurized fluid at the supply nozzle inlet in 21 of pipeline systems, and then based on the measurement of internal gas pressure of the dry main, the pressure of the pressurized fluid is adjusted.
00100189 Method and apparatus for manufacture of combustible gas and power generation equipment using the gas Hanzawa, M. and Hasegawa, S. Jpn. Kokai Tokkyo Koho JP 11 246,876 [99 246,876) (Cl. ClOJ3/46), 14 Sep 1999, Appl. 1998/50,781, 3 Mar 1998. 7. (In Japanese) The method for manufacture of combustible gas used for combinedcycle power generation consists of four steps: (1) the decomposition of coal slurry and heavy oil emulsion under supercritical or subcritical conditions; (2) the separation stage, which involves the oil fraction and residues being separated from each other under subcritical or supercritical conditions; (3) active hydrogen is formed by adding a source of oxygen to the residues separated in a partial oxidation stage, the hydrogen formed is supplied to the decomposition reaction stage; and (4) the oil fraction is gasified at reduced pressure and/or decreased temperature conditions to produce combustible gases with high temperature and high pressure.
00100184 High temperature gasification of solid fuels Yoshikawa, K. Proc. Intersor. Energy Comers. Eng. Conf., 1999, 34th, 584-588. This report proposes a new energy extraction and utilization system for low grade solid fuels, including wastes and coals. The procedure involves the fuels being gasified with high temperatures and air The syngas is first cooled in a waste heat recovery boiler to extract its sensible thermal energy followed by conventional low temperature gas cleaning. A part of this cleaned-up syngas is used for high temperature air preheating while the rest is used for various energy utilization and conversion systems such as industrial furnaces, boilers and gas turbines. In addition, this paper also reports on the systems two main components, namely, the gasifier and high temperature preheater.
Investigation of the deactivation of a circulating ash catalyst due to coke formation from tar cracking
00100185
Lu, J. and Yue, G. Gongcheng Rewuli Xuebao, 1999, 20, (5), 637-641. (In Chinese) With the object of two main tar components: benzene and toluene, the deactivation of a kind of circulating ash of circulating fluidized bed boiler (CFBB) for coking is investigated in a fixed bed reactor. The deactivation mechanism and the measured deactivation parameters of this circulating ash are discussed. The experimental results demonstrate that increasing the coke content of ash results in the tar cracking more slowly.
00100186 Kerosene space heater and heat-resistant coating for use in its gasification chamber Muraoka. Y. and Morita, K. Jnn. Kokai Tokkvo Koho JP 11279.436 199 279,436] (Cl. C09Dl/OO); 12 dct 1999, Appl. i998/84,616,30 Mar 19’98. 4. (In Japanese) The heat resistant coating comprises of (i) 100 parts silica, alumina or/ and silica-alumina composite oxides and optionally tar-removing oxide fillers, (ii) 20-100 parts binders primarily containing Al phosphate and (iii) 2-50 parts hydroxide compounds as curing agents. Thus, a coating contained 40%-solids Al phosphate 100, silica particles 130, hydrocarbon-oxidizing catalyst containing mainly Mn oxide 115, Al hydroxide curing agent 5, a black pigment 43 and 70 g of water.
00/00187 Mechanistic studies of methane partial oxidation to syngas over LiNiLaOx/Alz03 catalyst
Miao, Q. et al. React. Kinet. Catal. Let!., 1999, 66, (2), 273-279. Temperature-programmed reduction of the LiNiLaOJAlzOs catalyst was characterized before and after the partial oxidation of methane and a series of Oz., CH4 and CHJOz pulse reaction experiments over the catalyst under different pre-treatments. It was found that CH., dissociatively adsorbs on active centre nickel producing Hz and surface carbon, C(a). The surface carbon reacts with surface lattice oxygen or surface adsorbed oxygen to produce CO. Because the activation barrier
00100190 Method and device for power generation with gasification of hydrocarbon fuels Akiyama, T. ef al. Jpn. Kokai Tokkyo Koho JP 11263,987 [99 263,987] (Cl. ClOKl/lO), 28 Sep 1999, Appl. 1998/68,110, 18 Mar 1998. 5. (In Japanese) A method for generating power through the gasification of hydrocarbons such as coal and heavy oil is described. The process is performed in a gasifier, combustible gases containing hazardous gas and solids are generated. The generated gas is cooled in a waterwashing tower at <60”, ammonia and solids are removed from the gas, then the gas is introduced into a catalytic converter for converting COS to HzS, this is followed by the removal of a sulfur-containing compound from the gas in an absorbing tower for removing HzS from the combustible gas to have a clean gas. The clean gas is returned to the washing tower where it undergoes indirect heat-exchange with hot gas, then the heated clean gas is used in a gas turbine for generating power to improve heat efficiency.
00100191 Method for manufacture of synthetic fuel gas by aas bubblina fiuang, C. Flming Zhuanli Shenqing Gongkai Shuomingshu CN 1,127,289 (CLClOL3/00), 24 Jul 1996, Appl. 95,100,082, 17 Jan 1995. 7. (In Chinese) A method for the manufacture of svnthetic fuel eas is nresented. The process of fuel gas manufacturing i&olves mixingsolvent oil CsHts (or benzene) 60-80, hexane 8-12, industrial alcohols (or n-BuOH) 5-10, and MeOH (or acetone, EtOAc, toluene, or BuOAc) 5-20% in a sealed container at atmospheric pressure at room temperature. Oz-contgaining gas (pressure > 1 atm) is introduced into the container from the bottom and fuel gas is collected from a gas outlet at the top of the container. The Oz-containing gas is either air, a mixture of Or and Nr or purely Oz.
00/00192 Microwave effect on partial oxidation of methane to syngas over NflZrOz
Bi, X. J. et al. Chin. Chem. Left., 1998, 9, (8) 775-777. The partial oxidation of methane to syngas over Ni/ZrOz catalyst irradiated by microwave has been studied. Compared with a conventional heating mode, the temperature of the catalytic bed is much lower and there is a higher selectivity of CO and Hz with microwave irradiation.
00100193 Microwave effect on partial oxidation of methane to syngas
Bi, X-J. ef al. Read. Kinet. Catal. Letf., 1999, 66, (2), 381-386. Reported in this paper are the results of the partial oxidation of methane over Ni-based and Co-based catalysts activated by two different heating modes, namely, conventional and microwaves. The Fuel and Energy Abstracts
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