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02457 Method and apparatus for treating wastes by gasification
03 Gaseous fuels (derived 00/02451 Laboratory test unit for study of gasification of carbonaceous materials Shul’ga, 1. V. er U/ Koks K/m., 1999, 2, 19-23. (In Russian) A description of a drum-type apparatus for studying coal gasification provided. As an example, a steam-air gasification of of semi-coke presented.
is is
00102452 Manufacture of synthesis gas with mixed conducting membranes Nataraj, S. et crl. Eur. Pat. Appl. EP 926,096 (Cl. COlB3/38), 30 Jun 1999. US Appl. 997,642, 23 Dee 1997. 29. A two-stage process is required for the conversion of hydrocarbon feedstocks into synthesis gas. The first step involves steam reforming and the second, the conversion to synthesis gas in a mixed-conducting membrane reactor. The steam reforming converts a portion of methane into synthesis gas and essentially all of the hydrocarbons heavier than methane into methane, hydrogen, and carbon oxide. The steam reforming produces an intermediate feed stream containing methane, carbon oxide, hydrogen and steam, which can be processed in a mixed-conducting membrane reactor. For maximum efficiency, the steam reforming and mixed-conducting membrane reactors can be heat integrated. 00102453 Methanogenesis of carbohydrates and their fermentation products by syntrophic methane producing bacteria isolated from freshwater sediments Tabassum, R. and Rajoka. M. I. Bioresource Technology, 2000, 72, (3), l99205. Anaerobic conversion of substrates namely cellulose, cellobiose, glucose, volatile fatty acids, and methanol with a co-culture of fermentative, acidogenic, acetogenic. and methanogenic organisms isolated from freshwater sediments was performed. Maximum reduction of volatile solids (VS) was from cellulose, cellobiose and glucose followed by methanol and other compounds with a product yield coefficient (Y,,,) of 0.59 m’/kg VS consumed with a volumetric productivity (Qr) of 15.7 mmol/l/d. after I2 d fermentation of cellulose. Maximum methane content in the gas mixture was 86.1% with an average of 82.5 k 3.6%. Batch culture methane production characteristics were analysed and compared. The maximum glucose, methanol, formate. acetate. values of Ypil from cellobiose, propionate, and butyrate were 4.0, 2.2, 0.71, 0.22, 0.90. 1.6 and 1.43 mmol/M substrate used and are higher than those values reported in the literature. 00/02454 Methanol synthesis in a multifunctional reactor Amor, H. B. and Halloin, V. L. C/rem. Eq. Sci., 1999, 54. (IO), 1419-1423. A multifunctional reactor is used to conduct the catalytic production of methanol from syngas. The reactor consists of an annular catalyst layer surrounded by a wound copper tube acting as a condenser. The condensed products are separated in siru from the reacting medtum through a hydraulic seal, in order to drive the equilibrium component towards the product. A small laboratory prototype at 35-50 bar wtth maximum temperature in the catalyst layer 240’ was used to perform the first batch of experiments. Conversions to 80% in carbon monoxide and 84”/u in hydrogen were obtained Method and apparatus for gasification of solid 00/02455 carbonaceous material Stoholm, P. C. PCT Int. Appl. WO 99 32,593 (Cl. ClOJ3/56), 1 Jul 1999, DK Appl. 199711,423, 9 Dee 1997. 33. (In Danish) Solid carbonaceous material is gasified in a circulating fluidized bed (CFB) gasifier which includes a CFB reaction chamber, a particle separator for separation of char-containing particles from the outlet gas of the CFB reaction chamber, and a particle recirculation duct for sending the separated particles back to the CFB-reaction chamber. The particle recirculation duct comprises a char-reaction chamber for gasification of char contained in the recirculating particles. The function of the CFB gasifier may be controlled in different ways. A cheaper and more compact construction is achieved compared to the use of more traditional CFB gasifiers in which the char must be converted in the CFB reaction chamber. There is also increased efficiency and increased fuel flexibility. The gasification process is also well suited for biofuels and waste products containing high alkali and chlorine content.
gaseous fuels)
A process for treating wastes by gasification recovers useful resources including energy, valuable metals, and gases for use as synthesis gas in chemical industries or as fuel. The wastes are gasified in a fluidized-bed reactor at a relatively low temperature. Gaseous material and char produced in the fluidized-bed reactor are introduced into a hightemperature combustor, and low calorific gas or medium calorific gas is produced in the high-temperature combustor at a relatively high temperature. It is preferable for the fluidized-bed reactor to he a revolving flow-type fluidized-bed reactor, and for the high-temperature combustor to be a swirling-type high-temperature comhustor. 00102458 Mixed metal oxide ionic conductor membranes for air separation in oxygen-steam coal gasification Keskar, N. R. er crl. Eur. Pat. Appl. EP 916,385 (Cl. BOlD53/22). I9 May 1999. US Appl. 972,412, I8 Nov 1997. 16. The manufacture of an oxygen-steam process gas for a coal gasifier is performed by the separation of a compressed and heated oxygen-containing gas (i.e. air) in an ion-transport separation module consisting of an iontransport membrane to form a heated oxygen-enriched gas on the permeate side and an oxygen-depleted gas on the retentate side. The permeate side is purged with a purge gas stream containing steam to produce the gasifier feed stream; at least a portion of the gas stream containing oxygen and steam is fed to the coal gasifier after blending with a pure Oz stream (recovered from the remaining portion of the purge stream or by a parallel non-purged ion transport separator in the system) to achieve the appropriate steam-to-oxygen ratio for the downstream process. In this way, a gasifier feed is produced with the desired Oz-steam ratio. The oxygen-depleted (nitrogen from air separation) retentate side can be used as a transport gas for handling of pulverized coal during gasification. 00102459 Modelling of bubbling fluidized bed coal gasifiers Yan, N.-M. ef ul. Far/. 1999, 78, (9). 102771047. In order to incorporate an overall energy balance, further improvements were made to a previous numerical model of fluidized-bed coal gasifiers. The improved model was used to simulate the performance of different scales of bubbling fluidized-bed coal gasifiers. Simulations show that the predicted overall carbon conversion, operating bed temperature and concentrations of individual gas species compare well with the experimental data from three pilot-scale and a full-scale fluidized bed coal gasifiers. The water-gas shift reaction, either driven by kinetics or in equilibrium in the diluted phase has significant effects on the predictions for the pilot-scale air-blown gasifiers but has little effect on a blown commercialized gasifier. This is attributed to the much faster oxidation rate of H, and carbon monoxide near the distributor in the oxygen-blown commercialized gasifier than in the air-blown pilot-scale gasifiers. Results also illustrate that approximately 26-41% of feed oxygen is consumed in the homogeneous combustion reactions in the simulated gasifiers, the percentage of which increases with a decrease in coal rank and with an increase in operating pressure and temperature. New procedure for calculation of residual methane 00102460 content by an analytical method based on results of studies in the central part of the Upper Silesian Coal Basin Grzybek. I. Zes:. 1Vouk. Polrrech. S/ask., Gorn., 1997. 235. 71-78. (In Pohsh) In Polish praxis, direct methods of residual methane content testing are not common. Therefore, the content is only assessed by an indirect method, namely analysis. It is based on hAgh correlation between total methane content (G) and desorption ratio (=PZ), and to assess the residual methane content (C,) it uses regression equation in the form: G = a,, + alZPz; where a, and at, are the equation coefficients: and a, = G,. But to date results of such calculations have not been satisfactory, because a rank of coal has not been taken into account. Calculations by the author, made for coals from central part of the Upper Silesian Coal Basin (Poland) show, that for hard coals, characterized by volatile matter content (Vdaf) higher than 28%, the residual methane content is strongly dependent on Vd”‘(correlation coefficient r = -0.95). The dependence can be expressed by the regression equation: G, = 6.51 0- 0.17V”” On the other hand, below 28% of volatile matter content, down to 14%, the residual methane content does not show any dependence (r= -0.211, and different calculations of it oscillate the average value of 2.345 m-r’Mg. On account of all these problems the paper proposes a new proceclure of analysis method.
00102456 Method and apparatus for pretreatment of coal for coke oven Yokomizo, M. ef rr/.Shihara, Y. Jpn. Kokat Tokkyo Koho JP I I 116,970 (99 ll6,970] (Cl. ClOB57jlO). 27 Apr 1999, Appl. 971278.750, 13 Ott 1997. 7. (In Japanese) A method is described for the pre-treatment of coal for coke ovens. It comprises keeping the pulverized coal passageway and solid-gas separation apparatus warm, cooling the pulverized coal and coarse coal during and after classification, mixing the pulverized coal with additives to form pseudo-particles, and feeding the coal particles to the coke oven.
00/02461 Optimization of coking naphtha hydrotreating process Meng, F. Hirugortg Shikun. 1999. 13. (I), 13-16 (In Chinese) In this study, the effect of the hydrotreating condition on the resin and iodine value and nitrogen content of rhe hydrotreated gasoline was investigated using uniform distribution and experimental design. A mathematical model was established and analysed, based on which the process conditions were optimized. The resin value in hydrotreated gasoline was <5 mg/lOO ml, iodine value <5 g I1100 g, and nitrogen content <9.0 x 10 s under the optimum process conditions of reaction temperature 350”, hydrogen-oil volume ratio 400:1, and space velocity 2.0 h I.
00102457 Method and apparatus for treating wastes by aasification Fujimura H. rf ol. U.S. US 5,922.090 (Cl. 48-197R; CIOJ3/54). I3 Jul 1999. US Appl.’ 753,607. ?7 Nov 1996. 20.
00102462 Petroleum coke and its circulating fluidized bed combustion technology Shen, B. er ul. .Sh+nr Licuxhi Yu Nuugong. 1999. 30, (3). 25-29. Chinese)
Fuel and Energy Abstracts
September
2000
(In
277
is is
00102452 Manufacture of synthesis gas with mixed conducting membranes Nataraj, S. et crl. Eur. Pat. Appl. EP 926,096 (Cl. COlB3/38), 30 Jun 1999. US Appl. 997,642, 23 Dee 1997. 29. A two-stage process is required for the conversion of hydrocarbon feedstocks into synthesis gas. The first step involves steam reforming and the second, the conversion to synthesis gas in a mixed-conducting membrane reactor. The steam reforming converts a portion of methane into synthesis gas and essentially all of the hydrocarbons heavier than methane into methane, hydrogen, and carbon oxide. The steam reforming produces an intermediate feed stream containing methane, carbon oxide, hydrogen and steam, which can be processed in a mixed-conducting membrane reactor. For maximum efficiency, the steam reforming and mixed-conducting membrane reactors can be heat integrated. 00102453 Methanogenesis of carbohydrates and their fermentation products by syntrophic methane producing bacteria isolated from freshwater sediments Tabassum, R. and Rajoka. M. I. Bioresource Technology, 2000, 72, (3), l99205. Anaerobic conversion of substrates namely cellulose, cellobiose, glucose, volatile fatty acids, and methanol with a co-culture of fermentative, acidogenic, acetogenic. and methanogenic organisms isolated from freshwater sediments was performed. Maximum reduction of volatile solids (VS) was from cellulose, cellobiose and glucose followed by methanol and other compounds with a product yield coefficient (Y,,,) of 0.59 m’/kg VS consumed with a volumetric productivity (Qr) of 15.7 mmol/l/d. after I2 d fermentation of cellulose. Maximum methane content in the gas mixture was 86.1% with an average of 82.5 k 3.6%. Batch culture methane production characteristics were analysed and compared. The maximum glucose, methanol, formate. acetate. values of Ypil from cellobiose, propionate, and butyrate were 4.0, 2.2, 0.71, 0.22, 0.90. 1.6 and 1.43 mmol/M substrate used and are higher than those values reported in the literature. 00/02454 Methanol synthesis in a multifunctional reactor Amor, H. B. and Halloin, V. L. C/rem. Eq. Sci., 1999, 54. (IO), 1419-1423. A multifunctional reactor is used to conduct the catalytic production of methanol from syngas. The reactor consists of an annular catalyst layer surrounded by a wound copper tube acting as a condenser. The condensed products are separated in siru from the reacting medtum through a hydraulic seal, in order to drive the equilibrium component towards the product. A small laboratory prototype at 35-50 bar wtth maximum temperature in the catalyst layer 240’ was used to perform the first batch of experiments. Conversions to 80% in carbon monoxide and 84”/u in hydrogen were obtained Method and apparatus for gasification of solid 00/02455 carbonaceous material Stoholm, P. C. PCT Int. Appl. WO 99 32,593 (Cl. ClOJ3/56), 1 Jul 1999, DK Appl. 199711,423, 9 Dee 1997. 33. (In Danish) Solid carbonaceous material is gasified in a circulating fluidized bed (CFB) gasifier which includes a CFB reaction chamber, a particle separator for separation of char-containing particles from the outlet gas of the CFB reaction chamber, and a particle recirculation duct for sending the separated particles back to the CFB-reaction chamber. The particle recirculation duct comprises a char-reaction chamber for gasification of char contained in the recirculating particles. The function of the CFB gasifier may be controlled in different ways. A cheaper and more compact construction is achieved compared to the use of more traditional CFB gasifiers in which the char must be converted in the CFB reaction chamber. There is also increased efficiency and increased fuel flexibility. The gasification process is also well suited for biofuels and waste products containing high alkali and chlorine content.
gaseous fuels)
A process for treating wastes by gasification recovers useful resources including energy, valuable metals, and gases for use as synthesis gas in chemical industries or as fuel. The wastes are gasified in a fluidized-bed reactor at a relatively low temperature. Gaseous material and char produced in the fluidized-bed reactor are introduced into a hightemperature combustor, and low calorific gas or medium calorific gas is produced in the high-temperature combustor at a relatively high temperature. It is preferable for the fluidized-bed reactor to he a revolving flow-type fluidized-bed reactor, and for the high-temperature combustor to be a swirling-type high-temperature comhustor. 00102458 Mixed metal oxide ionic conductor membranes for air separation in oxygen-steam coal gasification Keskar, N. R. er crl. Eur. Pat. Appl. EP 916,385 (Cl. BOlD53/22). I9 May 1999. US Appl. 972,412, I8 Nov 1997. 16. The manufacture of an oxygen-steam process gas for a coal gasifier is performed by the separation of a compressed and heated oxygen-containing gas (i.e. air) in an ion-transport separation module consisting of an iontransport membrane to form a heated oxygen-enriched gas on the permeate side and an oxygen-depleted gas on the retentate side. The permeate side is purged with a purge gas stream containing steam to produce the gasifier feed stream; at least a portion of the gas stream containing oxygen and steam is fed to the coal gasifier after blending with a pure Oz stream (recovered from the remaining portion of the purge stream or by a parallel non-purged ion transport separator in the system) to achieve the appropriate steam-to-oxygen ratio for the downstream process. In this way, a gasifier feed is produced with the desired Oz-steam ratio. The oxygen-depleted (nitrogen from air separation) retentate side can be used as a transport gas for handling of pulverized coal during gasification. 00102459 Modelling of bubbling fluidized bed coal gasifiers Yan, N.-M. ef ul. Far/. 1999, 78, (9). 102771047. In order to incorporate an overall energy balance, further improvements were made to a previous numerical model of fluidized-bed coal gasifiers. The improved model was used to simulate the performance of different scales of bubbling fluidized-bed coal gasifiers. Simulations show that the predicted overall carbon conversion, operating bed temperature and concentrations of individual gas species compare well with the experimental data from three pilot-scale and a full-scale fluidized bed coal gasifiers. The water-gas shift reaction, either driven by kinetics or in equilibrium in the diluted phase has significant effects on the predictions for the pilot-scale air-blown gasifiers but has little effect on a blown commercialized gasifier. This is attributed to the much faster oxidation rate of H, and carbon monoxide near the distributor in the oxygen-blown commercialized gasifier than in the air-blown pilot-scale gasifiers. Results also illustrate that approximately 26-41% of feed oxygen is consumed in the homogeneous combustion reactions in the simulated gasifiers, the percentage of which increases with a decrease in coal rank and with an increase in operating pressure and temperature. New procedure for calculation of residual methane 00102460 content by an analytical method based on results of studies in the central part of the Upper Silesian Coal Basin Grzybek. I. Zes:. 1Vouk. Polrrech. S/ask., Gorn., 1997. 235. 71-78. (In Pohsh) In Polish praxis, direct methods of residual methane content testing are not common. Therefore, the content is only assessed by an indirect method, namely analysis. It is based on hAgh correlation between total methane content (G) and desorption ratio (=PZ), and to assess the residual methane content (C,) it uses regression equation in the form: G = a,, + alZPz; where a, and at, are the equation coefficients: and a, = G,. But to date results of such calculations have not been satisfactory, because a rank of coal has not been taken into account. Calculations by the author, made for coals from central part of the Upper Silesian Coal Basin (Poland) show, that for hard coals, characterized by volatile matter content (Vdaf) higher than 28%, the residual methane content is strongly dependent on Vd”‘(correlation coefficient r = -0.95). The dependence can be expressed by the regression equation: G, = 6.51 0- 0.17V”” On the other hand, below 28% of volatile matter content, down to 14%, the residual methane content does not show any dependence (r= -0.211, and different calculations of it oscillate the average value of 2.345 m-r’Mg. On account of all these problems the paper proposes a new proceclure of analysis method.
00102456 Method and apparatus for pretreatment of coal for coke oven Yokomizo, M. ef rr/.Shihara, Y. Jpn. Kokat Tokkyo Koho JP I I 116,970 (99 ll6,970] (Cl. ClOB57jlO). 27 Apr 1999, Appl. 971278.750, 13 Ott 1997. 7. (In Japanese) A method is described for the pre-treatment of coal for coke ovens. It comprises keeping the pulverized coal passageway and solid-gas separation apparatus warm, cooling the pulverized coal and coarse coal during and after classification, mixing the pulverized coal with additives to form pseudo-particles, and feeding the coal particles to the coke oven.
00/02461 Optimization of coking naphtha hydrotreating process Meng, F. Hirugortg Shikun. 1999. 13. (I), 13-16 (In Chinese) In this study, the effect of the hydrotreating condition on the resin and iodine value and nitrogen content of rhe hydrotreated gasoline was investigated using uniform distribution and experimental design. A mathematical model was established and analysed, based on which the process conditions were optimized. The resin value in hydrotreated gasoline was <5 mg/lOO ml, iodine value <5 g I1100 g, and nitrogen content <9.0 x 10 s under the optimum process conditions of reaction temperature 350”, hydrogen-oil volume ratio 400:1, and space velocity 2.0 h I.
00102457 Method and apparatus for treating wastes by aasification Fujimura H. rf ol. U.S. US 5,922.090 (Cl. 48-197R; CIOJ3/54). I3 Jul 1999. US Appl.’ 753,607. ?7 Nov 1996. 20.
00102462 Petroleum coke and its circulating fluidized bed combustion technology Shen, B. er ul. .Sh+nr Licuxhi Yu Nuugong. 1999. 30, (3). 25-29. Chinese)
Fuel and Energy Abstracts
September
2000
(In
277