03679 Oxygen-blowing coal gasification combined-cycle power generation apparatus

03679 Oxygen-blowing coal gasification combined-cycle power generation apparatus

03 Gaseous fuels (derived gaseous fuels) temperature, near homogeneous reaction conditions, is emphasized. Methane homologation, as a two step proc...

204KB Sizes 3 Downloads 176 Views

03

Gaseous

fuels (derived gaseous fuels)

temperature, near homogeneous reaction conditions, is emphasized. Methane homologation, as a two step process integrated in one reactor, is unsuitable due to low yield and selectivity. The clue for such an attempt to direct methane conversion might be in finding more selective catalysts and an appropriate co-reactant for methane.

Effect of change in hydrogen and nitrogen partial pressures in syngas on ammonia conversion percentage on molten iron catalyst

99103668

Wang, R. Huafei Gongye, 1998, 25, (1), 19-25, 40. (In Chinese) Theoretical analysis and experiments were used to derive a relationship between the change in hydrogen and nitrogen partial pressures in syngas and the change of ammonia conversion percentage on molten iron catalyst under industrial conditions. The calculated values were in good agreement with the experiment results.

Experimental development of a gasification system for solid fuel combined cycle power generation

99103669

Suchkov, S. I. et al. Teploenergerika, 1998, (6) 43-49. (In Russian) A pilot-scale, top-loaded, slagging gasifier was used to gasify two brown coals, a lean coal, anthracite and briquettes to evaluate the technology for combined cycle power generation. The product gas is dry cleaned on metal mesh.

An experimental study of coal gasification 99103670 Dervisoglu, M. and Hortacsu, 0. Energy, 1998, 23, (12) 1073-1076. To study the effects of air-supply pressure, steam-saturation temperature and generator-gas exit temperature on fuel heating value, experiments were carried out on a 2 m diameter gas generator for a ceramics factory. Sixtyfour gasification experiments were performed in total, using a standard coal mixture. With heating values ranging from 1100 to 1400 Cal/l, gaseous fuels were obtained. The heating value of the gas could be raised by up to 27% by maintaining the three process variables close to their optimum values. 99103671

Gasification combined-cycle power generation

equipment Koga, Y. and Shinada, 0. Jpn. Kokai Tokkyo Koho 325,505] (Cl. F22Dl/OO), 8 Dee 1998, Appl. 97/136,587, (In Japanese) Comprising a-gassier, a waste heat recovery boiler of steam turbine condenser, the gasification combined-cycle equipment is characterized by water extraction from outlet of a coal economizer of the boiler for cooling equipment. After cooling, the water is recovered from

JP 10 325,505 [98 27 May 1997, 6 pp. a gas turbine and a power generation the middle part or the machine of the the boiler.

Horizontal cylindric cartridge evaporator for hightemperature gas In coal gasification

concentrations of individual gas species compare well with the experimental data from three pilot-scale and a full-scale fluidized bed coal gasifier. The water-gas shift reaction, either driven by kinetics or in equilibrium in the dilute phase has significant effects on the predictions for the pilot-scale airblown gasifiers but has little effect on a commercial-scale oxygen-blown gasifier. This is attributed to the much faster oxidation rate of Hz and CO near the distributor in the oxygen-blown commercialized gasifier than in the air-blown pilot-scale gasifiers. Results also illustrate that about 26-41% of feed oxygen is consumed in the homogeneous combustion reactions in the gasifiers simulated, the percentage of which increases with a decrease in coal rank and with an increase in operating pressure and temperature. Carbon conversions due to char gasification are significant when compared to those due to char combustion in the gasifiers simulated.

Natural and secondary feedstock resources for production of reducing gases

99103676

Zubilin, I. 16-20. (In Reducing reforming

G. and Starovoit, A. G. MetalL Gomorudn. Prom-st., 1997, (4), Russian) gas (synthesis gas) production by coal gasification and steam of liquid hydrocarbon feedstocks and natural gas is discussed.

99103677 Nitrogen release during fixed-bed gasification of several coals with CO*: factors controlling formation of N2

Ohtsuka, Y. and Wu, 2. Fuel, 1999, 78, (5) 521-527. A study has been performed on the nitrogen release from several coals with different ranks during COz gasification at 0.1 MPa and 1000°C with a fixedbed quartz reactor. Among HCN, NH,, Nz and tar-nitrogen analysed, Nz is the main product for all the samples in the whole range of coal conversion. As the gasification of every char after devolatilization proceeds, Nz increases with a corresponding decrease in the nitrogen in each residue. This shows that the Nz formed originates mostly from solid-gas reactions. When Nz yield is evaluated on the basis of char-nitrogen remaining just after devolatilization, it is almost independent of type of parent coal and demineralization with HCI washing. Only the extent of char gasification can determine the yield, which reaches about 65% after complete gasification. The rate of Nz formation is always lower than that of CO production. It is thus suggested that accumulation of nitrogen-containing surface species is necessary for the start of Nz formation.

Operation of Texaco units for coal gasification and 99103676 failures analysis Wang, X. Huafei Gongye, 1998, 25, (4). 22-26. (In Chinese) In the Shanghai Coking and Chemical Co. Ltd., the operation of Texaco units for coal gasification was investigated. Several common failures were analysed and solutions were proposed.

99iO3672

99103679

Tsumida, Y. Jpn. Kokai Tokkyo Koho JP 10 300,001 [98 300,001] (Cl. F22B1/18), 13 Nov 1998, Appl. 97/105,669,23 Apr 1997, 4 pp. (In Japanese) The evaporator improves stable two-phase flow, is especially suitable for use in crossover duct between gas coolers in coal gasification. It consists of a pair of ring-shaped end pipes to horizontally divide two end sections, a ring-shaped middle pipe having smaller diameter than that of the end pipe to be annularly arranged in the central section, a plurality of horizontal pipes and a plurality of heat-transfer plates connected to the horizontal pipes.

Konishi, S. Jpn. Kokai Tokkyo Koho JP 10 331,606 [98 331,606) (Cl. FOlK23/10), 15 Dee 1998, Appl. 97/140,123, 29 May 1997, 9 pp. . (In Japanese) Using a gasifier for the manufacture of fuel gas from fuel and oxygen and a gas turbine for power generation by combustion of fuel gas, the apparatus comprises an air separator for the separation of high-purity nitrogen gas and supply of the remaining air component to the gasifier and an oxygensupply line for passing at least a part of nitrogen-separated air component to the combustor of gas turbine.

Hydrogen production from cellulose using a reduced nickel catalyst

99103673

Minowa, T. and Ogi, T. Caral. Today, 1998, 45, (l-4) 411-416. The gasification of cellulose, a major component of biomass, was performed in hot-compressed water using a reduced nickel catalyst at different reaction temperatures (200-350°C). The reaction mixture was separated to gases, oil, char and water-soluble products to discuss reaction mechanism based on the product distribution. The water-soluble products were considered as intermediates and the obtained hydrogen was consumed by methanation reaction. The paper proposes a simplified reaction mechanism and the effect of supports was also examined.

Mechanistic lnvestlgations on the partial oxidation 99103674 of methane to synthesis gas over a nickel-on-alumina catalyst

Lu, Y. ef al. Appl. CataZ., A, 1998, 174, (l-2) 121-128. An investigation into the mechanism of the partial oxidation of methane to synthesis gas (CO+Hz) was conducted over a nickel-on-alumina catalyst. The pulse reaction experiments combining XPS and TPR investigations were used to verify the active sites and selective oxygen species present on the working catalyst. The authors propose that the primary surface reaction of the partial oxidation of methane over Ni/AizOx proceeds via methane pyrolysis followed by the reduction of NiO, by the surface carbon atoms which is reoxidized by incorporation of Oz into the catalyst. 99103676 Modelling of bubbling fluidlsed bed coal gaslfiers Yan, H.-M. et al. Fuel, 1999, 78, (9), 1027-1047. Further improvements have been made to a previous numerical model of fluidized-bed coal gasifiers to incorporate an overall energy balance. The improved model has been used to simulate the performance of bubbling fluidized-bed coal gasifiers of different scales. Simulations show that the predicted overall carbon conversion, operating bed temperature and

386

Fuel and Energy Abstracts

November 1999

Oxygen-blowing coal gasification combined-cycle power generation apparatus

99103660

Pressurized fluidized-bed gasifier

Miyoshi, T. er al. Jpn. Kokai Tokkyo Koho JP 11 80,756 [99 80,756] (Cl. ClOJ3/48), 26 Mar 1999, Appl. 97/252,837,2 Sep 1997, 13 pp. (In Japanese) With particular use for IGCC power generation systems by gasification of solid combustibles, a pressurized fluidized-bed gasifier is detailed. It comprises a gasification chamber and a heat recovery chamber inside the pressurized gasifier with two connection openings between two chambers, where one connection opening is on the bottom surface of the gasification chamber and the other connection opening is near upper boundary of fluidized-bed. The heat recovery chamber contains a heat exchanger tube for recovering the heat from the fluidizing medium; the amount of recovered heat for control of bed temperature can be adjusted by changing the flow rate of gasifying gas.

Production of raw material of synthetic gas from rich tail gas of coking plant

99103661

Fang, Q. et al. Faming Zhuanli Shenqing Gongkai Shuomingshu CN 1,122,766 (Cl. COlB3/50), 22 May 1996, Appl. 95,108,811, 31 Aug 1995, 9 pp. (In Chinese) The paper presents a method for the production of raw material of synthetic gas from rich tail gas of a coking plant. The rich tail gas of coking is treated by gasoline absorption at 38-50°C under 0.9-1.6 MPaG with the ratio of oil to gas 0.04-0.15 V/V, diesel oil absorption at 38-55°C under 0.91.6 MPaG with the ratio of oil to gas 0.01-0.025 V/V, ethanolamine absorption at 35-5,5”% undgr 0.7-1.4 MPaG with the ratio of liquid to gas 1 x lo-. -2.0 x lo- m./Nm-, catalytic hydrogenation at 200-380” under 2.04.0 MPaG with space velocity 500-1500 h- and hydrogen partial pressure 0.2-0.7 MPaG and ZnO desulfurization at 300-380” under 2.0-3.0 MPaG with gas space velocity 300-1500 hh’. The rich tail gas of coking is composed of methane, ethane, propane, butane, ethylene, propylene, butylene, carbon and other >CS saturated and unsaturated alkenes, -10