EP0249255A1 - Cycle combiné à turbines à gaz et à vapeur - Google Patents

Cycle combiné à turbines à gaz et à vapeur Download PDF

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Publication number
EP0249255A1
EP0249255A1 EP87200488A EP87200488A EP0249255A1 EP 0249255 A1 EP0249255 A1 EP 0249255A1 EP 87200488 A EP87200488 A EP 87200488A EP 87200488 A EP87200488 A EP 87200488A EP 0249255 A1 EP0249255 A1 EP 0249255A1
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EP
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Prior art keywords
gas
gas turbine
combustion
gasification
steam
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Granted
Application number
EP87200488A
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German (de)
English (en)
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EP0249255B1 (fr
Inventor
Lothar Dr. Reh
Rolf Dr. Graf
Martin Hirsch
Ludolf Dr. Plass
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GEA Group AG
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Metallgesellschaft AG
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Application filed by Metallgesellschaft AG filed Critical Metallgesellschaft AG
Priority to AT87200488T priority Critical patent/ATE40182T1/de
Publication of EP0249255A1 publication Critical patent/EP0249255A1/fr
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Publication of EP0249255B1 publication Critical patent/EP0249255B1/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/061—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle with combustion in a fluidised bed
    • F01K23/062—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle with combustion in a fluidised bed the combustion bed being pressurised

Definitions

  • the invention relates to a method for operating a combined gas / steam turbine process, in which the gas turbine process is operated by means of a fuel gas obtained from solid carbon-containing material and then desulfurized, and the steam turbine process is operated by means of the steam obtained in the combustion of the carbon-containing gasification residue and in which the combustion of the carbon-containing gasification residue with oxygen-containing exhaust gases from the gas turbine process takes place.
  • coal is supplied to a gasification plant for partial gasification, the gas is freed of pollutants with the aid of a scrubber and then burned in the gas turbine.
  • the coke remaining in the partial gasification is burned in the furnace of a steam generator with the oxygen-containing exhaust gases from the gas turbine and the steam is fed to a steam turbine (K. Weinzierl, "Coal gasification to improve efficiency in the power plant” VGB-Krafttechnikstechnik 62 (1982), No. 5, page 365 ff. and Issue 10, page 852 ff.).
  • the aforementioned configuration of the gasification stage is associated with a shift of energy from the gas turbine branch into the steam turbine branch, as a result of which - as can be determined thermodynamically - at least a substantial part of the improvement in efficiency is consumed.
  • the object of the invention is to provide a combined gas / steam turbine process which does not have the disadvantages of the known, in particular the aforementioned, process (s) and the combustion of solid carbon-containing fuels in an environmentally friendly manner with a high degree of fuel efficiency and power generation with a high degree of efficiency enables.
  • the object is achieved by designing the method of the type mentioned at the outset in accordance with the invention in such a way that the fuel gas in a circulating fluidized bed is gasified by 70 to 95% by weight of the carbon content in the carbon-containing material at a temperature of 900 to 1100 * C generated freed from pollutants in the suspension state at 850 to 950'C with calcium hydroxide, calcium oxide and / or calcium carbonate-containing solid and for the most part burns for the operation of the gas turbine to a gas containing at least 5% by volume oxygen of at least 1000 ° C, the combustion of the carbon-containing gasification residues with the production of process steam in a further circulating fluidized bed at a temperature of 800 to 950 ° C. in a near-stoichiometric manner with at least 2 partial streams of oxygen-containing gases supplied at different levels, the majority of which are formed from the gas turbine exhaust gas.
  • EP-Al-62 363 It is known from EP-Al-62 363 to carry out gasification from carbon-containing material as a first stage at a pressure of maximum 5 bar and a temperature of 800 to 1100 ° C. by means of oxygen-containing gases in the presence of water vapor in a circulating fluidized bed and to implement 40 to 80% by weight of the carbon contained in the starting material, to remove sulfur compounds from the gas formed at a temperature in the range from 800 to 1000 ° C.
  • this concept pursues the goal of helping the industry to equip the production of certain products with energy in various forms, for example as steam for heating purposes, in the form of other high-temperature heat and in the form of clean fuel gases, the combustion of which does not adversely affect the product quality.
  • the degree of conversion of the primary energy (eg coal) into the secondary energies fuel gas and process heat should be variable within a wide range in accordance with the respective existing need for one or the other secondary energy.
  • solid carbon-containing material means solid fuel at ambient temperature.
  • Such materials are, for example, all types of coal including washing piles, coke, petroleum coke, wood waste, peat, oil shale, asphaltenes and refinery residues.
  • the principle of the circulating fluidized bed used in the gasification and combustion stage is characterized by the fact that - in contrast to the " classic" fluidized bed, in which a dense phase is separated from the gas space above by a clear density stress - distribution states without a defined boundary layer are available. A leap in density between the dense phase and the dust space above it does not exist; however, the solids concentration within the reactor decreases continuously from bottom to top.
  • the desulfurization of the gas produced can take place in any suspension state, e.g. in a pneumatic conveyor or in a Venturi fluidized bed with solids discharge in a downstream separator.
  • a circulating fluidized bed can also advantageously be used for desulfurization.
  • the gasification process can be carried out below 1000 ° C, e.g. Because fuel gases with a comparatively low calorific value are permissible for the operation of the gas turbine, the desulfurization can also take place in the gasification reactor itself, that is to say in situ.
  • the gasification stage can be carried out under any pressure deemed appropriate. It will generally result from the operating data of the gas turbine and will be in the range of 15 - 30 bar. In this case, the highest possible pressures are preferable from thermodynamic conditions.
  • the oxygen-containing gas required for the gasification and the water vapor which is generally required should be fed to the fluidized bed reactor of the gasification stage at different heights. It is expedient to supply water vapor predominantly in the form of fluidizing gas and oxygen-containing gas predominantly in the form of secondary gas. Of course, the entry of minor amounts of water vapor can also take place together with the oxygen-containing secondary gas and the entry of minor amounts of oxygen-containing gases together with water vapor as the fluidizing gas.
  • the residence time of the gases in the gasification stage - above the Entry point of the carbonaceous material - should be set to 3 to 20 seconds, preferably 10 to 15 seconds. This condition is usually realized by entering the carbonaceous material at a higher level in the gasification stage. On the one hand, this produces a gas which is richer in hydrocarbon and has a correspondingly higher calorific value, and on the other hand ensures that the gas has practically no hydrocarbons condensing in the exhaust system.
  • the desulfurization of the fuel gas is expediently carried out using desulfurization agents whose particle size dp50 is 5 to 200 / ⁇ m.
  • An average suspension density of 0.1 to 10 kg / m 3 , preferably 1 to 5 kg / m 3 , and an hourly solids circulation rate which is at least 5 times the solids weight in the reactor shaft should be set in the fluidized bed reactor.
  • the desulfurization agent dosage should be at least 1.2 to 2.0 times the stoichiometric requirement be. It should be noted that when using dolomite or burnt dolomite, practically only the calcium component reacts with the sulfur compounds. In the case of in-situ desulfurization in the gasification reactor, the effective desulfurization agents introduced with the inorganic constituents of the carbon-containing material must also be taken into account.
  • the gas rate during desulfurization is in Depending on the gas pressure set to approx. 1 to 5 m / sec (calculated as empty pipe speed).
  • the entire desulfurization agent also required for the combustion stage can be added to the gas desulfurization stage. In this way, the thermal energy required for heating and possibly for deacidification is withdrawn from the gas and thus the gasification and combustion stages are maintained.
  • the combustible constituents that are not converted in the gasification stage are considered to be difficult fuels, particularly with regard to environmentally friendly combustion.
  • the by-products from gas cleaning are also considered to be very difficult to process. They are advantageously processed in a further circulating fluidized bed.
  • the by-products from gas cleaning are removed in an environmentally friendly manner.
  • the loaded desulphurization agents coming from the gas cleaning stage in particular insofar as they are in sulfidic form, such as calcium sulfide, are sulfated and thereby converted into landfill-compatible compounds, such as calcium sulfate.
  • the heat of oxidation released in the sulfation process is also obtained as steam.
  • the other by-products, such as dust from gas dedusting are also converted into environmentally compatible products.
  • the combustion takes place in two stages with different amounts of oxygen-containing gases. Their preference lies in a "soft" combustion, with the local one Overheating can be avoided.
  • the staged combustion also largely suppresses NO formation.
  • the fuel is fed into the zone between the supply points for oxygen-containing fluidizing gas and secondary gas.
  • an average suspension density of 15 to 100 kg / m 3 is expediently created above the upper gas supply by adjusting the amounts of fluidization and secondary gas and at least a substantial part of the heat of combustion is removed by means of cooling surfaces located above the upper gas supply in the reactor space.
  • the gas velocities prevailing in the fluidized bed reactor above the secondary gas supply are usually above 5 m / s at normal pressure and can be up to 15 m / s, and the ratio of the diameter to the height of the fluidized bed reactor should be chosen such that gas residence times of 0.5 to 8 , 0 s, preferably 1 to 4 s, are obtained.
  • any gas which does not impair the nature of the exhaust gas can be used as the fluidizing gas.
  • Inert gases such as recirculated flue gas (exhaust gas), nitrogen and water vapor are also suitable.
  • exhaust gas recirculated flue gas
  • nitrogen and water vapor are also suitable.
  • oxygen-containing gas it is particularly advantageous to use oxygen-containing gas as the fluidizing gas.
  • a plurality of supply openings for secondary gas are advantageous within each entry level.
  • Another expedient embodiment of the combustion process consists in creating an average suspension density of 10 to 40 kg / m 3 above the upper gas supply by adjusting the amounts of fluidization and secondary gas, removing hot solids from the circulating fluidized bed and in the fluidized state by direct and indirect heat exchange cool and return at least a partial flow of cooled solid into the circulating fluidized bed.
  • the temperature can be kept constant practically without changing the prevailing in the fluidized bed reactor Achieve operating conditions, i.e. without changing the suspension density, among other things, only by controlled return of the cooled solid.
  • the recirculation rate is more or less high.
  • the combustion temperatures can be set at will from very low temperatures, which are close above the ignition limit, to very high temperatures, which are limited, for example, by softening the combustion residues. They can be between 650 and 950 ° C.
  • the output in steam generation can be increased - without interfering with the gasification stage - if the combustion stage is additionally fed with carbon-containing material.
  • the possibility of the separate addition of solid carbon-containing material into the combustion stage allows, especially in the start-up phase, the start of steam turbine operation, regardless of the gasification residue of the gasification stage,
  • air as an oxygen-containing gas
  • air enriched with oxygen or technically pure oxygen can also be used.
  • air enriched with oxygen or technically pure oxygen can also be used.
  • Within the combustion stage it is possible to work at normal pressure, but also under pressure, up to about 10 bar.
  • Preferred refinements of the invention consist in generating the fuel gas by gasifying at least 80% by weight of the carbon content of the solid carbon-containing material or in cooling the desulfurized fuel gases to a temperature in the range from 350 to 600 ° C. and freeing them from halides.
  • the increase in the degree of gasification to at least 80% by weight is generally associated with the advantage that an additionally increased degree of efficiency is achieved.
  • the halides are removed dry using calcium oxide or hydroxide, in principle under the same process conditions that are mentioned with regard to the separate desulfurization of the fuel gases.
  • the predominant part of the fuel gas produced in the above described manner and purified is burned in a combustion chamber of stoichiometry to produce NO x -deficient flue gases, so that a flue gas is formed with at least 5 vol .-% oxygen. Since the temperature of the flue gas has to be based on the operating conditions of the gas turbine and is usually set to the maximum permissible value under full load operation, the amount of oxygen-containing gases required for combustion will be selected such that this permissible maximum temperature is established. However, the minimum oxygen content of 5% by volume must not be undercut. If necessary, care must be taken to ensure that the fuel gas has a high calorific value.
  • the operating temperature of the gas turbine is currently a maximum of 1200 ° C.
  • a further advantageous embodiment of the invention provides for the possibly remaining part of the fuel gas to be burned near-stoichiometrically with the formation of low-NO smoke gases, to be cooled and to be fed to a second gas turbine. For the reasons already mentioned, cooling should not go below the permissible gas turbine inlet temperature if possible.
  • This embodiment of the invention has a particularly advantageous effect in that a high degree of efficiency can be achieved even in part-load operation.
  • the degree of conversion of the primary energy, such as coal, into fuel gas and steam and thus ultimately the overall efficiency of the combined gas / steam turbine process is essentially dependent on the permissible inlet temperature of the flue gas for the Gas turbine determined.
  • the ratio of the outputs from the gas turbine to the steam turbine increases with increasing permissible inlet temperature of the flue gases in favor of the gas turbine. This means that as the permissible inlet temperature of the flue gas increases, the extent of gasification increases, and with it that of residue combustion. At gas inlet temperatures of 1200 * C, efficiencies of 45% can be achieved.
  • the figure shows a flow diagram of the method according to the invention in a simplified form.
  • the fuel gas is generated in the circulating fluidized bed illustrated by (1), which is supplied with oxygen-containing fluidizing gas or with steam or coal via the lines (2 or 3 or 4). It is fed via line (5) to a first heat exchanger (6) and from there to the device (7) for desulfurization. After passing through a further heat exchanger (8), the removal of hydrogen halide, in particular hydrogen chloride, takes place in the device (9) and the dedusting in device (10). The sorbents obtained in the devices (7 and 9), loaded with pollutants of the fuel gas, and the dusts obtained in the device (10) are discharged via the lines (11, 12, 13).
  • the fuel gas then passes via line (14) into the combustion chamber (15), which is additionally supplied via line (16) introduced oxygen-containing gas is supplied.
  • the flue gas intended for driving the gas turbine (17) is generated in the combustion chamber (15) by superstoichiometric combustion.
  • the metering of the oxygen-containing gas is selected such that the optimum temperature is created for the operation of the gas turbine (17).
  • Part of the exhaust gas from the gas turbine (17) is fed to the circulating fluidized bed (20) for the combustion of the gasification residue via line (18 and 19) as a fluidizing gas or as a secondary gas. If necessary, fresh oxygen-containing fluidizing gas can be introduced by means of the blower (21).
  • the gasification residue is entered via line (22) together with the loaded sorbents and the dusts separated from the fuel gases.
  • further desulfurizing agent and, if necessary, additional coal can be fed to the circulating fluidized bed (20) (line 23).
  • the steam generated in the steam registers (24) of the circulating fluidized bed (20) is fed via line (25) to the steam turbines (26, 27 and 28) operated under high pressure, medium pressure and low pressure.
  • the exhaust gas from the circulating fluidized bed (20) passes through a further heat exchanger (29) into a dedusting system (30) and then into the chimney (31).
  • Oxygen-containing flue gas emerging from the gas turbine (17) and not required in the circulating fluidized bed (20) can be fed to a heat exchanger system (33) via line (32) and can be cooled there in a conventional manner. It then also gets into the chimney (31).
  • a second gas turbine 34
  • the commissioning of which is advantageous particularly in the case of partial load operation. It is preceded by a combustion chamber (35) with a waste heat boiler (36), which can also be designed as a wall-cooled combustion chamber.
  • a flue gas obtained by near-stoichiometric combustion.
  • the flue gas is generated from fuel gas supplied via line (37) and oxygen-containing gas supplied via line (38).
  • the exhaust gas from the gas turbine (34) passes through line (39) into line (32) and, as described above, is utilized.
  • 223,000 Nm 3 of gas are generated per hour in the circulating fluidized bed (1).
  • 155,000 Nm 3 of air at 350 ° C. and 20 bar are fed in via line (2), 3.9 t of steam at 400 ° C. via line (3) and 70 t of gas coal with a mean particle size of less than 6 mm via line (4) .
  • the gas flame coal (35 wt .-% volatile constituents, stated water / ash free) contains and has a calorific value H u of 26 MJ / kg.
  • the temperature in the gasification stage is 1050 ° C, the carbon conversion about 85 wt .-%.
  • the gas generated is drawn off via line (5), cooled to 900 ° C. in the heat exchanger (6) and desulfurized in the device (7) by adding 5 t / h of CaCO 3 .
  • the dates of the gas are
  • the gas is then fed to the combustion chamber (15) via line (14) and burned there with 3.6 times the stoichiometric amount of air which is introduced via line (16).
  • the resulting flue gas of 1100 ° C is then expanded in the gas turbine (17).
  • the exhaust gas from the gas turbine has a temperature of 550 ° C, a pressure of 1.35 bar, an oxygen content of 13 vol.% And an NO x content of 200 mg / Nm 3 .
  • Terminal power of the gas turbine (17) assigned generator is 97.MW.
  • the gasification residue of 26.7 t / h and the discharges from the devices (7.9 and 10) in a total amount of 5.0 t / h are mixed with a mixing temperature of 955 ° C via line (22) of the circulating fluidized bed (20 ) forwarded. There the combustion takes place with a 25% excess of oxygen at 850 ° C.
  • the distribution of the volumes of fluidizing gas to secondary gas takes place in a ratio of 30:70, the fluidizing gas being composed 1/3 of air (blower 21) and 2/3 of gas turbine exhaust gas supplied via line (18) and having a temperature of 300 ° C. .
  • the secondary gas for the fluidized bed reactor (20) consists exclusively of gas turbine exhaust gas of 550 ° C (line 19).
  • a total of 10% by volume of the gas turbine exhaust gas thus reaches the circulating fluidized bed (20).
  • Steam of 100 bar and 535 ° C. is generated in the circulating fluidized bed (20) and is fed to the steam turbine set (26, 27 and 28) via line (25).
  • the generator assigned to these steam turbines delivers a net output of 116 MW.
  • the exhaust gas from the circulating fluidized bed (20) is cooled in the heat exchanger (29), dedusted in the system (30) and fed to the chimney (31). Due to the favorable combustion conditions, the NOx values are below 175 mg / Nm 3 and the SO x values are below 200 mg / Nm 3 .
  • the gas turbine exhaust gas (90% by volume) not used in the combustion process is fed via line (32) to the heat exchanger system (33), where it is cooled to 100 ° C. with preheating of condensate and generation of steam and finally fed to the fireplace (31).
  • the G achieved in the present example is 42% efel Kochsgrad, wherein the power proportions of steam and gas turbines, such as about 1: 0.83 behave.
  • 40% of the fuel gas generated in the gasification stage (1) is burned with an air excess of 5% in the pressurized combustion chamber (35) to a flue gas of 1100 ° C and expanded in the gas turbine (34).
  • the exhaust gas from the gas turbine (34) has a temperature of 550 ° C., a pressure of approx. 1 bar and an oxygen content of approx. 1 vol.%. It is cooled in the heat exchanger system (33) and placed in the chimney (31) at approx. 100'C.
  • the terminal power of the generator assigned to the gas turbine (34) is 26 MW.
  • the major part of the fuel gas namely the remaining 60%, are fed to the combustion chamber (15) via line (14) and burned with the addition of air of 3.6 times the stoichiometric requirement.
  • the flue gas formed at 1100 ° C is then expanded in the gas turbine (17) and cooled to 550 ° C.
  • the gas turbine exhaust gas has an oxygen content of 13% by volume and a pressure of 1.35 bar.
  • the generator of the gas turbine (17) delivers a terminal power of 58 MW.
  • the gasification residue of 26.7 t / h and the discharges from the devices (7, 9 and 10) in a total amount of 5 t / h are fed through line (22) of the circulating fluidized bed (20) and there with at 850 * C. burnt an excess of oxygen of 25%.
  • the distribution of the volumes of fluidizing gas to secondary gas is 30:70, the fluidizing gas being composed 1/3 of air (blower 21) and 2/3 of gas turbine exhaust gas supplied via line (18). Its temperature is 300 ° C.
  • the secondary gas for the fluidized bed reactor (20) consists exclusively of gas turbine exhaust gas of 550 * C (line 19). A total of 17 vol.% Of the gas turbine exhaust gas reaches the circulating fluidized bed.
  • Steam of 100 bar and 535 ° C. is generated in the circulating fluidized bed (20) and is fed to the steam turbine set (26, 27 and 28) via line (25).
  • the generator of this steam turbine set delivers a net output of 129 MW.
  • Example 1 The exhaust gas from the circulating fluidized bed (20) and the gas turbine exhaust gas not used in the combustion process are carried out as in Example 1.
  • the overall efficiency is 42%.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Treating Waste Gases (AREA)
EP87200488A 1986-04-17 1987-03-17 Cycle combiné à turbines à gaz et à vapeur Expired EP0249255B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT87200488T ATE40182T1 (de) 1986-04-17 1987-03-17 Kombinierter gas-/dampfturbinen-prozess.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19863612888 DE3612888A1 (de) 1986-04-17 1986-04-17 Kombinierter gas-/dampfturbinen-prozess
DE3612888 1986-04-17

Publications (2)

Publication Number Publication Date
EP0249255A1 true EP0249255A1 (fr) 1987-12-16
EP0249255B1 EP0249255B1 (fr) 1989-01-18

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ID=6298844

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Application Number Title Priority Date Filing Date
EP87200488A Expired EP0249255B1 (fr) 1986-04-17 1987-03-17 Cycle combiné à turbines à gaz et à vapeur

Country Status (13)

Country Link
US (1) US4996836A (fr)
EP (1) EP0249255B1 (fr)
JP (1) JPH0680294B2 (fr)
CN (1) CN1011999B (fr)
AT (1) ATE40182T1 (fr)
AU (1) AU586923B2 (fr)
CA (1) CA1297683C (fr)
DE (2) DE3612888A1 (fr)
ES (1) ES2007290B3 (fr)
GR (2) GR880300114T1 (fr)
IN (1) IN165413B (fr)
PT (1) PT84712B (fr)
ZA (1) ZA872750B (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0495130B1 (fr) * 1990-08-13 1996-10-30 Asahi Kasei Kogyo Kabushiki Kaisha Nouvelle resine fluoree et materiau d'enduction a base de celle-ci
CN1304734C (zh) * 2000-06-29 2007-03-14 福斯特能源公司 联合循环发电站以及运行该电站的方法

Families Citing this family (28)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2694870B2 (ja) * 1988-03-04 1997-12-24 ピーピーエス プロジェクト プロモーション サービス アクティーボラーグ 熱・電力同時発生プラント
JPH0617650B2 (ja) * 1988-11-14 1994-03-09 バブ日立エンジニアリングサービス株式会社 ガスタービン排ガス処理方法
DE3907217A1 (de) * 1989-03-07 1990-09-13 Steinmueller Gmbh L & C Verfahren zum betreiben eines kombinierten gasturbinen-/dampfturbinen-prozesses
SE463776B (sv) * 1989-05-26 1991-01-21 Nonox Eng Ab Foerfarande foer att producera elenergi med en acfbc aanggenerator kombinerad med en aangturbinenhet och tvaa gasturbinenheter
DE3924615A1 (de) * 1989-07-26 1991-01-31 Babcock Werke Ag Kombinierter gas/dampfturbinen-prozess
US5078752A (en) * 1990-03-12 1992-01-07 Northern States Power Company Coal gas productions coal-based combined cycle power production
DE4040699A1 (de) * 1990-04-27 1991-10-31 Siemens Ag Kombinierte gas- und dampf-turbinenanlage
DE59203618D1 (de) * 1991-02-26 1995-10-19 Oberoesterr Ferngas Verfahren und Vorrichtung zum Verbrennen von stückigen, biogenen Brennstoffen.
US5190451A (en) * 1991-03-18 1993-03-02 Combustion Power Company, Inc. Emission control fluid bed reactor
US5236354A (en) * 1991-03-18 1993-08-17 Combustion Power Company, Inc. Power plant with efficient emission control for obtaining high turbine inlet temperature
GB9111157D0 (en) * 1991-05-23 1991-07-17 Boc Group Plc Fluid production method and apparatus
JP2544267B2 (ja) * 1991-12-30 1996-10-16 川崎重工業株式会社 石炭部分ガス化発電方法及び装置
RU95105440A (ru) * 1992-07-24 1997-01-10 Феаг Ферайнигте Энергиверке АГ (DE) Способ эксплуатации комбинированной электростанции и устройство для его осуществления
US5251433A (en) * 1992-12-24 1993-10-12 Texaco Inc. Power generation process
GB2274883B (en) * 1993-02-03 1996-09-11 Europ Gas Turbines Ltd Electric power generation system
US5319924A (en) * 1993-04-27 1994-06-14 Texaco Inc. Partial oxidation power system
US5375408A (en) * 1993-07-06 1994-12-27 Foster Wheeler Development Corporation Combined-cycle power generation system using a coal-fired gasifier
US5617715A (en) * 1994-11-15 1997-04-08 Massachusetts Institute Of Technology Inverse combined steam-gas turbine cycle for the reduction of emissions of nitrogen oxides from combustion processes using fuels having a high nitrogen content
DE19622299C2 (de) * 1996-05-21 2000-10-12 Ver Energiewerke Ag Verfahren zum Betrieb einer druckaufgeladenen zirkulierenden Wirbelschichtfeuerung zur Erzeugung eines arbeitsfähigen Gases für die Gasturbine eines Kombikraftwerkes
AU2007262669A1 (en) * 2006-06-23 2007-12-27 Bhp Billiton Innovation Pty Ltd Power generation
AT504863B1 (de) * 2007-01-15 2012-07-15 Siemens Vai Metals Tech Gmbh Verfahren und anlage zur erzeugung von elektrischer energie in einem gas- und dampfturbinen (gud) - kraftwerk
ITBO20070505A1 (it) * 2007-07-20 2009-01-21 Samaya S R L Gruppo per l'abbattimento degli inquinanti dei gas di scarico di macchine a combustione interna
JP5215673B2 (ja) * 2008-01-11 2013-06-19 三菱重工業株式会社 塩化水素供給装置、排ガス処理システム及び塩化水素供給管理システム
FR2947824B1 (fr) * 2009-07-09 2011-10-07 Michel Mazon Procede et installation de valorisation des polyolefines
WO2013010008A1 (fr) * 2011-07-13 2013-01-17 Conocophillips Company Procédé et système de production indirecte de vapeur
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US10414509B2 (en) 2017-02-23 2019-09-17 United Technologies Corporation Propulsor mounting for advanced body aircraft

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
LU83085A1 (fr) * 1981-01-23 1982-09-10 Cockerill Procede de production d'energie au depart de charbon et installation a cet effet
DE3338107A1 (de) * 1982-11-30 1984-05-30 BBC Aktiengesellschaft Brown, Boveri & Cie., Baden, Aargau Kohlegefeuertes kraftwerk mit wirbelschichtfeuerung
US4478039A (en) * 1980-12-29 1984-10-23 United Technologies Corporation Utilization of coal in a combined cycle powerplant
GB2148734A (en) * 1983-10-10 1985-06-05 English Electric Co Ltd Divided fluidised bed

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3086362A (en) * 1957-11-29 1963-04-23 Richard W Foster-Pegg Combined steam-gas turbine plant
US3986348A (en) * 1973-04-25 1976-10-19 Switzer Jr George W Coal-fueled combined cycle power generating system
US3991557A (en) * 1974-07-22 1976-11-16 Donath Ernest E Process for converting high sulfur coal to low sulfur power plant fuel
US4165717A (en) * 1975-09-05 1979-08-28 Metallgesellschaft Aktiengesellschaft Process for burning carbonaceous materials
DE2624302C2 (de) * 1976-05-31 1987-04-23 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur Durchführung exothermer Prozesse
IE51626B1 (en) * 1980-08-18 1987-01-21 Fluidised Combustion Contract A fluidised bed furnace and power generating plant including such a furnace
JPS5752707A (en) * 1980-09-16 1982-03-29 Babcock Hitachi Kk Multi-stage fluidized boiler
DE3113993A1 (de) * 1981-04-07 1982-11-11 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur gleichzeitigen erzeugung von brenngas und prozesswaerme aus kohlenstoffhaltigen materialien
JPS59215906A (ja) * 1983-05-20 1984-12-05 Ishikawajima Harima Heavy Ind Co Ltd 石炭だき二段加熱複合サイクル発電装置

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4478039A (en) * 1980-12-29 1984-10-23 United Technologies Corporation Utilization of coal in a combined cycle powerplant
LU83085A1 (fr) * 1981-01-23 1982-09-10 Cockerill Procede de production d'energie au depart de charbon et installation a cet effet
DE3338107A1 (de) * 1982-11-30 1984-05-30 BBC Aktiengesellschaft Brown, Boveri & Cie., Baden, Aargau Kohlegefeuertes kraftwerk mit wirbelschichtfeuerung
GB2148734A (en) * 1983-10-10 1985-06-05 English Electric Co Ltd Divided fluidised bed

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
PATENT ABSTRACTS OF JAPAN, Band 6, Nr. 126 (M-142)[1004], 10. Juli 1982; & JP-A-57 52 707 (BABCOCK HITACHI K.K.) 29-03-1982 *
PATENT ABSTRACTS OF JAPAN, Band 9, Nr. 87 (M-372)[1810], 17. April 1985; & JP-A-59 215 906 (ISHIKAWAJIMA HARIMA JUKOGYO K.K.) 05-12-1984 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0495130B1 (fr) * 1990-08-13 1996-10-30 Asahi Kasei Kogyo Kabushiki Kaisha Nouvelle resine fluoree et materiau d'enduction a base de celle-ci
CN1304734C (zh) * 2000-06-29 2007-03-14 福斯特能源公司 联合循环发电站以及运行该电站的方法

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EP0249255B1 (fr) 1989-01-18
GR880300114T1 (en) 1989-03-08
DE3760042D1 (en) 1989-02-23
PT84712B (pt) 1989-12-29
CA1297683C (fr) 1992-03-24
ZA872750B (en) 1988-12-28
GR3000048T3 (en) 1990-10-31
PT84712A (de) 1987-05-01
AU7174987A (en) 1987-10-22
US4996836A (en) 1991-03-05
JPH0680294B2 (ja) 1994-10-12
JPS62251428A (ja) 1987-11-02
IN165413B (fr) 1989-10-14
ATE40182T1 (de) 1989-02-15
CN87102746A (zh) 1987-11-04
ES2007290B3 (es) 1990-03-16
DE3612888A1 (de) 1987-10-29
AU586923B2 (en) 1989-07-27
CN1011999B (zh) 1991-03-13

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