EP0363812A2 - Procédé et installation pour la génération de vapeur dans une centrale de cogénération de puissance et de chaleur - Google Patents
Procédé et installation pour la génération de vapeur dans une centrale de cogénération de puissance et de chaleur Download PDFInfo
- Publication number
- EP0363812A2 EP0363812A2 EP89118445A EP89118445A EP0363812A2 EP 0363812 A2 EP0363812 A2 EP 0363812A2 EP 89118445 A EP89118445 A EP 89118445A EP 89118445 A EP89118445 A EP 89118445A EP 0363812 A2 EP0363812 A2 EP 0363812A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- fluidized bed
- free space
- air
- combustion
- heat
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
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Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/002—Fluidised bed combustion apparatus for pulverulent solid fuel
Definitions
- the invention relates to a method for generating steam, in particular in thermal power stations, by means of combustion of solid fuels, in particular coal, by a fluidized bed process in which the combustion takes place in a fluidized bed comprising the fuels at - relatively low - temperatures up to approx. 900 ° C., whereby the gases above the fluidized bed are additionally supplied with heat, and a system for generating steam by burning solid fuels in a stationary fluidized bed boiler, a space for the generated heating gases being formed in the boiler above a fluidized bed, generally made of coal and lime.
- coal as a solid fuel, that is to say a sulfur-containing material, SO2 which forms is converted to calcium sulfate by means of the lime.
- the fluidized bed technology is used in practice, in particular, in thermal power stations with the aim of avoiding the aftertreatment of flue gases to reduce pollutants by regularly burning the solid fuels at low temperatures of around 850 ° C. This ensures that, on the one hand, no or hardly any thermal nitrogen oxide is formed and, on the other hand, SO2 on limestone which forms during the combustion process of coal is optimally converted to calcium sulfate.
- the disadvantage of burning at low temperatures is that toxic carbon monoxide emissions are higher than with conventional rust or coal dust furnaces.
- the atmospheric, stationary fluidized bed boiler which is customary in practice forms a chemical reactor in a steam boiler.
- the most important parameter, the temperature of the fluidized bed cannot be changed independently of the boiler output.
- the temperature in the fluidized bed cannot be raised above 900 ° C, because then the ash softening sets in, which brings the fluidized bed combustion to a standstill.
- a circulating fluidized bed has been developed in which the fluidized bed reactor, the steam boiler and the ash cooler are separate apparatuses. This technology is considerably more expensive to purchase and can therefore only be used economically for larger steam boilers (over 30 t / h).
- a method and a plant for generating steam of the type described at the outset aim to substantially reduce the amount of unburned fuel particles emerging from the fluidized bed in order to reduce the load on the downstream filter.
- solid particles should be combusted. This combustion takes place in the area of a drawn-in flow cross-section of the flue gas flue, that is to say in a zone which is largely dependent on Fluid bed is removed and in which there has already been a significant reduction in the temperature of the exhaust gases after exiting the fluid bed.
- an average temperature of substantially more than 900 ° C. must prevail in the afterburner area in order to be able to carry out the combustion of the solid particles completely.
- This temperature is usually between 1200 and 1600 ° C and the particles have to stay at this temperature for some time. This requires a relatively large space. Following this afterburning, the temperatures drop due to heat dissipation on the heating surfaces.
- This process aims at the combustion of solid particles, which necessitates constructive measures such as narrowing the cross-section of the boiler and a longer, uncooled residence zone behind the flame zone in order to achieve sufficient burnout.
- the disadvantage is that thermal nitrogen oxide is formed by the necessary high temperatures and excess air.
- JP 59-81409 a method is known (JP 59-81409) in which unburned constituents, that is to say both gaseous and solid, are to be burned in the free space above a fluidized bed by supplying gas in flame form.
- unburned constituents that is to say both gaseous and solid
- a coal storage container serves as a further heating gas source, from which exhaust gas is fed to another burner nozzle via a flap.
- the aim of this process is to lower the fluidized bed temperature to 700 ° in order in any case to generate thermal nitrogen oxides, that is to say additional nitrogen oxides to those which occur when the coal decays thermally during combustion to avoid the result of the nitrogen compounds present in this.
- thermal nitrogen oxides that is to say additional nitrogen oxides to those which occur when the coal decays thermally during combustion to avoid the result of the nitrogen compounds present in this.
- a two-stage furnace with a first stage in the form of a pyrolysis or smoldering chamber and a second stage in the form of a post-combustion chamber is known (DE-A1 35 03 603), in which the latter is designed as a cyclone. Otherwise the ash would not be separated.
- the aim of the two-stage incineration is to avoid the evaporation of heavy metals, such as those that occur in particular during waste disposal. The aim of this is to ensure that non-combustible, environmentally harmful substances such as heavy metals can be brought into the gas phase and released into the environment with the exhaust gas or have to be separated again by means of complex other processes.
- the low air supply therefore only serves to keep the temperatures in the smoldering chamber low.
- the reduced air supply for temperature control is used here, with the aim of avoiding excessive gas pressure of the heavy metals. Due to the low air supply in the first combustion stage and the - targeted - low temperatures, there are high unburned proportions, so that in the second combustion phase not only the air required for combustion has to be supplied, but also a particularly good mixing of the air with the combustion air Gases must occur, which is why the arrangement of a technically complex cyclone is expressly required.
- the invention is therefore based on the object to improve the fluidized bed technology and these realizing systems, that is to say steam generation using atmospheric, stationary fluidized bed boilers, in such a way that they meet the requirements for optimum air purity with regard to their emission behavior.
- the additional heat is supplied in the free space above the fluidized bed, the amount of air to be fed to the fluidized bed is kept below the stoichiometrically required amount of air while maintaining the combustion temperature, and the air supply to the free space is increased while the system is in operation
- the free space is assigned at least one heat source, for example a burner, for additional, targeted energy supply and a device for supplying additional air into the combustion gases located in the free space.
- the free space temperature can be made independent of the operation of the fluidized bed temperature by the supply of heat to the free space and can be influenced in a targeted manner.
- the reaction rate when converting the carbon monoxide with oxygen to carbon dioxide can be increased considerably. As experiments have shown, this achieves a considerably low level Lower levels of carbon monoxide in the exhaust gas and the temperature of the fluidized bed can be kept at low values.
- the free space is a zone of the boiler which belongs to the cross section of the combustion chamber caused by the fluidized bed, i.e. is not a constriction in the exhaust gas flue gas duct, but a space in which the fuel particles are caused to do so due to a reduction in the gas velocity - fall back into the fluidized bed due to gravity. How much free space ultimately depends on the design conditions.
- the air supply to the fluidized bed is not throttled in the invention for the purpose of reducing the fluidized bed temperature.
- the fluidized bed should always be kept within the economically sensible limits, i.e. at approximately 850 °, in order to remain just below the sintering limit and to be able to keep the size of the system to a minimum in the design of the system.
- the temperature in the fluidized bed should explicitly not be reduced, because such a drop in temperature would reduce the reaction rate in the conversion of CO and NO x to CO2 and N2.
- the atmospheric, stationary fluidized bed boilers for all performance classes can comply with the legally prescribed values for CO of less than 250 mg / m3 flue gas and for NO x of less than 500 mg / m3 at full load and part load .
- the heat can be applied directly above the fluidized bed.
- the lowering of the temperature caused by the substoichiometric air supply can advantageously be compensated for by an increased supply of coal to the fluidized bed.
- an increased supply of coal to the fluidized bed there is no loss of energy because the energy potential of the carbon that is not used in the fluidized bed is recovered in the oxidation of the CO in the free space.
- this shift in energy conversion from the fluidized bed to the free space is only in the order of 1 - 3%.
- air becomes air over an air boweinrichting 6 supplied controlled.
- Above the fluidized bed there is a free space 3 for the rising combustion gases, as well as the usual steam generation system, which need not be described in more detail here.
- Two burners 4 each, which are operated with natural gas, and two additional air supply devices 5 open into the free space.
- the burners 4 serve to increase the free space temperature; any other heat sources, for example electrical ones, can of course also be used in their place.
- the free space temperature is increased to values above 900 ° C and an effective conversion of CO in the flue gas to harmless CO2 is achieved.
- the air supply via the air supply device 6 By reducing the air supply via the air supply device 6, the CO formation is initially increased by the accumulation in the fluidized bed during combustion Convert nitrogen oxides to elemental nitrogen, while the excess CO is then converted to CO2 by supplying air via the additional air supply devices 5 and supplying heat via the heat source 4.
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE3834801 | 1988-10-10 | ||
| DE3834801 | 1988-10-10 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| EP0363812A2 true EP0363812A2 (fr) | 1990-04-18 |
| EP0363812A3 EP0363812A3 (fr) | 1991-02-27 |
Family
ID=6364978
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP19890118445 Withdrawn EP0363812A3 (fr) | 1988-10-10 | 1989-10-04 | Procédé et installation pour la génération de vapeur dans une centrale de cogénération de puissance et de chaleur |
Country Status (1)
| Country | Link |
|---|---|
| EP (1) | EP0363812A3 (fr) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1991005205A1 (fr) * | 1989-10-05 | 1991-04-18 | L. & C. Steinmüller Gmbh | Procede pour reduire la teneur en oxydes nitriques dans les gaz de fumee d'une installation de chauffe |
| WO1991016575A1 (fr) * | 1990-04-17 | 1991-10-31 | A. Ahlstrom Corporation | Procede et appareil de reduction des emissions de n2o produites par combustion de combustibles contenant de l'azote dans des reacteurs a lit fluidise |
| WO1993022600A1 (fr) * | 1992-04-30 | 1993-11-11 | Abb Carbon Ab | Procede permettant de maintenir une temperature de travail nominale dans les gaz de combustion d'une centrale electrique a lit fluidise sous pression |
| DE4224959A1 (de) * | 1992-07-24 | 1994-01-27 | Ver Energiewerke Ag | Verfahren und Anordnung zum Betreiben eines Kombikraftwerkes |
| US5634329A (en) * | 1992-04-30 | 1997-06-03 | Abb Carbon Ab | Method of maintaining a nominal working temperature of flue gases in a PFBC power plant |
| WO1997039280A1 (fr) * | 1996-04-12 | 1997-10-23 | Abb Carbon Ab | Methode de combustion et installation de combustion servant a bruler un combustible complementaire dans la zone de revanche d'un lit fluidise sous pression |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2023268A (en) * | 1978-04-08 | 1979-12-28 | Worsley & Co Ltd G P | Fluidized bed furnaces |
| US4308810A (en) * | 1980-04-09 | 1982-01-05 | Foster Wheeler Energy Corporation | Apparatus and method for reduction of NOx emissions from a fluid bed combustion system through staged combustion |
| JPS5981408A (ja) * | 1982-11-02 | 1984-05-11 | Babcock Hitachi Kk | 流動層ボイラ |
| JPS59167608A (ja) * | 1983-03-15 | 1984-09-21 | Babcock Hitachi Kk | 流動層燃焼装置 |
| US4543894A (en) * | 1983-05-17 | 1985-10-01 | Union Oil Company Of California | Process for staged combustion of retorted oil shale |
| JPS61173012A (ja) * | 1985-01-24 | 1986-08-04 | Hitachi Zosen Corp | 流動床ボイラ |
| GB2192141A (en) * | 1986-07-04 | 1988-01-06 | Politechnika Slaska Im Wincent | Combustion of solid fuels |
-
1989
- 1989-10-04 EP EP19890118445 patent/EP0363812A3/fr not_active Withdrawn
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2023268A (en) * | 1978-04-08 | 1979-12-28 | Worsley & Co Ltd G P | Fluidized bed furnaces |
| US4308810A (en) * | 1980-04-09 | 1982-01-05 | Foster Wheeler Energy Corporation | Apparatus and method for reduction of NOx emissions from a fluid bed combustion system through staged combustion |
| US4308810B1 (fr) * | 1980-04-09 | 1993-08-03 | Foster Wheeler Energy Corp | |
| JPS5981408A (ja) * | 1982-11-02 | 1984-05-11 | Babcock Hitachi Kk | 流動層ボイラ |
| JPS59167608A (ja) * | 1983-03-15 | 1984-09-21 | Babcock Hitachi Kk | 流動層燃焼装置 |
| US4543894A (en) * | 1983-05-17 | 1985-10-01 | Union Oil Company Of California | Process for staged combustion of retorted oil shale |
| JPS61173012A (ja) * | 1985-01-24 | 1986-08-04 | Hitachi Zosen Corp | 流動床ボイラ |
| GB2192141A (en) * | 1986-07-04 | 1988-01-06 | Politechnika Slaska Im Wincent | Combustion of solid fuels |
Non-Patent Citations (3)
| Title |
|---|
| PATENT ABSTRACTS OF JAPAN, Band 10, Nr. 381 (M-547)[2438], 19. Dezember 1986; & JP-A-61 173 012 (HITACHI) 04-08-1986 * |
| PATENT ABSTRACTS OF JAPAN, Band 8, Nr. 191 (M-322)[1628], 4. September 1984; & JP-A-59 81 408 (BABCOCK) 11-05-1984 * |
| PATENT ABSTRACTS OF JAPAN, Band 9, Nr. 22 (M-354)[1745], 30. Januar 1985; & JP-A-59 167 608 (BABCOCK) 21-09-1984 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1991005205A1 (fr) * | 1989-10-05 | 1991-04-18 | L. & C. Steinmüller Gmbh | Procede pour reduire la teneur en oxydes nitriques dans les gaz de fumee d'une installation de chauffe |
| WO1991016575A1 (fr) * | 1990-04-17 | 1991-10-31 | A. Ahlstrom Corporation | Procede et appareil de reduction des emissions de n2o produites par combustion de combustibles contenant de l'azote dans des reacteurs a lit fluidise |
| WO1993022600A1 (fr) * | 1992-04-30 | 1993-11-11 | Abb Carbon Ab | Procede permettant de maintenir une temperature de travail nominale dans les gaz de combustion d'une centrale electrique a lit fluidise sous pression |
| US5634329A (en) * | 1992-04-30 | 1997-06-03 | Abb Carbon Ab | Method of maintaining a nominal working temperature of flue gases in a PFBC power plant |
| DE4224959A1 (de) * | 1992-07-24 | 1994-01-27 | Ver Energiewerke Ag | Verfahren und Anordnung zum Betreiben eines Kombikraftwerkes |
| WO1997039280A1 (fr) * | 1996-04-12 | 1997-10-23 | Abb Carbon Ab | Methode de combustion et installation de combustion servant a bruler un combustible complementaire dans la zone de revanche d'un lit fluidise sous pression |
| US6260492B1 (en) | 1996-04-12 | 2001-07-17 | Abb Carbon Ab | Method and apparatus for burning fuel in the free board of a pressurized fluidized bed with solids recirculation |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0363812A3 (fr) | 1991-02-27 |
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| STAA | Information on the status of an ep patent application or granted ep patent |
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| 18W | Application withdrawn |
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