EP0302910B1 - Combustion de charbon avec un foyer a lit fluidise - Google Patents

Combustion de charbon avec un foyer a lit fluidise Download PDF

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Publication number
EP0302910B1
EP0302910B1 EP88901248A EP88901248A EP0302910B1 EP 0302910 B1 EP0302910 B1 EP 0302910B1 EP 88901248 A EP88901248 A EP 88901248A EP 88901248 A EP88901248 A EP 88901248A EP 0302910 B1 EP0302910 B1 EP 0302910B1
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EP
European Patent Office
Prior art keywords
fluidized bed
coal
steam generator
combustion
bed furnace
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.)
Expired - Lifetime
Application number
EP88901248A
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German (de)
English (en)
Other versions
EP0302910A1 (fr
Inventor
Hermann Brückner
Lothar Stadie
Gerhard Scholl
Karl-Ewald Stoll
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Saarbergwerke AG
Siemens AG
Original Assignee
Saarbergwerke AG
Siemens AG
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Filing date
Publication date
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Priority claimed from DE19873701798 external-priority patent/DE3701798A1/de
Priority claimed from DE19873733831 external-priority patent/DE3733831A1/de
Application filed by Saarbergwerke AG, Siemens AG filed Critical Saarbergwerke AG
Publication of EP0302910A1 publication Critical patent/EP0302910A1/fr
Application granted granted Critical
Publication of EP0302910B1 publication Critical patent/EP0302910B1/fr
Anticipated expiration legal-status Critical
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements or dispositions of combustion apparatus
    • F22B31/0007—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements or dispositions of combustion apparatus with combustion in a fluidized bed
    • F22B31/0069—Systems therefor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/30—Halogen; Compounds thereof
    • F23J2215/301—Dioxins; Furans

Definitions

  • the invention relates to a process for the combustion of coal and possibly a mixture of coal and organic substances, such as household waste, industrial waste or the like, using a fluidized bed combustion with an average combustion temperature of 800 ° C. and afterburning of unburned fuel discharged from the fluidized bed and firing system for carrying out the process.
  • fluidized bed furnaces have long been state of the art for a wide variety of applications.
  • the main advantages can be seen in the fact that, in contrast to other types of firing, low-quality fuels with high ballast content, such as.
  • B. ballast coal or processing waste which are a by-product of hard coal processing, or other organic substances, such as household waste, industrial waste and the like, can be burned in a wide variety of compositions.
  • fluidized bed combustion is its comparatively environmental friendliness, since at the relatively low combustion temperatures of approx. 800 ° C there are almost no nitrogen oxides and other pollutants, such as. B. sulfur oxides, by adding suitable adsorbents, such as. B. limestone, can already be largely bound in the fluidized bed.
  • the fluidized bed combustion is characterized by a homogeneous temperature distribution in the fluidized bed, so that especially when burning less homogeneous, waste containing organic substances, such as B. household waste or industrial waste, a good burnout is guaranteed.
  • the aim is therefore to reduce pollutant emissions from the outset through so-called primary measures that affect the combustion plants themselves, for example through low-NOx burners or through the use of fluidized bed combustion systems with heat exchanger heating surfaces.
  • the heat exchanger surfaces of fluidized bed furnaces are exposed to increased erosion and corrosion.
  • the fluidized bed combustion is also limited by the fact that due to the relatively low combustion temperatures in the event that the substances to be burned organic or inorganic chlorine compounds such as e.g. B. contain polychlorinated biphenyls (PCB), when burning highly toxic dioxins, such as. B. polychlorinated dibenzodioxins (PCDD) or polychlorinated dibenzofurans (PCDF).
  • PCB polychlorinated biphenyls
  • PCDD polychlorinated dibenzodioxins
  • PCDF polychlorinated dibenzofurans
  • a fluidized bed combustion is known with an afterburning zone arranged directly above the fluidized bed, into which a gaseous or liquid, ie a well-igniting additional fuel is inserted via pilot burners is brought to achieve a complete afterburning of unburned fuel discharged from the fluidized bed.
  • the known system does not reach temperatures high enough for the destruction of dioxins or furans, since only as much additional fuel is to be introduced as is necessary for complete post-combustion of the entrained primary fuel is.
  • the aim of the known system is therefore not the detoxification of the flue gases, but the discharge of the dust filter and the full utilization of the primary fuel, whereby it is expressly assumed that this more than compensates for the higher costs.
  • This system is also not suitable for burning waste materials such as waste. Since the flue gases from the fluidized bed combustion are only added to the flue gases from the steam generator, they are not heated to a high enough level to ensure that the pollutants generated when burning waste are destroyed.
  • DE-A-3 330 943 describes a system in which coal is burned in a charged fluidized bed with excess air and the flue gases are cooled in an unfired steam generator immediately downstream of the fluidized bed combustion. The flue gases are then dedusted so that they can be introduced into the combustion chamber of a gas turbine. A gas turbine fuel is also introduced and burned in the combustion chamber, the required combustion air being carried as excess air already in the flue gas of the fluidized bed furnace.
  • This known system is also not suitable for burning a coal-waste mixture in the fluidized bed, since the dioxins and furans formed during the combustion of the waste portion are at least to a large extent separated with the dust and are therefore not “reheated” at all. Rather, the separated dust is now contaminated with these pollutants and is therefore to be regarded as special waste and must be treated or disposed of accordingly.
  • the fluidized bed combustion must also be operated with excess air, since on the one hand the flue gases have to carry an air surplus sufficient for the combustion of the gas turbine fuel, and on the other hand it must be ensured that the flue gases no longer carry any combustible residual solids which lead to problems in the filters, especially in the electrostatic precipitator , being able to lead.
  • the object of the invention is to develop a method and a system which ensure that, on the one hand, the formation of highly toxic dioxins is prevented during the combustion of wastes containing organic substances, but which, on the other hand, also ensure that only coal is burned, that no large amounts of nitrogen oxides are formed at all, so that downstream DENOX systems for flue gas treatment become superfluous.
  • this object is achieved in that the flue gases of the fluidized bed combustion without cooling and cleaning together with the entrained flue dust below the flame zone into the combustion chamber of a steam generator fired with coal dust and introduced in this to the usual temperatures for coal dust furnaces be heated above 1 000 ° C.
  • the entire flue gases from the fluidized bed combustion system, together with the fly dust, are forcibly passed through the flame zone of the coal dust combustion system of the steam generator, where - in addition to the heating - the trace elements and heavy metals, which are partly molecularly or colloidally distributed in the coal dust combustion system and in the flue gas, cause the catalytic effect of the Hard coal on the regression of the Dioxins and furans have an optimal effect.
  • the fluidized bed combustion can, depending on the type and proportion of the waste to be incinerated, be operated stoichiometrically or - in particular when coal is being burned alone - under stoichiometric, whereby a substantial reduction in nitrogen oxide formation is achieved compared to an over-stoichiometric fluidized bed combustion .
  • the heat generated in the fluidized bed is discharged with the flue gas and released in the steam generator together with the heat generated there to the steam cycle of the power plant.
  • a constant temperature level of, for example, 800 ° C it proves to be expedient to continuously return part of the cooled and possibly already cleaned flue gases from the steam generator as cooling medium to the fluidized bed furnace, with the ratio of returned flue gas
  • Fresh air can also be set in a very simple manner in the fluidized bed firing a substoichiometric atmosphere if at least part of the recirculated flue gas is mixed with the fresh air.
  • a combustion system according to the invention with a fluidized bed combustion and a post-combustion zone is characterized in that the fluidized bed combustion as a post-combustion zone is a coal dust operated at a temperature above 1000 ° C. is fired steam generator of a coal-fired power plant, that the fluidized bed combustion is designed without heat exchange surfaces and that the flue gas discharge of the fluidized bed combustion is connected directly below the burner with the steam generator without the interposition of cooling or cleaning devices.
  • FIGS. 1 and 2 Further explanations of the invention can be found in the exemplary embodiments shown schematically in FIGS. 1 and 2.
  • Fig. 1 A furnace according to the invention for the combustion, in particular of waste containing organic substances.
  • Fig. 2 A furnace according to the invention using the example of a steam generator system.
  • FIG. 1 shows schematically a fluidized bed furnace 1 with a fluidized bed 11, in which organic waste materials fed via line 12, to which coal can optionally be added via line 13, are burned at an average combustion temperature of approximately 800 ° C.
  • the fluidized bed furnace 1 is followed by a steam generator 2 of a coal-fired power plant, which is fired with coal dust 21 - with the supply of fresh air 22.
  • the flue gases of the fluidized bed furnace 1 including entrained fuel and ash particles, are introduced into the steam generator 2 below the furnace zone 23 via line 14.
  • the flue gases introduced from the fluidized bed firing 1 are heated to temperatures above 1000 ° C.
  • pollutants such as dioxins which have arisen in the fluidized bed furnace 1 and are carried in the flue gas are destroyed.
  • the mixed flue gases from the fluidized bed furnace 1 and the steam generator 2 are drawn off via line 25 after they have given up the essential part of their heat to the water to be evaporated via a heat exchanger 24, dedusted in an electrostatic filter 3, and possibly further cooled in a heat exchanger 5 , cleaned in a flue gas scrubber 4 and largely discharged into the atmosphere via line 41.
  • a portion of the flue gases is branched off - either via line 42 before the flue gas scrubber 4 or via line 43 after the flue gas scrubber 4 and returned to the fluidized bed 11 via line 44 and a pressure-increasing blower 26 together with fresh air drawn in via line 27.
  • the combustion temperature of approx. 800 ° C. aimed at in the fluidized bed furnace 1 can be maintained via the amounts of the fuel supplied, the fresh air drawn in and the recirculated flue gas, and it may be expedient to limit part of the recirculated cold in order to limit the flow velocity in the fluidized bed 11 Introduce flue gases into the fluidized bed furnace 1 exclusively for the purpose of dissipating heat from the fluidized bed furnace 1 via line 45 above the fluidized bed 11.
  • the coarse ash is separated from the ash drawn off from the steam generator 2 via line 28 and is returned to the fluidized bed 11 via line 29, if necessary after additional cooling, as bed material.
  • the coarse ash is gradually crushed and entrained in the steam generator 2 together with the flue gases as flue dust.
  • the coarse-grained fraction can be separated from the fly ash separated in the electrostatic filter 3 and returned to the fluidized bed 11 via lines 31 and 29. The medium and fine-grained fractions are withdrawn via line 32.
  • FIG. 2 shows a schematic representation of the example of a steam generator system according to the invention.
  • This consists of a steam generator 2, which is equipped with a coal dust burner 30.
  • the surrounding walls 40 of the steam generator 2 are designed as fin tube walls and, in a manner known per se, together with the other heat exchanger heating surfaces 24 of the steam generator 2, are connected to a steam circuit, not shown here.
  • a dust filter 3, a suction fan 10 and a flue gas desulfurization system 4 are connected to the flue gas line 9 leaving the steam generator 2 and leading to the chimney 8.
  • the steam generator 2 is connected on the gas side to a fluidized bed furnace 1 with a stationary fluidized bed 11.
  • the nozzle base 15 is connected to a gas line 16 which is connected with one branch to the part of the flue gas line 9 leaving the flue gas desulfurization system 4 and with another branch to a fresh air intake opening 17.
  • a gas compressor 18 is installed on the nozzle bottom 15 to generate the necessary pressure difference.
  • a control valve 19, 20 is installed in each of the branch of the gas line 16 leading to the flue gas line 9 as well as to the branch leading to the fresh air intake opening 17.
  • the fluidized bed furnace 1 is also connected to the flue gas line 9 above the stationary fluidized bed 11 via an additional gas line 42. This branches off from the flue gas line 9 immediately behind the induced draft fan 10.
  • a control valve 6 is also installed in this additional gas line.
  • the fluidized bed furnace 1 is connected to a fuel supply line 53, which in turn is connected to a coal bunker 54 and a lime bunker 55.
  • the exhaust gas line 56 of the fluidized bed furnace 1 opens at the lower end of the steam generator 2. Above the level of the mouths of the exhaust gas lines 56 of the fluidized bed furnace 1 in Steam generator 2, the burner 57 of the coal dust burner 30 is installed in the peripheral wall 40 of the steam generator 2. The burner 57 is connected to a coal bunker 59 via a fuel line 58 and to a fresh air blower 33 via a fresh air line.
  • the steam generator system can also be equipped with a further auxiliary line 63, indicated by dashed lines, which on the one hand connects to the gas line 16 directly in front of the gas compressor 18 and connects it to the fresh air line 22 of the steam generator 2.
  • a flue gas blower 34 is installed in this auxiliary line 63.
  • flue gas is sucked in via the gas compressor 18 and pressed through the nozzle bottom 15 of the fluidized bed furnace 1.
  • Fresh air has previously been added to this flue gas via the fresh air intake opening 17.
  • the required mixing ratio, ie the required oxygen content can be set by the control valves 19, 20 installed both at the fresh air intake opening 17 and in the branches of the gas line 16 leading to the flue gas line 9.
  • the fluidized bed furnace 1 is supplied with finely ground coal and a predetermined amount of lime via the fuel supply line 53.
  • the carbon particles introduced into the fluidized bed furnace 1 oxidize in the fluidized bed 11, carbon monoxide predominantly being produced as a result of the substoichiometric addition of oxygen.
  • the sulfur contained in the fuel is bound to gypsum by the lime added to the coal in the fluidized bed 11 and discharged with the ash in a manner not shown here.
  • the oxidation of the sulfur previously required to bind the sulfur limits the extent of the sub-stoichiometric addition of oxygen in the fluidized bed 11.
  • the formation of nitrogen oxides can then not only be stopped by adding large amounts of flue gases via the additional gas line 42, but even to a small extent Reduce nitrogen oxides that have already formed.
  • the temperature in the fluidized bed furnace 1 can be lowered by the addition of cool flue gases, and the rate of formation of nitrogen oxides can be further reduced in this way.
  • the fluidized bed furnace 1 is designed without cooled peripheral walls and without other heat exchanger heating surfaces. As a result, local temperature drops in the fluidized bed 11 are avoided, which could otherwise result in the loss of turnover in the fluidized bed 11.
  • the introduction of flue gas via the additional line 42 has the effect that the calorific value of the exhaust gas from the fluidized bed furnace 1, which is fed into the steam generator 2 via the exhaust line 56, is greatly reduced. This in turn leads to a lower firing temperature of these gases in the steam generator 2 and also reduces the nitrogen oxide formation there.
  • the coal dust burner 57 is in turn the prerequisite for the stronger admixing of smoke gases from the steam generator 2 to the exhaust gases from the fluidized bed furnace 1.
  • the shunt line 62 makes it possible to selectively add flue gas to the fluidized bed furnace 1 and to remove this in front of the flue gas desulfurization system 4 of the flue gas line 9 at a somewhat higher temperature or behind the flue gas desulfurization system 4 at a somewhat lower temperature.
  • the temperature in the fluidized bed furnace 1 can thus be regulated in addition to the measures already described.
  • the flame temperature of the pulverized coal burner 57 of the steam generator 2 can also be reduced by adding flue gas to the fresh air line 22 via the auxiliary line 63.
  • a further flue gas blower 34 is installed in the auxiliary line 63 branching off in front of the gas compressor 18.
  • the fluidized bed combustion 1 is carried out without cooled peripheral walls and heat exchanger heating surfaces, local temperature drops in the fluidized bed 11 are avoided, which at these low temperatures the risk of local hypothermia of the fluidized bed 11 with the result of extinguishing reduced.
  • the formation rate of nitrogen oxides in the fluidized bed furnace 1 is also additionally reduced by the fact that fresh air is supplied to the fluidized bed furnace 1 in a substoichiometric amount. This lack of oxygen also hinders nitrogen oxide formation.
  • the operating conditions of the steam generator 2 can be regulated within wide limits and the advantages of both individual firing systems are used to a greater extent to prevent the formation of nitrogen oxides on the primary side to suppress that it can meet the emission conditions even without a DENOX system connected downstream of the flue gas stream.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

Dans un procédé pour la combustion de substances organiques, telles que des ordures ménagères, des déchets industriels ou analogue, dans un foyer à lit fluidisé (1) à une température de combustion moyenne de 800°C, les gaz de fumée dudit foyer (1) sont chauffés avec la poussière en suspension associée à une température d'au moins 900°C, de préférence 1000°C à 1200°C, dans une zone de chauffage (23) en aval, afin de détruire les substances toxiques, comme la dioxine, éventuellement produites lors de la combustion des substances organiques. Avantageusement, les gaz de fumée sont introduits dans la chambre de chauffe d'une chaudière industrielle, par exemple d'un générateur de vapeur (2) d'une centrale à charbon. En branchant côté gaz un foyer à lit fluidisé (1) en amont d'un générateur de vapeur (2) brûlant du charbon, on obtient une réduction sensible de la formation de NOx.

Claims (5)

1. Procédé de combustion de charbon et éventuellement d'un mélange de charbon et de substances organiques, telles que des ordures ménagères, des déchets industriels et des matières analogues, par utilisation d'un chauffage à lit fluidisé présentant une température de combustion moyenne de 800°C et une post-combustion de combustible non brûlé, évacué du lit fluidisé, procédé dans lequel les gaz de fumée du chauffage à lit fluidisé sont, sans refroidissement et purification, introduits, conjointement aux cendres volantes entraînées, en dessous de la zone des flammes de la chambre de chauffe d'un générateur de vapeur, chauffé au charbon pulvérisé, d'une usine génératrice et ils sont chauffés dans cette chambre à des températures supérieures à 1000°C, courantes pour des chauffages au charbon pulvérisé.
2. Procédé suivant la revendication 1, caractérisé en ce que le chauffage à lit fluidisé est mis en service dans une atmosphère ajustée d'une manière inférieure à la stoechiométrie à égale à celle-ci.
3. Procédé suivant la revendication 1, caractérisé en ce qu'une partie des gaz de fumée quittant le générateur de vapeur est recyclée en continu dans le chauffage à lit fluidisé après qu'un refroidissement et éventuellement une purification ont eu lieu.
4. Procédé suivant la revendication 3, caractérisé en ce que du gaz de fumée refroidi, recyclé, est mélangé à l'air de combustion qui s'écoule vers le fond à tuyères du chauffage à lit fluidisé.
5. Installation de chauffage pour la combustion de charbon et éventuellement d'un mélange de charbon et de substances organiques, pour la mise en oeuvre du procédé suivant l'une des revendications 1 à 4, comprenant un chauffage à lit fluidisé (1) présentant une température de combustion moyenne de 800°C et une zone de post-combustion, installation dans laquelle, en aval du chauffage à lit fluidisé (1) est monté, en tant que zone de post-combustion, un générateur de vapeur (2) d'une usine génératrice qui est mis en service à une température supérieure à 1000°C et est chauffé au charbon pulvérisé, le chauffage à lit fluidisé (1) étant réalisé sans surfaces d'échange thermique et l'évacuation des gaz de fumée (56) du chauffage à lit fluidisé (1) étant reliée au générateur de vapeur directement en dessous du brûleur (57), sans intercalation de dispositifs de refroidissement ou de purification.
EP88901248A 1987-01-22 1988-01-21 Combustion de charbon avec un foyer a lit fluidise Expired - Lifetime EP0302910B1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE19873701798 DE3701798A1 (de) 1987-01-22 1987-01-22 Dampferzeugeranlage mit einem kohlebefeuerten dampferzeuger
DE3701798 1987-01-22
DE3733831 1987-10-07
DE19873733831 DE3733831A1 (de) 1987-10-07 1987-10-07 Verfahren zur verbrennung von organischen substanzen, wie hausmuell, industriemuell und aehnlichem, unter verwendung einer wirbelschichtfeuerung

Publications (2)

Publication Number Publication Date
EP0302910A1 EP0302910A1 (fr) 1989-02-15
EP0302910B1 true EP0302910B1 (fr) 1992-07-15

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ID=25851774

Family Applications (1)

Application Number Title Priority Date Filing Date
EP88901248A Expired - Lifetime EP0302910B1 (fr) 1987-01-22 1988-01-21 Combustion de charbon avec un foyer a lit fluidise

Country Status (5)

Country Link
US (1) US4932335A (fr)
EP (1) EP0302910B1 (fr)
DE (1) DE3872787D1 (fr)
DK (1) DK165762C (fr)
WO (1) WO1988005494A1 (fr)

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US11919201B2 (en) 2018-12-19 2024-03-05 Next Generation Recyclingmaschinen Gmbh Processing plant and method for processing plastics material for the recycling thereof

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US5507238A (en) * 1994-09-23 1996-04-16 Knowles; Bruce M. Reduction of air toxics in coal combustion gas system and method
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ES2156095B1 (es) * 1999-12-07 2002-03-01 Gil Alfredo Peris Depurador de dioxinas y toxicos organicos volatiles de alta resistencia termica.
US6883444B2 (en) * 2001-04-23 2005-04-26 N-Viro International Corporation Processes and systems for using biomineral by-products as a fuel and for NOx removal at coal burning power plants
CN100396993C (zh) * 2005-05-27 2008-06-25 中国科学院工程热物理研究所 一种为煤粉锅炉的煤粉直燃提供高温空气的方法
DE102005036792A1 (de) * 2005-08-02 2007-02-08 Ecoenergy Gesellschaft Für Energie- Und Umwelttechnik Mbh Verfahren und Vorrichtung zur Erzeugung von überhitztem Dampf
CN101158468B (zh) * 2007-09-30 2011-08-31 中国科学院工程热物理研究所 煤粉高温预热方法
CN102276130B (zh) * 2011-05-31 2013-06-05 陈海渊 污泥资源化处理装置及其对污泥进行处理的方法

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DE3136480A1 (de) * 1981-09-15 1983-06-30 Steag Ag, 4300 Essen Verfahren und anordnung zum wiederaufheizen von nassentschwefelten rauchgasen
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Publication number Priority date Publication date Assignee Title
US11919201B2 (en) 2018-12-19 2024-03-05 Next Generation Recyclingmaschinen Gmbh Processing plant and method for processing plastics material for the recycling thereof

Also Published As

Publication number Publication date
WO1988005494A1 (fr) 1988-07-28
US4932335A (en) 1990-06-12
EP0302910A1 (fr) 1989-02-15
DK165762C (da) 1993-05-24
DK524388A (da) 1988-11-18
DE3872787D1 (de) 1992-08-20
DK524388D0 (da) 1988-09-21
DK165762B (da) 1993-01-11

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