EP0302910A1 - Combustion de charbon avec un foyer a lit fluidise. - Google Patents

Combustion de charbon avec un foyer a lit fluidise.

Info

Publication number
EP0302910A1
EP0302910A1 EP88901248A EP88901248A EP0302910A1 EP 0302910 A1 EP0302910 A1 EP 0302910A1 EP 88901248 A EP88901248 A EP 88901248A EP 88901248 A EP88901248 A EP 88901248A EP 0302910 A1 EP0302910 A1 EP 0302910A1
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
furnace
flue gas
combustion
steam generator
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.)
Granted
Application number
EP88901248A
Other languages
German (de)
English (en)
Other versions
EP0302910B1 (fr
Inventor
Hermann Bruckner
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
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=25851774&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=EP0302910(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Priority claimed from DE19873701798 external-priority patent/DE3701798A1/de
Priority claimed from DE19873733831 external-priority patent/DE3733831A1/de
Application filed by Saarbergwerke 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
Expired - Lifetime legal-status Critical Current

Links

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 of dispositions of combustion apparatus
    • F22B31/0007—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of 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 / or waste materials containing organic substances, such as household waste, industrial waste and the like, using a fluidized bed combustion with an average combustion temperature of approx. 800 ° C., and a combustion plant for carrying out the process .
  • Fluid bed furnaces have long been state of the art in numerous designs 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 a high ballast content, e.g. Ballast coal or processing exits, which are a by-product of hard coal processing, or other organic substances, such as in particular household waste, industrial waste and the like, can be burned in a wide variety of compositions.
  • ballast coal or processing exits which are a by-product of hard coal processing, or other organic substances, such as in particular household waste, industrial waste and the like, can be burned in a wide variety of compositions.
  • the fluidized bed combustion is its comparatively environmental friendliness, since at the relatively low combustion temperatures of approximately 800 ° C it is almost No nitrogen oxides are formed and other pollutants, such as sulfur oxides, can already be largely bound in the fluidized bed by adding suitable adsorbents, such as limestone.
  • the fluidized bed firing is characterized by a homogeneous temperature distribution in the fluidized bed, so that a good burnout is ensured, in particular when burning less homogeneous waste materials containing organic substances, such as household or industrial waste.
  • the aim is therefore to reduce the pollutant emissions from the outset by so-called primary measures which affect the combustion plants themselves, for example by low-NOx burners or by using fluidized-bed firing with heat exchanger heating surfaces.
  • the invention is based on the object of developing a method and a system which ensure that, on the one hand, the formation of highly toxic dioxins is prevented during the combustion of waste 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.
  • the invention succeeds in rendering highly toxic dioxins, which are known to oxidize to non-toxic organic substances at temperatures above 900 ° C., preferably between 1,000 and 1,200 ° C., harmless.
  • the flue gases from the fluidized bed furnace can be heated to a temperature of at least 900 ° C. either directly, for example by mixing with a hot gas, or indirectly by supplying heat by means of a suitable heat exchanger.
  • the waste materials to be burned can also be mixed with other organic substances, such as Hard coal or lignite are burned, in which case the entire amount of smoke gases to be heated to the minimum temperature of 900 ° C.
  • Such a procedure should always prove to be useful if a larger fluidized bed system is already in operation at an existing location.
  • the fluidized bed firing used in the method according to the invention is used without immersion heating surfaces, i.e. without heat exchanger surfaces in the fluidized bed, whereby the temperature can be regulated by regulating the material turnover.
  • the gas-side upstream of a fluidized-bed furnace can reduce the NOx emission on the primary side much more than in all other known processes.
  • the use of a fluidized bed chamber without built-in heat exchanger heating surfaces makes it possible to work with a reducing, ie low-oxygen, fluidized bed without having to fear cooling of the fluidized bed.
  • Can also be used for cooling the Surrounding walls can be dispensed with. The nitrogen oxide formation can thereby be reduced further.
  • the heat generated is discharged from the fluidized bed furnace by means of the flue gas and can be given off, for example in the downstream industrial boiler, together with the heat generated there, to a steam circuit or another heat consumer.
  • a steam circuit or another heat consumer To regulate the temperature in the fluidized bed furnace to a constant temperature level of, for example, 800 ° C., it proves to be expedient to return a portion of the cooled and possibly already cleaned flue gases from the downstream industrial boiler as cooling medium to the fluidized bed furnace continuously.
  • the fluidized bed furnace can also be cooled by fluidized bed material which is continuously introduced into the fluidized bed furnace. If the fluidized bed combustion is operated in combination with the steam generator of a power plant, it proves to be advantageous to use the coarse ash produced in the boiler of the steam generator as a fluidized bed material. After it has been reduced in size by friction, the coarse ash is then removed as fly ash together with the flue gas. This procedure has the advantage that not only the flue gas, but also the bed ash is introduced into the downstream steam generator and is exposed there to the desired high temperatures, so that no toxic components can be discharged from the fluidized bed furnace via the bed ash either.
  • part of the coarse fly ash obtained in the electrostatic filter of the power plant can of course also be used as the fluidized bed material. If there is no heat source or no industrial boiler for the high-temperature treatment of the flue gases and the fly ash of the fluidized bed system in the case of the increase in the cost of organic waste, it is also possible in this case, according to another feature, to use the waste materials to only partially burn in the fluidized bed with a lower air supply to CO, ie to gasify, and then to further burn the CO-containing gasification product in a downstream furnace at correspondingly higher temperatures to form CO 2. In this case too, it is possible to convert the toxic dioxins carried in the gasification product of the fluidized bed system into harmless products at the correspondingly high temperatures.
  • FIGS. 1 and 2 Further explanations of the invention can be found in the exemplary embodiments shown schematically in FIGS. 1 and 2.
  • Fig. 2 A furnace according to the invention using the example of a steam generating plant.
  • FIG. 1 schematically shows 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 on the flue gas side with coal dust 21 - with supply of fresh air 22 - fired steam generator 2, for example a coal-fired power plant, connected downstream.
  • the smoke gases from the fluidized bed furnace 1, including fuel particles and ash particles which are entrained, are introduced into the steam generator 2 below the furnace zone 23 via line 14.
  • the introduced flue gases from the fluidized bed 1 at temperatures above 900 "C, to temperatures vorzugswei ⁇ e zwi ⁇ chen 1000 ° C and 1200 C ⁇ heated.
  • pollutants such as dioxins which have arisen in the fluidized bed furnace 1 and are carried in the flue gas are destroyed.
  • ⁇ cher 5 possibly further cooled, 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 in front of 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 about 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, it being expedient to limit the flow velocity in the fluidized bed 11 can be a part of the recirculated cold flue gases exclusively for the purpose of heat dissipation from the vortex Initiate ⁇ layer furnace 1 via line 45 above the fluidized bed 11 into the fluidized bed furnace 1.
  • the coarse ash is separated from the ash drawn off from the steam generator 2 via line 28 and is returned as line material into the fluidized bed 11 via line 29, possibly after additional cooling.
  • the coarse surface is gradually shredded and entrained into the steam generator 2 together with the smoke 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 in a schematic representation the example of a steam generator system according to the invention.
  • This consists of a steam generator 2, which in the embodiment is equipped with a coal dove firing 30.
  • the circumferential walls 40 of the steam generator 2 are designed as tube walls and are connected in a manner known per se together with the other heat exchanger heating surfaces 24 of the steam generator 2 to a water vapor circuit (not shown further here).
  • a dust filter 3, a suction fan 10 and a flue gas desulfurization system 4 are connected to the smoke gas line 9 leaving the steam generator 2 and leading to the chimney 8.
  • a fluidized bed furnace 1 with a stationary fluidized bed 11 is connected upstream of the steam generator 2 on the gas side. Its 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 suction opening 17.
  • a gas compressor 18 is installed for generating the necessary pressure difference on the nozzle base 15.
  • a control valve 19, 20 is installed in each of the branch of the gas line 16 leading to the flue gas line 9 and 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 line 56 of the fluidized bed furnace 1 opens at the lower end of the steam generator 2.
  • the burner 57 of the coal dust furnace 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 smoke duct fan 34 is installed in this auxiliary line 63.
  • 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 still bound to gypsum in the fluidized bed 11 by the lime added to the coal and is removed with the ash in a manner not shown here.
  • the previously required to integrate the sulfur Oxidation of the same limits the extent of the sub-stoichiometric addition of oxygen in the fluidized bed 11.
  • the formation of nitrogen oxides can not only be stopped, but even to a small extent, by adding larger amounts of flue gases via the additional gas line 42 Reduce SiOxides 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 firing 1 is carried out without a cooled peripheral wall and without any 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 smoke 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 reduced significantly. 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 Kohlen ⁇ taubbrenner 57 is foundedseit ⁇ turn Voraus ⁇ requisite for stronger admixture of flue gases from the steam generator 2 • to the exhaust gases of the fluidized bed furnace 1.
  • the Kohlen ⁇ taubbrenner 57 could otherwise au ⁇ supplied through the Abga ⁇ technisch 56 extremely low calorific Abga ⁇ of FBC 1 do not burn reliably in the steam generator 2.
  • the shunt line 62 makes it possible to optionally add the flue gas to the fluidized bed furnace 1 and this in front of the flue gas desulfurization system 4 of the flue gas line 9 with a approximately higher temperature or behind the flue gas desulfurization system 4 with a lower temperature. In this way, the temperature in the fluidized bed furnace 1 can be regulated in addition to the measures already described. Finally, the flame temperature of the coal dust burner 57 of the steam generator 2 can also be reduced by admixing the fresh air line 22 with flue gas via the auxiliary line 63. For this purpose, a further smoke duct fan 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 sinks in the fluidized bed 11 are avoided, and at these low temperatures the risk of local undercooling of the fluidized bed 11 is reduced, with the result that it is lost.
  • the formation rate of the nitrogen oxides in the fluidized bed furnace 1 is also additionally reduced by the fact that the fluidized bed furnace 1 fresh air is sub-stoichiometric Amount is supplied. This lack of oxygen additionally 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 suppress the formation of nitrogen oxides on the primary side to such an extent that it can satisfy the immission conditions even without a DENOX system connected downstream of the flue gas flow.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (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.
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
DE3701798 1987-01-22
DE19873701798 DE3701798A1 (de) 1987-01-22 1987-01-22 Dampferzeugeranlage mit einem kohlebefeuerten dampferzeuger
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 true EP0302910A1 (fr) 1989-02-15
EP0302910B1 EP0302910B1 (fr) 1992-07-15

Family

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)

Families Citing this family (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4102959A1 (de) * 1991-02-01 1992-08-13 Metallgesellschaft Ag Verfahren zum verbrennen von kohle in der zirkulierenden wirbelschicht
NL9401269A (nl) * 1994-08-02 1996-03-01 Kema Nv Werkwijze en verbrander voor het uitvoeren van met zuurstof verrijkte verbranding.
US5507238A (en) * 1994-09-23 1996-04-16 Knowles; Bruce M. Reduction of air toxics in coal combustion gas system and method
CH689312A5 (de) * 1995-01-10 1999-02-15 Von Roll Umwelttechnik Ag Verfahren zum Verbrennen von Abfallmaterial unter Gewinnung von thermischer Energie.
US5626088A (en) * 1995-11-28 1997-05-06 Foster Wheeler Energia Oy Method and apparatus for utilizing biofuel or waste material in energy production
WO1998003250A1 (fr) * 1996-07-18 1998-01-29 Hoelter Heinz Procede de traitement des gaz brules se degageant dans une installation d'incineration de dechets organiques
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
AT522051B1 (de) 2018-12-19 2021-04-15 Next Generation Recyclingmaschinen Gmbh Aufbereitungsanlage sowie Verfahren zur Aufbereitung von Kunststoffmaterial für dessen Wiederverwertung

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US3884193A (en) * 1974-03-22 1975-05-20 Foster Wheeler Corp Vapor generating system and method
EP0037858B1 (fr) * 1980-04-16 1984-01-25 BBC Aktiengesellschaft Brown, Boveri & Cie. Centrale à vapeur avec générateur de vapeur à combustion sous pression et à lit fluidisé
DE3136480A1 (de) * 1981-09-15 1983-06-30 Steag Ag, 4300 Essen Verfahren und anordnung zum wiederaufheizen von nassentschwefelten rauchgasen
US4355601A (en) * 1981-09-25 1982-10-26 Conoco Inc. Recirculating flue gas fluidized bed heater
CH656936A5 (de) * 1982-04-26 1986-07-31 Sulzer Ag Dampferzeuger mit wirbelschichtfeuerung.
US4628833A (en) * 1983-04-11 1986-12-16 The Garrett Corporation Fluid bed hog fuel dryer
DE3330943A1 (de) * 1983-08-27 1985-03-07 BBC Aktiengesellschaft Brown, Boveri & Cie., Baden, Aargau Kombiniertes gasturbinen-/dampfturbinenkraftwerk mit aufgeladenem wirbelschicht-dampferzeuger
JPH0229372Y2 (fr) * 1984-09-26 1990-08-07
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Also Published As

Publication number Publication date
WO1988005494A1 (fr) 1988-07-28
DK524388D0 (da) 1988-09-21
DK165762C (da) 1993-05-24
DK165762B (da) 1993-01-11
DE3872787D1 (de) 1992-08-20
DK524388A (da) 1988-11-18
EP0302910B1 (fr) 1992-07-15
US4932335A (en) 1990-06-12

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