EP0154986B1 - Procédé et dispositif pour l'obtention de fumées pauvre en SOx dans des installations d'incinération - Google Patents

Procédé et dispositif pour l'obtention de fumées pauvre en SOx dans des installations d'incinération Download PDF

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Publication number
EP0154986B1
EP0154986B1 EP85102862A EP85102862A EP0154986B1 EP 0154986 B1 EP0154986 B1 EP 0154986B1 EP 85102862 A EP85102862 A EP 85102862A EP 85102862 A EP85102862 A EP 85102862A EP 0154986 B1 EP0154986 B1 EP 0154986B1
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European Patent Office
Prior art keywords
fuel
gas
additive
transport
transport gas
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Expired
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EP85102862A
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German (de)
English (en)
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EP0154986A2 (fr
EP0154986A3 (en
Inventor
Klaus-Dietrich Nickel
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Kasa Technoplan GmbH
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Kasa Technoplan GmbH
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Priority claimed from DE19843409014 external-priority patent/DE3409014C1/de
Priority claimed from DE19853508650 external-priority patent/DE3508650C1/de
Application filed by Kasa Technoplan GmbH filed Critical Kasa Technoplan GmbH
Priority to AT85102862T priority Critical patent/ATE42110T1/de
Publication of EP0154986A2 publication Critical patent/EP0154986A2/fr
Publication of EP0154986A3 publication Critical patent/EP0154986A3/de
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/10—Treating solid fuels to improve their combustion by using additives
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/02—Treating solid fuels to improve their combustion by chemical means

Definitions

  • the invention relates to a method and to devices for obtaining low-SO x flue gases in combustion plants operated with finely divided carbon-containing fuels, in particular coal, in which the sulfur contained in the fuel is converted into a finely divided additive, preferably limestone powder (CaCO a ), quicklime powder ( CaO) or calcium hydroxide powder (Ca (OH) 2 ) and then the desulfurized fuel is burned in the combustion chamber and the additive particles loaded with sulfur are sintered and removed with the ash.
  • a finely divided additive preferably limestone powder (CaCO a ), quicklime powder ( CaO) or calcium hydroxide powder (Ca (OH) 2 )
  • Harmful by-products of fossil fuel combustion are well known.
  • One of the main pollutants is sulfur dioxide, from which - according to the current state of technology - around 4 million tons are blown off into the air in the Federal Republic of Germany, whereby power plants and industry are the main causes.
  • sulfur dioxide from which - according to the current state of technology - around 4 million tons are blown off into the air in the Federal Republic of Germany, whereby power plants and industry are the main causes.
  • the fossil fuel coal contains sulfur either as a mineral accompanying substance, in particular as pyrite (FeS 2 ), or as so-called organic sulfur.
  • FeS 2 pyrite
  • organic sulfur is part of the coal substance, the type of its binding to the coal is not yet known. Depending on its occurrence in the coal, it can be desulfurized by mechanical or chemical processes. Both processes are tedious, with the chemical processes requiring particularly high investment and operating costs.
  • combustion chamber or the flue gas outlet of the boiler system must consist of materials that are compatible with the SOr components contained in the flue gas. As a result, the increased price for such materials must be accepted when the boiler system is being designed.
  • the effectiveness of desulfurization of flue gas in the boiler depends on a large number of parameters and is highly complex.
  • the type of coal, the partial pressure of SO 2 , the excess of oxygen in the flue gas, the reaction temperature or the reaction temperature gradient, the dwell time of the additive in the flame zone, the turbulence in the combustion chamber, and the place where the additive is blown in play an important role into the combustion chamber, the speed of the additive blown in and other conditions, all of which are difficult or impossible to control.
  • calcium sulfate formed cleaves SO 2 again at temperatures above 1200 ° C.
  • the invention has for its object to provide an inexpensive method and devices with which fossil fuels can be desulfurized so that when they are burned in the boiler room, significant amounts of SO " no longer arise or can have a harmful effect.
  • the fuel and the additive are prepared in separate disintegration processes, that an amount of freshly prepared additive corresponding to its sulfur content is then added to the disintegrated fuel, and that this fuel-additive mixture is then under a controllable positive pressure and heated transport gas - while maintaining the mixing - is transported to a reactor designed as a leading section, in which the transport gas pressure suddenly relaxes and, in a low-oxygen inert gas atmosphere within a controllable temperature range above the boiling point of sulfur, the residence time of the mixture is adapted to the thermodynamic and reaction-kinetic sulfur transfer process taking place is, in which the sulfur is expelled from the fuel and the additives are loaded with the sulfur vapor or the gaseous sulfur compounds, whereupon in which fuel largely freed of sulfur is blown into the combustion chamber and burned at a temperature at which the loading of the additive particles likewise blown into the combustion chamber with the sulfur vapor or the gaseous sulfur compounds is maintained until sintering.
  • the disintegration of the fuel normally takes place in an inert gas atmosphere in a disintegrator, preferably in accordance with German patent application DE-OS 3 034 849.3, in order to avoid self-ignition of the fuel when it is comminuted.
  • the disintegration of the additive also takes place in a disintegrator, but in an independent disintegration process (preferably in a normal air or oxygen atmosphere), as a result of which oxygen is added to the additive particles, which causes the later loading of the additive Particles favored with the sulfur vapor or the gaseous sulfur compounds that are expelled from the fuel.
  • the fuels and additives prepared in separate disintegration processes are then mixed with one another, with the finely divided fuel being mixed with a quantity of freshly prepared fine-grained additive corresponding to its sulfur content — in no case deposited, already aged additive powder.
  • the mixture of finely divided fuel and highly active additive is then preferably transported through an inert transport gas heated to approximately 500 ° to 600 ° C. to a reactor designed as a leading section, this transport preferably taking place under a controllable excess pressure between 4 and 6 bar.
  • This overpressure is necessary to prevent degassing of the fuel in the transport line, the length of which depends on the structural conditions available in front of the combustion chamber. For safety reasons, the disintegration of the fuel and the additive to fine dust is usually not carried out near the combustion chamber.
  • the pressure of the hot transport gas (controllable) is suddenly released by the enlarged cross-section of the reaction chamber and the pressure drop is used via a control device to build up a vortex zone, in its agglomeration-inhibiting and agglomeration-dissolving turbu limits temperature and residence time are so controllable that the thermodynamic and reaction kinetic process of sulfur transfer from the fuel to the additive can be adapted to the chemophysical properties of the fuel-additive mixture.
  • a sulfur transfer takes place from the pulverized fuel heated up to the given reaction temperature in the advance conveyor section to the highly active, reactive additive, which is also brought to the given reaction temperature, due to the fact that the shock-like pressure release of the conveying gas when it flows into the Reactor of the leading section, the vaporization temperature of the sulfur and the reaction temperature of the gaseous sulfur compounds are also reduced in a shock, so that the sulfur is expelled from the fine fuel particles by almost explosive evaporation, or the gaseous sulfur compounds are suddenly split off and released from the more reactive additive with the release of oxygen in the spinal zone.
  • the pressure in the vortex zone of the reactor is specified by the process control for this process sequence by 0.25 bar. A release of volatile components of the fuel is limited, which in no way negatively affect the combustion process.
  • the fine-grained solid fuel which has largely been freed of its sulfur content, together with its already released volatile components and the sulfur-laden additive particles, is fed to the burner via a short delivery line behind the inlet section and blown into the combustion chamber there, enriched with combustion air. Due to the already released volatile constituents, the fuel burns out immediately after the burner nozzle. Under certain safety precautions, support torches can therefore be dispensed with.
  • the additive By blowing the very fine-grained additive particles, which have already been heated to a temperature between 500 ° and 600 ° C in the lead section, into the hot flame zone of the combustion chamber immediately after the injection nozzle, the additive is sintered almost shockingly and thus does not “seal” together with the others combustible fiber of the fuel supplied to the ashes.
  • the combustion temperature can be operated below 1850 ° C, but above 1250 ° C, so that the sintering of the shock ensures that sulfur is incorporated into the additive, but that the sulfur molecules are broken down into individual sulfur atoms by thermal energy, which can occur explosively, before Sintering is prevented. By splitting the sulfur molecules, the binding to the additive is lost due to a spontaneous rejection reaction.
  • the new process enables gaseous, or at least gaseous, sulfur compounds to be transferred to an additive. It is important that due to the pressure and temperature control in the lead section, coking of the fuel, i.e. an unwanted complete degassing before the combustion chamber can be prevented.
  • the solid additive itself is not combustible, due to its special reactivity it can hold vaporized sulfur or gaseous sulfur compounds at the given combustion temperature spectrum in such a way that desorbation does not take place.
  • the advantage here is that the burner, chimney and flue gas outlet can consist of less good material, since they are not - as before - exposed to the aggressive S0 2 influence.
  • the mixture of non-degassed, but freed from the sulfur constituents or fuel particles and additive particles with the incorporated sulfur reaches the combustion chamber in a well preheated state and does not extract as much thermal energy from the flame cone as cold-introduced mixtures of coal particles and additive Particles.
  • coal can be used as fuel, which is processed in a turbo disintegration process.
  • the expulsion of the sulfur from the fuel and the intensive reactions between the expelled sulfur and the additive are promoted according to the invention in that the sulfur transfer process takes place in a vortex zone, the turbulence of which builds up optimal reaction zones.
  • the system for achieving low-SO x smoke gases in the operation of combustion systems for carrying out the method according to the invention with a device for injecting mixtures of fuels and finely divided additive parts into the combustion chamber and with a deashing plant, through which - with the ashes - the sintered additive particles loaded with sulfur are also removed, has a pressure transmitter vessel designed as a buffer for an intimate mixture of fuel and additive particles prepared in separate disintegration processes on.
  • This pressure transmitter vessel is on the one hand connected to a line for compressed, heated, inert transport gas and on the other hand via an arrangement for loading this transport gas with the mixture of fuel and additive particles, via a further transport line to one for evaporating the sulfur to 500 ° C. to 600 ° C. ° C heatable flow lines connected.
  • the temperature within the lead section must be above the equilibrium temperature of sulfur and its steam, preferably between 500 ° C and 600 ° C.
  • All control valves, mixing valves, metering and throttling devices can be operated electrically, but also pneumatically or hydraulically, or via a process computer that controls the entire process in connection with an SO Z measuring device installed in the flue gas outlet - if necessary also in connection with one in the lead section installed thermometer - can control.
  • an optimal desulfurization of the fuel can be made possible without the coal being completely degassed in front of the combustion chamber.
  • the parameters for the proper course of the desulfurization process can be optimally set by many control means, for example in accordance with the coal.
  • suitable measuring devices, evaluation circuits and control devices are therefore provided, with the aid of which the reaction temperature in the lead section or in the reactions and the pressure can be optimally adjusted.
  • FIG. 1 schematically shows a furnace 1, of which a combustion chamber 2 and a flue gas outlet 6 are shown in simplified form.
  • An evaporation pipeline 3 is indicated above the combustion chamber 2, for example.
  • a burner device 4 is supplied with combustion air in a conventional manner via a combustion air supply line 11 and a conveying fan 12.
  • a dust separator 7 and a conventional SOr knife 8 are provided in the flue gas outlet 6.
  • the combustor 4 is supplied with the necessary fuel in the form of gas or fuel particles from a lead section 27 via a transport gas line 9, in which finely divided, preferably solid fossil fuels, the bound sulfur is removed.
  • the lead section 27 has a double wall 28 which is connected via a heating gas line 26 and a heat exchanger 25 in the combustion chamber 2 and via a further heating gas line 24 to a flue gas extraction 13 in the flue gas outlet 6.
  • a flue gas extraction 13 inert flue gas is removed behind the dust separator 7 by means of a fan 15, behind which the flue gas line 14 is divided into the heating gas line 24 already mentioned and a transport gas line 16, which will be explained later.
  • the heating gas portion of the amount of flue gas withdrawn is heated to the predetermined temperature in order to heat the lead section 27.
  • pressure and temperature can be regulated so that the sulfur components are expelled from the fuel without the fuel, for example coal, being degassed.
  • the temperature of the feed section 27 is kept between 500 ° and 600 ° C., ie above the boiling point of the sulfur. The temperature required in each case is regulated by means of temperature controllers known per se, which are not explained in detail here.
  • the amount of flue gas extracted by the blower 15 passes via the transport gas line 16 and a suction filter 17 to a compressor 18 and then via a control valve 23 via the control valve 31 into the inlet line 30 or via a branched line to a transport gas inlet 47 at a pressure transmitter vessel 44.
  • a heat exchanger 20 for the transport gas is provided parallel to the control valve 23 and, like the heat exchanger 25, can be arranged in the combustion chamber 2.
  • the control valve 23 By means of the control valve 23, the temperature of the transport gas which is branched off for the floating fluidized bed or fluidized bed 29 and also at the Transport gas inlet 47 arrives, can be adjusted or controlled in a manner known per se. It should be noted here that the dedusted flue gases removed from the flue gas outlet already have a not inconsiderable initial temperature. The transport gas therefore does not need to be heated up from the relatively cold ambient temperature.
  • the temperature of the transport gas is set between 500 ° and 600 ° C for both purposes.
  • the temperature is controlled, for example, by an electronic process computer 55, which will be explained later.
  • the gases entering the lead section 27 through the inlet line 30 are used in the usual manner known per se to form a floating fluidized bed or fluidized bed 29, the intensity of which can be influenced by the control valve 31.
  • a further metering device 39 known per se can be provided, with which a further influencing of the floating-fluidized or fluidized bed within the lead section 27, for example the pressure within the lead section, is possible.
  • the intimately mixed fuel and additive particles are fed to the advance section 27 via a transport gas line 49 from a known pressure transmitter vessel 44 with an inlet slide 45 and an outlet slide 46 for secure shut-off, which in turn via a delivery line 42 to one in connection with the present invention not explained, known mixing device for coal dust and additive particles, is connected. Via an additional line 43 with a corresponding control valve 48, additive can be introduced into the delivery line 42 as required.
  • a throttle device 38 is provided in front of the outlet slide 46.
  • All the control valves preferably the control valves 23, 31, 48, but also the throttle device 38, can be influenced, for example, by means of an electronic process computer, generally designated 55, by the SO 27 knife 8 in the flue gas outlet 6, if appropriate also by the temperature in the lead section. so that the reactions in the upstream section, ie the desulfurization of the fuel and the incorporation of the sulfur components into the additive particles, take place fully under the control of the electronic process computer 55.
  • the temperature control via the electronic process computer 55 can be influenced by a thermometer 21 arranged, for example, in the lead section 27 by acting on the control valves 23 and / or 31.
  • the electronic process computer 55 is also operatively connected to the metering devices 38, 39 in order to influence the dwell time in the lead section 27. Without changing anything at the core of the invention, the control or regulation of the fuel desulfurization in front of the combustion chamber 2 can also be carried out by other controls or by hand.
  • a metering device 34 and a throttle valve 59 are provided in front of and behind the lead section 27, which are also connected to the electronic process computer 55. With these control elements, the dwell time in the lead section 27 and also the internal pressure conditions can be precisely controlled.
  • 1 shows a very general process flow diagram to explain the new process for the desulfurization of fuel and a device suitable therefor. It is important that 4 short lines are provided between the lead section 27 and the burner device so that fuel and additive cannot cool down and agglomerate. 1 shows that with relatively simple means the new fuel desulfurization process can be used advantageously with the aid of the device explained both on new combustion plants and also on existing combustion plants 1. In all applications, the fuel particles are largely or completely desulfurized in front of the burner device 4. This minimizes or completely avoids the SO, 7 emissions in the combustion chamber and in the flue gas outlet 6, as well as the resulting contamination and destruction of these parts of the boiler system. The S0 2 is not blown off into the atmosphere.
  • a new feature of the first exemplary embodiment is that a storage container 19 for compressed transport gas is provided in the transport gas line 16 behind the compressor 18, and a control valve 54 for the transport gas is connected to the outlet thereof.
  • an oxygen meter 56 can be provided which, when the oxygen content in the conveying gas line 16 becomes too high, switches an inert gas source 50 on and off via a control valve 51 in order to introduce more or less inert gas into the Inject transport gas line 16. This ensures that the mixture of fuel and additive particles cannot ignite before or in the lead section.
  • the transport gas line 16 divides behind a further control valve 52.
  • a bypass line 41 is guided over a heating device 37, in which the conveying gas is heated.
  • a line 40 for normal-temperature conveying gas branches off via a mixing valve 53, which line is connected to the bypass line 41 in front of the transport gas inlet 47 in the pressure transmitter vessel 44 reunited.
  • the control valve 52 and the mixing valve 53 can be actuated by the electronic process computer 55, which can be influenced by the SO, 7 knife 8, in order to adjust the temperature of the transport gas for the intimately mixed fuel and additive particles.
  • the heating device 37 can be arranged in the combustion chamber 2. In the present exemplary embodiment, it is installed in a double wall 36 of a fluidized bed reactor 32, which is heated via the heating gas line 26, in which a regulating valve 58 is provided, which can be controlled, for example, by a thermometer 57 in the fluidized bed reactor 32.
  • the temperature in the fluidized bed reactor is set depending on the fuels fired. In principle, the temperature has to be regulated so high that the sulfur components certainly escape from the fuel particles. It is advantageous if the temperature inside the fluidized bed reactor is above the boiling point of sulfur. Quick and good results can be achieved if the temperature inside the fluidized bed reactor is kept between 500 ° and 600 ° C.
  • An inlet 33 of the fluidized bed reactor 32 is connected via a metering device 34 connected to the process computer 55 and / or via a metering device 39 and via the transport gas line 49 to the outlet of the pressure transmitter vessel 44.
  • a throttle or deflection device 38 is arranged within the temperature-controlled fluidized bed reactor 32, behind which a fluidized bed 35 is formed from the transport gas loaded with the intimately mixed fuel and additive particles.
  • the sulfur components are driven out of the fuel and taken up by the additive.
  • the dwell time required for this can be controlled via the metering device 34 and / or via the metering device 39, but also with the aid of a throttle valve 59 behind the lead section 27, for example by the electronic process computer 55. Due to the temperature control, the sudden drop in pressure and the adjustable dwell time, the additive is loaded with the sulfur components. If the sulfur components expelled from the fuel were not absorbed to the required extent by the additive, SO 2 components would form during combustion in the combustion chamber and are displayed by the SOrMesser.
  • the process control then either causes more additive powder to be fed into the line 42 via the control valve 48, the residence time in the fluidized bed reactor is increased, the reaction temperature is increased or the pressure difference between the transport line 49 and the flow path 27 is changed.
  • an additional amount of additive particles can be entered via an additional line 43 and a control valve 48.
  • the control valve 48 is likewise connected to the electronic process computer 55 in order to always ensure the excess of additive particles in the mixture which is necessary for the desulfurization. It is advantageous if at least four times the amount of additive particles contained in the fuel is available for the integration of the sulfur components.
  • the plants shown in FIGS. 1 and 2 can also be combined with one another if the fuel used requires that a residual desulfurization of the fuel must be carried out behind the fluidized bed reactor 32 in a reaction zone 27 before harmful combustion of the sulfur to S0 2 takes place in the combustion chamber 2.
  • coal dust particles are used as fuel, which, for example, by means of the turbo disintegration process with impact speeds of over 100 m / sec. and a grain size of 50% under 40 ⁇ has been prepared from coal if possible.
  • Particularly good results are achieved when the carbon particles are processed at impact speeds of over 200 m / sec. he follows.
  • the carbon particle surfaces are then not compressed - as is the case, for example, when the coal is crushed in ball mills - but "broken up" in preparation for a more effective desulfurization.
  • the temperature and pressure control practiced in the leading sections according to the invention only cause the sulfur constituents to be expelled, but not a simultaneous full degassing of the fuel. Fuel particles that are led into the boiler room 2 over the short distance between the lead section and the burner chamber are therefore not coked, but rather fully-fledged, sulfur-free fuel.
  • Highly active sulfur-binding additives for example limestone powder, quicklime powder or calcium hydroxide powder
  • limestone powder, quicklime powder or calcium hydroxide powder are also obtained by processing these additives using the turbo disintegration process at high impact speeds of up to over 200 m / sec. With this preparation, grain sizes of 50% below 30 11m are achieved.
  • the additive particles do not have a compacted surface, as is the case with comminution in ball mills, but a surface with a broken structure that is highly active. It can saturate faster with the expelled sulfur components at the temperatures maintained and during the adjustable dwell time.
  • the device according to the invention allows it to be adjusted to different fuels without difficulty.
  • One is able to vary the constituents of fuel particles in the mixture and also to optimally adapt the temperature control and the dwell time in the leading sections to the fuel and its sulfur content.
  • oxygen-poor gas is already available for pneumatic conveying addition. The mixture cannot ignite. If the oxygen content in the transport gas nevertheless exceeds the values to be observed for safety reasons, inert gas can also be added to the transport gas removed from the flue gas.
  • the sulfur is largely removed from it, so that the combustion chamber S0 2 can no longer be formed in a dangerous concentration or is no longer present.
  • the fuel and additive are processed in separate disintegration processes.
  • the fuel is processed or comminuted in an inert gas atmosphere, primarily to prevent the fuel from spontaneously igniting.
  • the additives are processed in a normal air or oxygen atmosphere in which oxygen can accumulate on the additive particles, which contributes significantly to the activation of the additive particles and promotes the binding of the sulfur components to the additive.

Claims (29)

1. Procédé pour obtenir des gaz brûlés pauvres en SO. dans des installations de chauffage opérées avec des combustibles à particules fines contenant du carbone, particulièrement du charbon, dans lequel le soufre contenu dans le combustible est lié dans un additif à particules fines, préférablement du carbonate de calcium (CaCOa) en poudre, poudre de chaux vive (CaO), ou d'hydroxyde de calcium, et ensuite le combustible désulfuré est brûlé, et les particules de l'additif chargées du soufre sont frittées et déchargées avec le cendre, caractérisé en ce, que le combustible et l'additif sont préparés dans des procédés de désintégration séparés, qu'ensuite une quantité d'additif fraîchement préparé, adaptée à la teneur en soufre du combustible désintégré, est mélangée au dernier, qu'ensuite ce mélange combustible/additif - le mélange étant maintenu - est transporté par un gaz de transport chauffée et de surpression réglable à un réacteur formé en voie de marche avant (27, 32), dans lequel la pression du gaz de transport se détend soudainement, et le temps d'exposition du mélange dans une atmosphère pauvre en oxygène de gaz inerte est adapté dans une gamme de température réglable au dessus du point d'ébullition du soufre au procédé thermodynamique et de réaction cinétique de transmission de soufre se déroulant, dans lequel le soufre est expulsé du combustible, et les additifs sont chargés de la vapeur du soufre respectivement des composés de soufre gazeux, sur quoi le combustible, largement libéré de soufre et injecté dans la chambre de combustion, est brûlé dans une température, dans laquelle le chargement de vapeur de soufre respectivement de composés de soufre gazeux des particules des additifs également injectées dans la chambre de combustion est maintenu jusqu'au frittage.
2. Procédé selon revendication 1, caractérisé en ce que la désintégration du combustible a lieu dans une atmosphère de gaz inerte, tandis que la désintégration de l'additif se fait dans une atmosphère normale d'air respectivement d'oxygène.
3. Procédé selon les revendications 1 et 2, caractérisé en ce que les additifs de haute activité liant le soufre sont traités par moyen de la technique de désintégration sous des vitesses de rebond élevées, de préférence au moyen de la technique de turbo-désintégration à des vitesses de rebond au dessus de 100 m/sec.
4. Procédé selon les revendications 1 à 3, caractérisé en ce qu'au moins la quantité quadruple d'additif fraîchement traité de haute activité, en grosseur de grain de 50% sous 30 pm, de la teneur en soufre du combustible est mélangée au dernier.
5. Procédé selon les revendications 1 à 4, caractérisé en ce que des fines de charbon sont utilisées comme combustible transformées à l'aide de la technique de turbo-désintégration à des vitesses de rebond au-dessus de 100 m/sec. en poussière de charbon d'une grosseur de grain de 50% sous 40 !lm.
6. Procédé selon les revendications 1 à 5, caractérisé en ce que le transport du mélange de poussière de charbon et d'additif en fines particules se fait par un gaz de transport inerte chauffé et pauvre en oxygène.
7. Procédé selon les revendications 1 à 6, caractérisé en ce que la voie de marche avant (27, 32) est chauffée à une température entre 500° et 600°C.
8. Procédé selon les revendications 1 à 7, caractérisé en ce que pour le transport du mélange de poussière de charbon et d'additif en fines particules ainsi que pour le chauffage de la voie de marche avant (27, 32) du gaz brûlé inerte dépoussiéré est pris de l'évent de gaz brûlé (6) de l'installation de chaudières.
9. Procédé selon les revendications 1 à 8, caractérisé en ce qu'une quantité partielle de la quote-part en gaz de transport de la quantité de gaz brûlé prélevée est chauffée à une température entre 500° et 600 °C et avant d'être chargée de sa fonction de transport est mélangée pour réglage de température avec une quantité de gaz de transport non chauffée.
10. Procédé selon les revendications 1 à 9, caractérisé en ce que la quote-part en gaz de transport de la quantité prélevée de gaz brûlé sur commencement de sa fonction de transport a une surpression entre 4 et 6 bar.
11. Procédé selon les revendications 1 à 10, caractérisé en ce que la voie de marche avant de configuration imperméable au gaz, inclue un lit fluidisé (29) et/ou un réacteur à lit fluidisé (32), dans lequel le lit fluidisé (35) est formé par tourbillonnement du gaz de transport chargé avec le mélange poussière-de-charbon/additif et/ou par injection de gaz brûlé chauffé dans le courant de gaz de transport chargé du mélange poussière-de-charbon/additif.
12. Procédé selon les revendications 1 à 11, caractérisé en ce que la relation de mélange entre la poussière de charbon et l'additif est réglé en fonction de mesurages de S02 dans l'évent de gaz brûlé dans l'installation de chauffage.
13. Procédé selon les revendications 1 à 12, caractérisé en ce qu'en cas d'une augmentation inadmissible de sa teneur en oxygène le gaz de transport est additionné de gaz inerte.
14. Procédé selon les revendications 1 à 13, caractérisé en ce que la combustion du combustible dans la chambre de combustion se fait à une température entre 1850°C et 1250°C.
15. Procédé selon les revendications 1 à 14, caractérisé en ce que le soufre est expulsé du combustible en manière de choc dans la voie de marche avant par le relâchement de la pression du gaz de transport de 4-6 bar à 0,25 bar.
16. Procédé selon les revendications 1 à 15, caractérisé en ce que les particules d'additif chargées du vapeur de soufre respectivement des composés de soufre gazeux sont frittées dans la chambre de combustion en manière de choc.
17. Mécanisme pour obtenir des gaz brûlés pauvres en SO. dans l'opération des installations de chauffage pour exécuter les procédés selon les revendications 1 à 16, ayant un dispositif pour injecter des mélanges de combustibles et d'additivs en particules fines dans la chambre de combustion ainsi qu'une installation pour éliminer les cendres, par laquelle, avec les cendres, aussi les particules d'additif chargées du soufre et frittées sont éliminées, caractérisé en ce, qu'un vaisseau émetteur de pression (44) configuré comme accumulateur intermédiaire pour un mélange intime de particules de combustible et d'additif traitées dans des procédés séparés de désintégration est raccordé d'une part à une conduite (16) pour du gaz de transport comprimé, chauffé, inerte et de l'autre, par un mécanisme (38, 46) pour charger le gaz de transport d'un mélange de particules de combustible et d'additif et par une conduite de transport (49), à une voie de marche avant (27; 29, 32) chauffable à une température suffisante pour évaporer le soufre, dans laquelle la pression du gaz de transport par rapport à celle-ci dans la conduite de transport (49) se détend et le temps d'exposition du mélange dans la zone de tourbillonnement est réglable par des dispositifs d'étranglement respectivement de renvoi (34, 38, 59) et/ ou des tôles tamis (39).
18. Mécanisme selon revendication 17, caractérisé en ce que, pour chauffer la voie de marche avant (27; 29, 32) et comme gaz de transport pour le mélange de particules de combustible et d'additif, du gaz brûlé est employé, pour le prélèvement (13) duquel une soufflante (15) est prévue, connectée derrière un séparateur de poussière (7) dans un évent pour gaz brûlé (6) dans l'installation de chauffage (1).
19. Mécanisme selon les revendications 17 et 18, caractérisé en ce que la conduite de gaz brûlé (14) se bifurque derrière la soufflante (15) en une conduite de gaz de chauffage (24) et une conduite de gaz de transport (16).
20. Mécanisme selon les revendications 17 à 19, caractérisé en ce que la conduite de gaz de chauffage (24) est connectée via un échangeur de chaleur (25) disposé dans la chambre de combustion (2) de l'installation de chauffage (1) au dispositif de chauffage (28) pour la voie de marche avant (27; 29, 32).
21. Mécanisme selon les revendications 17 à 20, caractérisé en ce que la conduite de gaz de transport (16) est connectée via un compresseur (18) à un réservoir de pression (19) pour le gaz de transport.
22. Mécanisme selon les revendications 17 à 21, caractérisé en ce que la sortie du réservoir de pression (19) est connectée via une soupape de réglage (54) et une soupape de mélange (53) pour le réglage de la pression respectivement de la température du gaz de transport au vaisseau émetteur de pression (44), et que devant la soupape de mélange (53) un by-pass (41) est branché de la conduite de gaz de transport (16), qui est mené par un dispositif de chauffage (37) et devant la jonction de la conduite de gaz de transport (40) au vaisseau émetteur de pression (44) est joint de nouveau à la dernière.
23. Mécanisme selon revendication 22, caractérisé en ce que le dispositif de chauffage (37) pour le chauffage de la quote-part de gaz de transport menée par le by-pass (41) est disposé dans la voie de marche avant (27; 29, 32) chauffée.
24. Mécanisme selon les revendications 17 à 23, caractérisé en ce qu'à la sortie (19) du vaisseau émetteur de pression (44) une source de gaz inerte (50) est raccordée via une soupape de réglage (52).
25. Mécanisme selon les revendications 17 à 24, caractérisé en ce que l'entrée et la sortie du vaisseau émetteur pression (44) pour charger le gaz de transport du mélange de particules de combustible et d'additif sont fermables par un tiroir d'entrée (45) et un tiroir de décharge (46).
26. Mécanisme selon revendication 17, caractérisé en ce que la voie de marche avant comporte un réacteur à lit fluidisé (32) avec des dispositifs de rebond et de conduction (35, 36) et/ou un lit fluidisé (29) avec une entrée additionnelle (30) pour gaz brûlé ainsi qu'un dispositif réglable d'étranglement respectivement de dosage (59/39) pour gaz de transport.
27. Mécanisme selon revendication 26, caractérisé en ce que le réacteur à lit fluidisé (32) est pourvu d'une paroi double (36) raccordée à la conduite de gaz de chauffage (24, 26), dans laquelle le dispositif de chauffage (37) pour la quote-part de gaz de transport menée par le by-pass (41) est disposé.
28. Mécanisme selon revendication 24, caractérisé en ce que la soupape de réglage (51) pour la source de gaz inerte (50) se trouve en connexion d'opération avec un oxymètre (56) dans la conduite de gaz de transport (16).
29. Mécanisme selon les revendications 17 à 28, caractérisé par un SO2-mètre (8) dans l'évent de gaz brûlé (6), qui, le cas échéant avec un thermomètre (21) dans la voie de marche avant (27), se trouve, par un ordinateur de procès (55), en connexion d'opération avec la soupape de réglage (54) pour gaz de transport derrière le réservoir (19) pour gaz de transport comprimé, une autre soupape de réglage (23) pour gaz de transport, une soupape de réglage (48) dans une conduite additionnelle (43) pour additif et le dispositif de dosage (34, 59) devant respectivement derrière la voie de marche avant (27; 29, 32) ainsi qu'avec une soupape de réglage (31) et des dispositifs d'étranglement respectivement de dosage (38, 39).
EP85102862A 1984-03-13 1985-03-13 Procédé et dispositif pour l'obtention de fumées pauvre en SOx dans des installations d'incinération Expired EP0154986B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT85102862T ATE42110T1 (de) 1984-03-13 1985-03-13 Verfahren und vorrichtung zum erzielen sox-armer rauchgase in feuerungsanlagen.

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DE3409014 1984-03-13
DE19843409014 DE3409014C1 (de) 1984-03-13 1984-03-13 Verfahren und Vorrichtung zum Erzielen SO↓x↓-armer Rauchgase in Feuerungsanlagen
DE3508650 1985-03-12
DE19853508650 DE3508650C1 (de) 1985-03-12 1985-03-12 Verfahren und Vorrichtung zum Erzielen SO↓x↓-armer Rauchgase in Feuerungsanlagen

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EP0154986A2 EP0154986A2 (fr) 1985-09-18
EP0154986A3 EP0154986A3 (en) 1985-12-11
EP0154986B1 true EP0154986B1 (fr) 1989-04-12

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EP (1) EP0154986B1 (fr)
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US4846081A (en) * 1987-04-08 1989-07-11 General Signal Corporation Calorimetry system
US4895081A (en) * 1987-04-08 1990-01-23 General Signal Corporation Gravimetric feeder, especially adapted for use in a calorimetry system
US4893315A (en) * 1987-04-08 1990-01-09 General Signal Corporation Calorimetry system
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Also Published As

Publication number Publication date
CS268518B2 (en) 1990-03-14
US4635572A (en) 1987-01-13
YU39885A (en) 1988-04-30
YU45705B (sh) 1992-07-20
CS175985A2 (en) 1989-06-13
EP0154986A2 (fr) 1985-09-18
EP0154986A3 (en) 1985-12-11

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