EP0142437B1 - Verfahren und Vorrichtung zum Wiedereinblasen von flugstaub in einen Heizkessel für festen Brennstoff - Google Patents

Verfahren und Vorrichtung zum Wiedereinblasen von flugstaub in einen Heizkessel für festen Brennstoff Download PDF

Info

Publication number
EP0142437B1
EP0142437B1 EP84402258A EP84402258A EP0142437B1 EP 0142437 B1 EP0142437 B1 EP 0142437B1 EP 84402258 A EP84402258 A EP 84402258A EP 84402258 A EP84402258 A EP 84402258A EP 0142437 B1 EP0142437 B1 EP 0142437B1
Authority
EP
European Patent Office
Prior art keywords
particles
boiler
buffer storage
separation
flow
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
Application number
EP84402258A
Other languages
English (en)
French (fr)
Other versions
EP0142437A2 (de
EP0142437A3 (en
Inventor
Michel Couarc'h
Roger Bessouat
Marc Lafaye
Robert Bernet
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.)
Stein Industrie SA
Manutair Moller SA
Original Assignee
Stein Industrie SA
Manutair Moller SA
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
Priority claimed from FR8317811A external-priority patent/FR2554552B1/fr
Priority claimed from FR8401774A external-priority patent/FR2559239B2/fr
Application filed by Stein Industrie SA, Manutair Moller SA filed Critical Stein Industrie SA
Priority to AT84402258T priority Critical patent/ATE45025T1/de
Publication of EP0142437A2 publication Critical patent/EP0142437A2/de
Publication of EP0142437A3 publication Critical patent/EP0142437A3/fr
Application granted granted Critical
Publication of EP0142437B1 publication Critical patent/EP0142437B1/de
Expired legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J3/00—Removing solid residues from passages or chambers beyond the fire, e.g. from flues by soot blowers
    • F23J3/06—Systems for accumulating residues from different parts of furnace plant
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23B—METHODS OR APPARATUS FOR COMBUSTION USING ONLY SOLID FUEL
    • F23B5/00—Combustion apparatus with arrangements for burning uncombusted material from primary combustion
    • F23B5/02—Combustion apparatus with arrangements for burning uncombusted material from primary combustion in main combustion chamber

Definitions

  • the present invention relates to a method and a device for re-injecting flown particles into a solid fuel boiler of the so-called “jet engine with retro grid” type.
  • Such a boiler is characterized by the fact that it is supplied with fuel, for example coal with a particle size of up to several tens of millimeters, or else wood, bark, bagasse, that is to say sugar cane, or other comparable solid fuels, by means arranged in a first zone of the boiler and which continuously project a determined charge of the fuel along a trajectory bringing the latter into a second zone of the boiler, on a grid animated by a return movement from this second zone to the first; combustion begins during said trajectory and continues not only during the end thereof but also on the grate, where this combustion ends so that the grate brings only clinkers into the first zone, where these bottom ash are evacuated.
  • fuel for example coal with a particle size of up to several tens of millimeters, or else wood, bark, bagasse, that is to say sugar cane, or other comparable solid fuels
  • boilers of this type When compared with boilers of other known types, boilers of this type have a number of interesting advantages.
  • boilers of this type provide the advantage of using coals of varied particle size, and in particular coals of much larger particle size, which eliminates grinding means, costly in investment, in maintenance and energy consumption, inextricably linked to pulverized coal boilers.
  • the object of the present invention is to eliminate such a risk, to allow a total reinjection of the solid particles sampled by the various successive dust collectors or separators, including the finest particles separated immediately before rejection of the fumes into the atmosphere.
  • the flow rate, in fine particles, of the corresponding separation means can possibly be very irregular, for example during an accidental or voluntary unclogging of the latter, or by repercussion, after a certain time, of a significant variation in the load of the boiler, and that, however, the transformation of this irregular flow into a continuous flow, at least approximately proportional to the load of the boiler, makes it possible not to disturb the combustion in this boiler by reinjection, it is that is to say to reinject to all the load values without heating irregularity, whatever the disturbances which may affect the instantaneous flow rate of the means for separating fine particles.
  • the flow of transport air must be such that this air does not disturb the combustion inside the boiler either, and in particular that it does not disturb the combustion of the reinjected particles thus transported; taking into account the high carbon content of these particles and their almost zero volatile matter content, the concentration of fine particles reinjected relative to the air which transports them should be sufficiently high, and we have obtained good results with a ratio of the mass flow rate of fine particles to the mass flow rate of transport air of the latter of between 1 and 10 approximately, these figures being given by way of nonlimiting example.
  • volume flow rate of the transport air is advantageously substantially constant, although adjustable, only the flow rate of fine particles in this air varies, in order to ensure a regular injection speed.
  • the method according to the invention makes it possible to reinject all of the solid particles taken from the fumes before evacuation of the latter to the atmosphere, and to burn the com part. bustible with these particles in the best conditions, which makes it possible to achieve significant savings in fuel without, moreover, resulting in a complication of the installations; this results in an optimal use of the fuel, in every respect comparable to that obtained by a pulverized coal boiler, without the need to provide a grinder, a particularly significant drawback of such boilers.
  • the total reinjection makes it possible to extract waste, in practice clinkers, only in a single zone and in a space-saving form which is easy to reprocess.
  • the connection is made by pneumatic transport, on the one hand, the means for discharging particles from the second separation means into the buffer capacity and, on the other hand, the latter, which makes it possible to dissociate it from these dumping means and in particular to juxtapose them, that is to say not to place it immediately below;
  • the device comprises a second source of pressurized air, a second pneumatic transport line connecting this second source to the buffer capacity, the means for discharging particles from the second separation means in the buffer capacity opening into this second conduct by prohibiting direct communication between the latter and the second separation means.
  • the source of pressurized air mentioned first intended to supply the pneumatic conveying line leading to means for continuous sampling of particles in the buffer capacity by means of injection into the boiler, is constituted by an upper part of the buffer capacity; in other words, the same transport air is then used to successively route the particles from the discharge means to the buffer capacity, then to the particles from the buffer capacity to the boiler.
  • the second separation means comprise a plurality of separators connected in series and / or in parallel, between the first separation means and the smoke evacuation means, by the smoke transport means, it is then possible to provide for a discharge of all of these separators in a single buffer capacity without being obliged to communicate to the latter dimensions in plan corresponding to those of all of the second separation means thus formed;
  • the device according to the present invention is then characterized in that means are provided for discharging particles from each of the separators into the single buffer capacity, these means for discharging clogging in said second pipe, which is common, by prohibiting direct communication between this pipe and the separators.
  • This solution is advantageous not only in terms of space, but also in terms of simplification of the means used for regulating the operation, simply because of the uniqueness of the buffer capacity.
  • the means for controlling the flow rate of the means for continuously sampling particles in the or each buffer capacity to be charged to the boiler include means for controlling this flow rate to maintain an average level of particles in this buffer capacity, which makes it possible to gradually absorb, without disturbing the reinjection and combustion of the particles in the boiler, any sudden variations in the charge of particles received by the buffer capacity due to the repercussion, with delay, of an abrupt variation in the charge of the boiler, or also of unclogging the second separation means and more precisely, when the latter comprise several dust collectors, of unclogging one of these dust collectors or more of them.
  • FIG. 1 where we have designated by 1 a coal boiler, internally having a hearth 2 delimited downwards by an approximately horizontal grid 3 constituted by an endless conveyor 4 passing right through share the boiler 1, approximately horizontally, and respectively bypassing on either side thereof deflection means 5, 6 which define in particular in the conveyor 4 an upper strand 7, approximately horizontal, including an intermediate zone between the means bypass 5 and 6 constitutes grid 3; motor means, not shown, animate the conveyor 4 with a movement such that its upper strand 7, that is to say the grid 3, performs an approximately horizontal translational movement 8.
  • a combustion of the coal thus introduced into the hearth 2 begins during the crossing of the path 20 and continues on the grid 3, facilitated by an injection of primary air into the hearth 2 via a sheath 22 opening inside thereof under the upper strand 7 of the conveyor 4, that is to say under the grid 3, and by an injection of secondary air by nozzles such as 23 , 24 opening into the hearth 2, in the faces 108, 109 of the boiler corresponding respectively to the upstream 21 and downstream 9 zones of the grid 3, at an intermediate level between that of the grid 3 and that of the spraying device 17 as well as, preferably, at a level higher than that of the projection device 17, and close to this level.
  • the speed of movement of the grid 3 in the direction 8 is established so that the coal deposited on this grid in the upstream zone 21 thereof is reduced to clinker state upon its arrival in the downstream zone 9, this bottom ash being evacuated by gravity bypassing, by the conveyor 4, the deflecting means 6 placed downstream if one refers to the direction 8, as has been shown diagrammatically at 25.
  • the combustion of the coal during the crossing of the path 20 and on the grid 3 causes a release 26 of smoke that from the walls 27 of the boiler, delimiting the hearth 2 laterally and upwards, completely guide towards a duct 28 approximately horizontal, by making them pass through an evaporator 29 comprising a network of vertical tubes connecting a lower balloon 30 to an upper balloon 31 to vaporize a liquid completely filling the lower balloon 30 and the network of tubes, and partially the upper balloon 31; the latter is connected above the level of the liquid to a manifold 32 for steam outlet from the boiler, by means of a superheater 34 placed on the forced passage of the fumes, and below the level of the liquid to a manifold 33 of water entering the boiler, via an economizer exchanger 35 also placed on the forced passage of fumes.
  • the output speed of the motor 16 is controlled by the flow of steam to be produced to meet the needs of the user, or load of the boiler.
  • the conduit 28 successively routes the fumes taken from the boiler 1 to first separation means 36 intended to separate the larger particles therefrom, then to second separation means 43 intended to separate the finer particles before routing the fumes thus dedusted towards means of evacuation to the atmosphere, shown schematically in 44.
  • the first separation means 36 can be constituted by any known device, capable of producing coarse dusting; they can be constituted for example by a mechanical dust collector, for example centrifugal, or by the first field of an electrostatic separator.
  • these withdrawal and reinjection means comprise a vertical pipe 38, provided with two juxtaposed valves 39 , 40 and in which the hopper 37 opens downwards, this pipe 38 opening itself downwards in an intermediate zone of a horizontal pipe 84 for pneumatic transport joining a source of pressurized air 42 to the hearth 2 of the boiler 1, into which this pipe 84 opens approximately horizontally, as indicated at 41, above the upstream zone 21 of the grid 3, at a level corresponding approximately to that of the designer 17 or at a lower level, such so that the particles thus reinjected at 41 inside the boiler 1 are taken up by the coal projected along the path 20 by the sprayer 17, and then follow this path with the e coal thus projected.
  • the parameters of this reinjection of the largest particles separated from the fumes in the means 36 can be easily determined by a person skilled in the art; one could also choose other modes, already known, of reintroducing such particles into the hearth, such as for example a reintroduction by the sprayer 17, taking into account the particle size of the particles thus reinjected at 41, the combustion of these particles without re-flight, together with the coal introduced along the path 20 by the sprayer 17, does not pose the particular problems indicated above, linked to the re-injection of particles of finer particle size, which are resolved in accordance with the present invention.
  • the second separation means 43 consist of three separators 45, 46, 47, that the smoke travels successively in this order, in series, losing particles of increasingly fine collected in a respective lower hopper 48, 49, 50 of these separators 45, 46, 47; these separators can be either fields of the same electrostatic dust collector, or dust collectors of a different type.
  • Each of these hoppers 48, 49, 50 opens downwards onto a respective valve 51, 52, 53 capable of closing it in a gas-tight manner or to open it to allow the descent, by gravity, of the solid particles collected.
  • each of the valves 51, 52, 53 is disposed a respective intermediate hopper 54, 55, 56, sealed, having an interior volume such that each opening of the associated valve 51, 52, 53, it can receive all of the load of solid particles from the lower hopper 48, 49, 50 of the associated separator 45, 46, 47.
  • each valve 51, 52, 53, normally closed, to empty the lower hopper 48, 49, 50 of the corresponding separator is carried out either when the latter contains a predetermined volume of particles, in function of which is chosen the volume of the associated intermediate hopper 54, 55, 56, either cyclically with a chosen periodicity so that the volume of particles in this lower separator hopper never exceeds this predetermined volume.
  • Each of the intermediate hoppers 54, 55, 56 opens downwards onto a valve 57, 58, 59 at any point similar to the valves 51, 52, 53.
  • each of the intermediate hoppers 54, 55, 56 at the bottom of the lower part thereof opens a respective pipe 100, 101, 102 connected in branch to a pipe 97 which will be described later, and which conveys pressurized air supplied by a volumetric booster 98; each of these pipes 100, 101, 102 makes it possible to inject into the associated intermediate hopper 54, 55, 56, an air for fluidizing the particles therein, the flow rate of this air being able to be adjusted individually by an appropriate valve 103 of line 100, 104 of line 101, 105 of line 102.
  • each of the intermediate hoppers 54, 55, 56 in a state of fluidity such that they can easily flow down out of it when the valve 57, 58, 59 is open.
  • each valve 57, 58, 59 opens onto a respective vertical gravity discharge pipe 94.
  • 95, 96 and the various pipes 94, 95, 96 themselves open down into the pipe 97 mentioned above. , approximately horizontal, in locations distributed along it downstream of the zone from which the fluidization air lines 100, 101, 102 are derived, if one refers to a direction 99 of circulation of the air in this pipe 97, imposed by the volumetric booster 98; a diphragm 106 is interposed in the pipe 97 between the outlet of the various pipes 94, 95, 96 and the mouth of the pipes 100, 101, 102 to cause an air passage in the latter.
  • the air conveyed by the pipe 97 at a flow rate adjusted by adjusting the volumetric booster 98 can successively take charge of the particles taken from the intermediate hopper 56 when the valve 59 is open, and which fall via the pipe 96, the particles taken from the intermediate hopper 55 when the valve 58 is open, and which fall via the line 95, and the particles taken from the intermediate hopper 54 when the valve 57 is open, and which fall via the line 94; it will be noted that this order, chosen by way of example, is not characteristic of the invention and is therefore not limiting of the latter.
  • the air circulating in the pipe 97 conveys in this direction 99 all the particles thus received up to the part upper 107 with a single buffer capacity 60, waterproof, delimiting an internal volume greater than the sum of the respective volumes of the intermediate hoppers 54, 55, 56 so that it can permanently contain a volume of particles much greater than the volume which can reach the intermediate hoppers 54, 55, 56 when the valves 51, 52, 53 connecting them with the respective associated separators 45, 46, 47 are open; in addition, the volume and the shape of the buffer capacity 60 are such that, when the latter receives, via the pneumatic conveying line 97, intermediate hoppers 54, 55, 56 a load of solid particles by opening the valves 57, 58, 59, there follows in the buffer capacity a small variation in the level of the charge of solid particles therein.
  • the buffer capacity 60 has a hopper-shaped lower part, tapering gradually downwards, and an upper part 107 of constant cross section in a horizontal plane, the lower part being intended to be permanently filled with particles over the whole of its height, as well as the upper part 107 over part of its height.
  • Buffer capacity 60 is thus associated with an upper average level 63 of its particle charge; a level sensor 91, associated with the buffer capacity 60, makes it possible to detect and either quantify or compare to a predetermined threshold or to several predetermined thresholds, the possible differences between the actual level of particles in the buffer capacity and the level predetermined means 63, corresponding to this buffer capacity; such sensors are known to those skilled in the art.
  • Each intermediate hopper 54, 55, 56 constitutes an airlock allowing the passage of particles from the lower hopper 48, 49, 50 of the respective associated separator 45, 46, 47 to the buffer capacity 60, via line 97, while preventing communication direct, with the possibility of gas passage, between the interior volume of this buffer capacity and the separators 45, 46, 47; for this purpose, in service, each of the valves 51, 52, 53 is only open on condition that the valve 57, 58, 59 associated with the same intermediate hopper 54, 55, 56 is closed, and each of these valves 57, 58, 59 is only open on condition that the valve 51, 52, 53 associated with the same intermediate hopper 54, 55, 56 is closed; in practice, an opening then closing of each valve 57, 58, 59, normally closed, to empty the associated intermediate hopper 54, 55, 56 occurs after each opening ture-closing of the corresponding valve 51, 52, 53.
  • a pipe 85 which makes it possible to inject into the buffer capacity 60 a fluidizing air of the particles therein, the flow rate of this air can be regulated by a suitable valve 88 of the pipe 85; this air comes for example from the source 42, the pipe 85 then being connected in bypass on the pipe 84, between this source 42 and the outlet of the pipe 38, in a manner not shown but similar to what has been described with reference to lines 100, 101, 102 and 97.
  • the particles are thus maintained, in the buffer capacity 60, in a state of fluidity such that they can be easily sampled by means of sampling at a continuous, adjustable flow rate, onto which this buffer capacity 60 opens down;
  • these removal means are advantageously designated by 69 constituted by a rotary airlock or alveolar distributor, comprising, as is known, a plurality of pallets driven to rotation about an axis, by a motor 72, inside a envelope with which these pallets delimit cells which the rotation of the pallets puts in communication alternately with the buffer capacity 60, upwards, and, downwards, with a vertical evacuation pipe by gravity 75;
  • the flow rate of such a honeycomb distributor in terms of volume flow rate or mass flow rate, is controlled by the speed of rotation of the pallets, that is to say by their driving speed by the associated motor 72.
  • the pipe 75 opens into an approximately horizontal section of a pipe 66 which takes up the air under pressure, supplied by the volumetric booster 98 via the pipe 97, in the upper part 107 of the buffer capacity 60 and conveys this air in a direction of flow 78; a throttle 68 is interposed in the pipe 66, between its mouth in the upper part 107 of the buffer capacity 60 and the outlet of the pipe 75 in this pipe 66, to establish at the outlet of the pipe 75 a pressure lower than that which prevails in the upper part 107 of the buffer capacity 60.
  • the air conveyed through line 66 at a flow rate adjusted by adjusting the volumetric booster 98, takes care of the particles taken from the buffer capacity 60 at a flow rate determined by the alveolar distributor 69, and which fall via the driving 75.
  • the air circulating in the pipe 66 conveys in this direction 78 the particles thus received up to injection means 79 of any type known in itself, used for injecting pulverulent materials into boilers, which injection means 79 open into the hearth 2 approximately horizontally, above the upstream zone 21 of the grid 3, at a level which is intermediate between the levels nozzles 23, 24 for injecting secondary air and corresponding at least approximately to the level of injection 41 of the larger particles separated by the first separation means 36; the injection means 79 are oriented towards the path 20, and more precisely towards a part thereof close to the grid in the upstream region 21 thereof, to favor the handling of the fine particles thus injected at 79 by the coal projected by the spraying device 17 along the path 20, and the monitoring of this path to the grid 3 by these fine particles.
  • injection means 79 of any type known in itself, used for injecting pulverulent materials into boilers, which injection means 79 open into the hearth 2 approximately horizontally, above the upstream zone 21 of the grid 3, at a level which is intermediate between the levels nozzles
  • the flow of air for transporting the particles in the pipe 66 and the flow of particles in this air, via the withdrawal means in the buffer capacity 60, here constituted by the alveolar distributor 69, are continuous, and the flow of particles downstream of the outlet of the pipe 75 in the pipe 66, expressed in terms of mass flow or volume flow, is at least approximately proportional to the load of the boiler, for example to the flow of the supply means 10 expressed in the same units, which is representative of this charge.
  • the flow rate of the withdrawal means in the buffer capacity 60 is controlled by the load of the boiler so as to be at least approximately proportional to it.
  • the flow of solid particles received in the dust collectors 45, 46, 47 then conveyed to the buffer capacity 60 is substantially proportional to the feed rate of the coal boiler 14 from the hopper 11, itself representative of the load of the boiler, there is provided for this purpose, in the illustrated embodiment, a servo motor 72 to the information supplied by the level sensor 91, so as to limit the variations in the level of particles in the buffer capacity 60 in comparison with the predetermined average level 63; it will be noted that in this way it is also ensured that the sampling means 69 receive particles, in the buffer capacity 60, an approximately constant force allowing them to work under conditions themselves approximately constant, independently of the respective emptying intermediate hoppers 54, 55, 56.
  • the means making it possible to control the speed of rotation of the motor 72 to the information supplied by the level sensor 91 have been shown diagrammatically by a link in dashed lines 81; they can be chosen by a person skilled in the art in a wide range of possibilities without departing from the scope of the present invention, depending in particular on the type of level sensor 91 used, depending on the case, a possibility of step-by-step correction or a possibility of continuous correction.
  • the means used for this purpose which can be chosen by a person skilled in the art from a wide range of possibilities and have therefore only been shown diagrammatically by a dashed line 80, tend, for example, to link in a predetermined proportionality relationship , as a function of the quantities of solid particles expected in the dust collectors 45, 46, 47 for determined loads of the
  • the mode of control of the flow rate of the withdrawal means in the buffer capacity 60 charged to the boiler in the direction of at least approximate proportionality, which has just been described, giving priority to the detection of the level of particles in buffer capacity 60 and involving only in terms of trend the load of the boiler at the instant considered, could be replaced by a control mode in the direction of such proportionality which will be described more far with reference to FIGS. 2 to 4, involving primarily the charge of the boiler and by way of correction of level detection in the buffer tank or in each buffer tank; conversely, the mode which has just been described may be adopted for all or for each of the buffer capacities which will be described with reference to FIGS. 2 to 4.
  • the flow of transport air in this line is adjusted by action on the volumetric booster 98 so that the mass flow of the particles introduced into line 66 either in a ratio to the mass flow of air in this line, of between 1 and 10 approximately; these figures, given by way of nonlimiting example, correspond to a high concentration of the particle-air suspension injected at 79 into the boiler, such a high concentration being favorable to the combustion of the particles upon their arrival in the boiler and to their sintering in the form of bottom ash once they have burned and they are on the grid 3.
  • each valve 57, 58, 59 opens downwards onto a respective buffer capacity 360, 361, 362 sealed, delimiting an interior volume greater than that of the intermediate hopper 54, 55, 56 associated so that it can permanently contain a volume of particles much greater than the volume which can reach the associated intermediate hopper 54, 55, 56 when the valve 51, 52, 53 connecting it ci with the associated separator 45, 46, 47 is open; in addition, the volume and the shape of each buffer capacity 360, 361, 362 are such that, when the latter receives from the associated intermediate hopper 54, 55, 56 a load of solid particles by opening the valve connecting them 57, 58, 59 it follows in the buffer capacity a small variation in the level of the charge of solid particles therein.
  • Each of the buffer capacities 360, 361, 362 has a hopper-shaped lower part, progressively narrowing downwards, and an upper part of constant section in a horizontal plane, the lower part being intended to be permanently filled with particles on its entire height, as well as the upper part of part of its height.
  • Each buffer capacity 360, 361, 362 is thus associated with an upper average level 363, 364, 365 of its charge in particles; a level sensor 391, 392, 393 respectively associated with each buffer capacity 360, 361, 362 makes it possible to detect and either quantify or compare to a predetermined threshold or to several predetermined thresholds, the possible differences between the actual level of particles in the buffer capacity considered and the predetermined average level 363, 364, 365 corresponding to this buffer capacity; such sensors are known to those skilled in the art.
  • Each intermediate hopper 54, 55, 56 constitutes an airlock allowing the passage of the particles of the lower hopper 48. 49. 50 of the separator respectively associated 45, 46, 47 with the corresponding buffer capacity 360, 361, 362 without at any time , the internal volume of the latter is put in direct communication, with the possibility of gas passage, with the separator 45, 46, 47; for this purpose, in service, each of the valves 51, 52, 53 is only open on condition that the valve 57, 58, 59 associated with the same intermediate hopper 54, 55, 56 is closed, and each of these valves 57, 58, 59 is only open on condition that the valve 51, 52, 53 associated with the same intermediate hopper 54, 55, 56 is closed; in practice, an opening and then closing of each valve 57, 58, 59, normally closed, to empty the associated intermediate hopper 54, 55, 56 occurs after each opening-closing of the corresponding valve 51, 52, 53.
  • each of the buffer capacities 360, 361, 362 there opens a respective pipe 385, 386, 387 connected in branch to a pipe 366 which will be described later, and which conveys pressurized air supplied by a fan 367; each of these lines 385, 386, 387 makes it possible to inject into the associated buffer capacity 360, 361, 362, an air for fluidizing the particles therein, the flow rate of this air being able to be adjusted individually by an appropriate valve 388 of line 385, 389 of line 386, 390 of line 387.
  • each of the removal means 369, 370, 371 is advantageously constituted by a rotary airlock or alveolar distributor, comprising, as is known, a plurality of pallets driven in rotation about an axis, by a respective motor 372, 373, 374 , inside an envelope with which these pallets delimit cells which the rotation of the pallets puts in communication alternately with the associated buffer capacity 360, 361, 362, upwards, and, downwards, with a vertical pipe gravity discharge 375, 376, 377; the flow rate of such an alveolar distributor, in terms of volume flow rate or mass flow rate, is controlled by the speed of rotation of the pallets, that is to say by their driving speed by the associated motor 37
  • each of the pipes 375, 376, 377 opens into the pipe 366 mentioned above, approximately horizontal, in locations distributed along it downstream of the area from which the pipes 385, 386 are derived, 387 of fluidizing air if one refers to a direction 378 of air circulation in this pipe 366, imposed by the fan 367; a diaphragm 368 is interposed in the pipe 366 between the outlet of the various pipes 375, 376, 377 and the mouth of the pipes 385, 386, 387 to cause an air passage in the latter.
  • the air conveyed through line 366 at a flow rate adjusted by adjusting the fan 367, successively takes care of the particles taken from the buffer capacity 362 at a flow rate determined by the alveolar distributor 371. and which fall via the line 377, the particles taken from the buffer capacity 361. at a rate determined by the honeycomb distributor 370, and which fall via line 376, and the particles taken from the buffer capacity 360 at a rate determined by the honeycomb distributor 369, and falling through line 375; it will be noted that this order, chosen by way of example, is not characteristic of the invention and is therefore not limiting of the latter; other connection methods will also be described later, with reference to FIGS. 3 and 4.
  • the air circulating in the pipe 366 conveys in this direction 378 all the particles thus received up to means injection 379 at all points similar to the injection means 79 described with reference to FIG.
  • the injection means 379 are oriented towards the path 20, and more precisely towards a part thereof close to the grid in the upstream zone 21 thereof, to favor the handling of fine particles as well injected in 379 by the coal projected by the spraying device 17 along the path 20, and the monitoring of this path to the grid 3 by these fine particles.
  • both the air flow in line 366 considered as a transport air flow taking into account the negligible nature of the part of this flow used for fluidization in the buffer capacities 360, 361, 362, and the flow of particles in this air, via the sampling means in the buffer capacities 360, 361, 362 here constituted by the alveolar distributors 369, 370, 371, are continuous, and the flow of particles downstream of the set of lines 375, 376, 377, expressed in terms of mass flow or volume flow, is at least approximately proportional to the load of the boiler, for example to the flow of the supply means 10 expressed in the same units.
  • the means making it possible to correct, step by step or continuously, depending on the type of level sensor 391, 392, 393 used, the speed of rotation of each of the motors 372, 373, 374 in a slave manner to the measurement of the sensor level 391, 392, 393 associated with the same buffer capacity 360, 361, 362 have been simply shown diagrammatically by dashed lines 381, 382, 383; like the means 380, they can be chosen by a person skilled in the art from a wide range of possibilities.
  • the air flow in this pipe is adjusted by action on the fan 367 so that the mass flow of the particles introduced into line 366 is in relation to the mass flow of air in this line , between 1 and 10 approximately;
  • these figures given by way of nonlimiting example, correspond to a high concentration of the particle-air suspension injected at 379 into the boiler, such a high concentration being favorable to the combustion of the particles upon their arrival in the boiler and to their frittate in the form of bottom ash once they have burned and are on the rack 3.
  • FIGS. 3 and 4 illustrate precisely two modifications, in this sense, of the device illustrated in FIG. figure 2.
  • a conduit 128 for conveying the fumes branches out into two parallel branches 128a and 128b each of which connects in series two separators, respectively 145a, 146a as regards line 128a, and 145b and 146b as regards line 128b.
  • Each of these separators 145a, 146a. 145b. 146b has a respective lower hopper 148a, 149a, 148b, 149b opening downwards. via a respective valve 151a, 152a, 151b, 152b, in a respective intermediate hopper 154a, 155a.
  • a single pneumatic conveying line 166 in every point comparable to the line 366 described above and supplied as it with pressurized air by a fan 167 at any point comparable to the fan 367, receives in a distributed manner the lower ends of the various pipes 176b, 176a, 175a, 175b, in this order, to convey the particles which it receives from these pipes, suspended in the 'air, up to single injection means 179, at any point comparable to the means 379 described above, in the focus of the boiler (not shown).
  • the number of separators traversed in series by the fumes, and the nature of these separators can vary to a large extent depending on requirements. estimated by the skilled person; in the case of the embodiments illustrated in FIGS. 3 and 4 in addition, the number of branches derived from the smoke delivery duct 128 or 228 could be greater than two, the ducts then corresponding to the ducts 175a, 176a, 175b, 176b or 275a, 276a, 275b, 276b which can open into a single pneumatic transport line of the type illustrated in 166 in FIG. 3, or into parallel pneumatic transport lines of the type illustrated in 266a and 266b in FIG. 4, or else in series in pneumatic conveying lines connected in parallel.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Thermal Sciences (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Control Of Steam Boilers And Waste-Gas Boilers (AREA)
  • Solid-Fuel Combustion (AREA)

Claims (28)

1. Verfahren zur Rückführung von Flugstaub in einen Heizkessel für feste Brennstoffe, der Brennstoff durch Mittel (10) versorgt wird, die in einer ersten Zone (9) des Heizkessels angeordnet sind und die kontinuierlich eine bestimmte Menge an Brennstoff auf einer Flugbahn (20) auswerfen, die diesen in eine zweite Zone (21) des Heizkessels auf einen Rost (3) führt, der durch einen Rückwärtsantrieb (8) von der zweiten Zone (21) zur ersten (9) bewegt wird, wobei eine Verbrennung über besagter Flugbahn (20) und über dem Rost (3) bewirkt wird, bei der ein Feststoffpartikeln mitführendes Rauchgas (26) gebildet wird, wobei dieses Verfahren aus dem Abzug des Rauchgases aus dem Heizkessel, dessen anschließender Förderung nacheinander in Abscheidemittel (36) für die gröbsten Partikeln und Abscheidemitteln (43) für die feineren Partikeln und im Austrag (44) des Rauchgases nach dieser Abscheidung besteht, während man die Gesamtheit der abgeschiedenen Partikeln in den Heizkessel zurückführt, wobei dieses Verfahren dadurch gekennzeichnet ist, daß man die gröbsten abgetrennten Partikeln und die feineren abgetrennten Partikeln getrennt in den Heizkessel zurückführt:
-derart, wie eventuell, was die gröbsten Partikeln betrifft, bekannt ist, und
- was die feinsten Partikeln betrifft, die durch die entsprechenden Abscheidemittel (43) in unregelmäßiger Fördermenge anfallen, aus folgenden Verfahrensschritten besteht:
a) Umwandeln dieser unregelmäßigen Fördermenge in eine kontinuierliche Fördermenge von Partikeln, die mindestens näherungsweise proportional zur Beschickung des Heizkessels ist,
b) kontinuierliches Einleiten dieser kontinuierlichen Fördermenge von Partikeln in eine kontinuierliche Fördermenge von Transportluft, die für diese feinsten Partikeln geeignet ist,
c) kontinuierliches Fördern dieser Partikeln mittels der besagten Luftfördermenge bis in die Nähe der zweiten Zone (21) des Heizkessels und Einblasen dieser in diese Zone in einen Bereich von besagter Flugbahn (20) nahe bei dem Rost (3) unabhängig von den gröbsten Partikeln.
2. Verfahren nach Anspruch 1, mit Abscheidemitteln (43) für die feineren Partikeln, die aus einer Vielzahl von Abscheidern (45, 46, 47) bestehen, von denen jeder Partikeln mit eigener, unregelmäßiger Fördermenge liefert, dadurch gekennzeichnet, daß man die vorgenannten Verfahrensschritte a) und b) bei der Umwandlung jeder dieser eigenen unregelmäßigen Fördermenge in eine eigene kontinuierliche Fördermenge von Partikeln anwendet, die mindestens näherungsweise proportional zur Beschickung des Heizkessels ist, und wobei diese eigenen, kontinuierlichen Fördermengen von Partikeln anschließend kontinuierlich in besagte kontinuierliche Fördermenge von Transportluft eingeführt werden.
3. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die besagte kontinuierliche Fördermenge von Partikeln von der Lieferung der Abscheidemittel (43) für die feineren Partikeln abhängig ist.
4. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß jede eigene, kontinuierliche Fördermenge an Partikeln abhängig von der eigenen Fördermenge des zugeordneten Abscheiders (45, 46, 47) ist.
5. Verfahren nach einem der Ansprüche 1 und 3, dadurch gekennzeichnet, daß die kontinuierliche Fördermenge an Partikeln von der Fördermenge der Mittel (10) zur Versorgung des Heizkessels mit Brennstoff abhängig ist.
6. Verfahren nach einem der Ansprüche 1 und 4, dadurch gekennzeichet, daß jede eigene, kontinuierliche Fördermenge an Partikeln von der Fördermenge der Mittel (10) zur Versorgung des Heizkessels mit Brennstoff abhängig ist.
7. Verfahren nach einem der Ansprüche 1 bis 6, dadurch gekennzeichnet, daß die Fördermenge an Transportluft im wesentlichen hinsichtlich des Fördervolumens konstant ist.
8. Verfahren nach einem der Ansprüche 1 bis 8, dadurch gekennzeichnet, daß man während dem Verfahrensschritt b) die kontinuierliche Fördermenge an Partikeln in die kontinuierliche Fördermenge an Transportluft in einem Verhältnis von Massenanfall an Partikeln zu Massenanfall an Transportluft zwischen ungefähr 1 und 10 einführt.
9. Vorrichtung zum Rückführen von Flugstaub in einen Heizkessel für feste Brennstoffe, der mit Brennstoff durch Mittel (10) versorgt wird, die in einer ersten Zone (9) des Heizkessels angeordnet sind und die kontinuierlich eine bestimmte Menge an Brennstoff auf einer Flugbahn (20) auswerfen, die diesen in eine zweite Zone (21) des Heizkessels auf einen Rost (3) führt, der durch einen Rückwärtsantrieb (8) von der zweiten Zone (21) zur ersten (9) bewegt wird, wobei eine Verbrennung über besagter Flugbahn (20) und über dem Rost (3) bewirkt wird, bei der ein Feststoffpartikeln mitführenden Rauchgas (26) gebildet wird, wobei sich diese Vorrichtung aufbaut aus:
- Mitteln (27) zum Abzug des Rauchgases aus dem Heizkessel,
- Mitteln (44) zur Abführung des Rauchgases,
- ersten Abscheidemitteln (36) für die Abscheidung von relativ groben Partikeln,
- zweiten Abscheidemitteln (43) für die Abscheidung von relativ feinen Partikeln,
- Mitteln (28) zur Führung des Rauchgases von den Mitteln (27) zum Abzug zu den ersten Abscheidemitteln (36), von den ersten Abscheidemitteln (36) zu den zweiten Abscheidemitteln (43) (und) von den zweiten Abscheidemitteln (43) zu den Mitteln (44) zur Abführung der Rauchgase,
- Mitteln (37, 38, 39, 40, 41, 42. 84) zum Abzug der Partikeln aus den ersten Abscheidemitteln (36) und zur Rückführung dieser Partikeln in den Heizkessel,
- Mitteln zum Abzug der Partikeln aus den zweiten Abscheidemitteln (43) und zur Rückführung dieser Partikeln in den Heizkessel, wobei diese Vorrichtung dadurch gekennzeichnet ist, daß die Mittel zum Abzug der Partikeln aus den zweiten Abscheidemitteln (43) und zur Rückführung dieser Partikeln in den Heizkessel von den Mitteln (37, 38, 39, 40, 41, 42, 84) zum Abzug der Partikeln aus den ersten Abscheidemitteln (36) und der Rückführung dieser Partikeln in den Heizkessel verschieden sind, (und) daß die Mittel zum Abzug der Partikeln aus den zweiten Abscheidemitteln (43) bestehen aus:
a) einem ersten Speicherbehälter (60, 160, 161, 62, 260, 261, 262, 360, 361, 362),
b) Mitteln (51 bis 59) zum Ablassen der ausschließlich von den zweiten Abscheidemitteln (43) kommenden Partikeln in den Speicherbehälter (60, 160, 161, 260, 261, 262, 360, 361, 362), die eine direkte Verbindung zwischen diesen letzteren verhindern,
c) Mitteln (69, 169, 170, 269, 270, 369, 370, 371) zum kontinuierlichen Abzug von Partikeln aus dem untersten Bereich des Speicherbehälters (60, 160, 161, 162, 260, 261, 262, 360, 361, 362) mit verstellbarer Fördermenge,
d) Mitteln (80, 81, 380, 381. 382, 383, 391. 392, 393) zur Steuerung der Fördermenge der Mittel (69, 169, 170, 269, 270, 369, 370, 371) für den kontinuierlichen Abzug der Partikeln aus dem Speicherbehälter (60, 160, 161, 162, 260. 261, 262, 360, 361, 362), abhängig von der Beschickung des Heizkessels, und daß vorgesehen ist:
- eine Quelle (98, 107, 42, 167, 267, 367) zur Lieferung von Druckluft,
- Mittel (79, 179, 279, 379) zur Einleitung von ausschließlich aus den zweiten Abscheidemittein (43) kommenden Partikeln, wobei diese Mittel (79, 179, 279, 379) zur Einleitung in der Nähe der zweiten Zone (21) des Heizkessels angeordnet sind und in einen Bereich der besagten Flugbahn (20) nahe dem Rost (3) in dieser zweiten Zone (21) münden,
- ein Leitungsrohr (66, 166, 266, 366) für den pneumatischen Transport von ausschließlich aus den zweiten Abscheidemitteln (43) kommenden Partikeln, wobei dieses Leitungsrohr (66, 166, 266, 366) die Quelle (98, 107, 42, 167, 267, 367) zur Lieferung von Druckluft mit den Mitteln (79, 179, 279, 379), zur Einleitung verbindet, wobei die Mittel (69, 169, 170, 269, 270, 369, 370, 371) zum kontinuierlichen Abzug der Partikeln in den Speicherbehälter (60, 160, 161, 162, 260, 261, 262, 360, 361, 362) in besagtes Leitungsrohr (66, 166, 366, 366) münden.
10. Vorrichtung nach Anspruch 9, bei der die zweiten Abscheidemittel (43) aus einer Vielzahl von Abscheidern (45, 46, 47, 145a, 146a, 145b, 146b, 245a, 246a, 245b, 246b) bestehen, die in Reihe und/oder parallel durch die Mittel (28, 128, 228) zur Führung der Rauchgase zwischen den ersten Abscheidemitteln (36) und den Mitteln (44) zur Abführung der Rauchgase geschaltet sind, dadurch gekennzeichnet, daß die Mittel zum Abzug der Partikeln aus den zweiten Abscheidemitteln (43) bestehen aus:
a) einer Vielzahl von Speicherbehältern (160a, 161a,160b,161b,260a,261a,260b,261b,360,361, 362), von denen jeder mit wenigstens einem der besagten Abscheidern verbunden ist und der unter diesen angeordnet ist,
b) Mitteln (51 bis 59, 151a, 152a, 151b, 152b, 154a, 155a, 154b, 155b, 157a, 158a, 157b, 158b, 251a, 252a, 251b, 252b, 254a, 255a, 254b, 255b, 257a, 258a, 257b, 258b) zum Ablassen der Partikeln aus diesem Abscheider in den damit verbundenen Speicherbehälter, wobei eine direkte Verbindung zwischen diesen verhindert wird,
c) Mitteln (169a, 170a, 169b, 170b, 269a, 270a, 269b, 270b, 369, 370, 371) zum kontinuierlichen Abzug von Partikeln aus dem untersten Bereich von jedem Speicherbehälter mit verstellbarer Fördermenge,
d) Mitteln (380, 381, 382, 383, 391, 392, 393) zur Steuerung der Fördermenge von jedem der kontinuierlichen Mitteln zum Abzug der Partikeln aus dem untersten Bereich eines Speicherbehälters, abhängig von der Beschickung des Heizkessels, und daß die kontinuierlichen Mittel zum Abzug der Partikeln aus dem untersten Bereich der verschiedenen Speicherbehälter in die besagte Förderleitung (66, 166, 266, 366) münden, die gemeinsam ist.
11. Vorrichtung nach Anspruch 9, dadurch gekennzeichnet, daß die Mittel zum Ablassen der Partikeln aus den zweiten Abscheidemitteln (43) in den Speicherbehälter (60, 160, 161, 162, 260, 261, 262, 360, 361, 362) eine Schleusenkammer (54. 55, 56, 154, 155, 156, 254, 255, 256) mit einem verfügbaren Volumen besitzen, das gegenüber dem dieses Speicherbehälters (60, 160, 161, 162, 260, 261, 262, 360, 361, 362) klein ist.
12. Vorrichtung nach Anspruch 10, dadurch gekennzeichnet, daß die Mittel zum Ablassen der Partikeln aus einem Abscheider (45, 46, 47) in einen damit verbundenen Speicherbehälter (60, 160, 161, 162, 260, 261, 262, 360, 361, 362) eine Schleusenkammer (54, 55, 56, 154, 155, 156, 254, 255, 256) mit einem verfügbaren Volumen besitzen, das gegenüber dem dieses Speicherbehälters klein ist.
13. Vorrichtung nach einem der Ansprüche 9 bis 12, dadurch gekennzeichnet, daß die Mittel (380, 381, 382, 383, 391, 392, 393) zur Steuerung der Fördermenge der Mittel (69, 169, 170, 269, 270, 369, 370, 371) zum kontinuierlichen Abzug der Partikeln aus dem oder jedem Speicherbehälter (60, 160, 161, 162, 260, 261, 262, 360, 361, 362) abhängig von der Beschickung des Heizkessels aus Steuermitteln (381, 382, 383, 391, 392, 393) bestehen, die die Fördermenge an Partikeln auf einem mittleren Niveau (363, 364, 365) in diesem letzteren (Speicherbehälter) halten.
14. Vorrichtung nach einem der Ansprüche 9 bis 13, dadurch gekennzeichnet, daß die Mittel (380, 381, 382, 383, 391, 392, 393) zur Steuerung der Fördermenge der Mittel (69, 169, 170, 269, 270, 369, 370, 371) zum kontinuierlichen Abzug der Partikeln aus dem oder jedem Speicherbehälter (60, 160, 161, 162, 260, 261, 262, 360, 361, 362) abhängig von der Beschickung des Heizkessels Mittel (380) für die Steuerung dieser Fördermenge abhängig von der Fördermenge der Mittel (10) für die Versorgung des Heizkessels mit Brennstoff besitzen.
15. Vorrichtung nach einem der Ansprüche 9 bis 14, dadurch gekennzeichnet, daß Mittel (385 bis 390) für die Fluidisierung der Partikeln in dem oder jedem Speicherbehälter (360, 361, 362) vorgesehen sind.
16. Vorrichtung nach einem der Ansprüche 9 bis 15, dadurch gekennzeichnet, daß die Mittel (69, 169, 170, 269, 270, 369, 370, 371) zum Abzug der Partikeln aus dem oder jedem Speicherbehälter (60, 160, 161, 162, 260, 261, 262, 360, 361, 362) ein Zellenrad besitzen.
17. Vorrichtung nach Anspruch 9, dadurch gekennzeichnet, daß vorgesehen ist,
- eine zweite Druckluftquelle (98),
- eine zweite Förderleitung (97) für den pneumatischen Transport, die diese zweite Druckluftquelle (98) mit dem Speicherbehälter (60) verbindet, wobei die Mittel (51 bis 59) zum Ablassen der Partikeln aus den zweiten Abscheidemitteln (43) in den Speicherbehälter (60) in diese zweite Förderleitung (97) einmünden und eine direkte Verbindung zwischen letzterer und den zweiten Abscheidemittlen (43) verhindern.
18. Vorrichtung nach Anspruch 17, wobei die zweiten Abscheidemittel (43) aus einer Vielzahl von Abscheidern (45, 46, 47) bestehen, die durch Mittel (28) zur Führung der Rauchgase in Reihe und/oder parallel zwischen den ersten Abscheidemitteln (36) und den Mitteln (44) zur Abführung des Rauchgases angeordnet sind, dadurch gekennzeichnet, daß ein einziger Speicherbehälter (60) mit Mitteln (51 bis 59) zum Ablassen der Partikeln aus jedem der Abscheider (45 bis 47) in den einzigen Speicherbehälter (60) vorgesehen ist, wobei diese Mittel zum Ablassen in besagte zweite Förderleitung (97), die gemeinsam ist, münden, und eine direkte Verbindung zwischen dieser und den Abscheidern verhindern.
19. Vorrichtung nach Anspruch 17, dadurch gekennzeichnet, daß die Mittel zum Ablassen der Partikeln aus den zweiten Abscheidemitteln (43) in den Speicherbehälter (60) eine Schleusenkammer (54, 55, 56) mit einem verfügbaren Volumen besitzen, das gegenüber dem des Speicherbehälters (60) klein ist.
20. Vorrichtung nach Anspruch 18, dadurch gekennzeichnet, daß die Mittel zum Ablassen der Partikeln aus den Abscheidern (45, 46, 47) in den einzigen Speicherbehälter (60) eine zugeordnete Schleusenkammer (54, 55, 56) besitzen, wobei das verfügbare Gesamtvolumen der Schleusenkammern geringer als das des Speicherbehälters ist.
21. Vorrichtung nach einem der Ansprüche 19 und 20, dadurch gekennzeichnet, daß Mittel (100 bis 105) zur Fluidisierung der Partikeln in dem oder jeder Schleusenkammer (54, 55, 56) vorgesehen sind.
22. Vorrichtung nach einem der Ansprüche 17 bis 21, dadurch gekennzeichnet, daß die Mittel (80, 81, 91) zur Steuerung der mittleren Fördermenge der Mittel (69) zum kontinuierlichen Abzug der Partikeln aus dem Speicherbehälter (60) abhängig von der Beschickung des Heizkessels aus Mitteln (81, 91) zur Steuerung bestehen, die diese Fördermenge auf einem mittleren Niveau (63) in diesem letzteren (Speicherbehälter) halten.
23. Vorrichtung nach einem der Ansprüche 17 bis 22, dadurch gekennzeichnet, daß die Mittel (80, 81, 91) zur Steuerung der mittleren Fördermenge der Mittel (69) zum kontinuierlichen Abzug der Partikeln aus dem Speicherbehälter (60) abhängig von der Beschickung des Heizkessels Mittel (80) besitzen, die diese Fördermenge abhängig von der Fördermenge der Mittel (10) zur Versorgung des Heizkessels mit Brennstoff steuern.
24. Vorrichtung nach einem der Ansprüche 17 bis 23, dadurch gekennzeichnet, daß Mittel (85, 88) für die Fluidisierung der Partikeln in dem Speicherbehälter (60) vorgesehen sind.
25. Vorrichtung nach einem der Ansprüche 17 bis 24, dadurch gekennzeichnet, daß die Mittel (69) zum Abzug der Partikeln aus dem Speicherbehälter (60) ein Zellenrad besitzen.
26. Vorrichtung nach einem der Ansprüche 17 bis 25, dadurch gekennzeichnet, daß die erste Quelle (98, 107) durch einen Oberbereich (107) des Speicherbehälters (60) und die zweite Quelle (98) gebildet wird.
27. Vorrichtung nach einem der Ansprüche 17 bis 25, dadurch gekennzeichnet, daß Mittel (66b) zur Rückführung des Gases aus dem Speicherbehälter gegen die zweiten Abscheidemitteln (43) vorgesehen sind und die beiden Quellen (98, 42) getrennt sind.
28. Vorrichtung nach einem der Ansprüche 17 bis 25, dadurch gekennzeichnet, daß der Speicherbehälter zur Umgebungsluft durch einen Filter (66b) geöffnet ist und die beiden Quellen (98, 42) getrennt sind.
EP84402258A 1983-11-09 1984-11-09 Verfahren und Vorrichtung zum Wiedereinblasen von flugstaub in einen Heizkessel für festen Brennstoff Expired EP0142437B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT84402258T ATE45025T1 (de) 1983-11-09 1984-11-09 Verfahren und vorrichtung zum wiedereinblasen von flugstaub in einen heizkessel fuer festen brennstoff.

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
FR8317811 1983-11-09
FR8317811A FR2554552B1 (fr) 1983-11-09 1983-11-09 Procede et dispositif de reinjection de particules envolees dans une chaudiere a combustible solide
FR8401774 1984-02-06
FR8401774A FR2559239B2 (fr) 1984-02-06 1984-02-06 Dispositif de reinjection de particules envolees dans une chaudiere a combustible solide

Publications (3)

Publication Number Publication Date
EP0142437A2 EP0142437A2 (de) 1985-05-22
EP0142437A3 EP0142437A3 (en) 1985-09-18
EP0142437B1 true EP0142437B1 (de) 1989-07-26

Family

ID=26223667

Family Applications (1)

Application Number Title Priority Date Filing Date
EP84402258A Expired EP0142437B1 (de) 1983-11-09 1984-11-09 Verfahren und Vorrichtung zum Wiedereinblasen von flugstaub in einen Heizkessel für festen Brennstoff

Country Status (7)

Country Link
US (2) US4648329A (de)
EP (1) EP0142437B1 (de)
JP (1) JPH0739842B2 (de)
AU (1) AU577563B2 (de)
CA (1) CA1252356A (de)
DE (1) DE3479148D1 (de)
WO (1) WO1985002246A1 (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3736912A1 (de) * 1986-10-31 1988-05-19 Babcock Hitachi Kk Denitrierungsbehandlungsverfahren

Families Citing this family (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2595789B1 (fr) * 1986-03-14 1989-06-16 Bekakis Basile Procede et dispositif de reinjection des particules separees dans une chaudiere a combustible solide
US4697530A (en) * 1986-12-23 1987-10-06 Dumont Holding Company Underfed stoker boiler for burning bituminous coal and other solid fuel particles
DE3724563A1 (de) * 1987-07-24 1989-02-02 Kernforschungsanlage Juelich Verfahren zur thermischen behandlung von abfaellen sowie vorrichtung zur durchfuehrung dieses verfahrens
US4905613A (en) * 1988-09-09 1990-03-06 Detroit Stoker Company Fuel feeder
US5030054A (en) * 1989-06-23 1991-07-09 Detroit Stoker Company Combination mechanical/pneumatic coal feeder
US4926764A (en) * 1989-08-17 1990-05-22 Den Broek Jos Van Sewage sludge treatment system
DE4132770A1 (de) * 1991-10-02 1993-04-08 Kurt Kugler Flugstaubentsorgung, minimierung der als sonderabfall zu entsorgenden flugstaubmenge
US5239935A (en) * 1991-11-19 1993-08-31 Detroit Stoker Company Oscillating damper and air-swept distributor
US5484476A (en) * 1994-01-11 1996-01-16 Electric Power Research Institute, Inc. Method for preheating fly ash
IT1276747B1 (it) * 1995-06-19 1997-11-03 Magaldi Ricerche & Brevetti Estrattore/raffreddatore di materiali sfusi
US5655463A (en) * 1995-06-19 1997-08-12 Douglas Nagel Apparatus and method for burning waste material
US5937772A (en) * 1997-07-30 1999-08-17 Institute Of Gas Technology Reburn process
EP1230515B1 (de) 1999-11-02 2006-12-27 Consolidated Engineering Company, Inc. Verfahren und vorrichtung zur verbrennung von restkohlenstoffen in flugasche
US7047894B2 (en) * 1999-11-02 2006-05-23 Consolidated Engineering Company, Inc. Method and apparatus for combustion of residual carbon in fly ash
DE102004027563A1 (de) * 2004-06-04 2005-12-22 Joint Solar Silicon Gmbh & Co. Kg Silizium sowie Verfahren zu dessen Herstellung
US7252134B2 (en) * 2004-06-28 2007-08-07 Consolidated Engineering Company, Inc. Method and apparatus for removal of flashing and blockages from a casting
US20070289713A1 (en) * 2006-06-15 2007-12-20 Crafton Scott P Methods and system for manufacturing castings utilizing an automated flexible manufacturing system
JP5508022B2 (ja) * 2006-12-07 2014-05-28 ダブリュティイー ウェイスト トゥ エナジー カナダ インコーポレイテッド バッチ式廃棄物ガス化工程
US20100206203A1 (en) * 2007-05-21 2010-08-19 Mario Magaldi System for dry extracting/cooling heterogeneous material ashes with control of the air inlet in the combustion chamber
LU91376B1 (en) * 2007-11-16 2009-05-18 Wurth Paul Sa Injections system for solid particles
PL383941A1 (pl) * 2007-12-03 2009-06-08 Witold Kowalewski Kocioł rusztowy, sposób modernizacji kotła rusztowego oraz sposób likwidowania szkodliwych przedmuchów powietrza, nie biorącego udziału w procesie spalania w kotle rusztowym
DE102010033307A1 (de) * 2010-08-04 2012-02-09 Clyde Bergemann Drycon Gmbh Vorrichtung und Verfahren zum Nachverbrennen von heißem Material auf einem Förderer
CN102042585B (zh) * 2011-01-25 2011-12-07 北京德普新源科技发展有限公司 生物质直燃发电锅炉炉渣和烟灰再燃烧及排放装置
CN102829466B (zh) * 2012-07-25 2015-04-01 北京国电富通科技发展有限责任公司 生物质锅炉炉渣燃烧装置
US9835326B2 (en) * 2014-01-27 2017-12-05 Valvexport, Inc. Automated biomass distribution system
US10125985B2 (en) * 2014-01-27 2018-11-13 Valvexport, Inc. Automated biomass distribution system
BE1025689B1 (nl) * 2017-11-08 2019-06-11 Europem Technologies Nv Systeem en werkwijze voor warmterecuperatie en reiniging van een uitlaatgas van een verbrandingsproces

Family Cites Families (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE935123C (de) * 1941-03-02 1955-11-10 Babcock & Wilcox Dampfkessel W Verfahren zum pneumatischen Abfoerdern des in Elektrofiltern aus Gasen abgeschiedenen Staubes
US2592701A (en) * 1946-07-13 1952-04-15 Comb Eng Superheater Inc Burning and disposal of furnace fly ash
US2686499A (en) * 1946-10-14 1954-08-17 Babcock & Wilcox Co Fuel burning and fly ash collecting apparatus
US2499766A (en) * 1948-11-30 1950-03-07 Lester R Macleod Dust conveying
FR1065398A (fr) * 1952-08-12 1954-05-24 C Ind Const Ltd B V Procédé et appareil de dépoussiérage pneumatique spéclaiement applicables aux trémies collectrices des chaudières marchant aux combustibles solides ou pulvérisés
GB834052A (en) * 1957-05-31 1960-05-04 Elisabeth Constance Schmitt Method of and apparatus for conveying particulate material
US3053577A (en) * 1960-09-29 1962-09-11 Schick Engineering Company Materials conveying system
US3876121A (en) * 1970-07-13 1975-04-08 Preikschat F K Linear pinch valve
FR2334914A1 (fr) * 1975-12-10 1977-07-08 Air Ind Procede d'elimination de poussieres combustibles imbrulees en suspension dans des fumees et installation pour sa mise en oeuvre
FR2342927A1 (fr) * 1976-03-04 1977-09-30 Toy Rene Doseur pour produit granuleux
LU80130A1 (fr) * 1977-08-19 1979-03-07 Flameless Furnaces Ltd Perfectionnements relatifs au chargement de matieres dans des lits fluidises
US4263857A (en) * 1979-01-05 1981-04-28 Dravo Corporation Traveling grate stoker for the combustion of difficultly ignited fuels
US4476790A (en) * 1979-04-23 1984-10-16 Combustion Engineering, Inc. Method of feeding particulate material to a fluidized bed
US4259911A (en) * 1979-06-21 1981-04-07 Combustion Engineering, Inc. Fluidized bed boiler feed system
DE3145017A1 (de) * 1981-02-27 1982-09-16 Gustav 8052 Moosburg König Pneumatische foerderanlage
US4355601A (en) * 1981-09-25 1982-10-26 Conoco Inc. Recirculating flue gas fluidized bed heater
FR2517025A1 (fr) * 1981-11-25 1983-05-27 Fives Cail Babcock Installation de chaudiere a combustible solide
NL8105903A (nl) * 1981-12-30 1983-07-18 Shell Int Research Werkwijze voor het verwijderen van vaste stofdeeltjes uit een gas.
US4416418A (en) * 1982-03-05 1983-11-22 Goodstine Stephen L Fluidized bed residential heating system
US4446799A (en) * 1982-05-07 1984-05-08 Combustion Engineering, Inc. Fluidized bed fuel feed system
US4474119A (en) * 1982-12-27 1984-10-02 Combustion Engineering, Inc. Fine particulate feed system for fluidized bed furnace
US4434724A (en) * 1983-04-01 1984-03-06 Combustion Engineering, Inc. Overbed distributor for feeding dual solid fuels to a stoker furnace
US4481892A (en) * 1983-08-03 1984-11-13 Mah Clifford S Atmospheric fluidized bed combustor
DE3406200A1 (de) * 1984-02-21 1985-08-22 Deutsche Babcock Werke AG, 4200 Oberhausen Dampferzeuger mit einer stationaeren wirbelschichtfeuerung
US4532872A (en) * 1984-12-17 1985-08-06 Combustion Engineering, Inc. Char reinjection system for bark fired furnace

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3736912A1 (de) * 1986-10-31 1988-05-19 Babcock Hitachi Kk Denitrierungsbehandlungsverfahren

Also Published As

Publication number Publication date
US4648329A (en) 1987-03-10
AU3613784A (en) 1985-06-03
WO1985002246A1 (fr) 1985-05-23
US4739715A (en) 1988-04-26
EP0142437A2 (de) 1985-05-22
JPS61500377A (ja) 1986-03-06
DE3479148D1 (en) 1989-08-31
AU577563B2 (en) 1988-09-29
JPH0739842B2 (ja) 1995-05-01
CA1252356A (fr) 1989-04-11
EP0142437A3 (en) 1985-09-18

Similar Documents

Publication Publication Date Title
EP0142437B1 (de) Verfahren und Vorrichtung zum Wiedereinblasen von flugstaub in einen Heizkessel für festen Brennstoff
EP0606608A1 (de) Verfahren und Vorrichtung zum Evakuieren von festen Abfällen aus einer Gasreinigungsvorrichtung
WO2013041779A1 (fr) Procédé de combustion en boucle chimique avec elimination des cendres et fines dans la zone de reduction et installation utilisant un tel procede
WO1995035439A1 (en) Biomass gasification system and turbine
FR2964114A1 (fr) Systeme et procede de gazeification de produits de la biomasse
EP1321014B1 (de) Vorrichtung zur plasmaerzeugung, ionisationsverfahren, verfahrensverwendungen und vorrichtung verwendende bearbeitungen
EP0112237B1 (de) Verfahren und Vorrichtung zur Rückführung unverbrannter fester Bestandteile in einem Wirbelbett
FR2668774A1 (fr) Procede et dispositif de production d'un combustible solide a partir de dechets combustibles.
FR2554552A1 (fr) Procede et dispositif de reinjection de particules envolees dans une chaudiere a combustible solide
CN203823788U (zh) 生物质锅炉布袋除尘设备
EP0727253B1 (de) Verfahren und Vorrichtung zum Regenerieren von Sorbentien, die verwendet werden zur Behandlung von Brennprodukten in Heizkesseln
FR2559239A2 (fr) Dispositif de reinjection de particules envolees dans une chaudiere a combustible solide
EP2655996B1 (de) Heizmodul, heizsystem mit mehreren heizungsmodulen und anlage mit einem solchen heizsystem
EP1184622B1 (de) Verfahren zur Wärmeerzeugung mit reduzierter Emission von Schwefeloxiden und niedrigem Verbrauch von Absorptionsmitteln
CH642870A5 (fr) Procede et dispositif de separation de particules en suspension dans un gaz.
KR890002920B1 (ko) 배출된 입자를 고체 연료 보일러로 재투사시키기 위한 방법과 장치
FR2773388A1 (fr) Procede et dispositif pour la combustion de combustible solide pulverise
US3489111A (en) Boiler fuel reclamation system
EP0026707B1 (de) Verfahren zur Behandlung durch Trocknen und/oder Erhitzen teilchenförmigen und/oder pulverförmigen brennbaren Materials und Anlage zur Durchführung des Verfahrens
EP0043607B1 (de) Verfahren und Vorrichtung zur uniformen pneumatischen Förderung feinkörniger Feststoffe und Anwendung zum Eintragen fester Brennstoffe in einen Schachtofen
EP0126001B1 (de) Verfahren und Vorrichtung zur Behandlung eines Brennstoffes in einer Wirbelschicht
FR2481783A1 (de)
FR2658589A1 (fr) Procede d'alimentation d'un foyer de chaudiere en charbon pulverise et en air, separateur pour la mise en óoeuvre de ce procede, et dispositif d'alimentation en charbon pulverise et en air d'un foyer de chaudiere selon ce procede.
LU82601A1 (fr) Procede et installation de transport pneumatique uniforme de matieres pulverulentes et application a l'injection de combustibles solides dans un four a cuve
FR2720078A1 (fr) Procédé et dispositif de postcombustion des fumées d'un cubilot.

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Designated state(s): AT BE CH DE FR GB IT LI NL SE

PUAL Search report despatched

Free format text: ORIGINAL CODE: 0009013

RTI1 Title (correction)
AK Designated contracting states

Designated state(s): AT BE CH DE FR GB IT LI NL SE

17P Request for examination filed

Effective date: 19860120

17Q First examination report despatched

Effective date: 19861105

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE CH DE FR GB IT LI NL SE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: THE PATENT HAS BEEN ANNULLED BY A DECISION OF A NATIONAL AUTHORITY

Effective date: 19890726

Ref country code: NL

Effective date: 19890726

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.

Effective date: 19890726

Ref country code: AT

Effective date: 19890726

REF Corresponds to:

Ref document number: 45025

Country of ref document: AT

Date of ref document: 19890815

Kind code of ref document: T

GBT Gb: translation of ep patent filed (gb section 77(6)(a)/1977)
REF Corresponds to:

Ref document number: 3479148

Country of ref document: DE

Date of ref document: 19890831

NLV1 Nl: lapsed or annulled due to failure to fulfill the requirements of art. 29p and 29m of the patents act
R20 Corrections of a patent specification

Effective date: 19891207

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

26N No opposition filed
REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

REG Reference to a national code

Ref country code: FR

Ref legal event code: DA

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19951103

Year of fee payment: 12

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19951123

Year of fee payment: 12

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: CH

Payment date: 19951128

Year of fee payment: 12

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19951208

Year of fee payment: 12

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Effective date: 19961109

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LI

Effective date: 19961130

Ref country code: CH

Effective date: 19961130

Ref country code: BE

Effective date: 19961130

BERE Be: lapsed

Owner name: STEIN INDUSTRIE

Effective date: 19961130

Owner name: MANUTAIR MOLLER

Effective date: 19961130

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 19961109

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19970801

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19991027

Year of fee payment: 16

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20010731

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST