EP0112237B1 - Procédé et installation de recyclage des imbrûlés solides dans un lit fluidisé - Google Patents

Procédé et installation de recyclage des imbrûlés solides dans un lit fluidisé Download PDF

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Publication number
EP0112237B1
EP0112237B1 EP83402340A EP83402340A EP0112237B1 EP 0112237 B1 EP0112237 B1 EP 0112237B1 EP 83402340 A EP83402340 A EP 83402340A EP 83402340 A EP83402340 A EP 83402340A EP 0112237 B1 EP0112237 B1 EP 0112237B1
Authority
EP
European Patent Office
Prior art keywords
recycling
fluidized bed
silo
particles
combustible material
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
EP83402340A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0112237A1 (fr
Inventor
Jean-Xavier Morin
Gérard Chrysostome
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.)
Creusot Loire SA
Original Assignee
Creusot Loire 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
Application filed by Creusot Loire SA filed Critical Creusot Loire SA
Publication of EP0112237A1 publication Critical patent/EP0112237A1/fr
Application granted granted Critical
Publication of EP0112237B1 publication Critical patent/EP0112237B1/fr
Expired legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/28—Control devices specially adapted for fluidised bed, combustion apparatus
    • F23C10/30—Control devices specially adapted for fluidised bed, combustion apparatus for controlling the level of the bed or the amount of material in the bed
    • F23C10/32—Control devices specially adapted for fluidised bed, combustion apparatus for controlling the level of the bed or the amount of material in the bed by controlling the rate of recirculation of particles separated from the flue gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber

Definitions

  • the subject of the invention is a process and an installation for recycling solid unburnt products produced during an exothermic reaction carried out in a litfluidized medium.
  • the fine dust collected in the cyclone contains not only unburnt particles but also a certain proportion of fine ash which is also entrained by the fumes.
  • an absorbent such as limestone or dolomite is used to desulfurize the fuel during combustion, this absorbent also contains, or else produced by attrition, fine particles which are also entrained with the fumes.
  • the proportion of non-combustible elements collected in the cyclone can range from 20 to 70% for example.
  • FR-A-2 328 507 a method of treating material in a fluidized bed system comprising an enclosure provided with means for supplying solid combustible material and with fluidization means and connected by a smoke evacuation duct to a device for separating the solid particles entrained with the fumes, the recovered particles being recycled to the fluidized bed.
  • the recycling circuit includes a reservoir chamber.
  • this reservoir chamber does not provide an accumulation phase for the solid particles recovered with the aim of periodically supplying the reaction chamber. In fact, recycling takes place continuously and the speed of recycling of the particles is controlled by the position of a ball valve.
  • GB-A-2089485 also discloses a material processing installation in a fluidized bed system comprising a separation member and a storage tank for the recovered particles which are injected, using a fan and after opening. of the storage valve, on the hearth of the supply of fresh fuel to the hearth.
  • the subject of the invention is an improved process and installation which avoids the addition of additional equipment and allows recycling of unburnt products in the fluidized bed without having the drawbacks observed so far.
  • the solid particles entrained with the fumes in the recycling phase are, after separation, accumulated in an intermediate silo interposed between the separation device and the recycling reserve silo.
  • the improvements according to the invention also make it possible, in a particular application, to improve the mode of supplying combustible materials to the fluidized bed.
  • the solid combustible materials when the latter operates under pressure as is generally the case, the solid combustible materials must be introduced by means of an airlock device which, for continuous supply, must include two pressure chambers supplied alternately by the 'through an orienting valve.
  • an airlock device which, for continuous supply, must include two pressure chambers supplied alternately by the 'through an orienting valve.
  • the circuits are reversed, the second chamber being isolated, pressurized, then connected to the combustion chamber for supplying the latter with combustible materials while the first chamber is isolated from the combustion chamber and brought to atmospheric pressure so that it can be refilled via the orienting valve.
  • the improved recycling process according to the invention makes it possible to simplify this arrangement.
  • the supply is made from a single chamber forming an airlock which, in turn, is put under the pressure of the combustion chamber for the supply thereof during the phase of normal operation then isolated from the combustion chamber during the recycling phase to be brought to atmospheric pressure and refilled with combustible materials.
  • FIG 1 there is shown by way of example a coal boiler operating in a fluidized bed and allowing desulfurization during combustion.
  • the installation comprises an enclosure 1 limited by an envelope 11 made of refractory material closed at its top and provided at its base with a fluidization grid 12 which supports a fluidized bed 2 and allows the distribution of the fluidization and combustion air. introduced by a circuit 13 into a plenum 14 placed below the fluidization grid 12.
  • the fluidized bed 2 there opens an inlet 15 through which the combustible material is fed, for example by a device 21 of known type.
  • the limestone allowing the desulfurization can be introduced with the combustible material or else by a particular supply circuit 23 which has not been shown in detail in the figure.
  • exchangers 22 placed in the fluidized bed and supplied with water make it possible to produce steam.
  • a duct 17 for evacuating combustion fumes loaded with solid particles in the form of fine dust constituted, in varying proportions, by fine ash from coal, fine unburnt particles and fine absorbent particles.
  • the fumes extracted through the conduit 17 pass through a separation device consisting for example of a cyclone 3 which comprises an upper gas outlet 31 and a lower outlet 32 for the separated solid particles.
  • the dedusted fumes discharged through the outlet 31 are directed to a subsequent treatment installation, not shown, which may include a heat recovery system and a final dedusting, before discharge to the atmosphere.
  • the outlet 32 of the cyclone 3 is connected by a pipe 33 provided with a valve 34 to an enclosure forming a silo 4 in which the particles collected by the cyclone 3 accumulate when the valve 34 is open.
  • the silo 4 is connected to the combustion chamber 1 by a recycling circuit comprising a pipe 41 opening out at 42 at the base of the fluidized bed and provided at its origin with a valve 43 making it possible to regulate the flow of particles recycled by the pipe 41.
  • the particles are reinjected by a gas such as air or an inert gas introduced through a pipe 44 opening into the valve 43 and which produces a fluidization of the particles in the pipe 41 of so as to transport them to the fluidized bed
  • the reinjection rate can be determined, for example, by the gas flow injected through line 44 and adjusted by valve 43.
  • the reinjection rate can be controlled the temperature of the fluidized bed by a regulating circuit comprising a control unit 5 which receives information corresponding to the temperature level in the fluidized bed, supplied by a detector 51 and issues an order to adjust the valve 43.
  • the silo 4 is provided with a drain pipe 46 preceded by a valve 47 which can be actuated by the regulation circuit 5, the end of the evacuation being controlled by a low level control member. 53 placed at the base of silo 4, above the drain orifice 48. Thanks to the arrangements which have just been described, the combustion chamber 1 can be supplied by successive periods alternately with combustible material in a phase of normal operation and with solid unburnt in a phase recycling particles accumulated in the silo.
  • silo 4 is empty.
  • the fluidized bed 2 is normally supplied with combustible materials through the inlet 15, with an adjustable flow rate to obtain the desired temperature in the fluidized bed, the latter being ignited by a burner 18.
  • the flow of coal supplied by the device 21 can be controlled by the temperature of the fluidized bed by the regulating circuit 5.
  • the flow rate of the injected limestone can itself be controlled by the flow of coal so as to keep the desulfurization at its optimum.
  • valve 43 being closed and the valve 34 open, the fine particles of unburnt ash and absorbent entrained with the fumes in the pipe 17 and separated in the cyclone 3 accumulate in the silo 4.
  • the large particles of ash of carbon and absorbent loaded with sulfur are eliminated by outlet 16 by appropriate means.
  • the control unit 5 controls the stopping of the device 21 for supplying combustible materials and l opening of the valve 43 allowing the recycling of the solid particles and then the adjustment thereof to maintain the temperature of the fluidized bed.
  • the air flow introduced by the circuit 13 normally remains constant.
  • the particles previously accumulated in the silo 4 are thus reintroduced into the fluidized bed with a flow rate at the temperature thereof, the injection of the fine particles taking place in the lowest layers of the fluidized bed through the orifice 42.
  • the absorbent flow rate introduced by the circuit 23 can be kept constant and equal to that of the first phase of normal operation or, depending on the composition of the recycled particles, can be canceled, modified or kept equal to a new value.
  • the evacuation of large particles through outlet 16 is also stopped.
  • the flow rate of the outlet 16 is modified to adapt to the circumstances. In particular, in the case where the flow rate of the outlet 16 is controlled at the level of the fluidized bed, there is no particular regulation to be provided on the outlet flow rate of large particles other than that normally provided.
  • the flow rate of the particles returning to the silo 4 during the recycling phase is lower than the flow rate of the recycled particles since some of them have burned but the capacity of the silo 4 can be chosen so as to withstand level fluctuations .
  • the installation therefore makes it possible to operate in a closed circuit, the unburnt particles passing several times through the silo 4 then through the fluidized bed until complete combustion.
  • the proportion of unburnt materials contained in the recycled particles decreases and the recycling rate must therefore increase so that the temperature measured by the detector 51 remains constant.
  • the control unit 5 which the information relating to the temperature level in the fluidized bed can control the closing of the valve 43 and the starting of the supply device 21 of so as to determine the stopping of the recycling phase and the resumption of the normal operating phase when the temperature level measured by the detector 51 drops below a fixed limit.
  • the flow rate of the recycled particles can be measured continuously so as to provide information to the control unit which determines the stopping of recycling and the resumption of normal operation when the recycling flow rate exceeds a limit. chosen.
  • valve 43 is therefore closed and the particles accumulated at this time are emptied in the order in which valve 43 is adjusted.
  • the silo 4 is provided with a drain pipe 46 preceded by a valve 47 which can be actuated by the regulation circuit 5, the end of the evacuation being controlled by a low level control member. 53 placed at the base of the silo 4, above the emptying orifice 48. Thanks to the arrangements which have just been described, the combustion chamber 1 can be supplied by successive periods alternately with combustible material in a phase of normal operation and in solid unburnt in a phase of recycling of the particles accumulated in the silo.
  • silo 4 is empty.
  • the fluidized bed 2 is normally supplied with combustible materials through the inlet 15, with an adjustable flow rate to obtain the desired temperature in the fluidized bed, the latter being ignited by a burner 18.
  • the flow of coal supplied by the device 21 can be controlled by the temperature of the fluidized bed by the regulating circuit 5.
  • the flow rate of the injected limestone can itself be controlled by the flow of coal so as to keep the desulfurization at its optimum.
  • valve 43 With valve 43 closed and valve 34 open te, the fine particles of unburnt ash and absorbent entrained with the fumes in line 17 and separated in cyclone 3 accumulate in silo 4. Large particles of coal ash and absorbent loaded with sulfur are eliminated by exit 16 by appropriate means.
  • the control unit 5 controls the stopping of the device 21 for supplying combustible materials and l opening of the valve 43 allowing the recycling of the solid particles and then the adjustment thereof to maintain the temperature of the fluidized bed.
  • the air flow introduced by the circuit 13 normally remains constant.
  • the particles previously accumulated in the silo 4 are thus reintroduced into the fluidized bed with a flow controlled by the temperature thereof, the injection of the fine particles taking place in the lowest layers of the fluidized bed through the orifice 42
  • the absorbent flow rate introduced by the circuit 23 can be kept constant and equal to that of the first phase of normal operation or, depending on the composition of the recycled particles, can be canceled, modified or kept equal to a new value.
  • the flow rate of the outlet 16 is modified to adapt to the circumstances.
  • the flow rate of the outlet 16 is controlled at the level of the fluidized bed, it does not have any particular regulation to be provided for on the outlet flow rate of large particles other than that normally provided.
  • the flow rate of the particles returning to the silo 4 during the recycling phase is lower than the flow rate of the recycled particles since some of them have burned but the capacity of the silo 4 can be chosen so as to withstand level fluctuations .
  • the installation therefore makes it possible to operate in a closed circuit, the unburnt particles passing several times through the silo 4 then through the fluidized bed until complete combustion.
  • the proportion of unburnt materials contained in the recycled particles decreases and the recycling rate must therefore increase so that the temperature measured by the detector 51 remains constant.
  • the control unit 5 which receives the information relating to the temperature level in the fluidized bed can control the closing of the valve 43 and the start of recycling and the resumption of the normal operating phase when a set limit.
  • the flow rate of the recycled particles can be continuously measured so as to supply information to the control unit which determines the stopping of recycling and the resumption of normal operation when the recycling flow rate exceeds a limit. chosen.
  • the valve 43 is therefore closed and the particles accumulated at this moment in the silo 4 are emptied by opening the valve 47 of the evacuation pipe 46.
  • the drain valve 47 is closed and the supply of the fluidized bed is resumed by the inlet 15 by restarting the supply device 21; we then returned to the first phase of normal operation.
  • the emptying of the silo 4 via the line 46 must be fast enough so that the temperature of the fluidized bed does not drop too much before returning to the first phase of normal operation.
  • the temperature of the fluidized bed varies little during the time necessary for emptying.
  • the level control 53 is then placed at a height sufficient for the volume between the level of the emptying orifice 48 opening into the pipe 46 and that of the control member 53 is greater than the volume of particles generated by the combustion of the coal during the emptying time through the pipe 46.
  • valve 62 is open and, of course, the valve 43 placed at the outlet of the silo 4 is closed.
  • the particles generated by combustion in the fluidized bed pass through capacity 6 and accumulate in silo 4.
  • valve 43 When we go into the recycling phase, the valve 43 is open but the valve 62 is closed.
  • the fine dust generated by the combustion of recycled unburnt material from silo 4 and which itself contains a small proportion of unburnt material accumulates in capacity 6 which therefore constitutes an intermediate silo interposed between cyclone 3 and silo 4.
  • the proportion of unburnt materials contained in the recycled particles is substantially constant and there is normally little variation in the temperature of the fluidized bed and in the recycling flow rate. This is therefore continued until the silo 4 is empty, that is to say when the level of the particles has reached the level fixed, for example, by the control member 53.
  • the valve 43 is then closed and immediate emptying of the intermediate silo 6 is immediately controlled by a emptying pipe 63, the emptying being stopped when the level of particles reaches the height of a control member 64 placed at the base of the silo 6.
  • valve 62 is opened and one returns to the first phase of normal operation by controlling the supply of combustible materials to the fluidized bed by the device 21.
  • the return to the normal combustion phase can be triggered at the end of the recycling phase, that is to say when the emptying of the silo 6 is carried out by line d 'evacuation 63.
  • This avoids any drop in temperature of the fluidized bed but it is necessary to leave in the silo 6 a sufficient capacity between the security level determined by the control member 64 and the level of the orifice 65 of the evacuation pipe 63, this capacity being greater than the volume of particles generated by the combustion of coal during the emptying of the silo 6. This thus avoids withdrawing by the orifice 65 of particles containing unburnt.
  • the duration of the second recycling phase will be of the order of 10 minutes, the rapid emptying having to be done in 1 minute.
  • the recycling phase then being 2 hours and emptying can still be done in 1 minute by appropriate means. It is then possible to minimize the drawbacks linked to the possibility of a temperature drop before returning to normal combustion.
  • the invention makes it possible to simplify the supply of the fluidized bed when it has to operate under pressure.
  • FIG. 3 Such an installation is shown in FIG. 3.
  • the assembly constituted by the combustion chamber 1, the separation device 3 and the recycling silo 4, can operate according to one of the variants which have just been described, l enclosure 1 is then kept under pressure by appropriate means. It is therefore necessary that the combustible material is brought to the pressure prevailing in the enclosure 1 before being introduced into the latter.
  • an airlock system which consists of a chamber 7 interposed on the supply circuit upstream of the supply device 21 and of the inlet 15 of the combustible material in the enclosure 1.
  • the chamber 7 can be isolated by inlet 73 and outlet 74 valves placed respectively on the fuel material supply circuit 71 and the pipe 72 which connects it to the supply device 21 and to the entrance 15 of enclosure 1.
  • the chamber 7 can be put either at the same pressure as the enclosure 1 by a pressurization circuit 75 which connects it to a gas reserve 76 and on which a valve 77 is placed, or at atmospheric pressure by a depressurization circuit 78 fitted with a valve 79.
  • the chamber 7 is filled with coal by the supply circuit 71, the valves 74 and 77 being closed.
  • the valves 73 and 79 are closed and the valve 77 is opened to bring the chamber 7 to the desired pressure, that is to say the one which, at this moment, prevails in the enclosure 1
  • the solid particles entrained with the fumes accumulate in the silo 4 until the recycling phase is started. At this moment, the supply device 21 is stopped and the valve 74 for leaving the chamber 7 is closed.
  • valve 77 Since the latter is isolated from the enclosure 1, which is then supplied with recycled unburnt materials, the valve 77 can be closed and the valve 79 of the depressurization circuit 78 opened.
  • the valve 73 When the chamber 7 is at atmospheric pressure, the valve 73 is opened and com requests the supply device 21 for filling the chamber 7 with combustible materials.
  • the filling must be done in a time less than the duration of the recycling phase, but it is not difficult to meet this imperative by using appropriate means and by choosing in a desired manner the relative volumes of the recycling silo. 4 and the supply chamber 7.
  • the valves 73 and 79 are closed and the valve 77 is opened to bring the chamber 7 to the pressure of the combustion chamber 1.
  • the installation is then ready for return to normal combustion phase since it suffices to open the valve 74 and to supply the fluidized bed at the desired time after the recycling has stopped and the silo 4 has been emptied.
  • the volume of the silo 4 must be chosen as a function of that of the chamber 7 so as to contain all the solid particles generated by the combustion of the coal contained in the chamber 7 during the normal combustion phase.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
EP83402340A 1982-12-08 1983-12-05 Procédé et installation de recyclage des imbrûlés solides dans un lit fluidisé Expired EP0112237B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR8220546 1982-12-08
FR8220546A FR2537701A1 (fr) 1982-12-08 1982-12-08 Procede et installation de recyclage d'imbrules solides dans un lit fluidise

Publications (2)

Publication Number Publication Date
EP0112237A1 EP0112237A1 (fr) 1984-06-27
EP0112237B1 true EP0112237B1 (fr) 1987-08-05

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EP83402340A Expired EP0112237B1 (fr) 1982-12-08 1983-12-05 Procédé et installation de recyclage des imbrûlés solides dans un lit fluidisé

Country Status (5)

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US (1) US4552078A (xx)
EP (1) EP0112237B1 (xx)
DE (1) DE3372876D1 (xx)
FR (1) FR2537701A1 (xx)
ZA (1) ZA838942B (xx)

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Publication number Priority date Publication date Assignee Title
FR2560967B1 (fr) * 1984-03-08 1988-08-26 Creusot Loire Procede et appareillage de controle du transfert thermique realise dans un lit fluidise
FR2563118B1 (fr) * 1984-04-20 1987-04-30 Creusot Loire Procede et installation de traitement de matiere en lit fluidise circulant
EP0176293B1 (en) * 1984-09-24 1991-04-03 Combustion Power Company Inc. Recirculating fluid bed combustor - method and apparatus
SE452359C (sv) * 1985-04-30 1994-04-11 Kvaerner Generator Ab Anordning för styrning av värmeövergångstalet vid en CFB-panna
DE3544425A1 (de) * 1985-12-16 1987-06-25 Steag Ag Verfahren zum verbrennen von festen brennstoffen in einer zirkulierenden wirbelschicht und vorrichtung zum durchfuehren dieses verfahrens
SE462446B (sv) * 1989-06-29 1990-06-25 Abb Stal Ab Foerraadsbehaallare foer baeddmaterial vid en kraftanlaeggning med braennkammare foer fluidiserad baedd
US5964085A (en) * 1998-06-08 1999-10-12 Siemens Westinghouse Power Corporation System and method for generating a gaseous fuel from a solid fuel for use in a gas turbine based power plant
JP5936946B2 (ja) * 2012-08-02 2016-06-22 メタウォーター株式会社 流動床ガス化装置
CN106635179B (zh) * 2017-01-23 2019-03-08 江苏华威机械制造有限公司 一种循环流化床与热解床复合气化的工艺及其装置

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NL295333A (xx) * 1962-08-11
US3902462A (en) * 1974-05-28 1975-09-02 Foster Wheeler Energy Corp System and method for generating heat utilizing fluidized beds of different particle size
GB1542862A (en) * 1975-02-14 1979-03-28 Exxon Research Engineering Co Combustion or part-combustion in fluidized beds
GB1523500A (en) * 1975-10-21 1978-09-06 Battelle Development Corp Method of operating a fluidized bed system
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
JPS5334374A (en) * 1976-09-10 1978-03-30 Babcock Hitachi Kk Method and device for burning shells
US4103646A (en) * 1977-03-07 1978-08-01 Electric Power Research Institute, Inc. Apparatus and method for combusting carbonaceous fuels employing in tandem a fast bed boiler and a slow boiler
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JPS5664208A (en) * 1979-10-30 1981-06-01 Kawasaki Heavy Ind Ltd Control of temperature of bed in fluidized bed combustion boiler
JPS5668708A (en) * 1979-11-08 1981-06-09 Babcock Hitachi Kk Method of starting fluidized boiler
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GB2089485A (en) * 1980-10-07 1982-06-23 Jones Cedric Richard Improvements In Solid Fuel Fired Boiler Operations

Also Published As

Publication number Publication date
EP0112237A1 (fr) 1984-06-27
ZA838942B (en) 1984-07-25
DE3372876D1 (en) 1987-09-10
FR2537701A1 (fr) 1984-06-15
FR2537701B1 (xx) 1985-03-08
US4552078A (en) 1985-11-12

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