EP2375152B1 - Dispositif et procédé de production de gaz chaud avec chauffage intégré d'un fluide caloporteur - Google Patents

Dispositif et procédé de production de gaz chaud avec chauffage intégré d'un fluide caloporteur Download PDF

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Publication number
EP2375152B1
EP2375152B1 EP11158981.8A EP11158981A EP2375152B1 EP 2375152 B1 EP2375152 B1 EP 2375152B1 EP 11158981 A EP11158981 A EP 11158981A EP 2375152 B1 EP2375152 B1 EP 2375152B1
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EP
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Prior art keywords
hot gas
flow
boiler
combustion chamber
cyclone
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EP11158981.8A
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German (de)
English (en)
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EP2375152A2 (fr
EP2375152A3 (fr
Inventor
Georg Obwaller
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Fritz Egger GmbH and Co OG
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Fritz Egger GmbH and Co OG
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Priority to PL11158981T priority Critical patent/PL2375152T3/pl
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Publication of EP2375152A3 publication Critical patent/EP2375152A3/fr
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/44—Details; Accessories
    • F23G5/46—Recuperation of heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • F23J15/022—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow
    • F23J15/027—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material for removing solid particulate material from the gasflow using cyclone separators
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying

Definitions

  • the invention relates to a device for hot gas production with integrated heating of a heat transfer medium comprising a bricked combustion chamber for hot gas production and arranged in the flow direction of the hot gas behind the combustion chamber and connected to the combustion chamber via a hot gas line boiler for heating the heat transfer medium. Furthermore, the invention relates to a method for hot gas generation with integrated heating of a heat transfer medium. Finally, the present invention relates to a drying device for drying lignocellulose-containing material, in particular wood and / or recyclable, wood-containing material.
  • Hot gas operated drying devices which are regularly used, for example, in the woodworking industry for drying particulate substances, eg chips, are known from the prior art ( DE 20 2007 005 195 U1 ).
  • the heat content of the hot gas is used not only for drying, but also for heating a heat transfer medium, for example water, steam or thermal oil, which in turn is used in various production processes, for example for heating hot presses for pressing chipboard.
  • a well known in the art apparatus for generating hot gas for a connected dryer with integrated thermal oil heating comprises a fully bricked Combustion chamber in which the hot gas is generated by a feed grate firing.
  • the hot gas is withdrawn from the combustion chamber in a fully lined hot gas line, which branches off immediately after the combustion chamber.
  • the main stream of the hot gas is then introduced into a hot gas cyclone, where in the hot gas still located fly ash is largely deposited. From the hot gas cyclone, the purified hot gas stream flows into a mixing chamber to set the desired dryer inlet temperature and from there into the dryer.
  • the partial flow of the hot gas branched off behind the combustion chamber flows into a thermal oil boiler having a radiant heat exchanger and a convection heat exchanger, where it delivers about two thirds of its heat energy to the thermal oil. Subsequently, the cooled partial stream before the mixing chamber is again introduced into the main stream purified in the hot gas cyclone and cools it down.
  • a disadvantage of this system is that the partial gas stream flowing into the thermal oil boiler, especially when using low-grade fuels, such as waste wood or waste wood, impregnated wood or production waste, leads to a continuous contamination of the thermal oil boiler. This is particularly problematic when due to increasing pollution, the hot gas temperature level in the thermal oil boiler in the region of the radiant heat exchanger increases, so that in the introduced into the thermal oil boiler part gas stream ash particles due to their at temperatures> about 700 ° C liquid or doughy consistency on the thermal oil Condensate heat exchanger flow through condense tube bundles.
  • the invention is based on the object to provide an apparatus and a method for hot gas production with integrated heating of a heat transfer medium, which is characterized by high system availability and compared to known from the prior art devices overall efficiency. Furthermore, the device and the method should ensure high reliability and longevity of the components used.
  • the entire hot gas stream is freed from the fly ash flowing out of the combustion chamber with the hot gas by complete introduction of the hot gas stream emerging from the combustion chamber into the bricked hot gas cyclone.
  • the hot gas stream is additionally strongly mixed, whereby a good burnout is achieved.
  • there is an additional combustion of carbon monoxide in the hot gas cyclone so that the energy content of the fuel burned in the combustion chamber can be used even more efficiently and the hot gas has a reduced pollutant content.
  • the purified hot gas stream from the hot gas cyclone After flowing out of the purified hot gas stream from the hot gas cyclone, it is completely or partially passed into a boiler for heating a heat transfer medium, for example water, steam or thermal oil.
  • a heat transfer medium for example water, steam or thermal oil.
  • the hot gas stream is divided after exiting the hot gas cyclone into a first and a second partial flow, wherein the second partial flow is introduced via the bypass line in the boiler for heating the heat transfer medium.
  • a first and a second hot gas cyclone may be provided.
  • a bypass line branches off from the hot gas line, so that the hot gas stream is split into a first and a second partial flow, wherein in turn the second partial flow is introduced via the bypass line into the boiler for heating the heat transfer medium.
  • the first hot gas cyclone is arranged in the flow direction of the hot gas behind the branch of the bypass line in the hot gas line, while the second hot gas cyclone is arranged in the bypass line in the flow direction of the hot gas in front of the boiler for heating the heat transfer medium. This in turn ensures that the entire hot gas flow and in particular the branched off to the boiler partial flow is purified in a hot gas cyclone.
  • the outlet of the boiler and the combustion chamber are gas-conductively connected to one another, so that the cooled second partial stream leaving the boiler is at least partially, in particular completely, returned to the combustion chamber as cooling gas flow.
  • the combustion chamber temperature is reduced and it needs less cooling air to be supplied.
  • a lower excess of air results in less fresh air being delivered to the system, thereby making the components, such as fans, air lines, flaps, etc., smaller.
  • a lower excess air also means a lower O 2 content and thus a more favorable conversion for emission measurements to a higher O 2 reference content.
  • a re-introduction of the second partial stream cooled in the boiler into the first partial stream flowing through the hot gas line can be omitted, so that it remains at a very high temperature level and thus can be used more efficiently for a wide variety of applications, for example for drying.
  • the output of the boiler is also gas-conductively connected to the hot gas line, so that the cooled second partial flow emerging from the boiler can be mixed with it at least temporarily to regulate the hot gas temperature in the first partial flow.
  • the device means for denitrification of the hot gas.
  • the denitrification can be carried out for example by selective non-catalytic reduction (SNCR).
  • SNCR selective non-catalytic reduction
  • at least one nozzle for introducing a reducing agent, in particular urea may be provided in the hot gas line.
  • the at least one nozzle is arranged in the tangential inflow channel of the hot gas cyclone, since there prevails the temperature required for efficient denitrification of the hot gas.
  • An efficient denitrification is also promoted by the intensive mixing of the hot gas in the cyclone, so that the urea consumption and the ammonia slip can be minimized.
  • the boiler for heating the heat transfer medium to a first flow stage with a radiant heat exchanger and a second flow stage with a convection heat exchanger, wherein the first flow stage can be flowed through by the hot gas flow in the downward direction and wherein the second flow stage of the hot gas flow in Upstream is flowed through.
  • the heat transfer to the heat transfer medium in the first flow section at very high hot gas temperatures corresponding in particular by thermal radiation, while after partial cooling already carried out the heat transfer in the second flow stage, in particular by convection.
  • the boiler has means for spraying a cleaning fluid, in particular water.
  • a spray of a cleaning fluid can be a regular Cleaning the boiler during operation of the device done.
  • the means for spraying a cleaning fluid are preferably designed as at least one nozzle arranged in the first flow stage of the boiler.
  • the cleaning fluid can be injected at high pressure into the first flow section of the boiler, wherein the nozzle can be designed such that it performs a pendulum motion so as to apply the cleaning fluid to the entire heat exchanger surface in the first flow stage.
  • the finely injected cleaning fluid causes thermal shock to break off adhering and sometimes hard deposits, which can prevent boiler stoppages. Furthermore, in this way an undesired temperature rise above 700 ° C. can be avoided in the first flow section, so that there is no longer any condensation of liquid or doughy ash particles in the vessel.
  • the combustion chamber of the device comprises a grate firing, in particular a traveling grate firing, wherein solid, granular or fibrous fuel is burned on the flowed through by an ascending primary air flow grate through the combustion chamber.
  • the combustion product is the hot gas which flows through the combustion chamber.
  • the continuous task of the fuel on the grid can be done by means of screw conveyor and a chute in the form of a chute, the chute is designed to be cooled by means of a water injection. This ensures that the chute in case of a Heat build-up, a blockage or a burn-back is protected by cooling and inerting. Furthermore, the projecting into the combustion chamber end of the chute is preferably bricked, so that there is no risk of deformation due to high thermal stress here.
  • At least one radially oriented burner or at least two tangentially arranged burners for combustion of gaseous and pulverulent fuel can also be provided in the combustion chamber. Due to the performance of such a burner, it can be operated for hot gas generation in combination with grate firing or even alone. Due to the tangential two or more burner arrangement, a better gas mixing in the combustion chamber is achieved, whereby the carbon monoxide content in the hot gas can be significantly reduced by afterburning thereof.
  • a further aspect of the invention relates to a drying device for drying, in particular, wood products and / or waste with a device according to one of claims 1 to 9, wherein the hot gas flowing out of the hot gas cyclone hot gas at least partially in a dryer for drying in particular chopped wood, sawdust, Wood shavings, wood fibers, animal feed, cereals and the like. Is initiated. For the advantages of this drying device, the above applies accordingly.
  • the inventive method can be carried out with limited equipment and high reliability, with a reduced contamination due to the purification of the entire hot gas stream in the hot gas cyclone by deposition of fly ash a longer life of the system components is guaranteed.
  • the hot gas stream is divided after exiting the hot gas cyclone into a first and a second partial stream, wherein the second partial stream is passed via a bypass line into the boiler for heating the heat transfer medium.
  • a first and a second hot gas cyclone may be provided.
  • the hot gas flow is again divided into a first and a second partial flow, wherein in turn the second partial flow is introduced via the bypass line into the boiler for heating the heat transfer medium.
  • the first partial flow is purified in the first hot gas cyclone arranged in the direction of flow of the hot gas behind the branch of the bypass line in the hot gas line, while the second partial flow is cleaned in the arranged in the bypass line in the flow direction of the hot gas before the boiler for heating the heat transfer medium second hot gas cyclone becomes. This is again a complete cleaning of the hot gas stream, in particular the branched second partial stream ensured.
  • the first partial flow can be introduced into a drying device according to a further advantageous embodiment of the method.
  • the cooled second partial stream emerging from the boiler is at least partially recirculated into the combustion chamber as a cooling gas stream.
  • the cooled second partial flow exiting from the boiler is at least temporarily admixed with it for regulating the hot gas temperature in the first partial flow.
  • the boiler during operation at least temporarily by spraying a cleaning fluid, in particular water, to be cleaned.
  • a cleaning fluid in particular water
  • the fuel input and the thus coupled supply of combustion air in the combustion chamber is controlled such that in the combustion chamber is a constant negative pressure.
  • the firing capacity of the combustion chamber is based on the hot gas power requirement of the respectively downstream application, for example a dryer and / or the boiler for heating the heat transfer medium. If a larger amount of hot gas is withdrawn and thus there is a greater need for hot gas, the negative pressure decreases in the combustion chamber and the power control promotes more fuel in the combustion chamber connected to a correspondingly increased air flow, whereby the total firing heat output increases in the desired manner.
  • the regulation of the fuel input preferably takes place steplessly by means of frequency-controlled screws.
  • Fig. 1 is a well-known from the prior art drying plant with a device for hot gas production with integrated thermal oil boiler and downstream dryer in a highly schematic view. Drying systems of this type serve, for example, the Drying of chopped wood, sawdust, wood shavings, wood fibers, animal feed, cereals, etc. With the dried material can then chip, fiber, OSB boards, wood pellets, grain concentrate pellets, etc. are produced.
  • the heat carrier heated by the hot gas in the present case thermal oil, is required for various processes, for example for pressing chipboard, fiber or OSB boards, for drying impregnated paper and pressing it onto support plates, for heating purposes etc.
  • the device for hot gas production of the plant Fig. 1 is executed with a fully lined combustion chamber 100.
  • This in turn comprises a feed grate firing 101, but may also have a grate firing, fluidized bed firing, coal, gas, oil, dust firing, etc. as primary firing.
  • a feed unit 102 solid or granular fuel is fed to the grate and burned by supplying primary air 103 below the grate and secondary air 104 above the grate, wherein the various combustion phases of drying, heating, gasification and combustion take place along the feed direction of the grate 101a ,
  • the ashes of the burnt fuel fall at the end of the grate into a wet stripper 160, which conveys the wet ash into a grate ash container 161 outside the boiler house.
  • the hot gas generated in the bricked combustion chamber 100 which has a high nitrogen oxide content (thermal NOx) due to the high combustion temperature of about 940 ° C is introduced via a preferably also fully lined hot gas line 107 in a hot gas cyclone 108, where it is largely of particulate impurities is cleaned. It is then fed to an external mixing chamber 130 and finally to the dryer 140.
  • thermal NOx nitrogen oxide content
  • the thermal oil boiler 110 here comprises a first flow stage in which the hot gas flows downwards (downstream part) and a part of its heat energy in a radiation heat exchanger 110a, in particular via radiation to the passing through the tubes of the first heat exchanger 110a flowing thermal oil.
  • the already partially cooled hot gas flows upwards again (upward part) and releases at lower temperatures further heat energy in a convection heat exchanger 110b, in particular via convection to the thermal oil.
  • the hot gases are cooled to a temperature of ⁇ 700 ° C before being overflowed into the second-stage convection heat exchanger 110b.
  • the deflection between radiant and convection heat exchangers 110a, 110b is presently designed as a large common (or alternatively) as two separate funnels, where the coarser ash content in the hot gas can settle due to gravity and double pendulum flap, feeder, screw, etc. (each not shown) dissipated and collected in the ash container 161.
  • the hot gas cools and transfers the heat to the heat transfer medium, in this case thermal oil.
  • This is heated, for example, from 255 ° C to 280 ° C.
  • the cooled to about 350 ° C hot gas is withdrawn via a suction 113 in a line 112 and passed through a control valve 114 and a line 115 back to the hot gas main stream and cools it.
  • the hot gas main stream in turn is fed to a mixing chamber 130, in which the hot gas is controlled with cold air or with dryer air / dryer exhaust air to the necessary hot gas temperature before entering the dryer 140.
  • soot blowers Even with so-called soot blowers, the contaminants can not be removed after a certain period of operation, which leads to a strong limitation of the heat transfer performance and in extreme cases to the complete growth of whole Konvemiesrohrbündeln. In the case of the use of sootblowers their use interval must be steadily shortened. Here, the pipes must be subjected to high air pressure, which also greatly increases the erosion tendency.
  • the recirculation of cooled hot gas is provided via a conduit 115 with a control flap 117 so as to ensure a temperature of ⁇ 700 ° C in front of the convection heat exchanger 110b.
  • this disadvantageously requires a higher blower output, with the resulting increased amounts of flue gas in the convection heat exchanger also causing higher erosions.
  • the introduction of the cooled hot gas from the thermal oil boiler 110 into the hot gas stream cleaned in the hot gas cyclone 108 leads to a lowering of the temperature level in the hot gas and consequently to an undesirable reduction of the dryer efficiency because the disadvantage is associated with the introduction of the cooled hot gas into the purified hot gas stream is that less dryer air can be used and thus more exhaust air is produced, which is to be supplied to an exhaust air cleaning system 170. More exhaust air means more waste heat and thus a worse energetic dryer efficiency.
  • Fig. 2 is now a second opposite of the plant Fig. 1 improved drying plant with a device for hot gas production with integrated thermal oil boiler and downstream dryer shown in a highly schematic view.
  • the plant in turn comprises a combustion chamber 1 having a feed grate furnace 2 and a boiler 6 for heating a heat transfer medium, in the present case again thermal oil.
  • the plant of Fig. 2 is characterized in that the entire hot gas stream is introduced after flowing out of the combustion chamber 1 in a bricked hot gas cyclone 4, whereby it is almost completely freed from the flowing with the hot gas from the combustion flue ash accordingly.
  • the hot gas cyclone 4 there is also a strong mixing of the hot gas, which leads to an improved burnout and in particular to an afterburning of carbon monoxide.
  • Fig. 2 branches in the flow direction of the hot gas behind the hot gas cyclone 4 from a bypass line 10a from the hot gas line 10, so that the hot gas stream is divided after exiting the hot gas cyclone 4 in a first and a second partial flow, the second partial flow via the bypass line 10a in a Boiler 6 is initiated to heat the thermal oil.
  • the boiler 6 is in to the system of Fig. 1 Comparably designed and includes a first flow stage with a radiant heat exchanger 6a and a second flow stage with a convection heat exchanger 6b.
  • the output of the boiler 6 is connected to the combustion chamber 1 via a hot gas line 12, so that the cooled hot gas stream emerging from the boiler can be returned to the combustion chamber 1 as a cooling gas stream.
  • This allows the Combustion chamber temperature, which would be more than 2000 ° C with stoichiometric combustion and dry fuel assuming an adiabatic combustion process, effectively limited to, for example ⁇ 940 ° C, without the combustion must be done with a high excess of air.
  • the cooled hot gas can be added to the hot gas main stream flowing through the hot gas line 10 via the control flap 9 before it flows into the mixing chamber 130. Likewise, a portion of the cooled hot gas via the control flap 13 of the exhaust air purification system can be supplied.
  • Fig. 3 is the drying plant of Fig. 2 shown in a more detailed schematic drawing, for reasons of clarity, mixing chamber, dryer and the exhaust air / filter system are not shown.
  • the drying plant is again designed for firing with solid, granulated and dust-like fuels.
  • a combustion chamber 1 with grate firing arranged immediately behind the hot gas outlet completely lined hot gas cyclone 4 and a thermal oil boiler 6, in which a part of the produced in the combustion chamber 1 and in the H strictlygaszykon 4 purified hot gas via a bypass line 10a and initiated there to heat the Thermal oil is used.
  • the solid fuels via Switzerlandböden 19, classifier (not shown) and 19 trough chain conveyor 19a via a distribution or - as in this case - via a distribution screw 21 and two gate valves 22 two dosing / supply bunkers 23 supplied.
  • the fuel is metered via a total of six frequency-controlled screws 24 via a special fuel chute 29 in the form of a chute on a divided into two grate halves feed grate 2.
  • the infinitely operable, frequency-controlled screws 24 make it possible to control the combustion in the combustion chamber 1 not only via burners but also via the fuel feed to the grate 2.
  • the fuel chute 29 initially runs vertically and then passes the fuel through an oblique section directly to the grate 2. In the vertical section of the fuel falls in free fall down. In this area pneumatic horizontal slide 25 are arranged. Upon interruption of the furnace, boiler failure or failure of the screw 24 close the respective slide 25 - in the event of an interruption of the furnace or boiler failure and the slide 22 - abruptly. The fuel metering is thus separated from the combustion chamber 1 and best sealed to the outside.
  • a water injection 26 is provided, which is activated upon reaching a presettable temperature (for example 100 ° C) by opening a solenoid valve 26a, so that water can be finely atomized injected via a nozzle.
  • a presettable temperature for example 100 ° C
  • a solenoid valve 26a opening a solenoid valve 26a
  • the chute 29 is cooled and rendered inert. This may be necessary, for example, in the case of a heat backlog of clogging or burn-back.
  • the combustion chamber-side end of the chute 29 is bricked, so that no metallic parts, which could deform in the long term under the action of the radiant heat, protrude into the combustion chamber 1.
  • granulate or fibrous fuels can also be incinerated on the grate 2.
  • a storage silo 20 via its own discharge system (usually rotating discharge screw, slide frame, etc.) and a conveyor screw (not shown in detail) added to the trough chain conveyor 19a and so also on the feed chute on the feed grate. 2 given up.
  • a conveyor screw not shown in detail
  • Fig. 3 is the possibility to supply the fuel to a blowing furnace.
  • the resulting ash falls at the end of the feed grate 2 via a shaft in a wet-Entschlacker 27 and is conveyed from there into a Rostaschecontainer 28.
  • the ashes are drawn off dry by means of screws and conveyed via further screws in the Rostaschecontainer 28.
  • Dust-form fuels from dust silos are fed to a dust-dosing container and conveyed via dosing screws, feeder and conveying air to at least two tangentially arranged burners 3 for gas and dust-like fuels.
  • the fuel supply is in Fig. 3 not shown in detail.
  • the tangential arrangement of the burner 3 improves the mixing and thus significantly reduces the CO value in the hot gas.
  • the multifunctional burners 3 are arranged above a secondary air injection 18a, 18b, which will be explained in more detail below.
  • the burners 3 are started with gaseous fuel and can then be switched to a dusty fuel operation.
  • the combustion in the combustion chamber 1 can thereby be operated exclusively with dust-like fuel, without having to install its own gas-fired starting torch.
  • at least one of the burners 3 can be operated both with high-grade pulverulent fuel (for example, dust from the dry chip preparation or grinding dust from the grinding of chipboard, etc.) and with inferior pulverulent fuel (for example, from the extraction of a recycling wood preparation), so that the installation of its own Einblas85ung can be omitted. Due to the sole operation with the burners 3, a maximum amount of dust can be burned, so that accumulating dust peaks can thus be utilized in the best possible way.
  • the burner 3 can be operated with minimal load to keep the system, for example, ready and hot.
  • Wood dust from the production of a wood processing plant is preferably used as fuel.
  • Another fuel for the heat supply in the solid fuel burning plant are the internal wood and production residues as well as bark and residual wood from the wood storage yard. Similarly, externally delivered untreated woods are burned.
  • the fresh air flow required for the combustion in the combustion chamber 1 is fed to the combustion chamber 1 via a primary air blower 16 and a secondary air blower 17.
  • the primary air is divided into several zones (windboxes) and flows in an ascending air flow in controlled amounts through the grate 2 and cools it.
  • the secondary air 18 is blown above the grate 2 via a plurality of front nozzles 18a and rear nozzles 18b.
  • the secondary air is used simultaneously as combustion air for the burner 3.
  • the negative pressure in the combustion chamber 1 is through the Trocknersaugzug (see. FIG. 2 ) and arranged behind the thermal oil boiler 6 arranged frequency-controlled induced draft 8, which subtracts the hot gas in the required amount on the bricked hot gas line 10.
  • the system is regulated in terms of fuel input and combustion air such that there is a constant negative pressure in the combustion chamber 1.
  • the hot gas power of the combustion chamber 1 is thus always oriented to the hot gas power requirement of the dryer. If a higher hot gas output is demanded by the dryer or the thermal oil boiler 6 (more amount of hot gas is withdrawn), the negative pressure in the combustion chamber 1 decreases and the power control promotes more fuel in combination with additional combustion air into the combustion chamber 1 and thereby increases the firing heat output.
  • the emerging from the combustion chamber hot gas flows, as well as in the schematic view of Fig. 2 It is preferably subjected to denitrification in a selective noncatalytic reduction reaction (SNCR).
  • SNCR selective noncatalytic reduction reaction
  • a suitable reducing agent in this case urea
  • An efficient denitrification is also promoted by the intensive mixing of the hot gas in the cyclone 4, so that the urea consumption and the ammonia slip can be minimized.
  • fly ash is separated up to a certain particle size (a grain with 50 ⁇ m is separated with about 50% probability).
  • the hot gas is strongly mixed in the cyclone 4 by the special cyclone flow, with a good burnout is achieved with afterburning of carbon monoxide.
  • the separated fly ash quantity in the cyclone 4 is fed via a double pendulum flap 14 and via a chute directly to a fly ash container 15 or the grate ash wet slagger 27 and discharged via this into the common ash container 28.
  • an emergency chimney 5 On the exit spiral of the cyclone 4 an emergency chimney 5 is arranged, which is opened in an emergency shutdown of the system, the hot gases are withdrawn by the natural train of the chimney from the combustion chamber 1.
  • a pipe damage - cold air can also be sucked on the emergency chimney 5 after switching off the firing and thus the thermal oil boiler 6 effectively cooled.
  • a portion of the hot gas after leaving the hot gas cyclone 4 flows through a bypass line 10a in the Thermal oil boiler 6.
  • the thermal oil boiler 6 comprises, instead of a known in the prior art air circulation system in the first flow stage, a water spray 35, with the first flow stage depending on the pollution (temperature increase) during operation of the impurities can be cleaned so as to maintain the original heat transfer coefficients.
  • the water spraying device 35 in the present case comprises a hose reel with a multi-hole nozzle at its free end, which descends with a longitudinal and rotating pendulum motion, the heat exchanger surface of the first flow stage and through the nozzle fine water jets are sprayed at high pressure on the contaminated pipe surfaces.
  • the fine water jets lead by thermal shock to chipping the adhesive and sometimes hard deposits, which boiler stoppages due to required cleaning work can be avoided.
  • soot blowers 40 are provided in a manner known per se from the prior art.
  • the two flow stages of the thermal oil boiler 6 are present and in contrast to Fig. 2 connected by a common ash funnel. About this, the ash can be removed via a double pendulum flap 14 in the closed fly ash container 15.
  • the cooled in the thermal oil boiler 6 hot gas is recycled via a control valve 11 and a return air duct 12 of the combustion chamber 1 to reduce the adiabatic combustion chamber temperature as cooling air. Only in exceptional cases and to regulate a certain hot gas temperature is the cooled hot gas flowing through the bricked hot gas line 10 hot gas main stream through the control valve 9 in the direction of the dryer (see. Fig. 2 ) mixed.
  • the fuel output is 38.59MW for a required 20MW target hot gas power and 16MW target thermal oil power.
  • a certain hot gas minimum temperature of, for example, 750 ° C 2.41MW cooled hot gas can be passed into the hot gas main stream, while 5.33MW directly in the exhaust air purification system, such as a wet electrostatic precipitator 170, are disposed of.
  • the combustion air in this case is an exhaust air from a drying plant at 7.5 ° C and the introduced with the air volume heat output is 1.82MW over the primary air and 0.91MW via the secondary air.
  • the mixing temperature is only 533 ° C (in real terms, the heat losses are around 460 ° C). Accordingly, it would no longer be sensible to mix the dryer exhaust air with the hot gas and thus to operate the dryer efficiently in recirculation mode.
  • the fuel output is again only 34.41MW for 20MW nominal hot gas power and 16MW nominal thermal oil output, resulting in an efficiency increase of approx. 12%.
  • 2.41MW cooled hot gas can be passed into the main hot gas stream, while 5.33MW are recuperated to recover heat in the combustion chamber 1 for cooling.
  • the hot gas temperature would theoretically remain at 920 ° C, which is ideal for overall dryer efficiency. In reality, temperature losses in the hot gas due to heat losses, false air, etc., and the temperature will fall by up to about 100 ° C. It can be seen that it makes sense to return the hot gas amount of the thermal oil boiler 6 as 100% as possible back to the combustion chamber.

Claims (15)

  1. Dispositif de générateur de gaz chaud avec chauffage intégré d'un agent caloporteur complété d'une chambre de combustion (1) briquetée de générateur de gaz chaud et d'une chaudière (6) agencée dans la direction d'écoulement du gaz chaud à l'intérieur de la chambre de combustion (1) et reliée à la chambre de combustion (1) par un conduit de gaz chaud (10) pour le chauffage de l'agent caloporteur, sachant qu'au moins un cyclone à gaz chaud (4) briqueté intégré dans le conduit de gaz chaud (10) est agencé entre la chambre de combustion (1) et la chaudière (6), de sorte que le gaz chaud sortant de la chambre de combustion (1) soit entièrement dirigé à travers au moins un cyclone à gaz chaud (4), caractérisé en ce qu'à partir du conduit de gaz chaud (10) une conduite de dérivation (10a) se ramifie dans la direction d'écoulement du gaz chaud dans le cyclone à gaz chaud (4), pour que le flux de gaz chaud soit réparti à la sortie du cyclone à gaz chaud en un premier ou deuxième écoulement partiel, sachant que le deuxième écoulement partiel dans la conduite de déviation (10a) de la chaudière (6) a lieu pour le chauffage de l'agent caloporteur, que la sortie de la chaudière (6) est reliée au conduit de gaz chaud (10) guidant le gaz, de sorte que le deuxième écoulement partiel sortant de la chaudière (6) soit refroidi au moins temporairement selon la température du gaz chaud du premier écoulement partiel auquel il s'ajoute, et que la sortie de la chaudière (6) et de la chambre de combustion (1) guidant le gaz soient reliées l'une à l'autre de sorte qu'au moins le deuxième écoulement partiel soit en partie ou entièrement ramené en flux de gaz de refroidissement dans la chambre de combustion (1).
  2. Dispositif selon la revendication 1, caractérisé en ce que le dispositif comporte des moyens de dénitrations du gaz chaud, sachant que les moyens de dénitrations sont formés d'au moins une tuyère (30) à l'ouverture de l'agent de réduction, notamment à partir d'une urée, dans le canal d'entrée tangentiel du cyclone à gaz chaud.
  3. Dispositif selon les revendications 1 ou 2, caractérisé en ce que la chaudière (6) comprend un premier gradin d'écoulement avec un échangeur de chaleur par rayonnement (6a) et un deuxième gradin d'écoulement avec un échangeur thermique par convection (6b), sachant que le premier gradin d'écoulement du gaz chaud s'effectue dans le sens descendant et que le deuxième gradin d'écoulement du gaz chaud s'effectue dans le sens ascendant.
  4. Dispositif selon l'une quelconque des revendications 1 à 3, caractérisé en ce que la chaudière (6) est composée de moyens de vaporisation d'un fluide de nettoyage, et plus particulièrement d'eau.
  5. Dispositif selon les revendications 3 et 4, caractérisé en ce que les moyens sont composés d'au moins une tuyère (35) disposée dans le premier gradin d'écoulement de la chaudière (6).
  6. Dispositif selon la revendication 5, caractérisé en ce que la tuyère (35) est disposée de telle sorte qu'elle effectue un mouvement de balancier en vaporisant le fluide de nettoyage.
  7. Dispositif selon l'une quelconque des revendications 1 à 6, caractérisé en ce que la chambre de combustion (1) est composée d'un four à grille, et plus particulièrement d'un four à grille ambulant, sachant qu'un combustible solide, granulé ou fibreux est transporté par un premier écoulement d'air montant par la grille (2) à travers la chambre de combustion (1).
  8. Dispositif selon la revendication 7, caractérisé en ce que le dispositif est composé d'un transporteur à vis rotative (24) et d'une goulotte (29) formant une glissière du flux continu de combustible par la grille (2), sachant que la goulotte (29) est formée au moyen d'une injection d'eau (26) refroidie.
  9. Dispositif selon l'une quelconque des revendications 1 à 8, caractérisé en ce que dans la chambre de combustion (1) soient prévues au moins deux brûleurs (3) disposés de manière tangentielle pour la combustion d'un combustible gazeux et de poussière.
  10. Dispositif de séchage pour sécher notamment des produits en bois et/ou des déchets de bois au moyen d'un dispositif selon l'une quelconque des revendications 1 à 9, sachant que dans le cyclone à gaz chaud (4) le gaz chaud sortant est lancé au moins partiellement dans un séchoir (140) pour le séchage notamment de bois coupé, de sciure, de copeaux, de fibres de bois, d'aliments pour animaux et de céréales.
  11. Procédé de générateur de gaz chaud avec chauffage intégré d'un agent caloporteur, sachant que le gaz chaud est généré dans une chambre de combustion (1) briquetée et conduit dans une chaudière (6) agencée dans la direction d'écoulement du gaz chaud à l'intérieur de la chambre de combustion (1) pour le chauffage de l'agent caloporteur, et sachant qu'il est conduit dans la chambre de combustion (1) en un courant de gaz chaud sortant avant d'entrer totalement dans la chaudière par au moins un cyclone à gaz chaud (4) briqueté, caractérisé en ce que le courant de gaz chaud est réparti après la sortie du cyclone à gaz chaud (4) en un premier et un deuxième écoulement partiel, sachant que le deuxième écoulement partiel est conduit par une conduite de dérivation (10a) dans la chaudière pour le chauffage de l'agent caloporteur et que le deuxième écoulement partiel sortant refroidi de la chaudière (6) est ramené en flux de gaz de refroidissement dans la chambre à combustion (1).
  12. Procédé selon la revendication 1, caractérisé en ce que le premier écoulement partiel de gaz chaud s'effectue dans un dispositif de séchage (140).
  13. Procédé selon les revendications 11 ou 12, caractérisé en ce que le deuxième écoulement partiel sortant refroidi de la chaudière (6) est mélangé au moins temporairement au gaz chaud dans le premier écoulement partiel pour régler la température.
  14. Procédé selon l'une quelconque des revendications 11 à 13, caractérisé en ce que la chaudière (6) est nettoyée en fonctionnement au moins temporairement par vaporisation d'un fluide de nettoyage, et plus particulièrement d'eau.
  15. Procédé selon l'une quelconque des revendications 11 à 14, caractérisé en ce que l'apport en carburant et l'alimentation en air comburant dans la chambre de combustion (1) sont réglés de telle sorte qu'une dépression constante soit présente dans la chambre de combustion (1).
EP11158981.8A 2010-04-09 2011-03-21 Dispositif et procédé de production de gaz chaud avec chauffage intégré d'un fluide caloporteur Active EP2375152B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PL11158981T PL2375152T3 (pl) 2010-04-09 2011-03-21 Urządzenie i sposób wytwarzania gorącego gazu ze zintegrowanym podgrzewaniem medium przenoszącego ciepło

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE201010014479 DE102010014479B4 (de) 2010-04-09 2010-04-09 Vorrichtung und Verfahren zur Heißgaserzeugung mit integrierter Erhitzung eines Wärmeträgermediums

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EP2375152A2 EP2375152A2 (fr) 2011-10-12
EP2375152A3 EP2375152A3 (fr) 2014-04-09
EP2375152B1 true EP2375152B1 (fr) 2017-01-18

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EP (1) EP2375152B1 (fr)
DE (1) DE102010014479B4 (fr)
ES (1) ES2620463T3 (fr)
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PL (1) PL2375152T3 (fr)

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DE102012109917A1 (de) * 2012-10-17 2014-04-17 Dieffenbacher GmbH Maschinen- und Anlagenbau Vorrichtung und Verfahren zur Trocknung und Torrefizierung von Biomasse
EP3589891A1 (fr) 2017-03-03 2020-01-08 Douglas Technical Limited Appareil et procédé de séchage continu de produits en vrac, en particulier de copeaux de bois et/ou de fibres de bois comprenant un générateur de gaz chaud à particules solides
UA124778C2 (uk) * 2017-03-03 2021-11-17 Даґлас Текнікал Лімітед Установка та спосіб для безперервного сушіння насипних матеріалів, зокрема деревної стружки та/або деревних волокон, з використанням багатопаливного пальника з системою охолодження муфеля
EA038915B9 (ru) 2017-03-03 2021-12-06 Дуглас Текникал Лимитед Устройство и способ непрерывной сушки сыпучих продуктов, в частности древесной щепы и/или древесного волокна, включающие теплообменник
CA3053976A1 (fr) * 2017-03-03 2018-09-07 Douglas Technical Limited Appareil et procede de sechage continu de produits en vrac, en particulier de copeaux de bois et/ou de fibres de bois, comprenant un cyclone a gaz chaud
UA125909C2 (uk) 2017-06-06 2022-07-06 Даґлас Текнікал Лімітед Установка і спосіб безперервного сушіння насипних матеріалів

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Publication number Publication date
ES2620463T3 (es) 2017-06-28
PL2375152T3 (pl) 2017-07-31
EP2375152A2 (fr) 2011-10-12
HUE033510T2 (en) 2017-12-28
DE102010014479A1 (de) 2011-10-13
DE102010014479B4 (de) 2012-01-12
EP2375152A3 (fr) 2014-04-09

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