奥地利专利AT511684A1 DEVICE AND METHOD FOR GASIZING BIOMASS

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专利摘要:
The invention relates to a reactor (1) for gasifying biomass, in particular wood, comprising a filling shaft (7) and an ash bed arranged below the filling shaft (7). According to the invention, provision is made for a device with which biomass adhering to the filling shaft (7) can be detached and / or a heat exchanger is provided, with which a product gas produced from the biomass heats up the biomass in the hopper (7) and to an oxidizing air emits. The invention further relates to a fine filter (29) for purifying a product gas generated from biomass. According to the invention, it is provided that the filter medium contains biomass. In addition, the invention relates to a process for the gasification of biomass in a reactor (1), in particular a reactor (1) according to the invention, to a product gas. According to the invention, it is provided that biomass adhering to the filling shaft (7) is released and / or heat is released from the product gas to biomass and an oxidation air.
公开号:AT511684A1
申请号:T1033/2011
申请日:2011-07-14
公开日:2013-01-15
发明作者:Franz Ing Krammer
申请人:Rep Renewable Energy Products Gmbh；
IPC主号:

专利说明:

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Apparatus and method for gasification of biomass
The invention relates to a reactor for gasifying biomass, in particular wood, having a filling shaft and an ash bed arranged below the filling shaft.
Furthermore, the invention relates to a fine filter for cleaning a product gas generated from biomass.
Moreover, the invention relates to a use of such a fine filter.
Furthermore, the invention relates to a process for the gasification of biomass in a reactor, in particular in a reactor of the type mentioned, to a product gas.
Biomass gasifiers are known as such from the prior art. For example, from WO 2008/004070 A1 a device is known, gasified with the biomass such as wood, straw or biological waste in a reactor and a resulting gas is then passed into a gas-powered engine, where this gas is converted by combustion into mechanical energy , The motor is connected to a generator, which converts the mechanical energy into electrical energy.
Devices of the prior art have the disadvantages that a plant efficiency is low because on the one hand product gas exits the reactor at high temperatures, which suffers an efficiency of a downstream internal combustion engine, on the other hand consistency of the biomass often leads to sticking in the reactor, so frequent and expensive maintenance is the result. Furthermore, a high expenditure for the disposal of filter media, which are required for a product gas purification, has a negative effect on the system efficiency.
The object of the invention is to overcome or reduce the disadvantages of the prior art by providing a reactor with which a more efficient method is possible. • »* * • * * * * * * * * * * * * '' '* * * * * * * * * * * * * * * * * * * * * 2
In addition, a fine filter is to be specified, which further increases the efficiency of such a method,
The aim is further to specify a use of such a fine filter.
Furthermore, a method is to be specified which overcomes or reduces the disadvantages of the prior art.
The first object is inventively achieved in that in a reactor of the type mentioned a device is provided, with the biomass adhering to the hopper is solvable and / or a heat exchanger is provided, with a produced from the biomass product gas heat tracked in the hopper Biomass and gives off to an oxidation air.
Since the biomass must be moved during operation by the hopper from a first end to a second end at a flow rate, adhering to the hopper biomass impedes movement and thus proper operation. An advantage of the device with which biomass adhering to the filling shaft can be solved can therefore also be seen, in particular, in the fact that a downtime can be substantially reduced in which the reactor must be shut down for maintenance purposes. This increases the plant efficiency for a plant operator.
The heat exchanger with which the heat of the product gas can be transferred to the biomass in the hopper and the oxidation air, in particular also has the advantage that an energy required for pyrolysis and preheating the oxidation air can be taken from the product gas, so less Energy must be removed from the biomass and a temperature of the product gas can be reduced. If the product gas is further processed directly in an internal combustion engine, a lower temperature increases pure thermodynamic efficiency in the internal combustion engine. Thus, a heat transfer from the product gas to the oxidation air and biomass has several positive effects on the system efficiency. 3
It is advantageous that a Mehrfachmantei is provided, with which a heat of the product gas to the oxidation air and tracked biomass is transferable. Thus, this multiple jacket fulfills not only a mechanically supporting function but also the function of the heat exchanger, as a result of which the reactor can be produced particularly favorably. Preferably, the multiple jacket is formed such that it aulweist, a plurality of approximately concentric to each other, approximately cylindrical coats aulweist, wherein between a first jacket which forms the hopper, and a second jacket which encloses the first jacket, product gas in a preferred vertical installation due to thermal buoyancy can flow from bottom to top and around this second jacket, a third jacket is arranged such that the area between the second jacket and the third jacket of the oxidizing air can be flowed through. In this way, heat transfer from the product gas via the first jacket or biomass in the feed chute and over the second mantle to oxidation air can be carried out and the temperature of the product gas can be minimized until it leaves the multiple jacket. The multiple jacket is preferably made of steel, the first jacket, which on the one hand borders on the biomass and on the other hand on the product gas, preferably consists of temperature- and acid-resistant material, for example an austenitic chromium-nickel-molybdenum steel. The second jacket adjacent to the oxidizing air as well as to the product gas is preferably made only in a lower region of heat-resistant steel and in an upper region of a normal boiler plate in order to minimize manufacturing costs. It is advantageous if an insulating layer of a heat-insulating material is applied to the third jacket, which is preferably also made of steel, in order to prevent a heat of the oxidizing air is released to an environment,
In order to reduce maintenance times, it is particularly advantageous that a vibrating device is provided with which the hopper can be set into vibration so that adhering biomass can be detached from the hopper. Due to broad spectra of possible constituents and possible consistencies of the biomass, biomass can adhere to the hopper during operation, which can severely impair the ability of the reactor to function. In order to solve at best adhering biomass particularly favorable, the hopper can be added by means of the vibrator vibrated. The vibrating device may consist of a motor and an imbalance or other electromagnetic interference associated with the motor. · · · «« * * * · · · · · · · · · · · · · · · · · · · · · · · ·. ··· ♦ * 4 or mechanical devices exist, wherein vibrations of the vibrating device are preferably transferable by means of molding tubes to the hopper.
These forming tubes can form a direct connection between the vibrator and the hopper; but it can also be provided that the vibrator is connected indirectly via flexible connecting elements with the hopper. The connection between vibrator and hopper is preferably designed such that temperature-induced mechanical stresses throughout the reactor are minimized and a tightness of the hopper is permanently guaranteed. Preferably, the vibrator is activated at regular intervals between 10 and 30 minutes, preferably between 15 and 25 minutes, more preferably about 20 minutes for a few seconds, preferably for about 5 seconds.
It has been proven that a wedge slide is provided with which the biomass is fed to the hopper. Thus, the biomass can be fed to the hopper in a particularly simple and energy-efficient manner. The wedge slide preferably comprises a slide plate, which is guided linearly movable in a groove of a frame rigidly connected to the feed chute. The wedge slide and the frame are preferably components of a lock, via which the biomass is fed to the hopper. The connection of the slide plate with the frame is preferably carried out particularly wear with one or more ball bearings. Other types of storage are possible. Due to an acidic atmosphere in the hopper, the entire wedge slide or parts thereof in an acid-resistant material, preferably an acid-resistant steel executed.
It is advantageous that a sealed feed device is provided, with which the biomass can be fed to the feed chute in the absence of oxygen. This is particularly important, therefore, in order to prevent unwanted gases, in particular oxygen, from entering the feed chute in order to be able to trigger chemical reactions in the feed shaft that are dependent on a controlled or regulated air ratio.
It is preferably provided that the feed chute is designed to taper in a lower region, in particular with a ratio of a chute cross section to a fire zone cross section of 1.2 to 10, preferably 1.4 to 3, particularly preferably about 1.9. In this calculation, the hopper cross section is measured in a cylindrical upper area of the hopper and the fire zone cross section in a fire zone. Since the biomass changes its volume as it moves through the lower part of the pyrolysis that takes place in this lower region, it is advantageous if the hopper is adapted to a volume change of the biomass, to ensure a uniform flow velocity of the biomass and optimal conditions for the running chemical To enable processes. Preferably, a cone angle between a cone axis and a lateral surface of the conical lower region is between 20 ° and 60 °, more preferably between 30 ° and 50 °, in particular about 40 °. While the fire zone adjoining this conical region is preferably cylindrical, a lower region between the fire zone and a constriction, which further adjoins the fire zone, is preferably likewise conical, in order to constructively take into account the volume change of the biomass even in this lowermost region. A cone angle of this lowermost region is preferably between 20 ° and 60 °, more preferably between 30 ° and 50 °, in particular about 40 °. This cone angle can also correspond to the cone angle of the lower region.
It has been proven that an oxidation air supply is connected via an intermediate region and an oxidation air ring with oxidation air nozzles, which open into a fire zone. In this case, the oxidation air can be preheated both in the intermediate region, which is preferably thermally connected to a product gas region, as well as in the oxidation air ring, which is preferably thermally connected to the fire zone. This preheating the oxidation air is made particularly favorable. Another advantage can also be seen in the fact that the oxidation air can occur evenly over a circumference of the fire zone in this and thus can be evenly distributed in the fire zone. Over a cross-section of the oxidation air nozzles and an air pressure, an air outlet velocity at the oxidation air nozzles can be particularly favorably influenced, which has a high influence on a chemical reaction in the fire zone. Thus, a higher air outlet velocity results in a higher temperature in the fire zone, but a spatial extension of a glow zone is less. Depending on the composition and the calorific value of the biomass, an optimal air inlet cross section may change. It has proven particularly useful that a sum of all cross sections of the oxidation air nozzles corresponds to between 1% and 10%, preferably between 2% and 8%, in particular approximately 4%, of a constriction cross section. The constriction cross section is that cross section of the hopper at which the biomass can escape from the hopper to the ash bed.
It has been proven that the oxidation air nozzles are distributed so uniformly over a circumference of the fire zone, that between two oxidation air nozzles at the periphery of the fire zone, a distance of between 2 and 30 cm, preferably between 5 and 20 cm, in particular about 10 to 12 cm , In this case, the oxidation air nozzles are preferably arranged in a plane, but an arrangement in several levels is also possible. This results depending on the extent of the fire zone for the chemical reaction in the fire zone particularly favorable number of oxidation air nozzles and a favorable air velocity.
Preferably, it may be that a rotary grate is provided with at least one stirring pin on the ash bed, are solvable with the packaging of biomass. The rotary grate thereby enables a uniform burning of the biomass and additionally serves as an ash discharge in an underlying ash cone. A drive of the rotary grate is preferably carried out by means of a linear motor via a drive linkage. Other types of drive are possible. The drive linkage is preferably gas-tightly sealed by means of a stuffing box, which has a temperature-resistant graphite sealing cord for producing a tightness. The at least one stirring pin enables a loosening of the grate-gripping biomass in a particularly favorable manner.
It has been proven that sensors are provided with which a pressure before and after the ash bed can be measured in order to use data obtained during a measurement for a control and / or regulation of the stirring pins. With this arrangement, attachments of biomass to the rotating grate are particularly easily recognizable, since packaging leads to an increased difference between a pressure before and a pressure after the rotary grate. Thus, the stirring pins can be activated precisely if further Anpackungen would lead to problems and wear of the stirrer pins can be minimized. 7
In order to produce a product gas from biomass, it is advantageous that in a device for producing a product gas from biomass, comprising a fuel storage for the biomass, a reactor for gasifying the biomass, at least one conveying means for conveying the biomass from the fuel storage in the reactor and at least one filter system for purifying product gas produced from the biomass, the reactor being designed according to the invention.
This biomass can fully automatically transported from a fuel storage in the reactor and the product gas are then cleaned in a filter system. In particular, due to the particularly efficient reactor, the system efficiency of the entire device is better than in the case of devices of the prior art.
It is preferably provided that at least one cyclone filter is arranged downstream of the reactor. In the cyclone filter, the product gas is freed of dust and fly ash, so that the product gas has a higher quality for further use. Preferably, three parallel cyclone filters are provided, whereby only one cyclone filter or more than three cyclone filters are equally possible. A plurality of cyclone filters can be arranged in parallel or serially through which gas can flow, a cyclone filter ash container being arranged such that an ash which can be deposited in the at least one cyclone filter is preferably automatically directed into the cyclone filter ash container. When arranging the Zyklonfilteraschebehälters below the cyclone filter this is particularly easy. The operation of the cyclone filter is known and based on a centrifugal force, with the dust and fly ash in the cyclone filter are pushed outwards.
It is advantageous that at least one fine filter is connected downstream of the reactor, which contains biomass as a filter medium. This fine filter can be downstream of the cyclone filter, since it also allows smaller particles and tar residues to be removed.
It is advantageous that an internal combustion engine is provided, in which the product gas is conductive, and the internal combustion engine is coupled to a generator for generating electrical energy. As an alternative to the internal combustion engine, another internal combustion engine, for example a gas turbine, may also be provided. «·« ·
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This allows the device biomass fully automatically convert into electrical energy.
It is preferably provided that a waste heat heat exchanger is provided, with which a heat of an exhaust gas of the internal combustion engine to the biomass for preheating the same is transferable. Thus, a system efficiency of the entire system is further increased, since the heat of the exhaust gas of the internal combustion engine can be reused. Of course, it is also possible to use the heat of the exhaust gas of the internal combustion engine elsewhere, for heating purposes, for example.
The second object is achieved in that contains a fine filter of the type mentioned as a filter medium biomass. This biomass may preferably contain wood chips according to ÖNORM M7133 G50 or G30 as well as sawdust. Advantage of this design is that the filter medium can be transported after a long period of use in the fuel storage and processed in the reactor such as biomass, so this filter medium is easily recyclable. This filter medium is preferably flowed through in the fine filter from bottom to top of the product gas, with impurities present in the product gas, in particular tar, settling on the biomass. In this case, the biomass can be stored on one or more levels. A sensor can also be provided which measures a pressure drop across the filter and thus determines the optimum time for a transfer of the polluted biomass into the fuel storage and a filling of the filter with new biomass. Alternatively, a time-based refilling with biomass is possible.
Instead of wood chips and sawdust, of course, another type of solid biomass can be used, whereby the filtration effect changes with the filter medium. It is advantageous that the filter medium is on several levels in the filter on porous perforated plates, preferably perforated plates, and is serially from the product gas from bottom to top flowed through. It has a bottom layer about 20% wood chips and about 80% sawdust and a top layer about 70% wood chips and about 30% sawdust. In intermediate layers, a proportion of wood chips is above the lowest layer and rises to the top layer. It is preferred that wood chips and sawdust are made of spruce wood. *
The third object is achieved by using a filter according to the invention for purifying a product gas produced from biomass, in particular for depositing tar. This makes it possible to achieve a particularly cost-effective and environmentally friendly type of product gas purification.
The fourth object is achieved in that dissolved in a method of the type mentioned at the hopper biomass and / or released from the product gas heat to biomass and an oxidation air.
By a, in particular intermittent, dissolving adhering to the hopper biomass contamination of the hopper with biomass can be avoided, which would severely affect a function. This reduces maintenance times and increases system efficiency. By transferring heat from the product gas to biomass and an oxidizing air, the amount of energy leaving the reactor in the form of heat in the product gas can be minimized.
It is preferably provided that a shaking device at certain intervals, preferably at intervals of 10 to 30 minutes, in particular 15 to 25 minutes, preferably about 20 minutes, for the duration of less than 5 minutes, preferably less than 1 minute, particularly preferably for about 5 seconds, to release biomass attached to the hopper. This allows on the one hand to solve adhering contaminants particularly favorable and on the other hand, mechanical stresses of a material due to shaking remain minimal, so that a long life of the reactor is achieved.
It is advantageous that a flow velocity of the biomass in a lower region of the feed chute is kept approximately constant over a conical design of the feed chute in this region. Since the biomass in the lower region changes its volume due to chemical reactions, a conical formation of the feed chute, which leads to a uniform flow rate, has a particularly favorable effect on the conditions of these chemical reactions, such as pressure or temperature. • · • 4 ··· «« · · · »• 4« * · ♦ · • * 4 · «* · 4
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It is advantageous that in a lowermost region of the filling shaft, in particular in the region of a constriction, in more than 50%, in particular more than 70%, preferably more than 90% of the biomass, a temperature between 1000 ° C and 1600 ° C, in particular 1200 ° C and 1500 ° C, preferably 1220 ° C and 1470 ° C, is located. This ensures cracking of long-chain hydrocarbons (tars) and thus avoids or at least reduces the accumulation of long-chain hydrocarbons in pipelines and in any downstream internal combustion engine.
It has been proven that a pressure drop over an ash bed is measured continuously and when a predetermined limit value is exceeded, an agitator in the ash bed is activated. This makes it possible to detect and detach biomass packing on the ash bed or on a rotating grate so that the functioning of the device can be ensured.
It is advantageous that the oxidation air flows from an intermediate jacket via an oxidation air ring to air nozzles in a fire zone, where an oxidation of biomass is caused. This ensures that the oxidation air is sufficiently preheated, so that higher product gas temperatures are reached after the oxidation zone. Through the oxidation air ring and the oxidation air nozzles, the air can be distributed evenly into the fire zone, so that even temperatures are reached.
It is favorable if a product gas is used to drive an internal combustion engine and with this a generator for generating electrical energy is driven. This makes it possible to achieve in a particularly simple manner a fully automatic conversion of biomass stored chemical energy into electrical energy in a process.
It is preferably provided that a heat of an exhaust gas of the internal combustion engine is used for preheating the biomass. Thus, an efficiency of the method can be further increased because a waste heat of the internal combustion engine is returned to the process. Alternatively, this waste heat could also be used for heating purposes or other thermal processes. • * ♦ * ** ·········· • t 4 9 * * «·« · *** · 11
Further features, advantages and effects of the invention will become apparent from the embodiment illustrated below. In the drawings, to which reference is made, show:
Figure 1 is a schematic representation of a reactor according to the invention for gasification of biomass.
FIG. 2 shows a schematic illustration of a device for producing a product gas from biomass; FIG.
Fig. 3 is an illustration of a fine filter with biomass as a filter medium.
Fig. 1 shows a schematic representation of a reactor 1 for gasification of biomass, in particular wood. Via a lock 6, the biomass can be introduced with a head-side wedge gate in the reactor 1 and a hopper 7, which is sealed gas-tight by means of a temperature-resistant Graphitdichtschnur to accurately control an oxygen content in the reactor 1 can. The wedge gate valve is equipped with position sensors so that a current position of a slide plate can be detected at any time for automatic operation. A drive of the slide plate by means of an electric motor. Attached to the side of the reactor 1 is a vibrating device 8 with which biomass adhering to the filling shaft 7 can be released. A shaking movement is for this purpose of the vibrator 8 via one or more molding tubes 9 to the hopper 7 transferable. Also, a transmission of the shaking movement with other structural components instead of a forming tube 9 is possible, for example, mechanically softer or stiffer components to achieve optimum Rüttelergebnis, In the reactor 1 shown in the embodiment, the vibrator 8 is activated regularly every 20 minutes for about 5 seconds to dissolve adherent biomass from the hopper 7. The choice of longer intervals between the shaking intervals as well as longer shaking intervals are just as possible as the choice of shorter times for these intervals. Also, the regulation of the vibrator 8 is possible via a sensor which detects a volume or mass of an adherent biomass and tuned to the vibrator 8 activated. Alternatively, it is also possible to dissolve adherent biomass by other mechanical methods, such as direct or indirect exposure to a solid, liquid or gaseous medium. • * «· 4 * 9 § * ·» ·····················································································································································································
The Fülschacht 7 is formed by a first jacket 23, in which the biomass is moved in operation from a first end in an upper portion 10 to a constriction 17 by gravity. During the movement chemical processes take place in the biomass. Due to the chemical processes and the resulting chemical constituents, the first jacket 23 is made of an austenitic chromium-nickel-molybdenum steel at least in the lower region 12. Alternatively, other heat and acid resistant materials may be used. The first jacket 23 which is cylindrical in the upper region 10 and a central region 11 is enclosed by a second jacket 24 lying concentrically therewith. This second jacket 24 is further enclosed by a third jacket 25 lying concentrically therewith. On an outer side of the third jacket 25, an insulating layer 26 is arranged consisting of heat-insulating material, which minimizes a heat emission of oxidative air to an environment. First jacket 23, second jacket 24 and third jacket 25, which are preferably made of steel, are substantially rotationally symmetrical, the second jacket 24 and third jacket 25 are substantially continuous cylindrical. In the lower region 12 and a lowermost region 14 of the filling shaft 7, the first jacket 23 is partially conical, wherein an angle between a cone axis and a conical surface is about 40 °. The conical design is interrupted by a cylindrically shaped fire zone 13 and ends at a constriction 17, at which the biomass can escape during operation from the hopper 7 to an ash bed. A constriction ratio of a fire zone cross section to a feed chute cross section is about 1: 1.9, the constriction ratio with the cross section of the feed chute 7 being formed in the cylindrical upper region 10. This necking ratio and the angle are dependent on a composition of the biomass and may also be smaller or larger depending on the application. Thus, the necking ratio is about 1: 1.8 for a softwood as a major constituent of the biomass and about 1: 2 for hardwood as a major constituent of the biomass. However, this can change depending on the biomass used or type of wood used up or down. Thus, necking ratios of 1: 4 to 1: 1.1 are possible depending on the application.
In the lower region 12 of the hopper 7, an oxidation air ring 15 is arranged around the hopper 7, which is connected via a compensator, which can compensate for thermal expansion, with the intermediate region. Protruding from the oxidizer air ring 15 • * i * # * ft ft ft ft * • * β * t * * * '* * * * * * * * * * i n i
Oxidation air nozzles 16 in a plane in the fire zone 13. In the embodiment, the number of oxidation air nozzles 16 is selected such that over a circumference of the fire zone 13 between the centers of the oxidation air nozzles 16 remains a distance of about 10 to 12 cm in the circumferential direction. The cross section of the oxidation air nozzles 16 is selected such that the sum of all cross sections corresponds to about 4% of a constriction cross section. However, the function is at least limited in other cross-sectional ratios, for example 1% to 20%, or distances between the oxidation air nozzles 16, for example 1 to 30 cm. The constriction cross section is that smallest cross section of the hopper 7, through which the biomass exits from the hopper 7 to the ash bed.
Below the constriction 17 is the ash bed, on which the biomass falls after passing through the reactor 1. The ash bed in this case comprises a rotary grate 18, which is connected via a drive linkage with a motor, preferably a linear motor 20, and can be driven by this. A gas-tight implementation of the drive linkage from the rotary grate 18 for lying outside the reactor 1 motor is achieved via a stuffing box, which is sealed with a temperature-resistant graphite sealing cord.
Stirring pins 19 are arranged on the rotating grate 18, with which biomass adhering to the rotating grate 18 can be detached. Adhering biomass obstructs an ash discharge in a arranged under the rotary grate 18 ash cone 21 and due to an increased pressure loss on the rotary grate 18 unimpeded outflow of the product gas. By means of a pressure difference measurement, the optimum time is determined at which the stirring pins 19 are activated and biomass is released from the rotary grate 18. As a result, a function of the reactor 1 is constantly monitored.
In operation, in a space between the first jacket 23 and the second jacket 24, a product gas flows from the constriction 17 upwardly out of the reactor 1. In the space between the second jacket 24 and the third jacket 25, an oxidation air flows from an oxidation air supply 43 to an oxidation air ring 15. In the feed chute 7 is biomass, which is introduced by the wedge slide in the hopper 7 and this passes from top to bottom. In this case, the product gas gives heat via the first jacket 23 to the biomass in the filling shaft 7 and via the second jacket 24 to the 14 "*.
From oxidation air. Biomass adhering to the filling shaft 7 is achieved by activating the vibrating device 8 for 5 seconds after every 20 minutes. The biomass is dried in the upper region 10 of the hopper 7 by a heat of the product gas and preheated. In the central region 11, the pyrolysis begins, during which, among other things, organic acids such as acetic acid, methyl alcohol and tar arise in the course of a thermal decomposition. Further decomposes in this central region 11 at a temperature of 200 ° C to 300 ° C hemicellulose, which is possibly contained in the biomass. Upon further heating, between 325 ° C and 375 ° C contained in the biomass cellulose is split and it produces carbon dioxide, methane and organic acids, especially acetic acid. As the temperature rises above 375 ° C, lignin breaks down into smaller chemical compounds. Further fall hydrocarbons and tars in this central region 11. In a lower region 12 of the hopper 7, the oxidation of the biomass begins. A continuous flow rate and a high pressure, which are achieved in this area due to a decreasing solids volume of the biomass via the conical formation of the hopper 7, are required to ensure an optimal sequence of the oxidation. In the fire zone 13 of the biomass is supplied via the oxidation air nozzles 16, the oxidation air and burn stoichiometrically carbon and hydrogen with energy release. A temperature is about 650 DC to 850 ° C, with carbon dioxide, water and methane. A temperature range can be particularly favorable control over the amount of the supplied oxidizing air and a speed at which the oxidation air penetrates. Below the fire zone 13 in the lowermost region 14 of the hopper 7, a chemical reduction takes place. Here, the formation of combustible gas is made possible inter alia by a gasification of carbon. In this lowermost region 14, the intermediate products formed during the oxidation, such as carbon dioxide and water, are reduced at hot spots, resulting in carbon monoxide, hydrogen and higher hydrocarbons. Due to the special design of the reactor 1 in this lowermost region 14, ideal temperatures between 1220 ° C and 1470 ° C are reached here, especially in the region of the constriction 17, which are close to the ash melting point of the biomass. A limited function is also possible in a temperature range of 1000 ° C to 1600 ° C. Due to the conical design of the filling shaft 7 in the lowermost region 14, a constant temperature can be achieved over a large part of the volume of the biomass, in particular in the region 17, thus ensuring cracking of long-chain hydrocarbons (tars) and thus deposits of tars in particular be minimized in pipelines. Due to the temperatures near an ash melting point of biomass it comes in operation to the grate 18 adhering biomass, which is achieved with the stirring pins 19. Since the right choice of agitation intervals between the stirring intervals is relevant in order to obtain an optimal result of the chemical reaction in the reduction zone, the stirring pins 19 are actuated to the exact extent necessary to dissolve adherent biomass. For this purpose, a pressure difference is measured before and after the rotary grate 18 and these values are used for a control of the stirring pins 19. By means of a movement of the rotary grate 18, ashes are discharged particularly favorably into the ash tank 21, from where they are conveyed automatically by means of an ash conveyor 22 into an ash storage container 42. This process results in a gas yield of up to 2 standard cubic meters of product gas per kilogram of biomass fed.
Fig. 2 shows a device 2 in which the reactor 1 is embedded in order to produce a product gas from biomass. In this case, the biomass can be transported from a fuel storage 3 by means of a conveyor 4 via a biomass dryer 5 in the reactor 1. A gas outlet of the reactor 1 is connected to Zyklonfiltem 27, where the product gas can be freed of dust and fly ash. In this case, three parallel cyclone filters 27 are provided, which can be flowed through uniformly and in parallel by gas. In the cyclone filters 27, the product gas can be guided at a very high speed in a circular path, so that due to a centrifugal force, dust and ash are forced radially outward from where they can be discharged down into a cyclone filter ashtray 28.
Downstream of the cyclone filter 27 is a fine filter 29, in which the product gas is cleaned by means of wood chips and sawdust. A particular advantage of the wood chips as a filter material in this fine filter 29 is that the wood chips, after they are saturated with impurities, fed to the fuel storage room and thus can be recycled directly. In this way, no filter waste. Preferably, the fine filter 29 is formed such that it is flowed through during operation of the product gas from bottom to top, with dirt and tar on the wood chips «··················································································. ···········································. There may be provided a pressure sensor, via which an optimal time for emptying this filter can be determined. Alternatively, a purely time-based emptying of the filter would be possible.
A gas outlet of the fine filter 29 is connected to a four-cylinder gasoline engine or generally an internal combustion engine 30, which drives a generator 31 and thus can convert the energy of the gas into electrical energy. Alternatively, the use of a gas turbine or other machinery is possible, which can convert a chemical energy of a product gas into mechanical energy and subsequently into electrical energy. Downstream of the gas engine is a waste heat heat exchanger 32, which makes use of waste heat of the gas engine for preheating the biomass and for any heating purposes. 2 also shows a biomass preheating line 33 from which at least part of the residual heat of the product gas for the heating of biomass in the biomass dryer 5 can be used. There is also provided a heat storage 34 for temporary storage of waste heat.
The method for purifying biomass-derived product gas and further processing into electrical energy works with the device 2 such that the biomass is supplied from the fuel storage 3 by means of the conveyor 4 via the lock 6 to the hopper 7. Subsequently, the biomass is gasified as described above in the reactor 1 to product gas. After exiting the reactor 1, the product gas in the cyclone filters 27 and in the fine filter 29 is cleaned before it is passed into the internal combustion engine 30. There, the chemical energy of the gas is converted into mechanical energy, which is subsequently converted in a generator 31 into electrical energy. When the product gas is burned, the gas engine is regulated to an air ratio of lambda equal to 1.15. This results in particularly favorable pollutant values in the exhaust gas. A waste heat of the internal combustion engine 30 is discharged via the waste heat heat exchanger 32 to a heat transfer medium and temporarily stored for heating purposes in the heat storage 34 and partially used over the Biomassevorwärmeleitung 33 for drying the biomass in the biomass dryer 5 before entering the reactor 1. A high maintenance and disposal costs are avoided in this process by the fact that the filling shaft 7 freed regularly by shaking adhering biomass and the hopper 7 by regular • «•« • «« «
17 Stirring with stirring pins 19 is cleaned of packings and that contaminated wood chips in the fine filter 29 are recycled in a particularly favorable way by returning them to the fuel store 3 ". ***" ,
Fig. 3 shows a representation of the fine filter 29, is used in the biomass as a filter material. The product gas may enter the fine filter 29 via a product gas inlet 35 at a lower end. The filter medium is distributed over four layers 38, 39, 40, 41 on perforated plates 37, through which the product gas can flow. The perforated plates 37 are preferably formed from sheets with a plurality of holes, but it can also be another type of porous bottom can be selected, which is preferably formed temperature resistant. Alternatively, of course, the use of only a single layer or the use of more than four layers is possible. The product gas flows through the fine filter 29 during operation from bottom to top and flows serially through the individual levels until it leaves the fine filter 29 cleaned at the product gas outlet 36. When flowing through the individual layers particles located in the product gas, in particular tars, dust and impurities are largely attached to the filter material. The filter medium of the layer 38 consists of 20% wood chips and 80% sawdust, the filter medium of the layer 39 to 30% from wood chips and 70% from sawdust, the filter medium layer 40 to 50% from wood chips and 50% from sawdust and the filter medium of the layer 41 to 70% of wood chips and 30% of sawdust. Wood chips and sawdust are preferably made of spruce wood, but it is also conceivable to use other types of biomass, with a filter performance depends on the biomass used. A particular advantage of the use of biomass as a filter medium is that the biomass after contamination in the fine filter 29 fed to the fuel storage 3 and thus can be recycled in the simplest way. An optimal time for the exchange of the filter media due to contamination can be determined by a pressure difference measurement, wherein a pressure drop across the fine filter 29 is measured. Alternatively, a purely time-dependent exchange of the filter media is possible. If the filter media are replaced time-dependent, replacement after approx. 100 operating hours is recommended.

权利要求:
Claims (24)
[1]
1. Reactor (1) for gasifying biomass, in particular wood, comprising a filling shaft (7) and an ash bed arranged below the filling shaft (7), characterized in that a device is provided with which at the filling shaft (7 ) adhering biomass is solvable and / or a heat exchanger is provided with which a generated from the biomass product gas gives off heat in the Füilschacht (7) tracked biomass and an oxidation air.
[2]
2. Reactor (1) according to claim 1, characterized in that a multiple jacket is provided, with which a heat of the product gas to the oxidation air and tracked biomass is transferable.
[3]
3. Reactor (1) according to claim 1 or 2, characterized in that a vibrator (8) is provided, with which the hopper (7) is set into vibration so that adhering biomass from the hopper (7) is releasable.
[4]
4. Reactor (1) according to one of claims 1 to 3, characterized in that a wedge slide is provided, with which the biomass to the hopper (7) can be fed.
[5]
5. Reactor (1) according to any one of claims 1 to 4, characterized in that a sealed feeding device is provided, with which the biomass is supplied to the filling shaft (7) with the exclusion of oxygen.
[6]
6. Reactor (1) according to one of claims 1 to 5, characterized in that the filling shaft (7) is tapered in a lower region (12), in particular with a ratio of Füllschachtquerschnittes to a Feuerzonenquerschnitt from 1.2 to 10th , preferably 1.4 to 3, more preferably about 1.9.
[7]
7. Reactor (1) according to one of claims 1 to 6, characterized in that an oxidation air supply (43) via an intermediate region and an oxidation air ring (15) with oxidation air nozzles (16) is connected, which open into a fire zone (13). • · 9 · · · 9 ·

· · * 19
[8]
8. Reactor (1) according to one of claims 1 to 7, characterized in that a rotary grate (18) is provided with at least one stirring pin on the ash bed, with the packaging of biomass are solvable.
[9]
9. Reactor (1) according to claim 8, characterized in that sensors are provided with which a pressure before and after the ash bed is measurable to use data obtained in a measurement to control and / or regulation of the stirring pins (19) ,
[10]
10. Device (2) for producing a product gas from biomass, comprising a fuel storage (3) for the biomass, a reactor (1) for gasifying the biomass, at least one conveying means (4) for conveying the biomass from the fuel storage (3) in the reactor (1) and at least one filter unit for purifying product gas produced from the biomass, characterized in that the reactor (1) is designed according to one of claims 1 to 9.
[11]
11. Device (2) according to claim 10, characterized in that at least one cyclone filter (27) is arranged downstream of the reactor (1).
[12]
12. Device (2) according to claim 10 or 11, characterized in that at least one fine filter (29) downstream of the reactor (1) containing biomass as a filter medium.
[13]
13. Device (2) according to one of claims 10 to 12, characterized in that an internal combustion engine (30) is provided, in which the product gas is conductive, and the internal combustion engine (30) to a generator (31) for generating electrical energy is coupled.
[14]
14. Device (2) according to claim 13, characterized in that a waste heat heat exchanger (32) is provided, with which a heat of an exhaust gas of the internal combustion engine (30) to the biomass for preheating the same is transferable.
[15]
15. Fine filter (29) for cleaning a product gas generated from biomass, characterized in that the filter medium contains biomass. • »•» * · • · »« · * • * ♦ · · 20
[16]
16. Use of a fine filter (29) according to claim 15 for cleaning a product gas generated from biomass, in particular for the deposition of tar.
[17]
17. A process for the gasification of biomass in a reactor (1), in particular a reactor (1) according to one of claims 1 to 9, to a product gas, characterized in that the filling shaft (7) adhering biomass dissolved and / or heat from the product gas is delivered to biomass and an oxidation air.
[18]
18. The method according to claim 17, characterized in that a shaking device (8) at certain intervals, preferably at intervals of 10 to 30 minutes, in particular 15 to 25 minutes, preferably about 20 minutes, for the duration of less than 5 minutes, preferably less than one minute, more preferably for about 5 seconds, is activated to dissolve biomass adhering to the hopper (7).
[19]
19. The method according to claim 17 or 18, characterized in that a flow velocity of the biomass in a lower region (12) of the hopper (7) via a conical design of the hopper (7) is kept approximately constant in this area.
[20]
20. The method according to any one of claims 17 to 19, characterized in that in a lowermost region (14) of the filling shaft (7), in particular in the region of a constriction (17), in more than 50%, in particular more than 70%, preferably more than 90%, the biomass is a temperature between 1000 ° C and 1600 ° C, in particular 1200 ° C and 1500 ° C, preferably 1220 ° C and 1470 ° C.
[21]
21. The method according to any one of claims 17 to 20, characterized in that a pressure drop over an ash bed continuously measured and when a predetermined limit is exceeded, a stirring device is activated in the ash bed.
[22]
22. The method according to any one of claims 17 to 21, characterized in that the oxidation air from the intermediate jacket via an oxidation air ring (15) to air nozzles in a lower region (12) of the hopper (7) flows, where an oxidation of biomass is caused. • * 21
[23]
23. The method according to any one of claims 17 to 22, characterized in that a product gas for driving an internal combustion engine (30) is used and with this a generator (31) is driven to generate electrical energy.
[24]
24. The method according to claim 23, characterized in that a heat of an exhaust gas of the internal combustion engine (30) is used for preheating the biomass.

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同族专利:

公开号 | 公开日

IN2014MN00256A|2015-09-25|

RU2014105490A|2015-08-20|

JP2014527095A|2014-10-09|

AU2012283719A1|2014-02-13|

EP2732011A1|2014-05-21|

US20140290593A1|2014-10-02|

CN103797095A|2014-05-14|

WO2013006877A1|2013-01-17|

ECSP14013210A|2014-03-31|

AT511684B1|2013-12-15|

BR112014000781A2|2017-03-01|

CA2841898A1|2013-01-17|

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法律状态:
2019-03-15| MM01| Lapse because of not paying annual fees|Effective date: 20180714 |

优先权:

申请号 | 申请日 | 专利标题

ATA1033/2011A|AT511684B1|2011-07-14|2011-07-14|DEVICE AND METHOD FOR GASIZING BIOMASS|ATA1033/2011A| AT511684B1|2011-07-14|2011-07-14|DEVICE AND METHOD FOR GASIZING BIOMASS|

CN201280045157.5A| CN103797095A|2011-07-14|2012-05-24|Device and method for gasifying biomass|

EP12730142.2A| EP2732011A1|2011-07-14|2012-05-24|Device and method for gasifying biomass|

BR112014000781A| BR112014000781A2|2011-07-14|2012-05-24|device and method for biomass gasification|

RU2014105490/05A| RU2014105490A|2011-07-14|2012-05-24|REACTOR AND METHOD FOR GASIFICATION OF BIOMASS, DEVICE FOR PRODUCING GAS FROM BIOMASS, FILTER FOR FINE CLEANING OF GAS PRODUCED FROM BIOMASS, AND METHOD FOR CLEANING THE NAME GAS|

CA2841898A| CA2841898A1|2011-07-14|2012-05-24|Device and method for gasifying biomass|

JP2014519339A| JP2014527095A|2011-07-14|2012-05-24|Device and method for vaporizing biomass|

PCT/AT2012/050074| WO2013006877A1|2011-07-14|2012-05-24|Device and method for gasifying biomass|

AU2012283719A| AU2012283719A1|2011-07-14|2012-05-24|Device and method for gasifying biomass|

US14/232,468| US20140290593A1|2011-07-14|2012-05-24|Device and method for gasifying biomass|

IN256MUN2014| IN2014MN00256A|2011-07-14|2014-02-07|

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