EP4359654B1 - Mikro-kogenerator - Google Patents

Mikro-kogenerator Download PDF

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Publication number
EP4359654B1
EP4359654B1 EP22741849.8A EP22741849A EP4359654B1 EP 4359654 B1 EP4359654 B1 EP 4359654B1 EP 22741849 A EP22741849 A EP 22741849A EP 4359654 B1 EP4359654 B1 EP 4359654B1
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Prior art keywords
reaction chamber
cogenerator
micro
syngas
burner
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English (en)
French (fr)
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EP4359654A1 (de
EP4359654C0 (de
Inventor
Fabio Pellegrini
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Kira Technology Srl
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Kira Technology Srl
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01N—GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR MACHINES OR ENGINES IN GENERAL; GAS-FLOW SILENCERS OR EXHAUST APPARATUS FOR INTERNAL-COMBUSTION ENGINES
    • F01N5/00—Exhaust or silencing apparatus combined or associated with devices profiting by exhaust energy
    • F01N5/02—Exhaust or silencing apparatus combined or associated with devices profiting by exhaust energy the devices using heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23B—METHODS OR APPARATUS FOR COMBUSTION USING ONLY SOLID FUEL
    • F23B90/00—Combustion methods not related to a particular type of apparatus
    • F23B90/04—Combustion methods not related to a particular type of apparatus including secondary combustion
    • F23B90/06—Combustion methods not related to a particular type of apparatus including secondary combustion the primary combustion being a gasification or pyrolysis in a reductive atmosphere
    • 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
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • 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
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/10—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating electric
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02G—HOT GAS OR COMBUSTION-PRODUCT POSITIVE-DISPLACEMENT ENGINE PLANTS; USE OF WASTE HEAT OF COMBUSTION ENGINES; NOT OTHERWISE PROVIDED FOR
    • F02G2243/00—Stirling type engines having closed regenerative thermodynamic cycles with flow controlled by volume changes
    • 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
    • F23G2206/20—Waste heat recuperation using the heat in association with another installation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/50204—Waste pre-treatment by pyrolysis, gasification or cracking
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/10—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of field or garden waste or biomasses
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23N—REGULATING OR CONTROLLING COMBUSTION
    • F23N2227/00—Ignition or checking
    • F23N2227/02—Starting or ignition cycles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23N—REGULATING OR CONTROLLING COMBUSTION
    • F23N2227/00—Ignition or checking
    • F23N2227/12—Burner simulation or checking

Definitions

  • Biomass-fueled cogeneration systems consisting of three basic parts, i.e. a pyrolytic gasifier, a burner, and a Stirling engine, are well known.
  • the fuel syngas is produced starting from the biomass in the pyrolytic gasifier; the syngas produced is burned with a controlled supply of air in the burner; the Stirling engine, by virtue of the heat generated by the combustion of the syngas, sets the electric generator in oscillation, thus producing electrical energy.
  • Pyrolytic gasification is a thermal-chemical process by virtue of which a combustible gas (syngas), comprising a mixture of hydrogen, carbon monoxide, methane and, to a lesser extent, other compounds, can be extracted from organic material, such as biomass.
  • Syngas combustible gas
  • Pyrolytic gasification occurs by maintaining the biomass at a particularly high temperature in a low-oxygen environment.
  • the by-product of pyrolytic gasification is a solid residue, named char, which contains almost exclusively carbon.
  • pyrolytic gasification compared with direct combustion of the biomass, reduces carbon emissions into the atmosphere because, once the fuel syngas is extracted, only the char remains which contains the portion of carbon that will not be emitted into the atmosphere in the form of CO 2 , but is evacuated in solid form and collected. Furthermore, the use of pyrolytic gasification provides a fuel gas which is much more effective in the combustion in terms of maximum achievable temperature, emissions of particulate matter and heating of the heat exchangers.
  • WO 2015/018742 discloses an apparatus for generating energy by gasification.
  • CN 109 424 964 discloses a horizontal double-layer tube rotary superconducting waste pyrolysis gasifier.
  • the pyrolytic gasifier contains a reaction chamber inside which the biomass is gasified in the presence of a given amount of air, generating syngas.
  • the atmosphere inside said reaction chamber during its operation is strongly reducing, because, since it is rich in hydrogen, carbon monoxide and methane, it has a strong tendency to react with oxygen.
  • the refractory materials do not show the same heat resistance they would have in a neutral or oxidizing environment, but rather their classification temperature undergoes a significant reduction. As a consequence, said materials rapidly tend to degrade chemically.
  • the technical problem underlying the present invention is to provide a micro-cogenerator for domestic or small consumer use, in which the pyrolytic gasifier can ensure high performance characteristics and meet the requirements presented above.
  • micro-cogenerator as outlined in the accompanying claims, the definitions of which form an integral part of the present description.
  • the object of the present invention is a micro-cogenerator comprising:
  • biomass should by no means be understood as limiting.
  • said energy source is gasified in the presence of a sub-stoichiometric amount of air.
  • said polycrystalline alumina fiber-based material comprises at least 75% by weight of polycrystalline alumina, preferably at least 80% by weight, such as about 90% by weight.
  • said polycrystalline alumina fiber-based material further comprises an amount of silica of at least 5% by weight, preferably between 10% and 30% by weight, more preferably between 10% and 25% by weight, even more preferably between 10% and 20% by weight.
  • said polycrystalline alumina fiber-based material is produced by the company Unifrax under the trade name High Temperature Saffil ® Rigiform TM .
  • said material is produced by the company Unifrax under the trade name Saffil ® 160 HD.
  • said pyrolytic gasifier comprises an outer coating with respect to said reaction chamber, said outer coating having an annular shape.
  • the aforesaid outer coating having an annular shape consists of a plurality of superimposed rings made of said microporous insulating material.
  • the pyrolytic gasifier comprises a layer of said polycrystalline alumina fiber-based material having varying thickness interposed between said reaction chamber and said outer coating.
  • said reaction chamber and said layer of polycrystalline alumina fiber-based material form a monolithic structure.
  • said truncated-cone reaction chamber has an upper surface and a lower surface, wherein the diameter of the upper surface is smaller than the diameter of the lower surface, said diameters being such as to give the inner surface of the truncated-cone reaction chamber a draft angle comprised between 2° and 15°, preferably comprised between 2° and 10°, preferably of about 4°.
  • the pyrolytic gasifier comprises:
  • said hopper comprises an upper frame (or edge) adapted to support the aforesaid outer coating, preferably through an appropriate support plate.
  • said hopper comprises a lip, which projects below said frame and defines a support base for the reaction chamber through which the hopper receives the syngas produced.
  • the reaction chamber comprises an electric heater adapted to heat the reaction chamber to the gasification temperature, and a thermocouple adapted to monitor the temperature in the upper part of the reaction chamber.
  • the reaction front is comprised between said heater and said thermocouple.
  • the aforesaid heater integrates a special sensor inside it, e.g., a thermocouple.
  • the energy source under reaction is supported by the biochar produced during the gasification of said energy source, and the micro-cogenerator does not comprise any support grid for said energy source.
  • the micro-cogenerator object of the present invention comprises an exhaust system adapted to receive exhaust fumes exiting the hot exchanger of the Stirling engine.
  • Said exhaust system comprises an exchanger for the recovery of heat from said exhaust fumes, a lambda probe and a thermocouple which measures the temperature of said exhaust fumes.
  • Said lambda probe regulates the air-to-syngas ratio at the burner inlet; more in particular, it provides a signal based on which said air-to-syngas ratio is adjusted.
  • the micro-cogenerator object of the present invention further comprises an extraction fan connected to said exchanger for the recovery of heat from the exhaust fumes, such as to extract the exhaust fumes thus creating a vacuum inside the burner and the pyrolytic gasifier and, in turn, to adjust the inflow of the syngas from the pyrolytic gasifier to the burner and the inflows of air into both the pyrolytic gasifier and the burner.
  • the combustion air inflow to the burner is advantageously adjusted by means of an electronically-driven motorized valve.
  • a valve is driven based on the signal provided by the lambda probe, i.e., based on the information provided by the lambda probe about the amount of air present in the exhaust fumes.
  • the need to carefully control the amount of air is related to the fact that performance and emissions (CO, NO x ) are strongly affected by the fuel/combustion air ratio; an optimal ratio of combustion air to syngas can be maintained by virtue of the signal provided by the lambda probe.
  • the position of the valve which regulates the combustion air supply is preferably calculated by a PID (Proportional Integrative Derivative) control, which takes as input the value read by the lambda probe and outputs the position of the air adjustment valve.
  • PID Proportional Integrative Derivative
  • the lambda probe provides an electrical signal (in mV) through which it is possible to have a measurement of the "lambda value ( ⁇ )" properly so called, i.e., the ratio between the actual AFR ( air-fuel-ratio ) and the stoichiometric AFR ( air-fuel-ratio ); in other words, the "lambda value ( ⁇ )" properly so called is to be understood as the ratio of air to fuel relative to the stoichiometric ratio of the fuel used.
  • the electrical signal provided by the lambda probe is an indirect measurement of said lambda value ( ⁇ ); the higher the value of the electrical signal, the lower the lambda value ( ⁇ ).
  • the pyrolytic gasifier comprises a first butterfly valve at the input interface of the energy source into the reaction chamber such as to allow the inflow of the energy source into the chamber and the hermetic closure thereof during the shutdown phase.
  • the pyrolytic gasifier further comprises a second butterfly valve at the output interface of the biochar from the unloading auger such as to allow the evacuation of the biochar from the reaction chamber, if necessary.
  • the pyrolytic gasifier according to the present invention thanks to the peculiar characteristics mentioned above, both with regard to its structure and the materials with which it is made, can ensure high performance characteristics and remarkable durability, by virtue of a surprising chemical and mechanical resistance in a strongly reducing environment which reaches temperatures of approximately 1200-1400°C. Furthermore, the pyrolytic gasifier according to the present invention has compact dimensions, provides high thermal insulation and high resistance to thermal shock, and allows a good flow of the biomass inside it.
  • a micro-cogenerator according to an embodiment of the present invention is globally indicated with reference numeral 1.
  • Said micro-cogenerator 1 comprises a pyrolytic gasifier 2, a burner 3 and a Stirling engine 4.
  • the pyrolytic gasifier 2 is shown in more detail in Figure 2 , while the burner 3 and the Stirling engine 4 are more visible in Figures 6-10 .
  • the gasifier 2 in Figure 2 comprises:
  • the reactor 7 defines a reaction chamber 17 and comprises an electric heater 18 and a thermocouple 19.
  • the electric heater 18 brings the biomass contained in the reaction chamber 17 to the gasification temperature of, e.g., 900°C, while the thermocouple 19 monitors the temperature in the upper part of the reaction chamber 17 during the gasification process.
  • the heater 18 and the thermocouple 19, respectively, represent the lower limit and the upper limit of the zone within which the biomass reaction front 6 must be maintained.
  • a connecting element 20, named “buffer”, is interposed between the loading auger 10 of the biomass 6 and the inlet 11 of the reactor 7.
  • a sensor 21 detects the filling level of the buffer 20, and the loading auger 10 of the biomass 6 is started whenever said sensor 21 detects that the filling level of the buffer 20 is below a predetermined threshold value.
  • the biomass 6 under reaction is supported by the biochar 9 generated during the pyrolytic gasification process seamlessly inside the reaction chamber 17.
  • the pyrolytic gasifier 2 according to the present invention has no support grid for the biomass under reaction which separates it from the spent biochar 9.
  • the unloading auger 12 and the hopper 14 are constantly kept full of biochar 9.
  • the reactor 7 of the pyrolytic gasifier 2 is shown in greater detail in Figure 3 .
  • the reactor 7 comprises a reaction chamber 17 in which the biomass 6 is gasified in the presence of a given amount of air (sub-stoichiometric).
  • the reactor 7 further comprises an outer coating 71 to said reaction chamber 17.
  • Said reaction chamber 17 is truncated-cone in shape and is advantageously made of a polycrystalline alumina fiber-based material, preferably formed under vacuum, comprising at least 70% by weight of polycrystalline alumina and having a density preferably between 350 and 500 kg/m 3 .
  • said polycrystalline alumina fiber-based material is produced by the company Unifrax under the trade name High Temperature Saffil ® Rigiform TM , e.g. Saffil ® 160 HD.
  • the reaction chamber 17 has an upper surface 72 and a lower surface 73, wherein the diameter of the upper surface 72 is slightly smaller than the diameter of the lower surface 73 in order to give an adequate draft angle, e.g., about 4°, to the inner surface of the reaction chamber 17.
  • the diameter of the upper surface 72 is comprised between 70 and 90 mm and the diameter of the lower surface 73 is comprised between 100 and 120 mm. Said geometry of the reaction chamber 17 facilitates the downward flow of the biomass 6.
  • Said outer coating 71 has an annular shape and is advantageously made of a microporous insulating material comprising silica.
  • said microporous insulating material is produced by the company Promat under the trade name Promalight ® , or by the company Bifire under the trade name Microbifire ® , or by the company Unifrax under the trade name Excelfrax ® .
  • Said outer coating 71 consists of a plurality of overlapping rings 74 made of said microporous insulating material, which guarantee the thermal insulation of the reactor 7.
  • the reactor 7 further comprises a layer 75 of said polycrystalline alumina fiber-based material having varying thickness interposed between the reaction chamber 17 and the outer coating 71.
  • the reaction chamber 17 and the layer 75 of the polycrystalline alumina fiber-based material form a monolithic structure.
  • said monolithic structure is sealed on top with the structure by means of a rubber gasket 76; on the bottom, instead, given the high working temperature, it is sealed by means of a polycrystalline alumina fiber-based gasket 77.
  • the hopper 14 shown in Figures 2 and 3 comprises an upper frame (or edge) 78 adapted to support the outer coating 71 through an appropriate support plate 79, preferably annular.
  • an insulating plate 80 which is also preferably annular, made, e.g., with biosoluble refractory fibers, is placed above said support plate 79; said plate 80 ensures the thermal break with the support plate 79 and thus with the hopper 14, as well as an airtight seal.
  • Both the hopper 14 and the support plate 79 are advantageously made of stainless steel.
  • Said hopper 14 further comprises a lip 81, which projects below said frame 78 and defines a support base for the reaction chamber 17 through which the hopper 14 itself receives the produced syngas 8.
  • Said geometry allows creating an annular volume in the upper part of the hopper 14 through which the syngas 8 is sucked into the duct 13.
  • the syngas feeding duct 13 has a gasket at the interface with the support plate 79 consisting of polycrystalline alumina fiber-based rings 82.
  • the hopper 14 is advantageously insulated from the unloading auger 12 by means of an element 83 made of said microporous insulating material.
  • a first valve 22 separating the biomass 6 (shown in Figures 2 and 3 ) is placed at the inlet interface of the biomass 6 in the reactor 7, in particular above the buffer 20.
  • a second valve 23 separating the biochar 9 (shown in Figure 2 ) is positioned at the outlet interface of the biochar 9 from the unloading auger 12.
  • the separation valve 22 of the biomass 6 is opened at the process start-up and allows the inflow of biomass 6 and air into the reactor 7.
  • the air supply although limited, is necessary to support the gasification process by providing heat through the combustion of a small portion of the biomass 6 and the produced syngas 8.
  • the valve 22, 23 according to the embodiment of Figure 4 comprises an actuator 24, a cylindrical valve body 25, a plate-like shutter 26 and an insert 27 shaped as an arc of circumference.
  • the gasifier 2 is of the “downdraft” (i.e., the biomass 6 flows downward and the syngas 8 produced transits in the same direction) "open core” (i.e., with air supply from above along with the biomass) type.
  • Figures 6-10 illustrate the assembly consisting of the burner 3 and the Stirling engine 4.
  • the burner 3 comprises:
  • pre-mixing flanges 35 allow partial cooling of the fuel syngas 8 by means of the combustion air 31.
  • the Stirling engine 4 comprises a high-temperature heat exchanger 38 (so-called “hot exchanger") shown in Figures 7, 8 , 10 , a low-temperature heat exchanger (so-called “cold exchanger”), a regenerator and an electric generator 39.
  • the cold exchanger and the regenerator are not visible in the figures.
  • the hot exchanger 38 of the Stirling engine is inserted inside the combustion chamber 30.
  • a tubular element 40 Downstream of the hot exchanger 38 of the Stirling engine, a tubular element 40 is placed, also indicated as a cooling ring, inside which a cooling fluid flows, so that heat transfer downstream of said hot exchanger 38 is prevented.
  • the cooling ring 40 performs the thermal break function between the burner 3 and the Stirling engine 4, preventing unwanted heat from entering the part of the Stirling engine 4 under the hot exchanger 38 and safeguarding the underlying components from excessive heating.
  • the combustion chamber 30 of the burner 3 consists of a cylinder which integrates connections for the feeding duct 13 of the fuel syngas 8 coming from the gasifier 2 and for the feeding duct 41 of the combustion air 31. Furthermore, the combustion chamber 30 integrates the attachment flange 42 to the Stirling engine 4 and the attachment flange 43 to the exhaust system 33.
  • a bell 44 and an element 45 made of porous ceramic material are placed inside the combustion chamber 30 of the burner 3.
  • Said bell 44 is open at the bottom and houses the hot exchanger 38 of the Stirling engine inside.
  • said hot exchanger 38 is inserted from the open bottom of the bell 44.
  • Said bell 44 is such to convey the hot combustion gases 32 into the hot exchanger 38, where they undergo heat exchange providing heat and generating exhaust fumes 34 (or combustion fumes 34).
  • said bell 44 constrains the hot combustion gases 32 to flow through the entire hot exchanger 38 with minimal heat dissipation to the outside, thus optimizing the heat exchange with the Stirling engine 4.
  • Said bell 44 comprises steel walls internally lined with a refractory insulating material, preferably a material based on polycrystalline alumina fiber.
  • said material comprises at least 70% by weight of polycrystalline alumina, preferably at least 75% by weight, more preferably at least 80% by weight, such as about 90% by weight.
  • said material further comprises at least 5% by weight of silica, preferably between 10% and 30% by weight of silica, more preferably between 10% and 25% by weight of silica, even more preferably between 10% and 20% by weight of silica.
  • said polycrystalline alumina fiber-based material is produced by the company Schupp under the trade name ITM-Fibermax ® , preferably Blanket 1600-130.
  • the aforementioned nozzle or duct 36 may be replaced by a hole made in said refractory insulating material, such as to convey the fuel syngas 8 and the combustion air 31 inside the combustion chamber 30.
  • the porous ceramic means 45 is housed in the upper part of the bell 44 above the hot exchanger 38 and is supported at least partially by the refractory insulating material of the bell 44. Said porous ceramic means 45 is an optimized combustion volume in which the syngas 8 is combusted in the presence of combustion air 31 generating hot combustion gases 32 ( Figure 8 ). Furthermore, the porous means 45 allows a homogeneous temperature distribution, ensuring optimal heat exchange with the Stirling engine 4 and low polluting emissions.
  • the porous material with which said means 45 is made comprises silicon carbide, alumina and silica and is, for example, produced by the company Lanik under the trade name Vukopor ® S.
  • said porous ceramic material comprises alumina, silica, zirconia and magnesium oxide.
  • said porous ceramic material is produced by the company Lanik under the trade name Vukopor ® HT.
  • the bell 44 comprises an additional element 47 made of refractory insulating material, e.g., based on polycrystalline alumina fiber, immediately below the porous ceramic means 45, such as to prevent unwanted entry of heat through the top of the Stirling engine below.
  • Said element 47 mimics the shape of the upper dome of the hot exchanger 38 of the Stirling engine, visible in Figures 7, 8 , 10 .
  • the exhaust system 33 mentioned above receives the combustion fumes 34 exiting the hot exchanger 38 of the Stirling engine 4, once the latter have traveled upward through the gap 46 present between the combustion chamber 30 and the bell 44.
  • Said exhaust system 33 comprises an exhaust 55 from which combustion fumes 34 escape, a heat exchanger 56 connected to said exhaust 55 for recovering heat from the exhaust fumes 34 ( Figure 10 ), a lambda probe 57 which provides a signal based on which the air-syngas ratio at the inlet of burner 3 is adjusted ( Figures 6 , 10 ), and a thermocouple 58 which measures the temperature of the combustion fumes 34 ( Figures 6 , 10 ).
  • An extraction fan 59 (shown in Figures 6 and 10 ) of the combustion fumes 34 is connected to said heat exchanger 56, by virtue of which the combustible syngas 8 from the gasifier 2 and the combustion air 31 are sucked inside the combustion chamber 30.
  • Said extraction fan 59 has variable speed.
  • the micro-cogenerator 1 can advantageously be coupled to electrical energy storage systems (batteries) and thermal energy accumulation systems (puffers). The remaining capacity is measured for both accumulations so that micro-cogenerator 1 will only turn on if a minimum operating time necessary for heat regulation of all syngas ducts is guaranteed.
  • a temperature probe is used for the puffer, and a voltage probe is used for the batteries.
  • SoC state of charge
  • the micro-generator 1 is equipped with an electronic control, which manages the operation of the machine through the installed sensors and actuators and is independently powered by on-board batteries so that it can be safely shut down even in case the external electrical connection is interrupted. To be able to start up, the micro-generator 1 checks for the presence of the external power grid (both "on-grid” and “off-grid” via inverter).
  • the pyrolytic gasification process is started by means of the electric heater 18, which brings the biomass 6 to the gasification temperature, e.g., about 900°C.
  • the separation valve 22 of the biomass 6 is opened.
  • the extraction fan 59 is activated with a speed proportional to the temperature of the electric heater 18.
  • the biomass 6 is fed into the reactor 7 of the pyrolytic gasifier 2, through the inlet 11, by means of the loading auger 10.
  • the biomass loading auger 10 is started; when the filling level of the buffer 20 is above said threshold, the biomass loading auger 10 is stopped and the feeding of the biomass 6 to the reactor is interrupted.
  • reaction front advances from the bottom to the top where biomass 6 not yet gasified is located.
  • the reaction chamber 17 is maintained at a suitable gasification temperature at which the biomass reacts generating syngas and biochar, preferably comprised between 1000°C and 1200°C in order to maximize the syngas production.
  • thermocouple 19 keeps the temperature of the upper part of the reaction chamber 17 monitored; when the integral over time of the temperature measured by thermocouple 19 exceeds a given threshold value of said integral, the separation valve 23 of the biochar 9 is opened, the unloading auger 12 is started and part of the biochar 9 is extracted. In this manner, the reacting biomass 6 is made to flow downward and along with it the reaction front as well, which remains confined to the reaction zone delimited between the thermocouple 19 and the electric heater 18.
  • the gasifier 2 once fully operational, works with a slow and intermittent flow of biomass 6 such as to maintain the reaction front within the aforementioned reaction zone.
  • the extraction fan 59 By operating the extraction fan 59, the system consisting of the gasifier 2 and the burner 3 is depressurized and the inflows of fuel syngas 8 from the gasifier 2 to the burner 3 and of air to both the gasifier 2 and the burner 3 are adjusted.
  • the extraction fan 59 By operating the extraction fan 59, the combustion fumes 34 are extracted which travel upward through the gap 46 between the combustion chamber 30 and the bell 44, creating a vacuum inside the burner 3. In turn, the fuel syngas 8 exiting the gasifier 2 and the combustion air 31 are sucked into the combustion chamber 30 of the burner, respectively, through the supply ducts 13 and 41. In turn, air is sucked into the gasifier 2.
  • the fuel syngas 8 and the combustion air 31 are sucked inside the combustion chamber 30 passing through the pre-mixing flanges 35, then the nozzle or duct 36, until they arrive inside the porous ceramic means 45, which defines the volume in which the combustion takes place with the generation of the hot combustion gases 32.
  • the hot combustion gases 32 are subjected to heat exchange within the hot exchanger 38 of the Stirling engine 4, from which heat is recovered that puts the electric generator 39 in oscillation, thus obtaining the aforementioned combustion fumes 34 resulting from said heat exchange.
  • the combustion fumes 34 are extracted through the extraction fan 59. Said combustion fumes 34 travel upward through the gap 46 present between the combustion chamber 30 and the bell 44, pass through the exhaust 55 on which the lambda probe 57 and the thermocouple 58 are placed, then they are fed to the heat exchanger 56 for recovery of the heat contained therein.
  • the lambda probe 57 provides a signal based on which the air-syngas ratio is adjusted accurately by virtue of the valve 60 located on the inlet duct 41 of the combustion air 31, adjusting the pressure drop and thus the inflow.

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  • General Engineering & Computer Science (AREA)
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Claims (9)

  1. Mikro-Blockheizkraftwerk (1), umfassend:
    einen pyrolytischen Vergaser (2), welcher dazu eingerichtet ist, aus einer erneuerbaren und nachhaltigen Energiequelle (6), vorzugsweise holzartiger Biomasse, Synthesegas (8) und Biokohle (9) zu erzeugen,
    einen Brenner (3), welcher dazu eingerichtet ist, das durch den pyrolytischen Vergaser (2) erzeugte Synthesegas (8) aufzunehmen und heiße Verbrennungsgase (32) zu generieren,
    einen Stirlingmotor (4), welcher einen mit den heißen Verbrennungsgasen (32) gespeisten Wärmetauscher (38) umfasst, wobei der Stirlingmotor (4) dazu eingerichtet ist, elektrische Energie zu generieren,
    wobei der pyrolytische Vergaser (2) eine Reaktionskammer (17) umfasst, innerhalb welcher die Energiequelle (6) in der Gegenwart von Luft vergast wird, wodurch Synthesegas (8) und Biokohle (9) generiert wird,
    dadurch gekennzeichnet, dass
    die Reaktionskammer (17) eine Kegelstumpfform aufweist und aus einem polykristallinen Material auf Aluminiumoxidfaserbasis hergestellt ist, welches wenigstens 70 Gew.-% polykristallines Aluminiumoxid und, optional, wenigstens 5 Gew.-% Siliciumdioxid umfasst, wobei das Material eine Dichte von vorzugsweise zwischen 350 und 500 kg/m3 aufweist
    wobei das Mikro-Blockheizkraftwerk ein Abgassystem (33) umfasst, welches dazu eingerichtet ist, Abgase (34) aufzunehmen, welche den Wärmetauscher (38) des Stirlingmotors (4) verlassen,
    wobei das Abgassystem (33) einen Tauscher (56) für die Rückgewinnung von Wärme aus den Abgasen (34), eine Lambdasonde (57), welche ein Signal bereitstellt, auf Grundlage dessen das Verhältnis von Luft (31) zu Synthesegas (8) an dem Brenner- (3) -Einlass eingestellt wird, und ein Thermoelement (58) umfasst, welches die Temperatur der Abgase (34) misst,
    wobei das Mikro-Blockheizkraftwerk ferner einen mit dem Tauscher (56) verbundenen Absaugventilator (59) für die Rückgewinnung von Wärme aus den Abgasen (34) umfasst, wobei der Absaugventilator (59) dazu eingerichtet ist, die Abgase (34) zu extrahieren, wodurch ein Vakuum innerhalb des Brenners (3) und des pyrolytischen Vergasers (2) geschaffen wird, und wiederum den Zustrom des Synthesegases (8) von dem pyrolytischen Vergaser (2) zu dem Brenner (3) und die Zuströme von Luft in sowohl den pyrolytischen Vergaser (2) als auch den Brenner (3) einzustellen.
  2. Mikro-Blockheizkraftwerk (1) nach Anspruch 1, wobei das polykristalline Material auf Aluminiumoxidfaserbasis wenigstens 75 Gew.-% polykristallines Aluminiumoxid, vorzugsweise wenigstens 80 Gew.-%, bevorzugter etwa 90 Gew.-%, und eine Menge an Siliciumdioxid von wenigstens 5 Gew.-%, vorzugsweise zwischen 10 Gew.-% und 30 Gew.-%, bevorzugter zwischen 10 Gew.-% und 25 Gew.-%, noch bevorzugter zwischen 10 Gew.-% und 20 Gew.-%, umfasst.
  3. Mikro-Blockheizkraftwerk (1) nach Anspruch 1 oder 2, wobei der pyrolytische Vergaser (2) eine in Bezug auf die Reaktionskammer (17) äußere Ummantelung (71) umfasst, wobei die äußere Ummantelung (71) eine ringförmige Form aufweist und vorzugsweise aus einem mikroporösen isolierendem Material hergestellt ist, welches Siliciumdioxid umfasst.
  4. Mikro-Blockheizkraftwerk (1) nach Anspruch 3, wobei der pyrolytische Vergaser (2) eine Schicht (75) aus dem polykristallinen Material auf Aluminiumoxidfaserbasis umfasst, welche eine variable Dicke aufweist und zwischen der Reaktionskammer (17) und der äußeren Ummantelung (71) eingefügt ist, vorzugsweise wobei die Reaktionskammer (17) und die Schicht (75) aus polykristallinem Material auf Aluminiumoxidfaserbasis eine monolithische Struktur bilden.
  5. Mikro-Blockheizkraftwerk (1) nach einem der vorhergehenden Ansprüche, wobei die Kegelstumpf-Reaktionskammer (17) eine obere Fläche (72) und eine untere Fläche (73) aufweist, wobei der Durchmesser der oberen Fläche (72) kleiner ist als der Durchmesser der unteren Fläche (73), wobei die Durchmesser derart beschaffen sind, dass sie der inneren Fläche der Kegelstumpf-Reaktionskammer einen Verjüngungswinkel verleihen, welcher zwischen 2° und 15° umfasst ist, vorzugsweise etwa 4° beträgt.
  6. Mikro-Blockheizkraftwerk (1) nach einem der vorhergehenden Ansprüche, wobei der pyrolytische Vergaser (2) umfasst:
    einen Schneckenförderer (12) für die Abförderung der Biokohle (9),
    einen Trichter (14), welcher die Reaktionskammer und den Schneckenförderer (12) verbindet, wobei der Trichter (14) ein Sammelvolumen für das in der Reaktionskammer erzeugte Synthesegas (8) bildet, und
    ein Verbindungsrohr (13) zwischen dem Trichter (14) und dem Brenner (3), aus welchem das Synthesegas (8) gesaugt wird und dem Brenner (3) zugeführt wird,
    wobei der Trichter (14) einen oberen Rahmen (78), welcher dazu eingerichtet ist, die äußere Ummantelung (71) zu tragen, vorzugsweise durch eine geeignete Trägerplatte (79), und eine Lippe (81) umfasst, welche unterhalb des Rahmens (78) vorsteht und eine Trägerbasis für die Reaktionskammer (17) definiert, durch welche der Trichter (14) das erzeugte Synthesegas (8) aufnimmt.
  7. Mikro-Blockheizkraftwerk (1) nach einem der vorhergehenden Ansprüche, wobei die Reaktionskammer (17) einen elektrischen Heizer (18), welcher dazu eingerichtet ist, die Reaktionskammer (17) auf die Vergasungstemperatur zu erwärmen, und ein Thermoelement (19) umfasst, welches dazu eingerichtet ist, die Temperatur in dem oberen Teil der Reaktionskammer (17) zu überwachen,
    wobei die Reaktionsfront zwischen dem Heizer (18) und dem Thermoelement (19) umfasst ist.
  8. Mikro-Blockheizkraftwerk (1) nach einem der vorhergehenden Ansprüche, wobei die einer Reaktion unterliegende Energiequelle (6) durch die während der Vergasung der Energiequelle (6) erzeugte Biokohle (9) unterstützt wird, wobei das Mikro-Blockheizkraftwerk (1) kein Unterstützungsnetz für die Energiequelle (6) umfasst.
  9. Mikro-Blockheizkraftwerk (1) nach einem der vorhergehenden Ansprüche, wobei der pyrolytische Vergaser (2) ein erstes Drosselventil (22) an der Eingangsschnittstelle der Energiequelle (6) in der Reaktionskammer, um den Zustrom der Energiequelle (6) in die Reaktionskammer (17) zu ermöglichen, und/oder ein zweites Drosselventil (23) an der Ausgangsschnittstelle der Biokohle (9) aus dem Schneckenförderer (12) umfasst, um die Abförderung der Biokohle (9) aus der Reaktionskammer (17) zu ermöglichen, falls erforderlich, wobei die Drosselventile (22, 23) einen zylindrischen Ventilkörper (25), einen Plattenverschluss (26) und einen Einsatz (27) umfassen, welcher die Form eines Umfangsbogens aufweist,
    wobei, wenn sich das Ventil (22, 23) in der vollständig offenen Position befindet, der Verschluss (26) eine zu der longitudinalen Achse (X-X) des zylindrischen Ventilkörpers (25) parallele Position einnimmt,
    wobei der Einsatz (27) an einem Abschnitt (28) des Rands des Verschlusses (26) anhaftet, wenn sich das Ventil (22, 23) in der vollständig offenen Position befindet, wodurch der Raum zwischen dem Ventilkörper (25) und dem Verschluss (26) entlang der longitudinalen Achse (X-X) des zylindrischen Ventilkörpers (25) gefüllt wird und verhindert wird, dass sich die Energiequelle (6) oder die Biokohle (9) an dem Rand des Verschlusses (26) absetzen.
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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ITFI20000150A1 (it) * 2000-07-03 2002-01-03 Edelberto Pagliai Applicazione del processo di gassificazione endotermico su combustibili liquidi tramite h2o e/o h2o2 per la realizzazione di gas combustibil
US20090078176A1 (en) * 2006-01-11 2009-03-26 Eckhart Weber Wood-Pellet Cogeneration Unit With Stirling Engine in Condensing Technology
CN208382164U (zh) * 2017-08-29 2019-01-15 西安美润环保工程技术有限公司 双锥体回转式超导垃圾裂解炉
CN109424963A (zh) * 2017-08-29 2019-03-05 西安美润环保工程技术有限公司 双锥体回转式超导垃圾裂解炉
CN111690436A (zh) * 2019-03-14 2020-09-22 陕西博瑞新环保科技有限公司 高效安全垃圾裂解气化炉
WO2021004658A1 (en) * 2019-07-09 2021-01-14 Cmd Costruzioni Motori Diesel An improved reactor for the gasification of wood-cellulose residual materials

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7906695B2 (en) * 2004-10-25 2011-03-15 Res/Op Technologies Inc. Biomass conversion by combustion
ITMO20130235A1 (it) * 2013-08-08 2015-02-09 Marco Errani Impianto per la produzione di energia mediante gassificazione.
CN109424964A (zh) * 2017-08-29 2019-03-05 西安美润环保工程技术有限公司 卧式双层管旋转式超导垃圾裂解气化炉

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
ITFI20000150A1 (it) * 2000-07-03 2002-01-03 Edelberto Pagliai Applicazione del processo di gassificazione endotermico su combustibili liquidi tramite h2o e/o h2o2 per la realizzazione di gas combustibil
US20090078176A1 (en) * 2006-01-11 2009-03-26 Eckhart Weber Wood-Pellet Cogeneration Unit With Stirling Engine in Condensing Technology
CN208382164U (zh) * 2017-08-29 2019-01-15 西安美润环保工程技术有限公司 双锥体回转式超导垃圾裂解炉
CN109424963A (zh) * 2017-08-29 2019-03-05 西安美润环保工程技术有限公司 双锥体回转式超导垃圾裂解炉
CN111690436A (zh) * 2019-03-14 2020-09-22 陕西博瑞新环保科技有限公司 高效安全垃圾裂解气化炉
WO2021004658A1 (en) * 2019-07-09 2021-01-14 Cmd Costruzioni Motori Diesel An improved reactor for the gasification of wood-cellulose residual materials

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