• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Method and plant for the production of biochar, in which in retorts (1) located biogenic starting material (2) is pyrolyzed and the resulting by the pyrolysis combustible pyrolysis gases are burned to produce hot flue gases, wherein the retorts (1) temporally successive in at least one Reactor chamber (31, 31a, 31b, 31c) are introduced and are carried out by means of the flue gases in these the pyrolysis. The retorts (1) are at least largely closed to the entry of hot flue gases and the heating of the starting materials (2) located in the retorts (1) by means of the flue gases by heating the retorts (1) only indirectly.
    公开号:AT519020A4
    申请号:T438/2016
    申请日:2016-09-26
    公开日:2018-03-15
    发明作者:Schirnhofer Leo；Ing Holger Knautz Dipl
    申请人:Schirnhofer Leo；
    IPC主号:
    专利说明:

    SUMMARY
    Process and plant for the production of biochar, in which biogenic starting material (2) located in retorts (1) is pyrolysed and the combustible pyrolysis gases produced by the pyrolysis are burned to produce hot flue gases, the retorts (1) being successively divided into at least one Reactor chamber (31, 31a, 31b, 31c) are introduced and the pyrolysis is carried out in these by means of the flue gases. The retorts (1) are at least largely closed off from the entry of hot flue gases and the starting materials (2) located in the retorts (1) are only heated indirectly by means of the flue gases by heating the retorts (1).
    (FIG.1)
    1.30
    The subject invention relates to a method and a plant for the production of biochar, in which biogenic starting material located in retorts is pyrolyzed and the combustible pyrolysis gases produced by the pyrolysis are burned to produce hot flue gases, the retorts being introduced in succession in reactor chambers and by means of the flue gases the pyrolysis is carried out.
    Pyrolysis is a thermal conversion process in which pyrolysis gases and biochar are formed from organic raw materials in the absence of oxygen. The temperatures at which the starting materials pyrolyze are between 250 ° C and 900 ° C. The duration of a pyrolysis is between a few minutes and a few hours.
    Biochar, which is made from forestry and agricultural products, especially from wood, serves as barbecue coal, as a soil conditioner, as a carrier for fertilizers, as an auxiliary for composting, as a feed additive, as a food supplement, as a raw material in the pharmaceutical industry and as a raw material for technical purposes, e.g. for filtering air, water and the like. In particular for the use of biochar as an industrial raw material, high quality and certification of the individual batches are required during production.
    Using modern technical processes, biogenic starting materials with a water content of up to 50% by weight of the fresh substance can be pyrolyzed to high-quality biochar. In this process, the pyrolysis gases generated during the pyrolysis are burned. Some of the heat generated is used to dry and heat the biogenic raw materials that are conveyed and to support pyrolysis. The vast majority of the heat is used for heating purposes or in combined heat and power plants for the combined generation of electricity and heat.
    2/30 • ·
    It is known to produce biochar by means of a continuous pyrolysis process in which the biogenic starting materials are continuously subjected to hot flue gases in a screw reactor. In such a process, the pyrolysis of the starting materials takes place at temperatures from 500 ° C. to 700 ° C. and with a residence time in the range from 15 minutes to 45 minutes. The resulting pyrolysis gases are e.g. cleaned in a dust collector and then burned. The hot flue gases generated in this way serve on the one hand to heat the reactor and on the other hand by means of heat exchangers for energy generation.
    In this process, however, due to the continuous material throughput and the strong material movements through the reactor, strong dust emissions occur which have to be separated off before or after the combustion of the pyrolysis gases. Furthermore, this process places high demands on the lump size and on the water content of the starting materials. In addition, due to the continuous mode of operation, insufficient monitoring of the production conditions of individual batches is possible.
    It is also known to introduce biogenic starting materials in batches in retorts, which are each individually exposed to hot flue gases in order to initiate and support pyrolysis. This results in pyrolysis in the individual batches, the course of which can be controlled by the hot flue gases, whereby the quality of the individual batches of the biochar produced can be controlled. However, this method also has the disadvantage that the flue gases are exposed to pollutants absorbed by them during pyrolysis in the form of gaseous and particulate emissions. This known method also has the disadvantage of discontinuity, since the supply of the starting materials, the supply of the hot flue gases, the discharge of the cooled flue gases and the removal of the biochar produced take place discontinuously.
    3/30 • ·· ···· ·· ·· ·· ·· ··· · ··· ·
    Further developments in retort processes use the pyrolysis gases that are created to cover energy requirements. With these processes, too, the starting materials must meet defined framework conditions with regard to the lump size and the water content, which is why complex preparation steps for material reduction and drying are required. In addition, the pyrolysis gases emerging from the retorts usually have to be cooled before their combustion in order to separate off distillation products, since only then can the pyrolysis gases be burned and used to heat the reactor. These additional process steps increase the complexity of the plants and often also result in contaminated wastewater.
    WO 2010/132970 A1 discloses a pyrolysis process in which individual retorts are introduced into a pyrolysis chamber, the starting materials in the retorts being successively subjected to drying, heating and pyrolysis, and also the cooling of the pyrolysis chamber generated coal takes place, whereupon the retorts are removed from the pyrolysis chamber. According to this process, too, in which the pyrolysis is carried out at a temperature of 320 ° C. to 350 ° C., the starting materials are subjected directly to hot flue gases from the pyrolysis gas combustion during the drying and heating and during the pyrolysis. In order to enable continuous operation, at least three mutually independent reactor chambers are provided, with drying, pyrolysis and cooling taking place simultaneously in one reactor chamber.
    The pyrolysis gases are burned in a burner and the flue gases are used in direct contact with the raw materials for drying and pyrolysis. Furthermore, the temperature is set by admixing the pyrolysis gases emerging from the drying. The pyrolysis gases not required for drying are discharged through a chimney.
    This method is also disadvantageous because components of the starting materials and the coal produced get into the flue gases, which in other
    4/30 • · • · • · · ···· · · ·· • · · · ··· · ··· ·
    Episode must be filtered out. Since the coal is also cooled in the reactor chambers, this results in large heat losses. In addition, since the coal is cooled by water injection, heat recovery is not possible.
    The object of the present invention is to provide a process or a plant for carrying out a pyrolysis process by means of which the disadvantages inherent in the known prior art for producing biochar are avoided. This is achieved according to the invention in that the retorts are at least largely closed with respect to the entry of hot flue gases and the starting materials located in the retorts are only heated indirectly by means of the flue gases by heating the retorts.
    This ensures that no constituents of the starting materials in different stages of charring get into the flue gases, thereby avoiding the need to clean the cooled flue gases and that there is no oxidation of the starting materials that would result in a loss of production.
    In comparison to the known pyrolysis processes, the reactor chambers are connected directly to at least one pyrolysis gas burner, the pyrolysis gases formed being burned in immediate succession and the hot flue gases formed being used continuously to heat the reactor chambers. Since there are several retorts in a system, in which the pyrolysis takes place at different times, a continuous flow of pyrolysis gases is achieved. Furthermore, the retorts and the pyrolysis gases generated by the pyrolysis are heated indirectly without contact of the hot flue gases with the starting material for producing the biochar or the pyrolysis gases.
    The hot flue gases flowing into a reactor chamber or the cooled flue gases flowing out of it and the pyrolysis gases arising from the pyrolysis and flowing out of the reactor chamber preferably flow through one in the reactor chamber
    5/30 • · • · • ··· partition located in separate areas. The retorts can be arranged in at least one reactor chamber, the pyrolysis gases can also be passed through an annular space surrounding the respective retort to a combustion chamber in which the flue gases are generated, which are passed into the at least one reactor chamber in which the flue gases pass the outflowing pyrolysis gases and the outer wall of the retort are heated. Furthermore, the flue gases can be partly led into at least one reactor chamber and partly to at least one heat exchanger.
    The flows of the flue gases in the feed lines of the flue gases to the at least one reactor chamber and / or in the discharge lines of the cooled flue gases from the at least one reactor chamber are preferably controlled by means of regulating devices. Furthermore, the cooled flue gases flowing out of the at least one reactor chamber are preferably partially supplied to the flue gases generated in the combustion chamber and flowing to the at least one reactor chamber, as a result of which the pyrolysis taking place in the retorts is temperature-controlled.
    In addition, cooled flue gases flowing out of the at least one reactor chamber can be fed to at least one heat exchanger for obtaining the residual heat. In particular, residual heat obtained by the at least one heat exchanger can be used for drying and / or for preheating the biogenic starting materials. In addition, the thermal energy obtained when the biochar is cooled can also be used.
    The individual retorts are preferably inserted in succession into the at least one reactor chamber and the biogenic starting materials in the retorts are pyrolysed successively in time, whereby pyrolysis gases are continuously produced, by means of which flue gases are generated, by means of which the pyrolyses taking place in the retorts are supported or controlled , It is preferably a
    6.30
    first retort, in which the pyrolysis has ended, is removed from a reactor chamber and the biochar located in this retort is removed from the retort, is pyrolyzed in at least a second retort, which is located in a reactor chamber, and is in a reactor chamber uses at least a third retort in which the pyrolysis of the biogenic starting material located therein is initiated.
    At least one reactor chamber is preferably provided in a system for carrying out this method, which has a reactor space for receiving at least one retort, an inlet opening for flue gases into the reactor space and an outlet opening for the cooled flue gases, with one between the retort and the inlet opening or the outlet opening for the flue gases and further with a line connecting the annular space between the retort and the partition, in which the pyrolysis gases emerging from the retort are led to the combustion chamber.
    The at least one reactor chamber can be designed with an at least almost gas-tight cover. Furthermore, the at least one reactor chamber can be designed on its top wall with an opening, through which a retort can be inserted into the reactor chamber, and the retort can be designed with a laterally projecting flange which bears against the edge of the opening. As a result, the reactor space of the at least one reactor chamber can be at least almost gas-tightly closed by a retort inserted therein.
    Furthermore, in the line leading from the combustion chamber to the at least one reactor chamber for the flue gases, a mixing device can be provided, by means of which the flue gases cooled by the flue gases flowing from the combustion chamber to the at least one reactor chamber can be admixed, whereby the pyrolysis taking place in the retorts can be controlled. In addition, in the lines in which the flue gases flow from the combustion chamber to the at least one reactor chamber and / or
    7/30 «· ·» 4 4 · 4 • 4 * · 444 · 444 · • · · · ·· 4 4 · 4 4 4 4 · · • 4 4 4 · 4 4 4 444 ·
    Ί or in the lines in which the cooled flue gases flow from the at least one reactor chamber, devices for controlling the flue gases flowing in these lines can be provided.
    At least one heat exchanger for utilizing the thermal energy is preferably connected to the line for the flue gases flowing out of the combustion chamber, and devices for drying or heating the biogenic starting materials are connected to the at least one heat exchanger. Furthermore, at least one device is provided for cooling the biochar produced, the waste heat of which can be used.
    The method according to the invention and a system according to the invention are explained in more detail below with reference to two exemplary embodiments shown in the drawing. Show it:
    1 shows a first embodiment of a plant for performing the method according to the invention, in a schematic representation,
    1A shows a reactor chamber with a retort, which in a system according to FIG. 1 is used in compared to FIG. 1 enlarged and detailed illustration, in section, and
    2 shows an embodiment of a system for carrying out the method according to the invention which has been supplemented compared to the embodiment according to FIG.
    1 shows a plant in which biochar 2a is produced by means of retorts 1, in which there is a biogenic starting material 2. The retorts 1 are at least almost gas-tightly closed by means of a cover 11. In this plant there is a first conveyor, by means of which the retorts 1, as indicated by arrows A, are inserted into a reactor 3 located in the plant. In the reactor 3 there are four reactor chambers 31, 31a, 31b, 31c, in each of which retorts 1, which contain biogenic starting material 2, are inserted one after the other. Furthermore, a combustion chamber 4 is provided, to which of
    8/30
    9 • ··· ♦ · · • «· 9 999
    9 9 9 9 9 9 9
    9 9 9 9 9 9 9
    99 999 9 999 9 lead the retorts 1 to lines 41 through which the pyrolysis gases formed in the retorts 1 are fed to the combustion chamber 4. In the combustion chamber 4, the pyrolysis gases are burned by supplying air by means of a main burner 42 located therein. Furthermore, a support burner 43 is located in the combustion chamber 4. The combustion chamber 4 is connected by means of lines 44 to the reactor chambers 31, 31a, 31b, 31c, via which the hot flue gases generated in the combustion chamber 4 with a temperature of approximately 600 ° C. to 800 ° C can be supplied. Pyrolysis is initiated by the hot flue gases in the biogenic starting material 2 located in the retorts 1, as a result of which pyrolysis gases are produced which have a temperature of approximately 300 ° C. to 600 ° C. Furthermore, lines 45 are connected to the reactor chambers 31, 31a, 31b, 31c, through which flue gases cooled to about 350 ° C. to 600 ° C. are discharged.
    The auxiliary burner 43 located in the combustion chamber 4 serves to generate the flue gases required for the start of pyrolysis in the retorts 1 during the start of the process. The hot flue gases supplied to the retorts 1 via the lines 44 then serve to initiate, support and control the pyrolysis.
    In the lines 45 and 44 there are regulating devices 46 for controlling the volume of the flue gases flowing away from the reactor chambers 31, 31a, 31c, and towards them. Furthermore, a line 47 branches off from line 44, through which the heating gases flow from combustion chamber 4 to reactor chambers 31, 31a, 31b, 31c, which leads to a first heat exchanger 5. The output of this heat exchanger 5 is connected to a second heat exchanger 5a. The lines 45 via which the flue gases cooled in the reactor combs 31, 31a, 31b, 31c flow out are also connected to the second heat exchanger 5a.
    Excess thermal energy is dissipated and utilized by means of the heat exchangers 5, 5a. To the heat exchanger 5a, a dedusting system 6 is connected, the output of which is connected via a line 61
    9/30 • · • ··· * · · · ·· · · * · · · · · «φ ·· ·· · ♦ · · ··· ·
    Fan 62 is located, is connected to a chimney 63. A line 64 is also connected to line 61, in which a fan 65 is located and which is connected to a mixing device 48 located in line 44. The admixture of cooled flue gases to the flue gases supplied via lines 44 to the reactor chambers 31, 31a, 31b, 31c controls the heat supply to the retorts 1 located in the reactor chambers 31, 31a, 31b, 31c, which in combination with the control devices 46 the course of the pyrolysis can be controlled.
    By means of a second conveying device, as indicated by the arrows B, those retorts 1 in which the pyrolysis has ended and in which the biochar 2a produced is located are removed from the reactor chambers 31, 31a, 31b, 31c and then cooled. The cooling can take place by natural or forced convection with air. The resulting thermal energy can be used for further use. After cooling, the retorts are opened and the biochar 2a is removed.
    Below are based on FIG. 1A explains the formation of a retort 1, in which biogenic starting material 2 is located, and its arrangement in a reactor chamber 31, 31a, 31b, 31c:
    The reactor chambers 31, 31a, 31b, 31c are formed with temperature-resistant walls 33, which are provided with external insulation 34 and by which a reactor space 30 is enclosed. At the top there is a top wall 33a, 34a which is formed with an opening 30a through which a retort 1 can be inserted into the reactor space 30. Above it is a gas-tight hood 35, which e.g. consists of sheet steel and insulation. The retort 1 is formed on its cylindrical outer wall 13 with an annular flange 12, which comes into contact with the edges of the top wall 33a, 34a, as a result of which the retort 1 is held in the reactor chambers 31, 31a, 31b, 31c and also the reactor space 30 is at least almost gas-tight. There is one in the reactor chambers 31, 31a, 31b, 31c
    10/30 ** ·· * · ···· ···· ····
    • · • ··· cylindrical partition 14, which encloses the cylindrical outer wall 13 of the retort 1, whereby an annular space 15 is formed between the two walls 13 and 14, which is at least almost gas-tight with respect to the reactor space 30. In the area of the bottom, the retort 1 is formed with an opening 16, in which there is a grate through which the starting material 2 is held in the retort 1. Connected to the annular space 15 is a pipe socket 17 which passes through the wall 33, 34 of the reactor chambers 31, 31a, 31b, 31c and to which the line 41 leading to the combustion chamber 4 is connected. Furthermore, the reactor chamber 31, 31a, 31b, 31c is designed with an inlet opening 36 for the supply of hot flue gases via line 44 from the combustion chamber 4 and with an outlet opening 37 for the discharge of cooled flue gases via line 45.
    Such a retort 1 has, for example, a capacity of approximately 3 m 3 , in which biogenic starting material 2 with a weight of approximately 1000 kg can be introduced. The retort 1 itself, which is made of steel, has a weight of about 650 kg. The amount of charcoal 2a produced by the pyrolysis is about 1.5 m 3 with a weight of about 350 kg. Due to the large content of the retorts, the lumpiness of the starting materials is of little importance.
    The pyrolysis process is carried out as follows:
    A retort 1, in which there is biogenic starting material 2 for the production of biochar 2a, is inserted into one of the reactor chambers 31, 31a, 31b, 31c by means of the first conveying device in the direction of arrows A. In this case, the reactor chamber 30 of the reactor chambers 31, 31a, 31b, 31c is sealed off from the escape of gases by the retorts 1 inserted into them. The relevant reactor chamber 31, 31a, 31b, 31c is then fed from the combustion chamber 4 via line 44 with hot flue gases at a temperature of approximately 600 ° C. to 800 ° C., which flow into the reactor chamber 30 through the inlet opening 36. As a result, the partition wall 14, the pyrolysis gas located in the annular space 15 and the outer wall 13 of the retort 1 are heated, as a result of which the one located in the retort 1
    11/30
    biogenic material 2 pyrolyzed. A further retort 1 is then inserted into a further one of the reactor chambers 31, 31a, 31b, 31c, in which the pyrolysis is likewise initiated. Thereupon, retorts 1 are inserted successively into further ones of the reactor chambers 31, 31a, 31b, 31c. In all of these retorts 1, in which there is biogenic starting material 2, pyrolysis takes place, the pyrolyses taking place in the individual retorts 1 being in different stages. As soon as the pyrolysis in the first retort 1 has ended, this retort 1 is removed from the relevant reactor chamber and a further retort 1 is inserted in its place, in which biogenic starting material 2 is located. Pyrolysis is then also initiated in this retort 1. Subsequently, those retorts 1 in which the pyrolysis has ended are removed from the reactor chambers 31, 31a, 31b, 31c and further retorts 1 in which biochar 2a is to be produced are used.
    The resulting pyrolysis gases, which have temperatures of 300 ° C to 600 ° C, flow through the opening 16 in the bottom wall of the retort 1 into the annular space 15 and subsequently pass through the pipe socket 17 into the line 41, which leads to the combustion chamber 4, in which they are burned by means of the main burner 42.
    The flue gases flowing into the reactor space 30 through the inlet opening 36 are cooled in the reactor space 30 and flow through the outlet opening 37 into the line 45, through which they reach the second heat exchanger 5a, in which the heat contained therein is obtained. Smoke gases emerging from the heat exchanger 5a and cooled further are cleaned in the dedusting system 6 and are released to the free atmosphere by means of the fan 62 via the chimney 8 or via line 64 and the mixing device 48 to the from the combustion chamber 4 to the reactor chambers 31 , 31a, 31b, 31c fed flowing heating gases. By means of the mixing device 48, the addition of cooled / 30 from the combustion chamber 4 to the reactor 3 flue gases
    Flue gases, like the control devices 46, control the pyrolysis taking place in the retorts 1.
    The flue gases required for starting the pyrolysis when the system is started up are generated by the auxiliary burner 17. Only a small proportion of the flue gases generated by the combustion chamber 4 is used for the pyrolysis. The majority of the flue gases generated by the combustion chamber 4 are discharged to the heat exchangers 5 and 5a via the line 47, the heat energy generated thereby being generated outside the system, i.a. for heating and / or for the generation of electricity, is used.
    The system shown in FIG. 2 differs from the system shown in FIG. 1 in that two air preheaters 7 and 7a are connected to the heat exchanger 5a. A line 71a leads from the air preheater 7a, which leads to a device 8 in which the biogenic starting material 2 located in a retort 1 is dried. A line 71 leads from the air preheater 7, which leads to a device 9 in which the biogenic starting material 2 located in a retort 1 is preheated for the pyrolysis. The warm air leaving the preheating device 9 is fed to the drying device 8 via a line 72. Due to the predrying of the starting materials, these can have water contents of up to 50% by weight of the fresh substance. The retorts 1 containing the dried and preheated biogenic starting material 2 are conveyed successively into the reactor 3 in the direction of the arrows A by means of the first conveying device.
    The following facts are decisive for this procedure:
    In the reactor chambers 31, 31a, 31b, 31c, only the pyrolysis of the biogenic starting materials 2 takes place. In contrast, the drying and heating of the starting materials 2 and the cooling of the generated biochar 2a take place outside the reactor chambers 31, 31a, 31b, 31c.
    The flue gases required to initiate and control the pyrolysis are only one located outside the outer wall 13 of the retort 1
    13/30 • ft
    Partition 14 supplied. As a result, the pyrolysis gases flowing in the annular space 15 located between the partition 14 and the outer wall 13 of the retort 1 and the outer wall 13 of the retort 1 are heated. This prevents the flue gases from being contaminated with constituents of the starting materials which are in different stages of pyrolysis, which would subsequently have to be eliminated, and furthermore prevents undesired oxidation of the starting materials. This also heats the pyrolysis gases to a higher temperature, thereby avoiding the condensation of tars.
    Because the pyrolyses taking place in the individual retorts are staggered in time, a continuous flow of pyrolysis gases and a continuous flow of flue gases are brought about, which means that the entire system is operated semi-continuously.
    This process sequence enables efficient and very low-emission production of biochar with a high degree of flexibility of the feed material and good traceability of individual product batches.
    The biogenic starting materials 2 located in the retorts 1 can therefore, since the retorts 1 are located in the individual reactor chambers 31, 31a, 31b, 31c, be subjected to individually controlled pyrolysis, whereby specific requirements of the biochar 2a produced can be met and good traceability individual batches of the product is achieved. The use of at least one heat exchanger or the return of the largely cooled pyrolysis gases released by the latter to the heating gas stream achieves an optimal energy yield. This means that up to 85% of the calorific value of the raw material can be converted into usable energy in the form of biochar, thermal energy or electrical current.
    The pyrolysis takes place in the retorts 1 in batches, which enables heating, pyrolysis and cooling of the biogenic starting materials with minimal particle abrasion and with low dust emissions.
    14/30 ···· ·· · · • · · · ·· ·· ·· ·· ··· · ··· ·
    The following advantages are thus achieved by a method according to the invention:
    Low dust emissions due to the minimization of
    Material movements within the retorts and due to the indirect
    Heating of raw materials;
    Continuous operation by staggering the pyrolysis in the individual retorts, whereby a continuous generation of pyrolysis gases and flue gases is achieved;
    good traceability of the pyrolysis of individual batches, which guarantees defined qualities of the biochar produced; high flexibility in the use of the starting materials with low demands on the type, the lump size and the water content of the starting materials;
    low gaseous emissions due to the direct combustion of the pyrolysis gases;
    low costs due to a simple procedure and a high degree of possible automation;
    Achievement of high energetic efficiencies through extensive utilization of the generated process heat for heat and / or electricity production.
    15/30 • ·
    Α
    Β
    17
    2a
    30a
    31,31a, 31b, 31c
    33a
    34a
    5, 5a
    7a
    71a
    REFERENCE NUMBER LIST
    Funding using a first funding facility Funding using a second funding facility
    retorts
    cover
    annular flange
    External wall of the retorts
    partition wall
    annulus
    bottom opening
    Pipe socket biogenic starting material
    biochar
    reactor
    reactor chamber
    opening
    reactor chambers
    Brick wall
    top wall
    insulation
    insulation
    Hood
    Inlet opening for heating gases
    Outlet opening for heating gases
    combustion chamber
    Pipes for the pyrolysis gases
    main burner
    supporting burner
    Lines to the reactor chambers Lines for the cooled heating gas control devices
    Lines to heat exchangers mixing device
    heat exchangers
    dedusting
    management
    fan
    stack
    Line to the fan mixing device
    Air preheater for preheating Air preheater for drying Line to preheater Line to dryer Exhaust line
    drying device
    preheater
    16/30 ··> ··· · · · • ·· ···· ···· · ···· ·· · · ···· ·· · · ·· ·· ··· · ·· · ·
    权利要求:
    Claims (30)
    [1]
    1. A process for the production of biochar, in which biogenic starting material (2) located in retorts (1) is pyrolyzed and the combustible pyrolysis gases formed by the pyrolysis are burned to produce hot flue gases, the retorts (1) being successively in at least one Reactor chamber (31, 31a, 31b, 31c) are introduced and the pyrolysis is carried out in these by means of the flue gases, characterized in that the retorts (1) are at least largely closed off from the entry of hot flue gases and the heating of the in the retorts ( 1) located starting materials (2) by means of the flue gases by heating the retorts (1) only indirectly.
    [2]
    2. The method according to claim 1, characterized in that the hot flue gases flowing into at least one reactor chamber (31, 31a, 31b, 31c) or the cooled flue gases flowing out of the hot flue gases and the pyrolyses that arise and out of the reactor chamber (31, 31a , 31b, 31c) flowing out of the pyrolysis gases in the reactor chamber (31, 31a, 31b, 31c) through a partition (14) located therein in separate areas.
    [3]
    3. The method according to any one of claims 1 and 2, characterized in that the retorts (1) are arranged in at least one reactor chamber (31, 31a, 31b, 31c), furthermore the pyrolysis gases through an annular space surrounding the respective retort (1) ( 15) are passed through to a combustion chamber (4) in which the flue gases are generated, which are passed into the at least one reactor chamber (31, 31a, 31b, 31c) in which the pyrolysis gases flowing out and the outer wall (13 ) the retort (1) are heated.
    [4]
    4. The method according to any one of claims 1 to 3, characterized in that the flue gases partially in at least one reactor chamber (31, 31a,
    17/30
    31b, 31c) and partially to at least one heat exchanger (5, 5a).
    [5]
    5. The method according to any one of claims 1 to 4, characterized in that in the feed lines (44) of the flue gases to the at least one reactor chamber (31, 31a, 31b, 31c) and or or in the derivatives (45) of the cooled flue gases the flows of the flue gases are controlled from the at least one reactor chamber (31, 31a, 31b, 31c) by means of regulating devices (46).
    [6]
    6. The method according to any one of claims 1 to 5, characterized in that the cooled flue gases flowing out of the at least one reactor chamber (31, 31a, 31b, 31c) partially the generated in the combustion chamber (4) and to the at least one reactor chamber (31 , 31a, 31b, 31c) flowing smoke gases are supplied, whereby the pyrolysis taking place in the retorts (1) are temperature controlled.
    [7]
    7. The method according to any one of claims 1 to 6, characterized in that from the at least one reactor chamber (31, 31a, 31b, 31c) cooled flue gases flowing out are fed to at least one heat exchanger (5, 5a) for obtaining the residual heat.
    [8]
    8. The method according to claim 7, characterized in that residual heat obtained by the at least one heat exchanger (5, 5a) is used for drying and / or for preheating the biogenic starting materials (2).
    [9]
    9. The method according to any one of claims 1 to 8, characterized in that the thermal energy obtained when the biochar (2a) is cooled is used.
    [10]
    10. The method according to any one of claims 1 to 9, characterized in that the individual retorts (1) are inserted successively into the at least one reactor chamber (31, 31a, 31b, 31c) and
    18/30, the biogenic starting materials (2) located in the retorts (1) are pyrolyzed successively in time, as a result of which continuous
    Pyrolysis gases are produced, by means of which flue gases are generated, by means of which the pyrolysis taking place in the retorts (1) is supported or
    to be controlled.
    [11]
    11. The method according to claim 10, characterized in that at least a first retort (1), in which the pyrolysis has ended, is removed from a reactor chamber (31, 31a, 31b, 31c) and the biochar located in this retort (1) (2a) is removed from the retort (1), that in at least one second retort (1), which is located in a reactor chamber (31, 31a, 31b, 31c), the starting material (2) located therein is pyrolyzed and that at least a third retort (1) is inserted into a reactor chamber (31, 31a, 31b, 31c), in which the pyrolysis of the biogenic starting material (2) contained therein is initiated.
    [12]
    12. Plant for carrying out the method according to one of claims 1 to 11, characterized in that at least one reactor chamber (31, 31a, 31b, 31c) is provided which has a reactor space (30) for receiving at least one retort (1), with an inlet opening (36) for flue gases into the reactor chamber (30) and with an outlet opening (37) for the cooled flue gases, with one between the retort (1) and the inlet opening (36) or the outlet opening (37) for the flue gases partition (14) and further with a line (17) connecting to the annular space (15) between the retort (1) and the partition (14), in which line the pyrolysis gases emerging from the retort (1) to the combustion chamber (4) are led, is trained.
    [13]
    13. Plant according to claim 12, characterized in that the at least one reactor chamber (31, 31a, 31b, 31c) is formed with an at least almost gas-tight cover (35).
    19/30 • · · ··· · ··· · ···· ·· · · ···· · · · · ·· ·· ··· · ·· · ·
    [14]
    14. Plant according to one of claims 12 and 13, characterized in that the at least one reactor chamber (31, 31a, 31b, 31c) is formed on its top wall (33a, 34a) with an opening (30a) through which into the Reactor chamber (31, 31a, 31b, 31c) a retort (1) can be used and that the retort (1) is formed with a laterally projecting flange (12) which bears against the edge of the opening (30a).
    [15]
    15. Plant according to claim 14, characterized in that the reactor space (30) of the at least one reactor chamber (31, 31a, 31b, 31c) is at least almost gas-tightly closed by a retort (1) inserted therein.
    [16]
    16. Plant according to one of claims 12 to 15, characterized in that a mixing device (48) is provided in the line (44) leading from the combustion chamber (4) to the at least one reactor chamber (31, 31a, 31b, 31c) for the flue gases through which the flue gases cooled by the flue gases flowing from the combustion chamber (4) to the at least one reactor chamber (31, 31a, 31b, 31c) can be admixed, as a result of which the pyrolysis taking place in the retorts (1) can be controlled.
    [17]
    17. Plant according to one of claims 12 to 16, characterized in that in the lines (44) in which the flue gases flow from the combustion chamber (4) to the at least one reactor chamber (31, 31a, 31b, 31c) and or or in the lines (45) in which the cooled flue gases flow from the at least one reactor chamber (31, 31a, 31b, 31c), devices (46) are provided for controlling the flue gases flowing in these lines (44, 45).
    [18]
    18. Plant according to one of claims 12 to 17, characterized in that at least one heat exchanger (5, 5a) for utilizing the thermal energy is connected to the line (44) for the flue gases flowing out of the combustion chamber (4).
    20/30 • · • · · · · · · • ·· ···· · ··· • · · · · · • · · · · · ·· ·· ··· · ··· ·
    [19]
    19. Plant according to claim 18, characterized in that devices (8, 9) for drying or for heating the biogenic starting materials (2) are connected to the at least one heat exchanger (5, 5a).
    [20]
    20. Device according to one of claims 12 to 19, characterized in that at least one device for cooling the biochar produced (2a) is provided, the waste heat of which leads to use.
    [21]
    21/30
    [22]
    22/30 · * ···
    3i, 31, 31l>, 31c
    [23]
    23/30
    LL
    [24]
    24/30 ·· ·· • · · · • · · · · · • · · · · • · · · · • ·
    claims:
    1. A process for the production of biochar, in which biogenic starting material (2) located in retorts (1) is pyrolyzed and the combustible pyrolysis gases formed by the pyrolysis are burned to produce hot flue gases, the retorts (1) being successively in at least one Reactor chamber (31, 31a, 31b, 31c) are introduced and by means of the flue gases the pyrolysis is carried out in them, the retorts (1) being at least largely closed off from the entry of hot flue gases and the heating of those in the retorts (1) Starting materials (2) are only produced indirectly by means of the flue gases by heating the retorts (1), characterized in that the pyrolysis gases are passed through an annular space (15) surrounding the respective retort (1) to a combustion chamber (4) in which the flue gases are generated which are led into the at least one reactor chamber (31, 31a, 31b, 31c) s, in which the outflowing through the flue gases
    Pyrolysis gases and the outer wall (13) of the retort (1) are heated.
    2. The method according to claim 1, characterized in that in at least one reactor chamber (31, 31a, 31b,
    31c) flowing in hot flue gases or the cooled flue gases flowing out of them and the pyrolysis gases arising from the pyrolysis and flowing out of the reactor chamber (31, 31a, 31b, 31c) in the reactor chamber (31, 31a, 31b, 31c) by one in the latter located partition (14) flow in separate areas.
    [25]
    25/30
    LAST CLAIMS • · ·· · · · · · ·· • ·· · · · ·· ·· • ·· ··· · · ·· · · · • ·· ······ ·· ·· · • · · · ·· ·· ·· ·
    3. The method according to claim 1 or 2, characterized in that the flue gases are partly passed into at least one reactor chamber (31, 31a, 31b, 31c) and partly to at least one heat exchanger (5, 5a).
    4. The method according to any one of claims 1 to 3, characterized in that in the feed lines (44) of the flue gases to the at least one reactor chamber (31, 31a, 31b, 31c) and or or in the derivatives (45) of the cooled flue gases the flows of the flue gases are controlled from the at least one reactor chamber (31, 31a, 31b, 31c) by means of regulating devices (46).
    5. The method according to any one of claims 1 to 4, characterized in that the cooled flue gases flowing out of the at least one reactor chamber (31, 31a, 31b, 31c) partially the generated in the combustion chamber (4) and to the at least one reactor chamber (31 , 31a, 31b, 31c) flowing smoke gases are supplied, whereby the pyrolysis taking place in the retorts (1) are temperature controlled.
    6. The method according to any one of claims 1 to 5, characterized in that from the at least one reactor chamber (31, 31a, 31b, 31c) cooled flue gases flowing out are fed to at least one heat exchanger (5, 5a) for obtaining the residual heat.
    7. The method according to claim 6, characterized in that by the at least one heat exchanger (5, 5a) residual heat obtained for drying and or or
    [26]
    26/30 [LAST CLAIMS *) • · · »· · · · • · · · • · ♦ · · · • · · · I
    Preheating the biogenic starting materials (2) is used.
    8. The method according to any one of claims 1 to 7, characterized in that the thermal energy obtained when the biochar (2a) is cooled is used.
    9. The method according to any one of claims 1 to 8, characterized in that the individual retorts (1) are used in succession in the at least one reactor chamber (31, 31a, 31b, 31c) and the biogenic starting materials located in the retorts (1) (2) are pyrolysed successively in time, whereby pyrolysis gases are continuously produced, by means of which flue gases are generated, by means of which the pyrolyses taking place in the retorts (1) are supported or controlled.
    10. The method according to claim 9, characterized in that at least a first retort (1), in which the pyrolysis has ended, is removed from a reactor chamber (31, 31a, 31b, 31c) and the biochar located in this retort (1) (2a) is removed from the retort (1), that in at least one second retort (1), which is located in a reactor chamber (31, 31a, 31b, 31c), the starting material (2) located therein is pyrolyzed and that at least a third retort (1) is inserted into a reactor chamber (31, 31a, 31b, 31c), in which the pyrolysis of the biogenic starting material (2) contained therein is initiated.
    [27]
    27/30 [LAST CLAIMS *) • · ··· · · «· · · l ·« · · · · · * »•« · · · · · ··· ·· «• · · · ··· · · · · · · · ·
    24 ’·· * * ·· * · * ·· ** ·· * ··’
    11. Plant for carrying out the method according to one of claims 1 to 10, characterized in that at least one reactor chamber (31, 31a, 31b, 31c) is provided which has a reactor space (30) for receiving at least one retort (1), with an inlet opening (36) for flue gases into the reactor chamber (30) and with an outlet opening (37) for the cooled flue gases, with one between the retort (1) and the inlet opening (36) or the outlet opening (37) for the flue gases partition (14) and further with a line (17) connecting to the annular space (15) between the retort (1) and the partition (14), in which line the pyrolysis gases emerging from the retort (1) to the combustion chamber (4) are led, is trained.
    12. Plant according to claim 11, characterized in that the at least one reactor chamber (31, 31a, 31b, 31c) is formed with an at least almost gas-tight cover (35).
    13. Plant according to one of claims 11 and 12, characterized in that the at least one reactor chamber (31, 31a, 31b, 31c) is formed on its top wall (33a, 34a) with an opening (30a) through which into the Reactor chamber (31, 31a, 31b, 31c) a retort (1) can be used and that the retort (1) is formed with a laterally projecting flange (12) which bears against the edge of the opening (30a).
    14. Plant according to claim 13, characterized in that the reactor space (30) of the at least one reactor chamber
    [28]
    28/30 [LAST CLAIMS *) ·· ·· · ·· ·· ·· • »·» · · · »· * • · · * · · · · · ··· • · · · ··· (31, 31a, 31b, 31c) is at least almost gas-tightly closed by a retort (1) inserted into it.
    15. Plant according to one of claims 11 to 14, characterized in that in the from the combustion chamber (4) to at least one reactor chamber (31, 31a, 31b, 31c) leading line (44) for the flue gases
    Mixing device (48) is provided, by means of which cooled flue gases can be added to the flue gases flowing from the combustion chamber (4) to the at least one reactor chamber (31, 31a, 31b, 31c), as a result of which the pyrolysis taking place in the retorts (1) can be controlled.
    16. Plant according to one of claims 11 to 15, characterized in that in the lines (44) in which the flue gases flow from the combustion chamber (4) to the at least one reactor chamber (31, 31a, 31b, 31c) and or or in the lines (45) in which the cooled flue gases flow from the at least one reactor chamber (31, 31a, 31b, 31c),
    Devices (46) for controlling the flue gases flowing in these lines (44, 45) are provided.
    17. Plant according to one of claims 11 to 16, characterized in that at least one heat exchanger (5, 5a) for utilizing the thermal energy is connected to the line (44) for the flue gases flowing out of the combustion chamber (4).
    18. Plant according to claim 17, characterized in that on the at least one heat exchanger (5, 5a) devices (8, 9) for drying or for heating
    [29]
    29/30 [LAST CLAIMS *) of the biogenic raw materials (2) are connected.
    19. Device according to one of claims 11 to 18, characterized in that at least one device for cooling the biochar (2a) is provided, the waste heat of which is used.
    [30]
    30/30 [LAST CLAIMS *)
    类似技术:
    公开号 | 公开日 | 专利标题
    DE19945771C1|2001-02-22|Process for gasifying organic materials comprises cracking the materials by contacting with a hot heat carrier medium which is removed from a solid carbonaceous residue after leaving the pyrolysis reactor and conveyed to a heating zone
    EP2424955B1|2012-09-05|Device and method for drying and torrefying at least one carbon-containing substance stream in a multiple-hearth furnace
    EP2082013B1|2017-04-12|Method for producing a product gas rich in hydrogen
    DE2651302C3|1981-07-09|Device for generating distillation gas from waste
    EP1192234B1|2009-12-30|Method and device for pyrolyzing and gasifying organic substances or substance mixtures
    EP2261560B1|2016-03-23|Method and device for processing domestic and industrial organic waste
    DE2838749A1|1979-03-15|METHOD AND DEVICE FOR TREATMENT OF A CRUSHED SOLID CARBONIZABLE MATERIAL
    DE2432504B2|1976-12-16|PROCESS AND SYSTEM FOR PRODUCING COMBUSTION GASES FROM COMPONENT DOMESTIC AND INDUSTRIAL MANUFACTURING ETC.
    DE102010018197A1|2011-10-27|Process and apparatus for the gasification of biomass
    DE202013101154U1|2013-04-22|Pyrolysis aggregate for wet biomass
    DE102004008621A1|2005-09-08|Transportable or stationary hearth-type furnace reactor, to transform solid and paste organic materials to processed gas, comprises cubic reactor, vapor inlet, a chain conveyor, a cover with passages and a supporting flame mechanism
    EP2616530A2|2013-07-24|Method and device for producing a solid fuel from biomass
    EP3516011B1|2020-11-04|Process for producing biocoal and plant therefor
    DE19807988B4|2007-11-08|Process for the separation of volatile components from solid fuels
    DE60026264T2|2006-08-10|Process and plant for the production of combustible gases from operations rich in organic materials
    EP3214155B1|2020-05-20|Process for the production of synthesis gas for running an internal combustion engine.
    EP3508556A1|2019-07-10|Method for operating a system for energy recovery and system for same
    DE60225380T2|2009-03-26|Process and apparatus for producing fuel gas from gas generated by thermal decomposition of a solid additive
    DE10333279B4|2010-08-19|Process and apparatus for pyrolysis and gasification of organic matter or mixtures containing organic matter
    DE10312603B4|2005-08-11|Process and apparatus for gasification and combustion of lumpy renewable raw materials in the form of animal bones
    DE102007017859A1|2008-10-23|Double-walled direct current gasifier for organic components and water, has gas and/or vapor and/or combustion medium supplying devices arranged over each other in plane or multiple planes
    EP3446799B1|2021-05-19|Recovering process from waste products
    DE102012109917A1|2014-04-17|Apparatus and method for drying and torrefaction of biomass
    WO2009103289A1|2009-08-27|High-heat process for utilizing organic material
    DE102019007853A1|2021-05-20|Process for the production of hydrogen from biogenic carbon-containing residues
    同族专利:
    公开号 | 公开日
    EP3516011B1|2020-11-04|
    DK3516011T3|2021-02-01|
    EA201990825A1|2019-08-30|
    NZ752475A|2021-04-30|
    LT3516011T|2021-02-25|
    AT519020B1|2018-03-15|
    WO2018055003A1|2018-03-29|
    ZA201901911B|2020-10-28|
    AU2017329873A1|2019-05-02|
    CN109923192A|2019-06-21|
    HUE052717T2|2021-05-28|
    HRP20210140T1|2021-03-05|
    EA036674B1|2020-12-07|
    ES2846006T3|2021-07-28|
    PT3516011T|2021-01-20|
    UA122462C2|2020-11-10|
    US20200270528A1|2020-08-27|
    RS61299B1|2021-02-26|
    SI3516011T1|2021-02-26|
    PL3516011T3|2021-05-04|
    US10934490B2|2021-03-02|
    CA3038166A1|2018-03-29|
    EP3516011A1|2019-07-31|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    FR2606420A1|1986-11-07|1988-05-13|Fromager Gerard|Process for the carbonisation of wood and twinned ovens for making use of the process|
    DE10348987A1|2003-10-17|2005-05-25|Peggy Diana Berndt|Low-temperature pyrolysis assembly for the separation of steel from rubber found e.g. in used tyres, rubber-mantle chains, scrapped electronic products|
    WO2011101311A1|2010-02-17|2011-08-25|Clean Fuels B.V.|Batch-wise operated retort using temporary storage of heat|
    CH237758A|1942-09-04|1945-05-31|Chemische Holzverwertung Ag F|Process for charring wood and other organic substances.|
    DE3225441C2|1982-07-07|1989-06-29|C. Conradty Nürnberg GmbH & Co KG, 8505 Röthenbach|Process and device for the thermal cleaning of exhaust gases from ring furnaces|
    IT1276116B1|1995-11-10|1997-10-24|O E T Calusco S R L|PROCEDURE AND PLANT FOR THE PRODUCTION OF VEGETABLE COAL BY PYROLYSIS OF WOOD PRODUCTS OR VEGETABLE BIOMASS IN GENERAL|
    FR2818281B1|2000-12-18|2003-11-14|Biomasse En|PROCESS AND REACTOR FOR THE GASIFICATION OF BIOMASS AND BIOLOGICAL WASTE|
    US20060163053A1|2005-01-21|2006-07-27|Bengt-Sture Ershag|Batch pyrolysis system|
    CN201284301Y|2008-09-02|2009-08-05|赵陆凯|Dry distillation combined charing kiln|
    US20120308441A1|2008-12-15|2012-12-06|Andrew Hansen|Method and Apparatus for Production of Electrical Energy and Liquid Hydrocarbons from Oil Sands/Bitumen, Biomass and Waste Products by Means of Thermal Anaerobic Gasification Gas Up-Grading|
    BRPI0901948A2|2009-05-21|2011-02-08|Alvaro Lucio|process of obtaining charcoal that uses the gaseous constituents emitted during the carbonization of the vegetable matter as a source of energy for the process and constructive configuration of the respective equipment.|
    US8226798B2|2009-05-26|2012-07-24|Alterna Energy Inc.|Method of converting pyrolyzable organic materials to biocarbon|
    CN103361087A|2012-05-04|2013-10-23|张荣光|Pyrolysis and combustion coupled circular reaction method and device|
    DE102014015815A1|2014-10-24|2016-04-28|Christoph Adam|Device with a retort for charcoal production with combustion of the carbonization gases|
    CN104479760A|2014-11-21|2015-04-01|神华集团有限责任公司|Pyrolysis gas dust removal device|
    CN204356281U|2015-01-05|2015-05-27|建瓯市恒顺炭业有限公司|A kind of planer-type charring kiln|
    CN105368470A|2015-10-21|2016-03-02|邢献军|Preparation method of biomass organic carbon|WO2020245337A2|2019-06-07|2020-12-10|Torrgreen B.V.|Torrefaction reactor and process|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    ATA438/2016A|AT519020B1|2016-09-26|2016-09-26|Process for producing biochar and plant therefor|ATA438/2016A| AT519020B1|2016-09-26|2016-09-26|Process for producing biochar and plant therefor|
    EA201990825A| EA036674B1|2016-09-26|2017-09-20|Plant for producing biocoal and corresponding process|
    LTEP17769097.1T| LT3516011T|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    NZ752475A| NZ752475B2|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    AU2017329873A| AU2017329873A1|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    ES17769097T| ES2846006T3|2016-09-26|2017-09-20|Procedure for the manufacture of biochar and its corresponding installation|
    US16/336,769| US10934490B2|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    PCT/EP2017/073824| WO2018055003A1|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    SI201730606T| SI3516011T1|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    UAA201904489A| UA122462C2|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    CA3038166A| CA3038166A1|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    HUE17769097A| HUE052717T2|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    EP17769097.1A| EP3516011B1|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    CN201780059240.0A| CN109923192A|2016-09-26|2017-09-20|It is used to prepare the method and device thereof of charcoal|
    PT177690971T| PT3516011T|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    PL17769097T| PL3516011T3|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    DK17769097.1T| DK3516011T3|2016-09-26|2017-09-20|PROCEDURE FOR THE MANUFACTURE OF BIOKUL AND PLANTS FOR IT|
    RS20210038A| RS61299B1|2016-09-26|2017-09-20|Process for producing biocoal and plant therefor|
    ZA2019/01911A| ZA201901911B|2016-09-26|2019-03-27|Process for producing biocoal and plant therefor|
    HRP20210140TT| HRP20210140T1|2016-09-26|2021-01-26|Process for producing biocoal and plant therefor|
    [返回顶部]