• 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:
    The invention relates to a biogas reactor (10), in which biogas (12) is arranged from organic material (11). The biogas reactor comprises a tank structure (13), a tubular reactor space (14) arranged in the tank structure, in which organic material for the formation of biogas can be arranged, heat control devices (16) for influencing the temperature of the organic material arranged in the reactor space, connections (17, 18) for feeding organic material into the reactor space and for discharging from the reactor space and one or more connections (19.1 - 19.3) for removing biogas from the reactor space. With the heat control devices it has been arranged to form a two-layer construction of the tank structure, which is arranged to form the main part of the load-bearing structure of the tank structure and in which there is an empty space (39) for a heat transfer medium. The invention further relates to a process for the production of biogas and for the production of the biogas reactor.
    公开号:FI20195946A1
    申请号:FI20195946
    申请日:2019-11-04
    公开日:2021-05-05
    发明作者:Henri Viiru；Pasi Kolehmainen
    申请人:Lepikon Oy；
    IPC主号:
    专利说明:

    BIOGAS REACTOR AND METHODS FOR BIOGAS PRODUCTION AND BIOGAS
    The invention relates to a biogas reactor in which biogas is adapted to form biogas from organic material and which biogas reactor comprises - a tank structure, - a tubular reactor space adapted to be - connections for feeding and removing organic material from the reactor space, - one or more units for removing biogas from the reactor space. In addition, the invention also relates to methods for producing biogas and manufacturing a biogas reactor.
    Biogas is a gas produced under anaerobic conditions and formed by microbes from organic matter. Biogas is rich in methane, some carbon dioxide and small amounts of sulfur compounds.
    & = 25 The biogas process can be treated at either psychrophilic (0 - 3 15 ° C), mesophilic (15 - 45 ° C) or thermophilic (50 - E 75 * C) temperatures. These all have different bacterial strains. The warmer the process, the more intense the process.
    3 The most common temperature is mesophilic because it has good gas production and easy control. Gas is a renewable biofuel that is most commonly used in electricity and heat production. Biogas can be compared to natural gas in terms of its properties.
    Biogas can be produced with biogas reactors, for which a variety of technical solutions have been developed.
    The reactors can be roughly divided into two basic types, the full-stirred and plug-flow reactor.
    Fully stirred reactors can be, for example, continuous and stirred.
    In this case, the material is pumped into the reactor and at the same time it is taken out of it to the same extent, whereby the amount of pulp remains stable.
    Its advantages are the automation of feed additions and relatively stable gas production.
    A plug flow reactor is a type of reactor particularly suitable for dry materials.
    In it, the organic material is arranged in a horizontally arranged elongate reactor space, in which the mass to be treated passes in the feed order as a plug flow through the process while forming a gas.
    This achieves an almost constant residence time of the pulp.
    The plug flow is provided in a tubular reactor where the pulp is fed from one end and the pulp is discharged from the other end.
    The new pulp cannot mix with the old one, so the bacterial liquid collected from the process is fed to the pulp to speed up the process.
    The gas is removed, for example, from the upper part of the reactor.
    The reactor space is formed by a jacket with a cross-sectional profile 2, for example in the form of a rotating body, which is arranged in the generally 3-metal structures of the reactor. x a © Another type of reactor is a batch reactor.
    It is filled and 2 emptied at regular intervals.
    It has the advantages of easy maintenance during 2 30 processes and the disadvantage of relatively slow start-up of gas production N and is laborious to empty.
    In Finland, biogas is often produced in landfills and farms, in large biogas plants. Often the raw material is organic waste, such as food industry waste, household biowaste or manure. In developing countries, on the other hand, reactors are typically small, a few cubic meters of underground tanks. The structural implementation of biogas reactors makes them very heavy. In addition, their scalability is poor. Due to their heavy intensity, the hybrid gas reactors have to be transported to their site in several parts, which also results in their assembly work at the site. All of these increase the costs associated with the construction and acquisition of the biogas reactor and thus increase the payback time of the investment.
    The object of the present invention is to provide a biogas reactor which, due to its structure, can be precisely controlled and regulated in terms of process technology. It is a further object of the invention to provide methods for producing biogas and a biogas reactor, by means of which biogas can be produced with light structural implementations and in addition with improved logistics, for example for arranging a hybrid gas reactor at a biogas production site. The characteristic features of the biogas reactor 2 and the methods according to the invention are set out in the appended claims 1, 13 and 14. 3 E In the biogas reactor according to the invention the thermal control means o are adapted to form a major part of the load-bearing structure 3 of the tank structure. To this end, the thermal control means are adapted to form a two-layer structure from the tank structure. In addition, the © two-layer structure has a cavity for the heat transfer medium. More specifically, the thermal control means are adapted to form a hollow tubular profile arranged in a helical arrangement by helically winding to form a container structure from the tubular profile.
    The tank structure is adapted to form a pipe from a pipe profile formed by a welding method in connection with its helical winding.
    The tank structure improves the process technical controllability of the reactor.
    A significant advantage of the helical structure is that a clearly defined flow channel is formed in the two-layer structure forming the tank structure with the invention.
    The heat transfer medium circulating in the flow channel is thus forced by the invention to pass through the entire two-layer structure and, more particularly, the heat transfer structure formed by the helically arranged tubular profile.
    In this case, for example, the heat transfer medium cannot be deposited in any direction of the bilayer structure, but is forced to circulate through the entire tank structure formed by the bilayer structure and thereby act on the tank structure on all sides over its large heat transfer surface. - is made. Another significant advantage is that with the invention the supply and / or flow direction of the heat-> transfer medium in relation to the reaction space and the organic material to be placed therein and the progress of the process can be well taken into account by the invention.
    In other words, the invention makes it possible to apply and control the temperature effect at the right point in the reactor and thus in the process step.
    The thermal effect can then be said to be site-dependent for the reactor structure and thus also for the process step, because the heat transfer medium fed to a certain point in the tank structure acts from a certain point in the direction defined by the profile tube in the reactor structure. This is an essential advantage in terms of process control and controllability.
    The biogas reactor according to the invention and more particularly, its tank structure may be mainly made of plastic. Thus, its material can be recycled and recyclable. In addition, it is lightweight, durable and has lower manufacturing costs. It is corrosion-free, i.e. it does not rust or corrode as a result of a chemical reaction. The slippery surface characteristic of the reactor also prevents deposits from adhering to the surface of the reactor. The reactor also has a very long life cycle.
    In addition, due to its light weight, the reactor is easy to transport to its application and also fast and easy to install. The light and rigid structure makes it possible to prefabricate the reactor in the production facilities and, if necessary, also to transfer it to another application afterwards.
    The invention also improves the scalability of the biogas reactor. The invention achieves a cost-effective way both in the manufacture of a biogas reactor and in its in-service costs> (e.g. self-use). The biogas reactor and method according to the invention achieve profitable gas production x in relation to investment costs. Other features of the invention will be apparent from the appended claims, and further advantages are listed in the specification.
    In the following, the invention, which is not limited to the embodiments shown below, will be described in more detail with reference to the accompanying drawings, in which
    Figure 1 shows a schematic side view of an example of a biogas reactor seen from the side and a cross-section, Figure 2 shows the biogas reactor shown in Figure 1 seen from the side at an angle, Figure 3 shows a simplified schematic side view of a Fig. 5 shows an example of the principle of manufacturing a tank structure, Fig. 6 shows an example of the connection of a profile tube forming a two-layer structure to the tank structure, Fig. 7 shows a schematic example of the bicycle reactor shown in Figs. 1 and 2 with the reactor space now an example of a biogas reactor thermal management circuit.
    Figure 1 shows a schematic view of an example of a biogas reactor 10 seen from the side and in cross-section. Fig. 2, in turn, shows the biogas reactor 10 of Fig. 1 seen obliquely from the side in a transparent manner. The biogas = 25 actuator 10 is intended to form biogas 12 from the organic material 11. The organic material 11 is also referred to as E biomass. Examples of these are all kinds of organic wastes, such as manure, wastewater and industrial effluents.
    2 30
    N For the production of biogas 12, the biogas reactor 10 includes a reactor space 14 in which the organic material 11 can be adapted to form biogas 12. The reactor space 14 is adapted to form a tank structure 13. The reactor space 14 is now a horizontal elongate tubular cylindrical space. In the reactor space 14, the organic substance 11 is fed as an inlet (In) and, respectively, from which it is also removed (Out). Thus, at the same time, the organic matter 11 also advances in the reactor space 14, when biogas 12 is formed there from it by processes known per se. The biogas reactor 10 thus also includes connections 17, 18 for supplying organic material 11 to the reactor space 14 and for removing organic material 11 from the reactor space 14. One or more common components, such as discharge unit 18, can also be implemented, for example in the form of a pump. The biogas reactor 10 is in principle a plug flow reactor. The aim is to supply / discharge as evenly as possible in order to keep the process conditions as constant as possible. Further, the biogas reactor 10, more particularly, its tank structure 13 includes one or more connections 19.1 to 19.3 for removing the biogas 12 formed in the reactor space 14 from the reactor space 14 and thus, from the biogas reactor 10.
    Biogas 12 resulting from the anaerobic decomposition of organic matter 11 is recovered via 19.1 to 19.3. Biogas recovery means 12 (not = 25 shown) are connected to the common> 19.1 to 19.3. 3 E Anaerobic digestion can also be called digestion of organic matter o 11. It is the decomposition of organic matter under anaerobic conditions. Anaerobic microorganisms are responsible for degradation. The product of digestion mainly produces a solid corresponding to humus, water, carbon dioxide and methane gas, which can be utilized, for example, in energy production.
    The methane content of the biogas produced in the digestion process is 65-70%. Nitrogen compounds are reduced in digestion to ammonia and sulfur compounds to hydrogen sulfide.
    The digestion process may comprise four main steps known per se: hydrolysis, acid fermentation, acetogenesis and methanogenesis.
    The biogas reactor 10 also includes thermal control means 16 for influencing the temperature of the reactor space 14 and more particularly, the organic material 11 that can be adapted to the reactor space 14.
    It is also possible to talk about arranging the reactor space 14 for temperature control, i.e. reactor heating.
    The thermal control means 16 are arranged in a heat transfer manner in connection with the reactor space 14 so that they can either heat and / or cool the material in the reactor space 14.
    Thus, the change of state applied to the thermal control means 16 also affects the reactor space 14 and the organic material 11 arranged therein, either by heating it or by cooling it.
    In general, heating or cooling, more generally, the thermal control means 16 are intended to maintain the temperature of the reactor space 14 and thus also of the organic material 11 within certain limits optimal for gas formation.
    Thus, the influence of the temperature during the digestion process itself can be understood as maintaining the temperature. By means of the thermal control means 16, more generally, the reactor heating 3 is adapted to form the two-layer structure of the tank structure 13 of the biogas reactor 10 shown in Fig. 1 and in particular in Fig. 3.
    In this case, the two-layer structure formed by the thermal control means 16 is adapted to form the main part of the load-bearing structure of the tank structure.
    That is, the thermal control means 16 are then integrated, i.e. built-in, into the tank structure 13 of the biogas reactor 10. Thus, the reactor space 14 of the biogas reactor is free of thermal control means. More specifically, the thermal control means 16 are now adapted to form the container structure 13 as substantially self-supporting.
    The thermal control means 16 included in the tank structure 13 are adapted to form a substantial part of the body of the biogas reactor 10 in order to stiffen it and thus also to make it self-supporting. In this case, the biogas reactor 10 does not necessarily need a frame structure to stiffen the biogas reactor 10 around the tank structure 13 defining and thus delimiting the reactor space 14, but this feature is provided by a tank structure solution forming thermal control means 16. The thermal control means 16 integrated in the tank structure 13 carry a large part of the load. With the invention, the tank structure 13 of the biogas reactor 10 itself acts as a heat exchanger. The two-layer structure provides even and well-controlled heating of the reactor 10. In this case, the biogas reactor 10 can be precisely controlled and regulated in terms of process technology (heating / reactor load). This is essential because even small fluctuations in the temperature of the reactor space 14 can, in a known manner, have an adverse effect on gas formation. Thanks to the structure, the temperature is more even. No cold / overheat spots form in the reactor 10. = 25 3 Figures 3 and 4 show an example of the tank structure 13 of the biogas reactor 10, in which, according to the invention, o also thermal control means 16 are formed to form the main part of the load-bearing structure of the tank 13. The container structure 13 has a hollow jacket 2 30 and thus also a two-layer structure. That is, the two-layer structure formed by the heat control means 16 in the tank structure 13 has a cavity space 39 for the heat transfer medium 27. In the cavity 39 formed inside it, for example, a liquid heat transfer medium 27 is circulated in order to influence the temperature of the reactor space 14 and thus of the organic substance 11 which can be accommodated therein.
    The thermal control means 16 are adapted to form a hollow tubular profile 20. This tubular profile 20 is arranged in a spiral arrangement by twisting an elongate tube 28 from the tubular profile 20 to form a reservoir structure 13 from a tubular profile having a tubular reactor space 14 inside the reservoir structure. Figure 5 shows the manufacture of the pipe 28, i.e. the tank structure 13, and Figure 6 shows the connection of the pipe profiles 20 to each other. In connection with the helical winding, the hollow pipe profile 20 ”is connected by its welding surfaces 49.1, 49.2 to a previously formed pipe structure 28 and a continuous pipe profile 20 connected to the in connection with. The end product of the manufacturing process is a tubular continuous elongate and dense structural wall in the form of a rotating body, in which the tubular profile = 25 20 is helically wound and thus connected to each other in an ascending or helical manner by their side walls 49.1, 49.2. o The pipe profile 20 withstands the load of the whole organic material 11> on the biogas reactor 10 alone, and there is no need for a separate actual body.
    The pipe profile 20 'is wound helically on the welding drum 43 as shown in Fig. 5 at the same time as the profile surfaces 49.1, 49.2 to be welded are heated, for example with hot air, to the desired temperature. The welding mass 41 is then extruded onto the heated profile surfaces
    49.1, 49.2 in two strands 47.1, 47.2, for example along each edge of the profile surface 49.1, 49.2 and the pipe profile parts 20 ', 20 coated with welding mass are pressed together by means of at least one pressing roller 42. The shaft of the pressure roller 42 is oriented radially with respect to the welding drum 43 so as to form a double weld seam 48 between adjacent turns of the pipe profile. Welding is performed by a welding head 40 located between two profile surfaces 49.1, 49.2 to be welded together. One skilled in the art will appreciate that this was just one example of a welding method for making tube 28. According to one embodiment, the hollow tube profile 20 has the shape of a main rectangle in cross section, as shown in Figures 3, 4 and 6. In the form of a rectangle, the tubular profile 20 is easy to connect from its side walls 49.1, 49.2 to each other, it has a sufficiently rigid profile and, in addition, it forms a flat inner surface on the side of the reactor space 14. In addition, openings for various joints can be easily made in the rectangular tubular profile 20, for example connections 19.1 = 25 to 19.3 for removing biogas 12 from the reactor space 14 and / or connections 26.1 to 26.4 for conducting the heat transfer medium 27 in and out E to form and in the longitudinal direction L of the biogas reactor 10 to a helically advancing cavity space> 39. Since the microbes are sensitive to rapid heat fluctuations, the good insulation / poor thermal conductivity of the plastic material 2 provides a uniform heat transfer to the organic material 11 now over a large area. In this case, the microbial strains remain as constant as possible and under favorable conditions. This is essential for the functionality and continuity of the process.
    The pipe profile 20 can also be understood as a hole profile. Thus, it is closed in its casing. In other words, it is not split in its longitudinal direction, for example, as is the case with a half-pipe profile. In this case, the connection of the pipe profiles 20 takes place from their side surfaces 49.1, 49.2.
    On the outer side of the tube 28 formed of the hollow tube profile 20
    The profile wall 25 22.2 comprises joints 26.1 to 26.4 arranged to guide the heat transfer medium 27 into the hollow tube profile 20 and / or to remove it from the hollow tube profile.
    20. Since the size of the biogas reactor 10 can be scaled in its longitudinal direction L, the number of heating connections 26.1 to 26.4 can also vary accordingly. The heating connections 26.1 to 26.4 are arranged on the outside of the pipe 28 formed of the pipe profile 20.
    22.2 in the middle of the profile wall 25.
    The gas connections 19.1 to 19.3 can be arranged between the pipe profiles 20 as shown in Figure 3. In addition, they extend through the double wall formed by the tube profile 20 to the reactor space S 14. While in the profile tubes 20 the gas connections 19.1 - = 25 19.3 do not impede the circulation of the heat transfer medium 27 in the hollow spaces 39 of the tube profiles 20. . >
    O DO 30 According to another embodiment, the gas connection can also be placed in the middle of the pipe profile 20 and one heating circuit on both sides of the gas connection, if necessary. In this case, the pipe profile 20 is intentionally blocked and the liquid acting as the heat transfer medium 27 flows in different directions. In this way, it becomes possible to control the heating of the biogas reactor 10 even more precisely and to optimize the temperature to suit, for example, each stage of the digestion. One commercially available example of such a hollow pipe profile 20 pipe product is a pipe marketed by Uponor Corporation under the trade name Weholite. Another commercially available example of such a hollow pipe profile 20 is a pipe marketed under the trade name Kennorol by Parkanon Muovituote Oy. Their use is known, for example, from civil engineering to conduct various waters. As one example of the material of such a pipe profile 20, a thermoplastic such as PE plastic can be mentioned. It is very easy and quick to machine, which is a manufacturing advantage. Another example is antistatic plastic.
    The use of a tube 28 made by such a method allows good scalability for the biogas reactor 10. The size of the reactor 10 can be easily scaled from a diameter of 0.5 m to> 6 m, in addition to the diameter, the length of the reactor 10 is easily adapted to the residence time of each customer's feed. Thus, with the invention, it becomes possible to dimension 3 and manufacture reactor spaces 14 in terms of their size (diameter / length) E to meet the needs of each end customer. Commercially, there are several different pipe sizes available to make this possible. The inner wall 23 of the tube 28 forming the tank structure 13 defining the reactor space 14 is substantially smooth, although the helicality of the tube profile 20 is still more or less visible in the form of a weld seam 48.
    According to one embodiment, the inner wall 23 can also be coated.
    This results in a smoother surface and greater material thickness.
    In this case, the tank structure 13 may include a coating 21 arranged on the side of the reactor space 14.
    It is also possible to speak of a liner arranged on the inner wall 23 arranged to define the tank structure 13 and the tubular reactor space 14. In this case, the coating 21 adapted to define the reactor space 14 is arranged against the inner wall 23.1 of the tube 28 formed of the hollow tube profile 20.
    The material thickness of the coating 21 can be 1 to 20 mm.
    The coating 21 may also be made of plastic.
    By coating 21, the reactor space 14 is made completely smooth in its walls.
    In other words, it does not show the profile tubes 20 and the welds 48 between them in the direction of the reactor space 14. However, the coating 21 is by no means necessary.
    Especially if the weld seam 48 between the profile tubes 20 itself is made very flat, whereby no significant discontinuities due to the weld seams 48 are formed on the inner wall 23 of the tube 28.
    points.
    However, the material strength and effect o of the liner or coating 21 is non-existent, for example in the diameter of the profile tube 20 itself and in particular in its tank structure 13 stiffening and = 25 thus load-bearing nature, so it has no significant overall structure stiffening effect and thus no significance for the biogas reactor 10 self-supporting. from the point of view of forming the tank structure 13, but most of it is formed specifically by a> helically wound profile tube 20, which is also used in the biogas reactor 2 30 10 for temperature control of the reactor space 14 and thus the organic material 11 to be placed there.
    The biogas reactor 10 is well insulated from the outside of the tank structure 13.
    Figure 7 shows a schematic example of a biogas reactor 10 according to the invention, its reactor space 14 now being equipped with stirring and, in addition, still with compartmentation.
    The biogas reactor 10 then comprises mixing means 15 adapted to act on the reactor space 14 for mixing the organic material 11 in the reactor space 14. In the embodiment shown, the mixing means 15 comprises a longitudinal rotation axis 30 of the reactor space 14 arranged in the reactor space 14. or similar bodies.
    The mixing means 15 mix the organic material 11 in the reactor space 14 in a set manner, for example to maintain the gas formation process.
    In this case, the stirring means 15, for example, mechanically decompose the organic material 11 so that it cannot form larger structural units, for example at the bottom of the reactor space 14.
    In addition, the trays also immerse the 2-layer material floating on the surface of the organic material 11.
    In other words, mixing means 15 are also used to homogenize the material 11.
    The biogas reactor 10 can be implemented even without stirring means 15. This is especially the case for long reactors 10. = 25 3 According to one embodiment, in addition to mixing, the mixing means 15 are also adapted to move the organic material 11 arranged in the reactor space o 14 forward in the longitudinal direction L of the reactor space 3 14.
    To accomplish this, the pallets 31 may have a slight rotation in the manner of, for example, aircraft propellers.
    In this case, they also act in the reactor space 14 to provide a flow to the organic material 11 and thus push it towards the outlet end of the reactor 14, which has an outlet. According to one embodiment, mixing can also be achieved by pumping. In connection with pumping, for example, organic material 11 can be recycled.
    As can be seen, for example, from Figures 1, 2 and 7, the tubular reactor space 14 may also be divided into two or more gas chambers 24.1 to 24.3. For this purpose, the tubular reactor space 14 can, for example, be partitioned to provide partitioning and thus separation of the chambers. The gas bulkheads 29.1 to 29.3 during bulkheading are arranged in the upper part of the reactor space 14, i.e. also in the chambers 24.1 to 24.3. Chambers 24.1 -
    24.3 can be used to measure gas formation at different stages of the process and the measured data are used to optimize the feed throughput time. The aim is then to maximize the load capacity of the reactor 10 and thus reduce the physical size of the reactor. By studying the rate of gas formation and the methane content of the gas 12 as the process progresses, it is possible to optimize the throughput time of the feed, i.e. the organic material 11, and optimize it to justify the feed rates of possible additives. It should be noted that the biogas reactor 10 can be implemented equally without compartmentation. The purpose of the bulkheads 29.1 to 29.3 may be, in addition to or instead of partitioning, also to strengthen the structure of the tank 13 itself. This is especially true for long reactors. On the other hand, the partitioning of the formation and removal of the gas 12 according to the application E according to the partitions 29.1 to 29n, for example, can be carried out in other types of reactors of the design principle of the tank 3 13. It 2 30 thus acts as an independent solution without being tied to any special - tank structure. Even then, thanks to compartmentation, it is possible to study the rate and gas concentration of gas formation. With the compartmentation shown in connection with the tank structure 13 according to the invention, for example by bulkheads 29.1 -
    However, an advantage is achieved in that the temperature of the reactor space 14 can be controlled by chambers 24.1 to 24n according to the tank structure according to the invention, and biogas generation can be carried out in the same single reactor structure in a single process step in a precisely controlled manner. That is, the compartmentation combined with the helically wound tank structure 13 to adapt it to operate while maintaining the temperature of the reactor space 14 together provides a particular advantage in controlling gas formation. Temperatures in different compartments can vary with the invention, and the structure providing such control is easy to implement with a helically wound spiral tube.
    For example, the dry matter content of the organic material 11 to be processed in the biogas reactor 10 is such that it is in a liquid form. In this case, it is also possible to speak of a thick liquid slurry or a liquid thickener. The organic matter 11 has been pretreated as finely as possible. Its piece size can be, for example, a maximum of 5 cm. As an example, the dry matter content of the organic material 11 is less than 35%. In this case, there is no need to equip the biogas reactor 10 with means for moving the organic material 11 forward in the reactor space 14 = 25, but its migration and also the exit from the reactor space 14 takes place naturally. x a © According to an embodiment, the bulkhead referred to above can be> arranged in the upper part of the reactor space 14 so that the chambers 24.1 - 2 24 24.3 are adapted to be separated from each other by bulkheads 29.1 - © 29.3. In addition to the bulkheads 29.1 to 29.3, the organic material 11 adaptable to the reactor space 14 can also be used to separate the chambers 24.1 to 24.3. In this case, the bulkheads 29.1 = 29.3 are adapted to be sealed by their live material 11 from their lower parts. For this purpose, the surface height of the organic material 11, i.e. the surface 11 'in the reactor chamber 14, can be adjusted so that the organic material 11 condenses in the bulkheads.
    29.1 to 29.3 against the forming surfaces. As a result, the chambers 24.1 to 24.3 arranged for the biogas 12 are separated from each other by the water trap principle. Thus, the gas sealing of the chambers 24.1 to 24.3 takes place with an organic material 11 extending beyond the lower edge of the bulkheads 29.1 to 29.3, thus providing such a gas seal. For measuring the level, the reactor space 14 has a sensor with at least one unit 33 in the tank structure 13.
    According to one embodiment, the blades 31 belonging to the mixing means 15 are arranged on the rotation shaft 30 at the bulkheads 29.1 to 29.3 at least during the partitioning of the reactor space 14. In this case, their purpose is not only to mix the material 11 but also to keep the surfaces of the bulkheads 29.1 to 29.3 clean on the scraper principle. The blades 31 chamfer the bulkheads 29.1 to 29.3 and thus clean them mechanically by rubbing. The length of the shaft 30 and / or the blades 31 can in turn be arranged so that the blades 31 also extend to the bottom of the reactor space 14 or S at least close to it.
    = 25 3 According to one embodiment, the feed, mixing and deposition prevention of the biogas reactor 10 can even be performed on the same shaft 30. In this case, the beginning of the shaft 30, i.e. the feed end of the biogas reactor> 10, can have a feed screw 32 as shown in Fig. 7. the organic material 11 is transferred to the reactor space 14. With such a structural solution it is possible, for example, to minimize the self-operating energy of the biogas reactor 10. In addition, fault sensitivity is reduced and better operational reliability is achieved.
    The container structure 13 may further comprise one or more further units 34.1 to 34.3 for the recycling of the organic material 11. One purpose of recycling may be to stabilize the process. Of these common 34.1 to 34.3, sampling and possible additional material can also be made.
    Figure 8 shows a rough schematic example of an thermal management circuit of a biogas reactor 10. Outside the biogas reactor 10, there may be, for example, an electric (gas) boiler 45, which is connected to the common 26.1 to 26.4 via pipelines connected to the heating log 46. Figure 8 also shows the flow directions of the fluids. The circuit is configured to direct the maximum amount of heating energy to the beginning of the biogas reactor 10, i.e. the feed addition end (In). The adjustment, in turn, is made by changing the rotational speed of the heat transfer medium 27. The aim is to keep the rest of the reactor 10 as uniform as possible. o According to another embodiment, the heat transfer circuit can also have 2 in terms of its input / output connections, for example as shown in the figure = 25 1. The input is common 26.2 and 26.4 and the output 3 is common 26.1 and 26.3. Thus, for example, the heat transfer liquid 27 introduced in 26.2 E is distributed on the inlet o and outlet side of the reactor 10 and the liquid discharged through 26.3 is> from both directions in the longitudinal direction of the reactor 10. By plugging 2 30 adjacent spaces together, for example with a degassing connection N, the inlet / outlet connections of the heat transfer medium can be arranged almost side by side.
    In the embodiment shown, the adjustment is as follows. From the community
    26.2 Introduce all heating fluid. 50% of the heating fluid is led out of the joint 26.1 and 25% of the heating fluid is led out of the joint 26.3 and 26.4. The temperature sensing of the biogas reactor 10 can be implemented, for example, as follows. Temperature sensors 51, 52 adapted to measure the temperature are arranged in a heating circuit on its way to the heating log 46 and separately to the return side to the collector log 50. In this case, all outlets 26.2 may have a common temperature measurement temperature measurement 55 at at least one point. When scaling the reactor 10 longer in the longitudinal direction L, there may also be several thermal measurement points inside the shaft 30. The circulation speed of the heating fluid 27 is suitable when the return heat and the temperature measured inside the shaft 30 are the same. Thus, the temperatures are compared. The circulation is kept so high that the flow temperature is only slightly higher, a maximum of 4 ° C. In the circuit of Fig. 8, a mixing valve 53 and a circulation pump 54 of the heating liquid 27 are also shown as accessories of the circuit. In addition to the biogas reactor 10, the invention also relates to a method = 25 for producing biogas 12. In the method, biogas 12 is produced from 3 organic materials 11 in a biogas reactor 10 under temperature control. The biogas reactor 10 is the biogas reactor described above. >
    In addition, the invention also relates to a process for producing a biogas reactor. The biogas reactor 10 is intended to produce biogas 12 from the organic material 11 in the tubular reactor space 14 formed by the tank 13 in a temperature-controlled manner. The tank 13 of the biogas reactor 10 is formed by a welded tube 28, in which a hollow tube profile 20 is helically wound in a helical arrangement to form a wall-forming tube 28. In fact, for long reactor structures, they can be supplied in parts or connected to each other, e.g. With threaded connections fitted to 28 ends. In this case, the threading of the pipe profile between the different parts may even change. The invention also relates to the use of a tube 28 made of a hollow tube profile 20 by a welding method and helically wound into a helical arrangement as a biogas reactor 10.
    As an example of the dimensions of the tank structure 13, a diameter of 1 m and a length of 5 m can be shown. One example of a pipe profile is its dimensions of 70 mm x 40 mm. The wall thickness of the pipe profile can be, for example, 4 to 8 mm. It is to be understood that the foregoing description and the accompanying drawings are intended only to illustrate the present invention. Thus, the invention is not limited solely to the embodiments set forth above or defined in the claims, but many different variations and modifications of the invention will be apparent to those skilled in the art which are possible within the scope of the inventive idea defined by the appended claims. 3 OF
    权利要求:
    Claims (15)
    [1]
    A biogas reactor, in which biogas (12) is adapted to be formed from organic material (11) and which biogas reactor (10) comprises - a tank structure (13), - a tubular reactor space (14) adapted to the tank structure (13), to which organic material (11) for generating biogas (12), - thermal control means (16) for influencing the temperature of the organic material (11) adaptable to the reactor space (14), - connections (17, 18) for supplying the organic material (11) to the reactor space (14) and removing from the reactor space (14), - one or more units (19.1 to 19.3) for removing biogas (12) from the reactor space (14), characterized in that the thermoregulatory means (16) are adapted to form a two-layer structure from the tank structure (13). a main part of the load-bearing structure of the tank structure (13) and having a cavity (39) for the heat transfer medium (27). o
    [2]
    Biogas reactor according to claim 1, characterized in that the thermal control means (16) are arranged to form a hollow tubular profile (20) formed in a helical arrangement by helically winding to form said tank structure (13) E from the tubular profile (20). o 2
    [3]
    Biogas reactor according to Claim 2, characterized in that the tank structure (13) is adapted to form a pipe (28) formed in connection with its helical winding from the pipe profile (20) by a welding method.
    [4]
    Biogas reactor according to Claim 2 or 3, characterized in that the hollow tube profile (20) has a main rectangular cross-section.
    [5]
    Biogas reactor according to one of Claims 1 to 4, characterized in that the tank (13) has a coating (21) arranged on the side of the reactor space (14) with a thickness of 1 to 20 mm and made of plastic.
    [6]
    Biogas reactor according to Claim 5, characterized in that the coating (21) is arranged against the profile wall (22.1) of the inner wall (23) of the tube (28) formed by the hollow tube profile (20).
    [7]
    Biogas reactor according to one of Claims 1 to 6, characterized in that the tubular reactor space (14) is partitioned.
    [8]
    Biogas reactor according to Claim 7, characterized in that the tubular reactor space (14) is divided into two or more chambers (24.1 to 24.3) by said partitioning. Biogas reactor according to claim 8, characterized in that the bulkhead is arranged in the upper part E of the reactor space (14) so that said chambers (24.1 to 24.3) are arranged to be separated from each other by bulkheads (29.1 to 29.3) into which the organic 3 the material (11) is adapted to be sealed. = 30
    [9]
    OF
    [10]
    Biogas reactor according to one of Claims 3 to 9, characterized in that the profile wall (25) on the outer side (22.2) of the tube (28) formed of the hollow tube profile (20) has connections (26.1 to 26.4) arranged to guide the heat transfer medium (27) into the hollow tube profile (20). ) and / or to remove from the hollow pipe profile (20).
    [11]
    Biogas reactor according to one of Claims 1 to 10, characterized in that mixing means (15) are arranged in the reactor space (14), comprising - a longitudinal (L) rotation shaft (30) arranged in the reactor space (14), - a rotation shaft (30) ) provided with radial (R) blades (31) of the reactor space (14), which, in addition to said agitation, are adapted to move the organic material (11) arranged in the reactor space (14) forward in the longitudinal direction (L) of the reactor space (14).
    [12]
    Biogas reactor according to Claim 11, characterized in that the blades (31) are arranged on the axis of rotation (30) at least at the bulkheads (29.1 to 29.3), which are adapted to provide partitioning of the reactor space (14), to hold the bulkheads (29.1 to 29.3). clean on a scraper basis. o
    [13]
    A method for producing biogas, wherein the biogas (12) S is produced from organic material (11) by a biogas reactor = 25 (10) in a temperature-controlled manner, characterized in that the biogas reactor (10) is a biogas reactor according to one or more of claims 1 to 12 E. o 2
    [14]
    A method of manufacturing a biogas reactor, which biogas surgeon (10) is intended to produce biogas (12) from organic material (11) in a tubular reactor space (14) formed by a tank structure (13) under temperature control,
    characterized in that said container structure (13) is formed from a pipe (28) made by a welding method, in which a hollow pipe profile (20) is arranged in a helical arrangement by helical winding.
    [15]
    Use of a tube (28) made of a hollow tube profile (20) by a welding method and helically wound into a helical arrangement as a biogas reactor (10).
    o
    O
    N +
    O
    I Jami a
    O +
    O 0
    O
    O
    OF
    类似技术:
    公开号 | 公开日 | 专利标题
    US10717684B2|2020-07-21|Biosolids digester and process for biosolids production
    US8715501B2|2014-05-06|Solid waste digestion system
    CN100573003C|2009-12-23|Double return journey barrel type drying machines
    CA2647043A1|2008-10-23|Apparatus for fermenting and drying at high speed
    FI129019B|2021-05-14|Biogas reactor and methods for producing biogas and manufacturing biogas reactor
    CN201096447Y|2008-08-06|Highly effective energy-saving drying-machine
    CN101216241A|2008-07-09|Three return journey barrel type drying machines
    CN201149411Y|2008-11-12|Three back-travel barrel type dryer
    EA031914B1|2019-03-29|Heat exchanger for low temperatures
    FI125284B|2015-08-14|A process for the production of biogas from biomass by anaerobic digestion and a corresponding reactor
    FI60853B|1981-12-31|ANORDER FOER FOERBAETTRING AV METANPRODUKTION VID ANAEROB ROETNING AV ORGANISKA SUBSTANSER
    CN204097478U|2015-01-14|A kind of dry method fermentation system
    CN201149412Y|2008-11-12|Bi-back-travel barrel type dryer
    CN202440466U|2012-09-19|Splitting decomposition system for waste plastics splitting and producing oil
    CN102921697B|2014-12-10|Multilayer pipeline type fermentation tower
    CN101144156B|2010-10-13|Sealing technique for plating oil pipe by nickel phosphorus
    FI129001B|2021-04-30|Reactor for producing biogas from biomass using anaerobic digestion
    WO2013006086A1|2013-01-10|Multi-functional biogas complex
    US20210292693A1|2021-09-23|Biogas production by means of multi-stage fermentation in a mono-tank
    CN111233530B|2022-01-14|Split type multi-section ventilation roller fermentation reactor and fermentation method
    FR2531601A1|1984-02-17|METHOD AND PLANT FOR PRODUCING BIOGAS FROM AN ORGANIC LIQUID EFFLUENT, SUCH AS FOR EXAMPLE THERMAL SLURRY AND HEAT EXCHANGER AS THE MEANS NECESSARY FOR THE IMPLEMENTATION OF SAID METHOD OR PLANT
    KR101342893B1|2014-01-06|Low-temperature carbonization of organic waste, the device
    JP6651555B2|2020-02-19|Heat exchanger
    CN216106967U|2022-03-22|Dry anaerobic fermentation device with partitioned stirring function
    CN210509310U|2020-05-12|Steam heat energy recycling device based on high-purity toluene rectifying tower
    同族专利:
    公开号 | 公开日
    WO2021089918A1|2021-05-14|
    FI129019B|2021-05-14|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    GB673075A|1949-04-12|1952-06-04|Dorr Co|Improvements in and relating to apparatus for the digestion or alkaline fermentation of organic material|
    AU4825490A|1988-12-13|1990-07-10|Josef Probst|Biogas reactor|
    WO2018103055A1|2016-12-09|2018-06-14|卓金星|Fermentation tank|
    法律状态:
    2020-04-09| PC| Transfer of assignment of patent|Owner name: VIIRU Owner name: KOLEHMAINEN |
    2020-10-09| PC| Transfer of assignment of patent|Owner name: BGCNORDIC OY |
    2021-05-14| FG| Patent granted|Ref document number: 129019 Country of ref document: FI Kind code of ref document: B |
    优先权:
    申请号 | 申请日 | 专利标题
    FI20195946A|FI129019B|2019-11-04|2019-11-04|Biogas reactor and methods for producing biogas and manufacturing biogas reactor|FI20195946A| FI129019B|2019-11-04|2019-11-04|Biogas reactor and methods for producing biogas and manufacturing biogas reactor|
    PCT/FI2020/050727| WO2021089918A1|2019-11-04|2020-11-04|Biogas reactor and methods for producing biogas and manufacturing biogas reactor|
    [返回顶部]