The invention concerns a biogas reactor, in which biogas is arranged to be formed from organic matter and which biogas reactor includes

- a wall arranged to form a tank structure,

- a tubular reactor space arranged inside the tank structure, in which the organic matter can be placed to form biogas,

- a hollow space for heat-transfer medium, in order to influence the temperature of the organic matter to be arranged in the reactor space,

- connections for feeding organic matter to the reactor space and removing it from the reactor space,

- one or more connections for removing biogas from the reactor space.

In addition, the invention also concerns methods for produc ing biogas and for manufacturing a biogas reactor.

Biogas is a gas arising in anaerobic conditions, the microbes of which are formed from organic matter. Biogas contains a great deal of methane, some carbon dioxide, and a small amount of sulphuric compounds.

The biogas process can be run at a psychrophilic (0 - 15 °C), mesophylic (15 - 45 °C), or thermophilic (50 - 75 °C) temper ature. These all have different bacterial strains. The pro cess is the more vigorous the higher its temperature. The usual temperature is mesophylic. Using it obtains good gas production and easy controllability. The gas is a renewable biofuel, which is most usually used to produce electricity and heat. In its properties, biogas is comparable to natural gas.

Biogas can be produced using biogas reactors, for which many different technical solutions have been developed. Reactors can be roughly divided into two basic types. These are com plete-mix and plug-flow reactors. Complete-mix reactors can, for example, operate and mix continuously. Material is then pumped into the reactor and the same amount is also removed from it, the amount of mass thus remaining constant. It has the advantages of automation of the feeds and a relatively constant gas production.

A plug-flow reactor is a type particularly suitable for dry materials. In it organic matter is arranged in a horizontally arranged elongated reactor space. The mass to be processed in the reactor space travels, in the order it is fed, as a plug flow through the process, at the same time forming gas. This achieves a nearly constant delay time for the mass. The plug flow is created in a tubular reactor. The mass is fed into one end of the reactor and discharged at the other end. New mass cannot mix with the old, so bacterial liquid collected from the process can be fed into the mass to accelerate and/or stabilize the process. Gas is removed, for example, from the reactor's upper part. The reactor space forms a jacket with the cross-sectional profile of, for example, a rotational piece. This is arranged to the reactor's frame structures, which are generally of metal.

Yet another reactor type is a batch reactor. This is filled and emptied at regular intervals. Its advantage is ease of handling during the process and its drawback a relatively slow start to gas production and it is also laborious to emp ty.

In Finland, biogas is often produced in large biogas plants at landfill sites and farms. The raw material is usually or ganic waste. Examples of this are waste from the foodstuffs industry, domestic biowaste, or manure. In developing coun tries, instead of that, reactors are typically small under ground tanks measuring a few cubic metres.

In biogas reactors, temperature control plays an essential part in the operability and control of the process. Taking the aforementioned into account, it is problematic to arrange heat-exchange means in connection with the reactor. Using the heat-exchange means, it should be possible to influence the process's temperature as precisely and effectively as possi ble, but nevertheless so that the structural solution remains simple, both to make and also to operate. In addition, the structural solution should be, for example, for logistical reasons, a light structure.

The present invention is intended to create a biogas reactor, which, thanks to its construction, can be process-technically precisely controlled and regulated. In addition, the inven tion is intended to create methods for producing biogas and for manufacturing a biogas reactor, owing to which biogas can be produce with light and economical structural implementa tions and additionally using improved logistics concerning, for example, the arrangement of a biogas reactor at a biogas production site. The characteristic features of the biogas reactor and methods according to the invention are stated in the accompanying Claims 1, 18, and 20. In the biogas reactor according to the invention, the wall arranged to form the tank structure is arranged to form of hollow pipe profile arranged in a spiral arrangement by heli cal winding, to form a double-layered structure from the wall forming the tank structure. In addition, the double-layered structure formed to the wall is arranged to form a hollow space for the heat-transfer medium. The tank structure is ar ranged to be formed from the pipe formed of pipe profile, for example, using a welding method in connection with its heli cal winding. Owing to the tank structure the reactor's pro cess technical controllability improves.

One important advantage of the spiral structure is that to the double-layered structure forming the wall of the tank structure will be formed, owing to the invention, a clearly defined flow channel. The heat-exchange medium circulating in the flow channel is thus forced, owing to the invention, to travel through the entire double-layered structure, i.e. the wall of the tank structure, and even more particularly through the heat-exchange structure formed by the spirally arranged pipe profile. The heat-transfer medium cannot then, for example, stratify anywhere in the double-layered struc ture, more generally in the wall of the tank structure. In stead it is forced to circulate in a controlled manner in terms of flow, defined in an ordered manner, through the en tire double-layered structure forming the tank structure and in that way to affect the tank structure throughout on every side of its large heat-exchange surface area, which according to the invention to the tank structure's wall is formed, for example, using rectangular pipe profile. Another important advantage is that, owing to the invention, the feed and/or the flow direction relative to the reactor space and the organic matter to be placed in it and to the progress of the process are well taken into account owing to the invention. In other words, owing to the invention it be comes possible to target and control the temperature effect on the correct point in terms of the reactor and thus the process stage. The temperature effect can then be said to be location dependent in the case of the reactor structure and thus also of the process stage. The feed of the heat-transfer medium to a specific location of the tank structure affects, starting from that point, a specific direction defined by the flow channel formed by the profile pipe in the reactor struc ture. This is an essential advantage in terms of the process regulation and its controllability. It makes the process con trol precise.

The biogas reactor according to the invention, and especially its tank structure, can be mainly of a plastic material. Thus, its material can be recycled and can recycle. It is al so light, durable, and is cheap to manufacture. It is corro sion-free, i.e. it neither rusts nor corrodes as a result of chemical reaction. The reactor's characteristic slippery sur face also prevents deposits from adhering to the reactor's surface. The reactor also has a very long service life.

In addition, being light the reactor is easy to transport to its operating site and is also rapid and easy to install. The light and rigid structure permits the reactor to be made ready in production facilities and also if necessary to be moved afterwards to another operating site. The biogas reactor's scalability also improves owing to the invention. The invention allows the achievement of cost- effectiveness in both the biogas reactor's manufacture and its operating costs (for example, own operation). Using a bi ogas reactor and method according to the invention, profita ble gas production is achieved relative to investment costs. Other characteristic features of the invention are stated in the accompanying Claims and additional achievable advantages are itemized in the description portion.

In the following, the invention, which is not restricted to the embodiments described it, is described in detail with reference to the accompanying figures, in which

Figure 1 shows a schematic diagram of one example of the bi ogas reactor seen in cross-section from the side,

Figure 2 shows an angled side view of the biogas reactor shown in Figure 1,

Figure 3 shows a simplified schematic diagram of the biogas reactor's tank structure, seen in partial cross- section from the side,

Figure 4 shows an example of the tank structure's wall structure in partial cross-section,

Figure 5 shows an example of the tank structure's manufac turing principle,

Figure 6 shows an example of the joining together of the profile pipe forming the double-layer structure of the tank structure,

Figure 7 shows a schematic example of the biogas reactor shown in Figures 1 and 2, with its reactor space now equipped with mixing, Figure 8 shows a rough schematic diagram of an example of the biogas reactor's heat-control circuit, and Figure 9 shows schematically one way to arrange the gas and heat-transfer medium connections in the tank struc ture 's wall.

Figure 1 shows a schematic diagram of one example of the bio gas reactor 10, seen from the side and in cross-section. For its part, Figure 2 shows an angled side view of the biogas reactor 10 of Figure 1, with the tank structure 13 transpar ent. The biogas reactor 10 is intended to form biogas 12, more generally gas, from organic matter 11. The organic mat ter 11 can also be called biomass. Examples of this are all kinds of organic waste, such as, for example, manure, waste water, and industrial reject fractions. Of course the organic matter 11 need not necessarily be waste at all, but can be, for example, grown specifically for gas production.

To form biogas 12, the biogas reactor 10 includes a reactor space 14, in which the organic matter 11 can be placed to form biogas 12. The reactor space 14 is arranged to form a tank structure 13. The reactor space 14 is now a horizontally elongated, i.e. tubularly formed, cylindrical space. The cy lindrical space is now defined by a wall 35 arranged to form the tank structure 13. The organic matter 11 is fed to the reactor space 14 as feed (In) and correspondingly also re moved from it (Out). Thus, the organic matter 11 also pro gresses in the reactor space 14 at the same time as biogas 12 is formed from it, for example, in as such known processes. The biogas reactor 10 thus also includes connections 17, 18 for feeding the organic matter 11 into the reactor space 14 and for removing the organic matter 11 from the reactor space 14. The organic matters 11 can be fed from a feed connection 17', which can be in the vicinity of the reactor's 10 end 38.1. One or more of the connections, such as, for example, the outlet connection 18, can be implemented, for example, also in the form of a pump. The biogas reactor 10 can be, in its operating principle, for example, a plug-flow reactor. The feed / removal is sought to be implemented as the most even flow possible, so that the process conditions remain as even as possible.

Further, the biogas reactor 10, more particularly its tank structure 13, includes one or more connections 19.1 - 19.3 to take the biogas 12 formed in the reactor space 14 out from the reactor space 14 and thus from the biogas reactor 10. The biogas 12 arising as a result of, for example, the anaerobic decomposition of the organic matter 11, is collected through the connections 19.1 - 19.3. Biogas 12 recovery means (not shown) are attached to the connections 19.1 - 19.3.

The anaerobic decomposition can also be termed the digestion of the organic matter 11. This is the decomposition of the organic matter taking place in anaerobic conditions. Anaero bic micro-organisms are responsible for the digestion. The products arising from the digestion are mainly solids corre sponding to humus, water, carbon dioxide, and methane gas that can be utilized, for example, in energy production. The methane content of the biogas arising in the digestion pro cess is, for example, 50 - 70 %. In digestion, nitrogen com pounds reduce to ammonia and sulphur compounds to hydrogen sulphide. The digestion process can comprise four as such known main stages: hydrolyzation, acid fermentation, aceto- genesis, and methanogenesis. The biogas reactor 10 also includes heat-regulation means 16 for influencing the temperature of the reactor space 14 and even more particularly of the organic matter 11 to be placed in the reactor space 14. One can also speak of the reactor space 14 being arranged to be temperature regulated, i.e. of the reactor heating. The heat-regulation means 16 are ar ranged, in terms of heat exchange, in connection with the re actor space 14 in such a way that they can be used to either heat the material in the reactor space 14 and/or cool it. Thus, a change of state aimed at the heat-regulation means 16 also affects the reactor space 14 and the organic matter 11 placed in it, either heating or cooling it. Generally, heat ing or cooling, more generally the heat-regulation means 16 are intended to maintain the reactor space's 14, and thus al so the organic matter's 11 temperature within the specific optimal limits for gas formation. Thus, affecting the temper ature during the digestion process itself can be understood as maintaining the temperature.

By the heat-regulation means 16, more generally the reactor heating, is arranged to be formed, of the tank structure 13 of the biogas reactor 10 a double-layer structure of the wall 35 of the tank structure 13 seen in Figure 1 and particularly in Figure 3, for forming the hollow space 39 for the heat- transfer medium 27. The double-layer structure of the wall 35 of the tank structure 13 formed as the heat-regulation means 16 can then form most of the tank structure's 13 load-bearing structure. In other words, the heat-regulation means 16 are then integrated, i.e. built into the tank structure 13 of the biogas reactor 10 i.e. into its wall 35. Thus, the biogas re actor's 10 reactor space 14, and equally also the outside of the tank structure 13, can be free of the heat-regulation means 16. In the reactor space 14 the heat-regulation means 16 would dirty and outside the tank structure 13 they would hinder, for example, the possible insulation of the biogas reactor 10. Integrating the heat-regulation means 16 in the tank structure's 13 wall 35 and especially inside the wall 35 simplifies the biogas reactor's 10 construction.

The heat-regulation means 16 belonging to the tank structure 13 are arranged to form an essential part of the biogas reac tor's 10 frame to stiffen it and thus also to make it self- supporting. The biogas reactor 10 will then not necessarily need at all around the tank structure 13 that defines and de limits the reactor space 14 a frame structure stiffening the biogas reactor 10, instead this property is created using the tank-structure solution formed by the heat regulation means 16. The heat-regulation means 16 integrated in the tank structure 13, i.e. the wall 35 itself, carry most of the load. Owing to the invention the biogas reactor's 10 tank structure 13 and more particularly the tank structure's 13 wall 35 itself acts as a heat exchanger. Using its double layer structure the tank structure's 13 wall 35 provides even and well-controlled reactor 10 heating. The biogas reactor 10 is then process-technically precisely controllable and regu- latable (heating / reactor's loading). This is important, as even small swings in the reactor space's 14 temperature can cause in a known manner an unfavourable effect of gas for mation. Thanks to the construction, the temperature is more even. Cold / very hot points do not form in the reactor 10.

Figures 3 and 4 show an example of the biogas reactor's 10 tank structure 13, in which heat-regulation means 16 are also integrated, according to the invention. The heat-regulation means 16 can also be said for form most of the tank's 13 load-bearing structure. The tank structure 13, particularly the wall 35 it forms, has a hollow jacket and thus also a double-layer structure. In other words, in the double-layer structure formed by the wall 35 in the tank structure 13 is a hollow space 39 for the heat-transfer medium 27. For example, a liquid heat-transfer medium 27 is circulated in the hollow 39 formed inside the wall 35, to affect the temperate of the reactor space 14 and thus of the organic matter 11 to be placed in it.

Stated more generally, the biogas reactor's 10 heat- regulation means 16 are arranged to form from hollow pipe profile 20. This pipe profile 20 is arranged in a spiral ar rangement by helically winding an elongated pipe 28 of pipe profile 20 to form from the pipe profile 20 the tank struc ture's 13 wall 35, inside which tank structure 13 is the tub ular reactor space 14. Thus, the heat-regulation means 16 are not, for example, in the reactor space 14, where they could dirty. Thus, the reactor space 14 is unobstructed in the case of the heat-regulation means 16. Owing to the invention, the hollow space 39 can also be said to be divided thanks to the pipe profile 20 arranged spirally arrangement, sin which the heat-transfer medium 27 circulates along the channel arranged for it by the pipe profile 20. The channel winds throughout the entire length L of the tank structure 13 and thus also of the reactor space 14 inside it, acting on it in every direc tion. Here, the division of the hollow space 39 refers to its division to profile pipes parallel consecutively, according to the pitch defined by the spiralling pipe profile 20, in the reactor tank's 13 longitudinal direction L. In other words, in the reactor tank's 13 longitudinal direction L, the hollow space 39 is not unified, but winds around reactor space 14, rising in the reactor's 10 longitudinal direction

L.

Figure 5 shows the manufacture of the tube 28, i.e. the tank structure 13 and Figure 6, for its part, the joining of the pipe profiles 20 to each other, as some possible embodiments. In it, during the helical winding, the hollow pipe profile 20' is joined on its side surfaces 49.1, 49.2 by a welding method to the already previously formed tubular structure 28. The joining takes place to the side surface 49.2 of the con tinuous pipe profile 20 joined in a corresponding manner to the tubular structure 28. As a result of the joining, a wall 35 of the tank structure 13 and heat-transfer-medium channel is formed for the biogas reactor 10 from the pipe profile 20. Thus, the tube 28 is formed from the pipe profile 20 by the welding method, in connection with its helical winding. Ac cording to one embodiment, the pipe profile 20' can be made immediately before, for example, its helical winding and joining to the tubular structure 28, for example, by extru sion or some other corresponding method. Ready pipe profile 20' can also be discharged from a reel to be wound helically to form the tubular structure 28. The result of the manufac turing process is a tubular continuous elongated and tight structural wall 35 in the form of a solid of revolution. In it the pipe profile 20 is helically wound and thus joined with a rise, i.e. spirally, to each other by their side walls 49.1, 49.2 thus forming a double-layer spiral structure for the tank structure's 13 wall 35. According to one embodiment, the tank structure 13 formed from pipe profile 20 will alone withstand the entire loading cause by the organic matter 11 on the biogas reactor 10. There will then be no need for a separate load-bearing frame to be arranged around the tank structure 13.

According to the example shown, the pipe profile 20' is wound, as shown in Figure 5, helically onto a welding drum 43, at the same time as the profile surfaces 49.1, 49.2 to be welded together are heated to the desired temperature, for example, using hot air. After this, the welding mass 41 is, for example, 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 with the aid of at least one press roll 42. The press roll's 42 shaft can be aligned radially relative to the welding drum 43, so that a double welding joint 48 is formed between adja cent pipe-profile rounds. Welding is performed, for example, using a welding head 40, which can be between the two profile surfaces 49.1, 49.2 to be welded together. One skilled in the art will understand that this is only one example of a method to make the tube 28, which is now based on welding.

According to one embodiment, the hollow pipe profile 20 has, according to Figures 3, 4, and 6 a mainly rectangular cross- sectional shape. Having a rectangular shape, the pipe pro files 20 are easy to attach to each other by their side walls 49.1, 49.2. In addition, in its profile it is sufficiently rigid and it also forms a flat inner surface to the side of the reactor space 14. In addition, openings can be easily made in the rectangularly shaped pipe profile 20 for various connections, which are, for example, connections 19.1 - 19.3 for removing biogas 12 from the reactor space 14 and/or con- nections 26.1 - 26.4 for leading heat-transfer medium 27 into and out of the hollow space 39 formed by the pipe profile 20 and progressing helically in the longitudinal direction L of the biogas reactor 10. Because microbes are sensitive to rap id changes in temperature, the plastic material's good insu lation / poor heat transmission now create an even heat transfer to the organic matter 11 over a large surface area. The microbe strains then remain at the most even temperature and in the most favourable conditions as possible. This is essential for the operation of an unbroken process. Thus, the biogas reactor 10 according to the invention permits biogas 12 to be produced better also by using the thermophilic pro cess thanks to good controllability and precise heating.

The pipe profile 20 can also be seen as a perforated profile. It is thus closed from the jacket. In other words, it is not divided longitudinally from the jacket, such as, for example, is the case with a half-pipe profile. The attachment of the pipe profiles 20 to each other then takes place from their side surfaces 49.1, 49.2.

The profile wall 25 on the outside 22.2 of the tube 28 formed from hollow pipe profile 20 includes connections 26.1 - 26.4 arranged to lead the heat-transfer medium 27 to the hollow pipe profile 20 and/or to remove it from the hollow pipe pro file 20, more generally, from the wall 35 of the tank struc ture 13. Because the size of the biogas reactor 10 can be scaled in its longitudinal direction L, the number of heating connections 26.1 - 26.4 can vary accordingly. The heating connections 26.1 - 26.4 are arranged in the middle of the profile wall 25 on the outside 22.2 of the tube 28 formed from pipe profile 20. According to a first embodiment, the gas connections 19.1 - 19.3 can have been arranged, as shown in Figure 3, between the pipe profiles 20. Thus, they are then in the area of two adjacent pipe profiles. In addition, they extend through the double wall 35 formed by the pipe profile 20 into the reactor space 14, to lead gas out of the reactor space 14. Being be tween the pipe profiles 20, the gas connections 19.1 - 19.3 do not prevent the circulation of the heat-transfer medium 27 in the hollow spaces 39 of the pipe profiles 20, i.e. in the spiral heat-transfer-medium channel formed by the pipe pro file 20 on the tank structure's 13 jacket, as the gas connec tions 19.1 - 19.3 do not block the entire pipe profile 20.

According to yet another embodiment, the gas connection 19 can, if necessary, also be placed in the centre of the pipe profile 20 and the heating circulation connections 26.1, 26.2, for example, on both sides of the gas connection 19 in the pipe profile's 20 winding direction. Figure 9 shows sche matic example of this. The pipe profile 20, and thus also its heat-medium circulation to be arranged inside, are then in tentionally blocked by the gas connection 19. For their part, the heat circulation connections 26.1, 26.2 are then arranged before the gas connection 19 and after the gas connection 19, in the direction of winding of the pipe profile 20.

The arrangement permits many different possibilities for leading the liquid acting as the heat-transfer medium 27. The heating zones A, B can be connected consecutively in series or partitioned to form their own circuit, such as, for exam ple, Figure 9 shows. When the gas connection 19 acts as a di vider, in the reactor's 10 longitudinal direction L, of the hollow space 39 arranged helically, the heat-transfer medium 27 can be led, for example, in opposite directions in the re actor's 10 longitudinal direction L. Then both of the connec tions 26.1, 26.2 are feeds of the heat-transfer medium 27. On the other hand, the heat-transfer medium 27.1, 27.2 should then possibly be led, in the reactor's 10 longitudinal direc tion L, also in such a way that heating is performed in stag es in the reactor's 10 longitudinal direction L, precisely as shown in Figure 9. In other words, one heating zone A can then end at gas connection 19 in the reactor's 10 longitudi nal direction L and the following, second heating zone B can start after gas connection 19. In this way, the biogas reac tor's 10 heating can be controlled even more precisely and optimized the temperature correctly, for example, to suit each digestion stage. At one site, it can suffice for the heating liquid 27 to be led into the reactor 10 at one end and out at the other. At some other site, it can be necessary to regulate the optimal temperatures according to the various anaerobic decomposition stages (hydrolysis / acidogenesis / acetogenesis / methanogenesis), i.e. to divide the reactor 10 into as many as four different heating zones in its longitu dinal direction L. More generally, according to the embodi ment shown one or more of the connections 19 for removing bi ogas 12 from the reactor space 14 are arranged to close the pipe profile 20 to divide the spiral hollow space 39 arranged to form in it into heating zones A, B.

One commercially available example of a pipe product made from hollow pipe profile 20 is Uponor Ltd's pipe marketed un der the trade name Weholite. Another commercially available example of a pipe product made from such a hollow pipe pro file 20 is the pipe marketed under the trade name Kennorol by Parkanon Muovituote Ltd. Their use is known, for example, from water draining in earthworks.

An example of such a pipe-profile 20 material is a thermo plastic suitable for the purpose, such as, for example, poly ethylene (PE) or polypropylene (PP). The pipe profile 20 of plastic material can also contain fibre reinforcement. It is very easily and rapidly machinable, which is a manufacturing- technical advantage. Yet another example of plastic can also be an antistatic plastic. A biogas-reactor 10 of plastic ma terial, for example, PE plastic, will also withstand addi tives possibly used in biogas 12 production, if it is wished to improve production with additives. Some examples of these are lye, baking soda, or trace elements.

Thanks to the use of a tube 28 made using, for example, the method described above, it is possible to give the biogas re actor 10 good scalability. The size of the reactor 10 is eas ily scalable, for example, from a diameter of 0.5 m up to 6 metres. In addition to the diameter, the length of the reac tor 10 can easily be changed, for example, according to the delay time of each customer's feed. Thus, owing to the inven tion it is possible to dimension and make reactor spaces 14 corresponding in their size (diameter/length) to each custom er's requirements. There are several different pipe sizes commercially available that permit this.

The inner wall 23 of the tube 28 forming the tank structure 13 defining the reactor space 14 can be formed on the profile wall 22.1 of the pipe profile 20 on that side. The inner wall 23 itself is mainly smooth, though the spiral nature of the pipe profile 20 may nevertheless be more or less visible in the form of the welding seam 48. In Figure 4, the seams are shown exaggeratedly slightly protruding, to illustrate them. The tube's 28 inner wall 23 does not necessarily require spe cial coating, instead the material of the pipe profile 20 and thus the tubular structure 28 formed of it will withstand, for example, challenging process conditions and possible ad ditives, being of, for example, PE plastic. This also helps to improve heat transfer, because extra intermediate layers between the hollow space 39 and the reactor space 14 are not needed.

On the other hand, the reactor space 14, i.e. the tubular structure's 28 inner wall 23 can, however, also be equipped with sheathing, for example, to improve its wear resistance. One possibility is to coat the inner wall 23 of the tube 28 forming the tank structure 13, at least part over the reactor space 14, for example, to improve its wear resistance, if foreign substances are mixed with the organic matter 11. The reactor space 14 then gains a smoother surface and also a greater material thickness. The coating 21 or more generally the sheathing can be on at least part of the tank structure's 13 inner wall 23. It can then be in the lower part of the re actor space 14 and can cover, for example, 20 - 70% of the inner wall's 23 circumference. One purpose of the coating 21 can be to prevent damage to the inner wall 23, as there can be, for example, foreign objects in the organic matter 11.

Sheathing can also be implemented, instead by coating, for example, by one or more wear plates. These can be arranged on the inner wall 23 of the tube 28 forming the tank structure 13 and arranged to define the tubular reactor space 14. The coating 21 or wear plate arranged to define the reactor space 14 is arranged against the profile wall 22.1 of the pipe pro file 20, which is arranged to form the tube's 28 inner wall 23. The thickness of the coating 21 or more generally the sheathing 21' can be 1 - 20 mm, depending on its material. The coating 21 or more generally the sheathing 21' can also be of a plastic material. The coating 21 can also be used to increase the smoothness of reactor space's 14 walls. In other words, the profile pipes 20 in the direction of the reactor space 14 and the welding seams 48 between them are then not seen at all, at least to any substantial extent. The coating 21 or more generally sheathing 21' is, however, in no way es sential, as the welding seam 48 between the profile pipes 20 is itself already very smooth, so that no substantial discon tinuities, such as ridges or valleys, form on the tube's 28 inner wall 23.

The sheathing's 21' or coating's 21 thickness has, however, no effect on the profile pipe's 20 diameter and particularly on the stiffening and thus load-bearing nature of the tank structure 13. In other words, it has no essential effect in stiffening the overall structure and thus also no signifi cance on the biogas reactor 10, for example, in terms of forming the self-supporting tank structure 13. Most of it is formed using a helically wound profile pipe 20, which in the biogas reactor 10 is also used as a means of temperature reg ulating of the reactor space 14 and thus of the organic mat ter 11 to be placed in it. The biogas reactor 10 is well in sulated by insulation of the outside of the tank structure 13. The insulation is arranged, for example, directly on the surface of the tank structure 13, i.e. of the tube 28 it forms. The biogas reactor 10 can also be equipped with a base 37. Figure 7 shows a schematic example of one biogas reactor 10 according to the invention, its reactor space 14 being now also equipped with mixing and, in addition, in this case now also with partitioning. The biogas reactor 10 then includes mixing means 15 arranged to act on the reactor space 14 to mix the organic matter 11 in the reactor space 14. The mixing means 15 include, in the embodiment shown in the figure, a rotation shaft 30 arranged in the reactor space 14 in the re actor space's 14 longitudinal direction L. Blades 31, wings, or similar mixing elements are arranged to the rotation shaft 30 in the radial R direction of the reactor space 14. The mixing means 15 are used to mix the organic matter 11 in the reactor space 14 in a set manner, for example, to maintain the gas-forming process. The mixing means 15 then, for exam ple, disperse the organic matter 11 mechanically, so that it cannot form larger lumps, for example, on the bottom of the reactor space 14. In addition, the blades also submerge 2- layer material that may be floating on the surface of the or ganic matter 11. In other words, the mixing means 15 are also used to homogenize the matter 11. The biogas reactor 10 can also be implemented even without the mixing means 15. This is particularly the case in long reactors 10.

According to one embodiment, the mixing means 15 are arranged to also move the organic matter 11 placed in the reactor space 14 forwards in the reactor space's 14 longitudinal di rection L. To implement this the blades 31 can be slightly twisted, like, for example, aircraft propellers. They then also act to create a flow in the organic matter 11 in the re actor space 14 and thus to push it towards the reactor's 14 outlet end 38.2, in which there can be an outlet opening. Ac- cording to one embodiment, possible mixing can also be achieved by pumping with one or more pumps. During pumping the organic matter 11 can be, for example, circulated.

As can be seen, for example, from Figures 1, 2, and 7, the tubular reactor space 14 can also be partitioned into two or more gas chambers 24.1 - 24.3. For this purpose, the reactor space 14 can be, for example, partitioned by bulkheads to separate the chambers from each other. Gas bulkheads 29.1 - 29.3 creating partitioning are arranged in the upper parts of the reactor space 14, i.e., also of the chambers 24.1 - 24.3. They can be, for example, welded onto the inner wall 23. With the aid of the chambers 24.1 - 24.3 the gas-forming can be measured in the various stages of the process and the feed's through-put time optimized with the aid of the measured data. The aim is then to maximize the reactor's 10 loading and thus to reduce the reactor's physical size. By studying the speed of gas formation and the gas's 12 methane content as the pro cess progresses, the feed, i.e. the through-put time of the organic matter 11, as well as the feed amounts of possible additives can be optimized.

It should be noted that the biogas reactor 10 can equally al so be implemented without the partitioning described. In ad dition to or instead of partitioning, the bulkheads 29.1 - 29.3 can also be intended to reinforce the construction of the tank 13 itself. This is particularly the case in long re actors. On the other hand, the partitioning, for example, by bulkheads 29.1 - 29.n of the gas 12 forming and removal as described in the present application can also be used to im plement of the tank's 13 structural principle in other kinds of reactors. Thus, it can act as its own independent struc- tural solution without being bound to any particular tank structure, such as, for example, the honeycomb structure wall 35 of the tank 13 according to the invention. Then too the partitioning allows the speed and gas content of the gas for mation to be studied. The partitioning described in connec tion with the tank structure 13 according to the invention, for example, using bulkheads 29.1 - 29.3 however achieves an advantage in the sense that the reactor space's 14 tempera ture can be regulated, thanks to the tank structure according to the invention, by chamber 24.1 - 24.n and in that way the biogas formation can be performed in the same one reactor structure as single process stage precisely controlled by partition. In other words, the partitioning combined with the tank structure 13 formed by helical winding to adapt it to operate to maintain the reactor space's 14 temperature in a controlled manner, together achieve a particular advantage in terms of the control of the gas formation. Owing to the in vention, the temperatures can vary in different partitions and a structure to achieve their regulation can be easily im plemented by a helically wound spiral pipe structure.

The solids content of the organic matter 11 to be processed in the biogas reactor 10 can be, for example, such that it is in a fluid form. One can then also speak of a viscous fluid sludge, or a fluid viscous mass. The organic matter 11 is pre-processed to be as fine as possible. Its particle size can be, for example, a maximum of 5 cm. An example of the solids content of the organic matter 11 is less than 35 %. There is then not necessarily any need to equip the biogas reactor 10 with means to move the organic matter 11 forwards in the reactor space 14, instead its movements, and exit from the reactor space 14 takes place by itself. Thsse mixing means' 15 function can thus also be purely mixing without a special transfer function. The pump can operate for either or both of those purposes.

According to one embodiment, the bulkheads referred to above can be arranged to the upper part of the reactor space 14 in such a way that the chambers 24.1 - 24.3 are arranged to be separated from each other by the bulkheads 29.1 - 29.3. In addition to the bulkheads 29.1 - 29.3, the organic matter 11 to be placed in the reactor space 14 can also be used to sep arate the chambers 24.1 - 24.3 from each other. The organic matter 11 is then arranged to be sealed to the lower parts of the bulkheads 29.1 - 29.3. For this purpose, the organic mat ter's 11 surfaces height, i.e. surface 11' in the reactor space 14 can be arranged in such a way that the organic mat ter 11 seals against the surfaces formed by the bulkheads 29.1 - 29.3. Thanks to this the chambers 24.1 - 24.3 arranged for the biogas 12 are separated from each other on the water- trap principle. Thus, the chambers' 24.1 - 24.3 gas seal takes place by the organic matter 11 exceeding the lower edge of the bulkheads 29.1 - 29.3, which thus creates the relevant gas seal. To measure the surface height, there is sensoring in the reactor space 14, for which there is at least one con nection 33 in the tank structure 13.

According to one embodiment, blades 31 belonging to the mix ing means 15 are arranged to the rotation shaft 30 at least at the locations of the bulkheads 29.1 - 29.3 creating the partitioning of the reaction chamber 14. In addition to mix ing the matter 11, their purpose is also then to keep the bulkheads' 29.1 - 29.3 surfaces clean using the wiper princi ple. The blades 31 sweep over the bulkheads 29.1 - 29.3 and thus clean them mechanically by wiping. 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 reactor space's 14 bottom or at least close to it.

According to one embodiment, the biogas reactor's 10 feed, mixing, and layering-prevention can be done even using the same shaft 30. At the start of the shaft 30, i.e. at the bio gas reactor's 10 feed end, there can then be a feed screw 32, as shown in Figure 7. It is used to move the organic matter 11 into the reactor space 14. By such a structural solution, the biogas reactor's 10 internal-load energy can be mini mized, for example. In addition, fault sensitivity is reduced and improved operating reliability is achieved.

In the tank structure 13 there can be in addition one or more connections 36.1 - 36.4 for circulating the organic matter 11 (Figure 2). One purpose of circulation can be to stabilize the process. Sampling and possible additive dosing can also be carried out from these connections 36.1 - 36.4.

Figure 8 shows a rough schematic diagram of one example of the biogas reactor's 10 heat-control circuit. Outside the bi ogas reactor 10 there can be, for example, an electrical(gas) boiler 45, which is connected to the connections 26.1 - 26.4 by means of the pipelines connected to the heating tube 46. Figure 8 also shows the flow directions of the liquids. The circuit is formed in such a way that it is arranged to guide a large amount of heating energy to the biogas reactor's 10 starting end, i.e. to the feed-adding end (In). Regulation takes place in turn by altering the heat-transfer medium's 27 circulation velocity. The end part of the reactor 10 is sought to be kept at as even a temperature as possible.

According to another embodiment, the heat-transfer circuit can also be, for example, like that shown in Figure 1, in the case of its inlet / outlet connections. The inlet is from connections 26.2 and 26.4 and the outlet, in turn, from con nections 26.1 and 26.3. Then, for example, the heat-transfer liquid 27 led in from the connection 26.2 divides to the re actor's 10 inlet and outlet sides and the liquid outlet through connection 26.3 is from both directions in the reac tor's 10 longitudinal direction L. By plugging the gap be tween two adjacent connections, for example, by the gas re moval connection 19, the heat-transfer-medium's 27 in let/outlet connections can be arranged nearly next to each other, as shown in Figure 9.

In the embodiment shown in Figure 8, regulation can be, for example, as follows. All the heating liquid is led in from connection 26.2. 50 % of the heating liquid is led out from connection 26.1 and 25 % of the heating liquid is led out from each of connections 26.3 and 26.4. The division can be created, for example, through the size of connections 26.1, 26.3, 26.4. In the same time, more liquid can be released from the larger connection 26.1 on the inlet side of the re actor space 14 relative to the inlet connection 26.2, than is released from the smaller connections 26.3, 26.4 on the out let side of the reactor space 14 relative to the inlet con nection 26.2. In other words, the liquid then remains longer in the reactor's 10 latter half relative to inlet connection To state the aforesaid regulation example even more general ly, at least one connection 26.2 of the connections is the heat-transfer medium's 27 inlet feed, which is arranged to lead the heat-transfer medium 27 into the hollow pipe profile 20. In this case, the feed takes place to the biogas reac tor's 10 central area. One or more of the connections 26.1, 26.3, 26.4 are, in turn, outlets arranged to remove the heat- transfer medium 27 from the hollow pipe profile 20 before and/or after at least one inlet feed. In addition, at least one connection 26.1 of the outlet feeds is arranged before the inlet feed and one or more of connections 26.3, 26.4 are arranged after the inlet feed. Further, at least one of the outlet connections 26.1, being now before the inlet feed, is arranged to be removed more heat-transfer medium 27 than the individual connections 26.3, 26.4 after the inlet feed.

The temperature sensoring of the biogas reactor 10 can be im plemented, for example, as follows. Temperature sensors 51, 52, arranged to measure temperature, are arranged in the heating circulation on its inlet side in a heating manifold 46 and separately on its return side in a collector manifold 50. There can then be a common temperature measurement for all the inlet connections 26.2 and correspondingly a common measurement for the return side in the header tube 50. Inside the mixing shaft 30 too there can also be its own temperature measurement 55, at least at one point. When scaling the reac tor 10 to be longer in the longitudinal direction L, there can also be several temperature-measurement points inside the shaft 30. The circulation velocity of the heating liquid 27 is suitable if the return heat and the temperature measured inside the shaft 30 are as close as possible to each other. Thus, the temperatures are compared. The circulation is kept large enough that the inlet temperature is only slightly greater, at a maximum of, for example, 4 °C. This is influ enced by the reactor's size class. In the circuit of Figure 8, a mixing valve 53 and a heating-liquid 27 circulation pump 54 are also shown as circuit accessories.

In addition to a biogas reactor 10, the invention also con cerns a method for producing biogas 12. In the method, biogas 12 is produced from organic matter 11 using a biogas reactor 10 in a temperature-regulated manner. The biogas reactor 10 is the biogas reactor described above.

Further in addition, the invention also concerns a method for manufacturing a biogas reactor 10. The biogas reactor 10 is intended to produce biogas 12 in a temperature-regulated man ner from organic matter 11 in a tubular reactor space 14 formed by a tank 13. The biogas reactor's 10 tank 13 is formed by a tube 28 made by a welding method, in which hollow pipe profile 20 is arranged by helical winding in a spiral arrangement to form a wall 35 for the tube 28 being made. In this context, the term welding method refers to the pipe pro files 20 being joined together by their side walls 49.1, 49.2, for example, by heating, or some other possible manner of attachment. The side walls 49.1, 49.2 of the pipe profiles 20, or the material arranged between them, then melt, the pipe profiles 20 then attach to each other by their side walls 49.1, 49.2 and when cooled are joined to each other. Thus, welding can also be understood as the gluing of the pipe profiles 20 to each other by their side walls 49.1, 49.2, for example, with the aid of heat. In addition, in the method the tube 28 is equipped with connections for forming biogas 12, which are at least one gas connection 19 and one or more connections 26.1 - 26.4 for a heat-transfer medium 27.

Really long reactor structures can be delivered to the oper ating site, for example, in parts and joined together, for example, by hot welding or by screw connections arranged to the ends of the tubes 28. The handing of the helical nature of the pipe profile 20 can then even vary between different parts forming the tank structure 13. Flange connection is al so one alternative for joining parts to each other.

A reactor tank 13 formed of plastic material is economical also in terms of arranging the connections 19.1 - 19.3, 26.1 - 26.4. Holes can be drilled in the reactor tank 13 at the desired location for a connection, to which the connection is then screwed, for example, on the machine-screw principle, i.e. without a separate thread. Thus, connections particular ly for the heat-transfer-medium circulation can be added as required even as a retrofit on site, without the reactor 10 needing to be separately moved anywhere, or special means be ing needed to arrange the connection.

The invention also concerns the use of a tube 28 made from a hollow pipe profile 20 by a welding method and by helical winding into a spiral arrangement as a temperature-regulated biogas reactor 10, and even more particularly as the tank structure 13 of a biogas reactor 10.

One example of the tank structure's 13 dimensions is a diame ter of 1 m and a length of 5 m. One example of the pipe pro file 20 has dimensions of 70 mm x 40 mm. The pipe profile's 20 wall thickness can be, for example, 4 - 8 mm. In addition to implementing heating means 16, the biogas re actor 10 according to the invention's structural implementa tion is light. In addition, the biogas reactor 10 according to the invention has good scalability. The biogas reactor 10 according to the invention can, within the restrictions of volume capacity of transport means, be transported to its op erating site even as only a single component, thus avoiding, for example, its assembly at the operating site. This reduces the costs relating to the making and acquisition of the bio gas reactor 10 and thus also shortens the pay-back time of the investment.

The invention's objects have been described above largely with reference to biogas. There is, however, reason to note that, in the context of the invention biogas can be under stood in an appropriate context. More generally, as also stated, it is gas formation from material containing organic matter. Most conventionally it is known as the formation of a methane-rich gas, but equally it can also be, for example, the formation of hydrogen from material containing organic matter, either as its own process or then, for example, com bined with methane production. According to one exemplary em bodiment, the organic matter can then be, for example, turf. Crushed turf can pre-treated, for example, with lye before being processed in the reactor structure according to the in vention. According to the embodiment, the process taking place in the reactor can then in its initial stage produce hydrogen-rich gas, which can then be followed by methane pro duction. On the other hand, the reactor 10 according to the invention can equally be used only for hydrogen production from material containing organic matter. It should be understood that the above description and the related figures are intended only to illustrate the present invention. The invention is thus not restricted to only the embodiments described above or defined in the Claims, instead many different variations and adaptations of the invention, which are possible within the scope of the inventive idea de fined by the accompanying Claims, will be obvious to one skilled in the art.