DE3427976A1 - Process and apparatus for the anaerobic treatment of substrates containing organic substances for generating biogas - Google Patents

Abstract

The organic substances are biologically degraded and converted into biogas in a two-stage fermentation process. The apparatus is a combined reactor having a first reactor chamber for hydrolysis development and acid formation, which is freely connected to a second reactor chamber for the methane formation. The volume ratios between the first and second reactor chamber are 1:2 to 1:20, preferably 1:10. A continuous reduction of the hydrogen partial pressure, and thus pH adjustment, is undertaken via an annular gap in the free connection in the first reactor, in order to develop an elevated acetic acid content and an optimal distribution of more readily degradable metabolic products. A higher degree of degradation at short residence times is achieved and the methane content in the biogas is increased. <IMAGE>

Description

Method and device for anaerobic treatment

of substrates with organic substances for the production of biogas Die The invention relates to a method for the anaerobic treatment of organic substrates for generating biogas according to the preamble of claim 1 and a device to carry out this method according to the preamble of claim 3.

Since the energy crisis in 1973 there has been a rethinking process in the industry and agriculture initiated, since the energy supply for many companies becomes one Profitability issue became.

Thanks to new technologies such as heat recovery, energy consumption, microelectronics, Use of heat-insulating building materials etc. could already generate substantial energies can be saved. As alternative energy sources such as steam and solar heat are available especially for the invention described here waste products in agricultural and industrial companies for discussion. These waste products fall as so-called Organic substrates in the form of liquid excrement from animals - also called slurry - in farms, agricultural distilleries and slaughterhouses on, with the plant substrates and biomasses as stillage or wastewater organically high pollution load as well as vegetable waste in commercial distilleries, Canning and food factories incurred.

In the companies where the liquid manure from animals or sewage with a high proportion of organic pollution is available, is the possibility given to create a biogas plant in order to cover a corresponding share of consumption of heating oil, natural gas and electrical energy.

This is a bio-energy system, i.e. a system the methane gas generated from the aforementioned substrates, which is both in a water or steam boiler as well as in a gasoline engine that drives a three-phase generator, can be burned.

It is known that bacteria are degradable organic substances, ie Carbohydrates, proteins and fats both in the absence of oxygen and in their presence decompose or

can break down. In the present case, it is a process that involves complete darkness and exclusion of oxygen takes place in a substrate; one speaks here also from anaerobic fermentation.

The mesophilic temperature range 32 - 38 0C is up for discussion, whereby the thermophilic temperature range 53 - 58 0C predominantly with substrates dangerous pathogenic germs come into question. In the biomethanization of the organic Substances that run in four phases, are according to the current knowledge three different groups of bacteria are involved. In the hydrolytic and acid-forming The process phase is carried out by the facultative anaerobic bacteria with fermentative resp. acidogenic characteristics the organic high molecular weight compounds with the help of Enzymes to low molecular weight compounds such as amino acids, glycerine and fatty acids hydrolyzed, whereby in a further phase from the hydrolysis products vinegar, butter, Propionic, valeric, caproic, formic and lactic acid as well as ethanol, hydrogen, Carbon dioxide, ammonia and hydrogen sulfide are produced.

The composition of these metabolic products is, however, in influenced accordingly by the hydrogen partial pressure. While with one low pressure or a medium volume load, more propionic acid was formed more valeric acid is produced at a high H2 pressure with a medium volume load.

In addition, a high partial pressure of hydrogen acts as an inhibitor in the catalization of acetic acid.

The acetic acid and hydrogen forming process phase is of the obligatory anaerobic bacterial strains, but with acetogenic characteristics, taken over, whereby from this group the long-chain fatty acids, organic acids, alcohols and Aromatics are broken down into acetic acid, hydrogen and carbon dioxide.

The starting product for the methane bacteria - it is also here about the obligatory anaerobes, which have a methanogenic characteristic, are primarily acetic acid, hydrogen and carbon dioxide, which are the last resort converted to methane gas (CH4) and carbon dioxide (C02). It is interesting here that the methane bacteria need a redox potential of 330 m volts to grow, as well as living in a spatially close symbiosis with the acetogenic bacteria, pH-sensitive and cannot tolerate fluctuating substrate temperatures.

In addition, this community of earthquakes is particularly sensitive Against acting shear forces, e.g. by agitators. Also the presence of dissolved Oxygen is sometimes fatal for methane bacteria.

Since the H2 partial pressure in the substrate should be low, coupling reactions must take place, such as

Overall reaction: NAD = nicotinamide adenine dinucleotide E = free energy (KJ / mol).

A special aspect for the reduction of the hydrogen partial pressure are the coenzymes found in methane bacteria, especially NAD, which by means of a chemical-osmotic metabolic process to reduce the H2 pressure.

A corresponding reduction in the H2 pressure also takes place Influence on the free energy, i.e. that with decreasing H2 partial pressure the Conversion of organic compounds from an endergonic to an exergonic process flow changes.

Since the first phase of the process is a so-called acidic biological process and the methane bacteria only their vital activity can unfold in a weakly alkaline medium, it is therefore important that the individual process phases are in a so-called equilibrium. Should namely, the organic acids accumulate, which is also due to the measured pH value can be determined, this is a sign that for some reason the degradation activity of the acid-producing bacteria that of the acid-consuming bacteria Bacteria predominate and the equilibrium is disturbed, i.e. the methane bacteria are paralyzed and thus the putrefaction will overturn, unless appropriate countermeasures are taken to support the final phase of the process.

Are the organic substances in the substrate with a corresponding degree of degradation biomethanized, the technical silt limit has been reached, i.e. the substrate is sludgeed or discharged. The silted substrate - also digested sludge called- is almost odorless, largely sanitized, has a corresponding richness in nutrients and can be used as fertilizer.

According to the previous points of view has been used for the construction of biogas plants primarily the so-called continuous reactor - also called an inflow reactor - crystallized out. This reactor works in one stage, with the substrate being mixed.

All four bio-technological ones described run in this reactor Phases in a room under the same physical conditions. It's understandable, that with this method there are no optimal living conditions for the individual bacterial strains available. In addition, there is a risk that the reactor angry , i.e. the pH value sinks to a level that is no longer permissible for the methane bacteria Value below 7, as there is an overproduction of acids.

Also through the entry of toxic substances such as sulfonamides, copper, Zinc and chromium compounds etc. as well as the oxygen inhibitor becomes metabolic production the corresponding degradation phase disturbed. Another disruption of metabolic production can be used in the case of biological degradation of substrates, e.g. vinasse with high sulphate content, occur as the sulfate compound is reduced to hydrogen sulfide and thus the formed H2S content can significantly impair the process flow.

When methane bacteria are killed or paralyzed, i.e. a disorder the acetogenic-methanogenic phase, less hydrogen is broken down, i.e. the 112 - partial pressure increases. As this acts as an inhibitor for the acetogenic bacteria works, it must be expected that the metabolic production -in particular by acetic acid - this bacteria comes to a standstill as well as by the H2 accumulation more reduced products are formed.

In the case of a biological decomposition of stillage, it must have a hydrogen sulfide content in biogas of approx. 2.5% are expected, that means that this fuel gas in one Otto engine cannot be burned without prior elimination of the H2S component.

Another disadvantage is that with relatively long residence times of the substrate only economical gas yields of about 1 - 2 m3 / d biogas per m3 Digestion room or low degrees of degradation of the organic substances are possible.

The calorific value of the biogas in a single-stage reactor is Normal substrates treated anaerobically according to modern process technology, 7 KWh / 4 with a gas composition of 70% methane (CH4), 29.7% carbon dioxide (C02) and 0.3% hydrogen sulfide (K2S), Based on the aforementioned findings has already been proposed, a biotechnological separation into the hydrolysis and acid phase as well as in the methanation phase to provide for the corresponding To create optimal living conditions for bacterial cultures, see DE-OS 31 02 739.

It is important that the acid or methane formation phase does not take place in two separately installed reactors, as this system solution the formation of acetic acid is influenced by the H2 partial pressure, but rather that the hydrolysis and acid phase takes place in a combined reactor. In This two-stage reactor is the hydrogen partial pressure due to the methane bacteria present correspondingly reduced in the acid reactor and thus the pH value adjusted accordingly, while at the same time more acetic acid as well as an optimal composition to better degradable metabolic products such as acetic, butyric, caproic acid and ethanol are formed will. The reduction of the H2 partial pressure takes place in this process technology in the form of a coupling reaction -which are also referred to as mass transfer ksnn- by methane bacteria or the universal hydrogen carrier NAD and others Coenzymes instead. In this coupling reaction, the diffusion flow is of hydrogen molecules and electrons through the annular gap are decisive.

Another constructive point is the division of the fermentation rooms I and II, i.e. the acid or methane formation phase with a volume ratio of preferably 1:10.

It is known that in an acidification stage, depending on the environmental conditions of the substrate, considerably more bacteria -due to the short generation times facultative anaerobes are present than in a methane reactor. Through this Realization lies a different production ratio between acid and Methane bacteria before or is a space pollution of the hydrolysis and acidification reactor by more than ten times that of a single-stage reactor possible without a substantial Reduction of the generated Metabolic products or degrees of degradation in level I occurs. In addition, with a high volume load with ph-value adjustment an extensive stability of the metabolic products produced can be expected. Also the composition and distribution of the metabolic products produced such as Acetic, butyric, valeric, caproic, formic and lactic acid as well as ethanol, hydrogen and carbon dioxide, can in the fermentation stage I at the mesophilic temperature from 3000 in the pH range from 5 to 6 using the method described as well as the fixed room layout and high volume loading of the hydrolysis and acidification stage are expected to be optimal. With a pH value of 5 - 6 there is a maximum growth rate of acid-forming bacteria to be expected.

The metabolic products individually produced in the acid reactor can be converted faster and better into the end product methane gas and in the methane reactor Convert carbon dioxide, whereby the hydrogen-utilizing methane bacteria give their full potential Be able to develop efficiency in fermentation stage II. In this procedure the metabolic performance of the individual breakdown phases is significantly higher than in a single-stage reactor or is due to the lower carbon investment in the bacterial culture synthesized more methane.

In addition, the process control in the methane reactor increases the adaptation of the symbiotic population of CO2-processing methanogenic bacterial strains, ie the formation of acetic acid in fermentation stage II takes place according to the following equation.

As a result of this, the C02 partial pressure is reduced and thus a higher conversion of acetate to methane gas is possible.

The object of the present invention is now to provide a method and a device of the type mentioned at the beginning to enhance, that a high degree of degradation with short residence times and a larger proportion of methane are synthesized will.

This task is procedurally carried out by the characteristics in the indicator of claim 1 and in terms of device by the features in the characterizing part of the claim 4 solved.

Due to the training according to the invention, a continuous one takes place improved reduction of the hydrogen partial pressure over the annular gap or the deposited products take place in the first reactor space, whereby by the provided mechanical Circulation according to the circular principle takes place in the hydrolysis and acidification stage constant hydrogen partial pressure builds up. The invention increases Proportion of acetic acid and the less desirable production of propionic and valeric acid prevented world-wide. In the two-stage process designed according to the invention can determine the residence times of the substrates in the combined reactor with biogas outputs (CH4 + C02) can be reduced by 3-6 m3 / d per m3 digester. There will be a high degree of degradation of organic substances achieved. The biogas produced is almost completely free of the undesirable amount of hydrogen sulfide.

The two-stage reactor according to the invention is extremely reliable, Toxic substances can also be introduced and degraded within limits.

The results that can be achieved with the invention can be improved even further are achieved by superimposing the hydraulic circulation with a further circulation by thermal circulation as indicated in claims 5 and 5.

Advantageous expedient developments of the device according to the invention are specified in the subclaims 5 to 27.

In the hydraulic and thermal circulation provided according to the invention Circulation in the second reactor space results in a reduction of the hydrogen partial pressure, especially in sedi- mentation area of the first reactor room through the annular gap between the conical bottom and the mixer injector a hydrogen consumption of methane bacteria as well as through the diffusion of hydrogen molecules in the fermentation chamber 2 instead. This process technology results in a lower A small amount of propionic and valeric acid formed and at the same time an increased proportion of acetic acid as well as more easily degradable metabolic products with an optimal Volume distribution produced. For the optimal formation of the product range such as vinegar, Butyric acid and caproic acid as well as ethanol and methanol or hydrogen is after completion the charging phase of the stationary substrate in the sedimentation area (boundary layer surface of the annular gap 11) of the reactor space 1, the substrate stream flowing past from the reactor space 2 decisive.

When the first reactor room is charged, the ones produced flow Metabolic products of the first fermentation stage through the annular gap are with Activated sludge from the second fermentation stage of the second reactor space in the mixer injector Gentle on the substrate, i.e. without the effect of shear forces, mixed and over the cylindrical chamber enclosed by the cylindrical wall into the second reactor space promoted in a circle with backmixing, resulting in excellent distribution the metabolic products for a high degree of degradation is achieved.

The jet pump with the nozzle mixing chamber open at the side sucks over the Heat exchanger, which also serves as a guide tube in its double function, substrate from the bottom of the first fermentation room, the ratio of activated sludge to the fresh substrate fed in is at least 3: 1. The substrate upheaval takes place in a circle with backmixing. At the same time, the liquid jet the jet pump, any floating cover that may have formed, was broken up and dissolved. In addition, during the hydraulic circulation, those in the side of the cone bottom sedimented metabolic products are insignificantly disturbed or

whirled up. The heat exchanger causes additional circulation of the substrate by convection.

The double-walled cylinder wall 8 also has the function thermal insulation, in particular through the biogas enclosed in the space. The thermal insulation ensures that in the reactor rooms with different Substrate temperatures can be driven.

3 For biogas reactors with a volume of less than 300 m is the first reactor space in the middle of the second reactor space.

In the case of biogas reactors with a volume greater than 300 m3, several individual reactor rooms used for the first fermentation process.

Through the raised conical floor of the first reactor room you can no sedimentation layers form. The promoted in the reactor room 1 and non-degradable substances slip on the cone into the second reactor space and can be removed or discharged from there.

Through the provided double U-tube for discharging the biologically degraded Substances from the second reactor chamber have the option of storing compressed gas depending on the U-pipe leg height.

The invention is to be described in more detail below with reference to the accompanying drawing explained.

It shows: FIG. 1 a section through one designed according to the invention Biogas reactor, FIG. 2 schematically shows a horizontal section through one according to the invention Biogas reactor with several reactor rooms for the first fermentation process, Fig. 3 schematically shows the design of the biogas reactors according to FIGS. 1 and 2 Heat exchangers and FIG. 4 shows a preferred embodiment of one according to the invention Biogas reactor provided mixing injector.

The drawing shows a combined biogas reactor with a first Reactor space 1 and a second reactor space 2. In the first reactor space, the inside of the second reactor space, a first fermentation process (hydrolysis and acid formation) and in the second reactor room a second fermentation process (methane formation) instead of.

The first reactor space 1 has a raised floor with a conical shape Floor surface 19 and is formed by a double-walled cylinder 8 between the walls of which an annular cylindrical gap 40 is formed. The cylinder 8 ends above the conical bottom 19, so that between the cylinder 8 and the bottom 19 an annular gap 11 is formed, through which the first reactor chamber 1 with the second Reactor space 2 is in open communication. The lower part of the double-walled cylinder 8 is designed as a mixing injector 10.

The cylinder wall 8 is spaced apart from a further cylinder 9 surrounded so that a cylindrical annular chamber 44 is formed, which as an overflow chamber is formed and ends at a distance from the bottom of the second reactor space 2, so because £ a further annular gap 46 is formed, which like the annular gap 11 in a Injection mixing chamber 45 leads, which is limited by the cone bottom 19, the cylindrical Wall 9 and the mixing injector 10. Biogas can be pressurized via the intermediate space 40 be fed to the mixer injector by means of a gas compressor 5. The suction nozzle of the gas compressor 5 is connected to a biogas space 42 of the reactor space 2 and the pressure port of the gas compressor is with the space 40 of the double-walled cylinder 8 connected.

The lower end of the cylinder 9 is designed as a heat exchanger 12. With the aid of the mixing injector 10, the substrate is hydraulically circulated caused in the reactor space 2, as indicated by the line 48. Another thermal circulation of the substrate is brought about by the heat exchanger 12. This thermal circulation is superimposed on the hydraulic circulation.

A jet pump is centrally located in the reactor space 1 above the conical bottom 19 7 arranged with a laterally open nozzle mixing chamber, which the substrate in the reactor space 1 sucks in from below and pumps upwards. The jet pump 7 is surrounded by the helix a tubular heat exchanger 6, which thus acts as a guide tube, as well as the annular intermediate chamber 44, whereby a hydraulic circulation of the substrate is effected in the reactor space 1, as indicated by the lines So. These hydraulic circulation is superimposed by a thermal circulation that is produced is through the heat exchanger 6.

The flow and return connections of the heat exchangers 12 and 6 are denoted by the reference numerals 15 and 20 and 16 and 18, respectively.

The coiled heat exchanger tubes 23 are preferably made of plastic (e.g. polypropylene) (Fig. 3). Two each serve as a support structure individual U-shaped pipes 24, which are at the same time distribution pipes for the flow and form the return. The tubes are threaded through adjustable tube bushings 26 out the reactor wall. The reference numeral 25 denotes a vent valve. The substances biodegraded in the fermentation chamber 2 collect in the circumferential funnel-shaped bottom 29.

Two discharge nozzles 13 and 14 are also arranged in the reactor chamber 2, which can optionally be connected to a double U-tube 22 via a three-way valve 21 are for discharging biodegraded substrates. Discharge nozzle 13 is located near the floor and the discharge nozzle 14 approximately halfway up the reactor space 2. The first U-tube leg 28 is connected to the biogas space 42 via a line 30.

The biogas CH4 + C02 produced in reactor space 2 is via a shut-off device 3 and the acidic biogas C02 + H2S produced in the reactor room 1 is controlled by a differential pressure Overflow valve 4 can be diverted.

In the case of reactors with a capacity of less than 300 m3, only one Reactor room used for the first fermentation process, which is centrally located in the reactor room 2 is arranged for the second fermentation process, see Fig. 1. In reactors with a content of more than 300 m3, several, for example three individual ones Reactor spaces 32, 34, 36 used for the first fermentation process, which are uniform are arranged distributed in the reactor space 2 for the second fermentation process, cf. Fig. 2, the effective range of the individual reactor rooms being set so that with 3 reactor rooms it has a radius of action which is about 25% of the total diameter of reactor 2 makes up.

The two-stage reactor shown in the drawing is in one Space ratio of the first reactor space 1 for the acid formation phase to the second Reactor space 2 built for the methane formation phase of about 1:10.

The biogas reactor shown in the drawing works as follows. The first reactor space 1 is connected to the substrate to be treated via a gate valve 17 loaded. With the help of the jet pump 7, the substrate is circulated hydraulically, wherein a ratio of activated sludge to fresh substrate fed in of at least 3: 1 is set. The charging takes place via an external pump that is not shown. This pump is with the gate valve 17 as well as the jet pump 7 connected. During the loading, which takes place quasi-continuously, is carried out by means of of the jet pump 7, which are provided with lateral slots on the nozzle mixing chamber activated sludge is sucked in and mixed with the fed substrate. Included activated sludge flows into the heat exchanger from below during the charging process constantly after. After loading the reactor space 1 is entered by the Temperature drop of the heat exchanger 6 put into operation to the intended optimum Set a temperature of approx. 30 0C and keep it constant.

By switching on the heat exchanger takes place, as already mentioned, a further circulation takes place in the form of a thermal circulation of the substrate.

During the loading of the reactor space 1, the in the cone bottom area 19 accumulated metabolic products through the annular gap 11 into the injection mixing chamber 45 promoted and mixed with activated sludge from the reactor room 2 and with the help of the mixing injector conveyed into the reactor space 2 via the intermediate ring chamber 44 and distributed accordingly by simultaneous circular circulation. Takes place at the same time by the temperature drop in the reactor chamber 2, which is at an optimal temperature is operated from approx. 35 0C, the activation of the heat exchanger 12.

After the gas compressor 5 has been switched off, the reactor space 2 also takes place or of the mixing injector 10 through a thermal circulation via the intermediate space 44 the effect of the heat exchanger 12 takes place.

An arrangement of gas compressor 5, annular space 40 as Guide tube, mixing injector 10 and annular intermediate chamber 44 as a further guide tube is also known as a mammoth pump.

Due to the hydraulic and thermal circulation of the substrate in the Reactor space 2 is a reduction of the hydrogen partial pressure via the annular gap 11 made in the sedimentation area of the reactor chamber 1. That generated in the reactor space 2 Biogas (CH4 + CO2) is withdrawn via shut-off device 3 and fed to the consumers. The acidic biogas (002 + H2S) generated in the reactor room 1 can be controlled via the control valve 4 can be drained.

After appropriate biological degradation of the organic substances; These collect in the funnel-shaped bottom 29 or the digested sludge is from the Reactor space 2 via the discharge nozzle 13 or 14 according to the procedure in the reactor space 1 fed in fresh substrate amount discharged. The discharged digested sludge flows through the double U-pipe 22, which doubles as a siphon for pressurized gas storage serves, through the connection to the biogas room 42 with the help of the connecting line 30th

To achieve a favorable reactor efficiency at as possible low material consumption is a ratio between the height and diameter of the Reactor of about 2: 1 chosen.

Furthermore, the annular gap 11 can be made later with the aid of the device 27 can be adjusted in height.

To with different reactor loads - taking into account the a constant digester volume stored in the fermentation chamber 2 with the amount of gas stored under pressure to achieve is achieved by a differential pressure control, which between fermentation room l and fermentation chamber 2 takes place, the excess produced in fermentation chamber l Biogas (Co2 + H2S) drained through the overflow valve 4.

For special cases, the drain line of the overflow valve 4 can be used with the extraction line 3 are interconnected. In this case, depending on the type of substrate the gas can be cleaned using a gas scrubbing device or desulphurisation system.

As mentioned above, the lower part is the double-walled cylinder 8 designed as a mixing injector 10. Via this mixer injector, biogas is under Pressure is blown into the reactor space 2, namely via leading into the reactor space Holes 60.

The mixing injector is formed by the lower part of the inner Wall of the cylinder 8, one at an angle to this inner wall at the top in the reactor space 2 pointing circumferential floor 62 and through one of the outer Wall of the cylinder 8 pointing outwards into the reactor space at an angle circumferential part 64 which is connected to the bottom 62. The holes 60 are in this Part 64 is formed near the junction with the floor 62. The angle between the bottom 62 and the inner wall of the cylinder 8 is about 460 and the angle between the outer wall extension of the cylinder 8 and the part 64 about 180. Through this Training is an approximately triangular cross-section annular annular space in the formed lower part of the double-walled cylinder 8 as a mixer injector. The holes 60 are arranged distributed around the circumference. There can be several rere rows of holes be provided with mutually offset holes. In the drawing (Fig. 4) two rows of holes are indicated schematically. The holes preferably have a diameter of about 4 mm. From the lower end 66 which tapers at an acute angle of the mixer injector several drainage pipes 68 are guided upwards, which in the Bottom 62 open and end approximately at the level of the holes 60, preferably with a small amount Distance to the holes.

Claims (33)

CLAIMS 1. Process for the anaerobic treatment of substrates with organic substances, especially with a high proportion of high molecular weight organic substances Substances such as proteins, carbohydrates and fats contribute to the production of biogas the substrates in a fermentation process taking place in the first reactor chamber by fermentative and acid-forming bacteria, preferably in acetic acid, hydrogen and carbon dioxide are transferred and then the resulting products via an open Compound get into a second reactor room and there by acetogenic and methanogenic Bacteria in a second fermentation process in biogas (methane and carbon dioxide) be converted, d a d u r c h e -k e n n n n z e i c h n e t that the to be treated, Fresh substrate fed in together with activated sludge in the first reactor room is circulated according to the circular principle with back mixing and that in the first fermentation process resulting products mixed with activated sludge from the second fermentation process and are also circulated according to the circular principle with back mixing. 2. The method according to claim 1, d a d u r c h g e k e n n -z e i c h n e t that the ratio of fresh substrate to activated sludge is at least 1: 3 is. 3. The method of claim 1, d a d u r c h g e k e n n -z e i c h n e t that the circulation is superimposed by a further circulation by thermal circulation will and / or follow. 4. Device for performing the method according to one of the preceding Claims with a bioreactor which has a first reactor space for the transfer the metabolic products from an organic substrate, primarily in vinegar, Butyric acid and caproic acid as well as hydrogen and carbon dioxide and with a second Reactor room for converting the products created in the first reactor room into biogas (Methane and carbon dioxide), d u r c h e k e nn n n e i c h n e t that in the first Reactor space (1) and / or in the second reactor space (2) a device for mechanical or hydraulic circulation is provided. 5. Apparatus according to claim 4, d a d u r c h g e k e n n -z e i c h n e t that still in the first reactor space (1) and / or in the second reactor space (2) a device for the thermal circulation of those located in the reactor rooms Substances is intended to achieve higher circulation rates. 6. Apparatus according to claim 4, d a d u r c h g e k e n n -z e i c h n e t that the first reactor space (i) with a double-walled cylinder wall (8) is formed, via the intermediate space (40) biogas can be supplied under pressure from above and the lower end of which is designed as a mixing injector (10) for thorough mixing the products produced in the reactor space (1) with activated sludge from the second reactor space (2) and for conveying the mixture into the second reactor space. 7. Apparatus according to claim 6, d a d u r c h g e k e n n -z e i c That means that the mixture is conveyed via an overflow chamber annular cylindrical chamber is carried out by the cylinder wall (8) and a this spaced surrounding cylindrical wall (9) is formed, which is spaced ends above the bottom of the reactor space (2). 8. Apparatus according to claim 6 or 7, d a d u r c h g e k e n n z e i c h n e t that the first reactor space (1) has a raised floor with a conical shape Has bottom surface (19) that between the lower end of the cylinder wall (8) and the conical bottom (19) an annular gap (11) is formed through which the in the reactor space (1) The products produced arrive in an injection mixing chamber (45) which is limited is from the conical bottom (19), the lower part of the cylindrical wall (9) and the mixing injector (10). 9. Device according to one of claims 6 to 8, d a d u r c h g e It is not indicated that in the first reactor space (1) for the circular substrate circulation a jet pump (7) is arranged, which has a laterally open nozzle mixing chamber. 10. The device according to claim 9, d a d u r c h g e k e n n -z e i c h n e t that the jet pump (7) within a vertically arranged tubular Heat exchanger (6) is arranged. 11. The device according to claim 10, d a d u r c h g e k e n n -z e i c h n e t that the heat exchanger has U-shaped flow and return pipes (24), which serve as a support structure, manifold pipes and ventilation pipes and between which a coiled tubing (23) is arranged. 12. The device according to claim 8, d a d u r c h g e k e n n -z e i c h n e t that the lower part of the cylindrical wall (9) through a heat exchanger (12) is formed. 13. Device according to one of claims 4 to 12, d a d u r c h g It is not noted that the second reactor space (2) is the first reactor space (1) ring-shaped. 14. Device according to one of claims 4 to 13, d a d u r c h g It is noted that the first reactor chamber (1) consists of several individual there is cylindrical partial reactor spaces that are located within the second reactor space (2) are arranged. 15. The apparatus of claim 14, d a d u r c h g e k e n n -z e i c h n e t that three identical, individual cylindrical reactor sub-spaces (32, 34, 36) are provided. 16. The apparatus of claim 15, d a d u r c h g e k e n n -z e i c h n e t that the individual cylindrical reactor sub-spaces are divided in such a way that that the effective area of each reactor compartment has a radius that is approximately 25% of the diameter of the second reactor space (2). 17. Device according to one of the preceding claims, d a d u r c h g e k e n n n e i c h n e t that the reactor space (1) with its cylinder wall (8) and optionally the cylindrical wall (9) formed as an insert and together with the heat exchangers (6 and 12) can be pulled out upwards. 18. Device according to one of claims 4 to 17, d a d u r c h g It is not noted that the biologically degraded substrate is via a discharge nozzle (13) near the floor or a discharge nozzle (14) in the middle area of the second Reactor space (2) is discharged. 19. Device according to one of claims 4 to 18, d a d u r c h g It is not noted that the biodegraded substrate is via a double U-tube (22) is discharged, the first leg (28) of which to achieve compressed gas storage in the biogas room depending on the height of the leg via a pipe (30) is connected to the biogas space (42) of the second reactor space (2). 20. The device according to claim 6, d a d u r c h g e k e n n -z e i c h n e t that the biogas is supplied with the help of a gas compressor (5), whose Pressure connection to the intermediate space (40) and its suction connection to the biogas space (42) of the reactor room (2) is connected. 21. Device according to one of claims 4 to 20, d a through g e k It is noted that the ratio of the volume of the first reactor space (1) to the volume of the second reactor space (2) 1: 2 to 1:20, but preferably Is 1:10. 22. Device according to one of claims 4 to 21, d a through g e k It is noted that the temperature in the reactor space (2) is about 350 Celsius and is set to about 300 Celsius in the reactor space (1). 23. The device according to claim 22, d a d u r c h g e k e n n -z e i c h n e t that the temperatures are set using the heat exchangers (6 and 12) the temperature is monitored with the help of sensors. 24. Device according to one of the preceding claims, g e k e n n z e i c h n e t d u r c h Use in batch processes in breweries and distilleries and in the pharmaceutical industry. 25. Device according to one of the preceding claims, d a -d u Noted that the ratio of height: diameter of the biogas reactor is about 2: 1. 26. The device according to claim 8, d a d u r c h g e k e n n -z e i c h n e t that the annular gap (11) through a device (27) connected to the reactor space (1 and 2) is connected, can be adjusted in height. 27. Device according to one of claims 6 to 14, d a -d u r c h it is not noted that the floor in the reactor space (2) is in the form of a circumferential Funnel tip (29) is formed. 28. Device according to one of claims 4 to 26, d a -d u r c h it is noted that the same gas pressures are achieved through an overflow valve (4) be regulated in reactor space 1 and reactor space 2. 29. The apparatus of claim 6 or 8, d a d u r c h ge k e n n z e i c h n e t that the mixing injector (10) through the lower part of the cylindrical Inner wall of the double-walled cylinder (8), through an at an acute angle from the end of the cylindrical inner wall upwards into the reactor chamber 2 pointing circumferential Bottom (62) and one at an acute angle from the cylindrical outer wall of the The circumferential part (64) pointing downwards into the reactor chamber 2 is formed in the cylinder (8) which is connected to the bottom (62) and in which several holes (60) are trained. 30. The device according to claim 29, d a d u r c h g e -k e n n z e i c h n e t that the holes (60) just above the junction of the part (64) are arranged with the bottom (62). 31. The device according to claim 29 or 30, d a d u r c h g e k e n n z e i c h n e t that several spaced rows of holes with offset to one another arranged holes are provided. 32. Apparatus according to claim 29, d a d u r c h g e -k e n n z e i c h n e t that in the acute-angled end (66) of the mixing injector (10) several Drainage pipes (68) are arranged which open into the ground (62), outside the Bottom (62) are guided upwards and end at the level of the holes (60). 33. Apparatus according to claim 29, d a d u r c h g e -k e n n z e i c h n e t that the angle between the bottom (62) and the cylindrical inner wall of the cylinder (8) is about 460 and the angle between the extension of the cylindrical outer wall of the cylinder (8) and the part (64) about 180.