METHOD AND APPARATUS FOR THE PROCESSING OF BIOLOGICAL MATERIALS, IN PARTICULAR OF FERTILE AND ANIMAL ORIGIN, IN PARTICULARLY FROM BIOGAS PLANTS, MANURE OR OTHER ORGANIC WASTE PRODUCTS

Description

[0001] The present invention relates to a method and an apparatus for processing biological materials, in particular digestate of plant and animal origin, especially from biogas plants, liquid manure, or other organic waste products. Liquid manure can also be considered a biological material. Digestate, liquid manure, etc., are also referred to as liquid fertilizers.

[0002] There are now various systems for drying digestate, etc., but none of the known systems deliver satisfactory results. Currently, the separation of water and nitrogen compounds, such as ammonia (NH₃) or ammonium (NH₄⁺) salts, is being implemented. However, this is a complex and / or costly process. The drying of digestate, etc., is preferably carried out using residual heat from combined heat and power plants, partly because it can be combined with substantial subsidies. A major disadvantage here is the extremely high energy consumption of 600-1000 kW required to evaporate (dry) the liquid fraction of 1 m³ / h of digestate and thus obtain the digestate (approximately 7% of the digestate mass) as a solid. If ammonia treatment is also to be integrated, a stripper system or a sulfuric acid scrubber becomes necessary.However, in most applications ammonia is still released directly into the exhaust air, resulting in a significant environmental impact.

[0003] DE 69312690 T2 relates to a method, a device and a plant for extraction by evaporation of a solid residue from a flowable material.

[0004] DE 202014010811 US 1 discloses a device for drying digestate, consisting of a digestate dryer, the latter comprising an evaporator boiler with a digestate inlet and a digestate outlet, a steam outlet, a heating device with a steam or hot water inlet and a condensate or hot water outlet.

[0005] DE 102014005667 A1 discloses a device and a method for drying digestate. For drying digestate from biogas plants or liquid manure, a digestate dryer has an evaporator with a heating device. The heating device can be heated with steam or hot water. Various system configurations for the efficient drying of different types of digestate can be implemented using several digestate dryers.

[0006] Further, purely technological background information is provided by US 8637304 B1, US 2014045234 A1 and US 2015329399 A1.

[0007] The present invention is therefore based on the objective of separating water and nitrogen compounds from a biological substance and the nitrogen compounds from the water with relatively little energy, or at least achieving a reduction of nitrogen compounds.

[0008] According to a first aspect, this problem is solved by a device according to claim 1.

[0009] According to a second aspect, this problem is solved by a method according to claim 18.

[0010] The process may include the condensation of gaseous nitrogen compounds, in particular ammonia, after a first condensation stage, to condense the vapors containing nitrogen compounds in a second condensation stage.

[0011] According to a particular embodiment of the present invention, it comprises collecting the condensed nitrogen compounds, in particular ammonia, in a collection device, in particular an ammonia collector.

[0012] Alternatively, it can be provided that it includes mixing the condensed nitrogen compounds, especially ammonia, with an acid to produce liquid fertilizer.

[0013] In particular, it may include the storage of the liquid fertilizer for later use.

[0014] Alternatively, it may be provided that it includes condensation of the vapors containing nitrogen compounds in a first condensation stage and the removal of gaseous nitrogen compounds, especially ammonia, for further processing.

[0015] The device may be provided with a control unit for controlling the rotary drive and / or the heating device and / or the filling of the container and / or the discharge of the concentrated liquid phase and / or the gas phase.

[0016] According to a particular embodiment, the hollow cylindrical overflow walls are filled with water and steam to heat the biological material inside the container.

[0017] Advantageously, the device has a first conveying device for conveying the concentrated liquid phase, which is in fluid communication with the first container outlet opening.

[0018] In particular, it may be provided that the first funding facility comprises a funding spiral.

[0019] Advantageously, the first conveying device is also designed for thermal post-drying of the concentrated liquid phase.

[0020] According to another particular embodiment, the device has a torrefaction device downstream of the first conveying device for torrefaction of the predominantly solid product of the final drying.

[0021] In particular, it may be provided that the torsioning device has a second conveying device downstream of the first conveying device, in particular a conveying spiral.

[0022] According to another particular embodiment, the device has a nitrogen compound separation device which is in direct or indirect fluid contact with the second container outlet opening for separating nitrogen compounds, such as ammonia or ammonium, from the gas phase.

[0023] Advantageously, the nitrogen compound separation device has a separating device for separating a water content by condensing water from the gas phase in the radially outer or radially outermost overflow.

[0024] Advantageously, the nitrogen compound separation device includes a stripping device for nitrogen compound stripping in the radially inner overflow wall or in at least one of the radially inner overflow walls.

[0025] Advantageously, the device includes a nitrogen compound binding unit for producing liquid fertilizer from the separated nitrogen compounds.

[0026] It may also be provided that it has a discharge device for removing concentrated nitrogen compounds for further processing.

[0027] Advantageously, the device includes a heat recovery unit for recovering heat energy from the gas phase.

[0028] In particular, it may be provided that the heat recovery device has a vapor compressor which is in fluid contact with the second container outlet opening for the compression of the gas phase.

[0029] Advantageously, the heat recovery device has a heat exchanger for operating the vapor compressor, which is connected or connectable to an exhaust gas line of a combined heat and power plant for the use of thermal energy from exhaust gas of combined heat and power plants.

[0030] According to a particular embodiment, an outlet of the vapor compressor with a radially outer lower region is located inside the radially outer or radially outermost overflow wall for introducing the compressed gas phase into fluid contact.

[0031] In particular, it may be provided that a mixing nozzle, especially an annular mixing nozzle, is connected between the outlet of the vapor compressor and the radially outer or radially outermost overflow.

[0032] Finally, it may be provided that the mixing nozzle has a second inlet which is in or can be brought into fluid contact with the lower area inside the radially outer or radially outermost overflow.

[0033] The present invention is based on the surprising finding that, through the special process and / or the special device in an integrated system, fermentation residues etc. can be concentrated and the wastewater can be discharged directly.

[0034] Further features and advantages of the invention will become apparent from the attached claims and the following description, in which particular embodiments are explained in detail with reference to the schematic drawings. These show: Figure 1 shows a device for the processing of biological substances according to a particular embodiment of the present invention, partially in a vertical sectional view; Figure 2 shows a sectional view along line AA' in Figure 1 Figure 3: Details of one in the Figure 1 Figure 4 shows a schematically depicted ring mixing nozzle in sectional and side view; Figure 4 shows a device for the processing of biological substances according to a further particular embodiment of the present invention, partially in vertical sectional view; Figure 5 shows details of a device for the processing of biological substances according to a further particular embodiment of the present invention; and Figure 6 shows a pressure-temperature diagram for the ammonia equilibrium.

[0035] The in the Figures 1 to 3The device 100 shown comprises a separation device for separating water and nitrogen compounds, in this example ammonia, from a biological substance, in this example digestate 200. The separation device has a container 101 that is round in plan view, with a container bottom 101a, a container wall 101b and a container lid 101c, wherein two hollow cylindrical overflow walls 102 and 103 are arranged concentrically to the central axis M of the container 101, forming a feed chamber 104 that is round in plan view and an outer annular chamber 105, wherein the height of the overflow edges 102a and 103a decreases from the radially inner overflow wall 103 to the radially outer overflow wall 102 (height h102 of the overflow edge 102a < height h103 of the overflow edge 103a). Thus, depending on the feed rate, the feed chamber 104 and the annular chamber 105 can be filled from the inside out between the overflow walls 103 and 102.

[0036] The overflow walls 102 and 103 are sealed against the tank bottom 101a.

[0037] As in the Figure 5 As shown and described later, the number of overflow walls can be expanded or increased as desired to improve performance / efficiency.

[0038] Furthermore, the separation device comprises a rotatable bell 106 arranged concentrically in the container 101, the bell having a bell top 106a, wherein the bell is fitted over the overflow walls 102 and 103 and has a cylindrical outer wall 106b, wherein the underside 106c of the outer wall 106b of the bell 106 terminates above the container bottom 101a, and the outer wall 106b of the bell has an upper outlet opening 106d, wherein the container 101 has in its container wall 101b a first container outlet opening 101d above the overflow edge 102a of the radially outer overflow wall 102 and below the upper outlet opening 106d in the outer wall 106b of the bell 106, and a second container outlet opening 101e above the first container outlet opening 101d, wherein the second container outlet opening 101e is connected to the upper Outlet opening 106d in the outer wall 106b of the bell 106 is in fluid contact. The outlet opening 106d can also be located further up or...be positioned in the bell lid 106a or consist of several openings.

[0039] Furthermore, the separation device comprises a filling pipe 107, which extends concentrically from above to the central axis M of the container 101 through the container lid 101c and the upper surface of the bell 106a into the container 101, the lower side 107a of the filling pipe 107 ending above the bottom of the container 101a, and the filling pipe being fixedly connected to the bell 106 in this example and rotatably mounted in the container lid 101c about its longitudinal axis L. In addition, the filling pipe 107 is sealed to the container lid 101c by a seal 108, e.g., an annular seal. Thus, the interior of the container 101 can only be connected to the atmosphere (with fluid) via the filling pipe 107.

[0040] A rotary drive, which in this example includes a slewing ring 109 surrounding the filling tube 107 above the container lid 101c, allows the filling tube 107 and thus the associated bell 106 to be rotated about its central axis. The central feed chamber 104 can be filled with, for example, digestate via the filling tube 107. The filling tube 107 extends far enough into the feed chamber 104 that it forms a seal between the upper area (evaporation chamber 110) and the atmosphere, for example, via the digestate column. The siphon effect of the filled filling tube 107 seals the container 101 gas-tight.

[0041] When the bell 106 is driven via the rotary ring 109, it acts as an agitator for the spaces between the overflow walls 102 and 103 and the filling pipe 107. In addition, the rotation and the associated centrifugal forces cause the fermentation residues to move radially outwards from the filling pipe 107 in the container 101.

[0042] Furthermore, the separation device includes a heating element for warming the digestate inside the container 101 from the inside of the hollow overflow walls 102 and 103 of the container 101. For this purpose, hot water and steam flow through the inside of the hollow overflow walls 102 and 103. The rotating bell 106 keeps the digestate in the container 101 in motion, thereby improving the heat transfer between the overflow walls 102 and 103 and the digestate. More precisely, heat is transferred from the overflow walls 102 and 103 to the digestate. Evaporation occurs in such a way that the hollow overflow walls 102 and 103 are filled with water and steam, and the steam condenses at a higher vapor pressure (preferably 1300 mbar, corresponding to 107°C) and thus higher temperatures, and the condensation energy can pass through the walls to the digestate and cause it to evaporate at a low pressure (preferably atmospheric pressure of 1000 mbar, corresponding to 100°C).Condensation establishes a water temperature corresponding to the vapor pressure, which in this application is preferably 107 °C or 1300 mbar. Only the amount of steam required to heat or evaporate the digestate condenses in the overflow walls, and the temperature of the heating water remains at 107 °C as long as steam is present in the overflow walls. In the feed chamber 104 and the annular chamber 105, due to the heated overflow walls 102 and 103, water and other dissolved components, such as ammonia, are evaporated from the digestate. The vapor is also referred to as steam 111. It collects in the evaporation chamber 110 and is discharged from the vessel via the outlet 101e. The fermentation residues concentrate from the area between the filling pipe 107 and the overflow chamber 103 towards the ring chamber 105.

[0043] The entire system is controlled by a control unit (not shown) for the rotary drive, the heating element, and the filling of the container. The control unit can also manage the other functions of the device or component, or a part thereof.

[0044] In this example, a first conveying device in the form of a conveying spiral 112 projects from the outside through the first container outlet opening 101d in the container wall 101b to such an extent that the now concentrated, predominantly solid digestate can be conveyed away via the first conveying spiral. Furthermore, the first conveying spiral 112 is designed and equipped with corresponding components such that the concentrated digestate is extracted from the container 101 and, for example, subjected to thermal drying or other uses (direct use as fertilizer).

[0045] The evaporation chamber 110, via the outlet opening 106d in the bell 106 and the second container outlet opening 101e in the container wall 101b, allows air (oxygen and nitrogen) to leave the evaporation chamber 110 to the outside as the fermentation residues evaporate, preventing new oxygen from entering the container 101 via the filling pipe 107, which acts as a siphon. Furthermore, the second container outlet opening 101e is connected via a line 113, e.g., a pipeline, to a steam jet compressor, such as a vapor compressor 114. More precisely, the steam (water vapor) or vapor 111 is supplied to the vapor compressor 114 as the suction medium. Water vapor is preferably used as the driving medium for the vapor compressor 114, which is generated, for example, via a heat exchanger 115, wherein exhaust gas 116, for example from a combined heat and power plant (not shown), is preferably used to generate the water vapor in the heat exchanger 115.

[0046] The vapor compressor 114 is part of a heat recovery system for recovering thermal energy from the vapor 111. The vapor compressor 114 can raise the vapor pressure of the vapor 111, and thus its condensation temperature, in a manner comparable to a heat pump effect. A mechanical compressor (e.g., a radial fan or turbine) can also be used as the vapor compressor 114.

[0047] The exhaust gas 117 from the thermal post-drying in the first screw conveyor 112 can also be fed to the vapor 111, since in this example a direct connection to the evaporation chamber 110 remains.

[0048] Furthermore, the device 100 includes a torrefaction unit downstream of the first conveying spiral 112 for torrefaction of the predominantly solid product from the post-drying stage. The torrefaction unit comprises a second conveying spiral 118, and the product (solid), which is predominantly free of water and oxygen via the separation process in the container 101, can be torrefied with minimal effort by applying higher temperatures, e.g., approximately 300 °C, in the second conveying spiral 118, since the oxygen has already been removed in the upstream separation process.

[0049] Torrefaction involves heating biomass in the absence of oxygen at temperatures between approximately 250°C and 400°C, resulting in partial pyrolytic decomposition and the release of water, carbon dioxide, carbon monoxide, and organic acids. Torrefaction achieves a stable water content of only about 3%. The mass is reduced by approximately 30%, while the energy content decreases by only about 10%, and smoke-producing substances (i.e., substances that would otherwise burn incompletely, producing soot, among other things) are removed. The calorific value of the black, granular product (also called biochar) is approximately 19.9 to 22.7 MJ / kg (green, water-rich wood has approximately 10.5 to 17.7 MJ / kg). However, the energy "gained" by increasing the calorific value is required to evaporate the water contained in the process. The resulting product can easily be pressed into pellets or further crushed.

[0050] By means of pressure staggering or, for example, a lock 119, the contaminated exhaust gas from the torrefaction can be separated and, for example, the exhaust gas can be fed to another processing (for example, combustion) via a separate outlet 120.

[0051] Due to a different circuit configuration (see the one in the Figure 1 and 4 In the illustrated embodiments) of the hollow overflow walls 102 and 103, the device can fulfill various additional functions.

[0052] The vapor 111, which is compressed in the vapor compressor 114 and in this example contains ammonia, is fed via a ring mixing nozzle 121 and a line 122 into the outer area 124 of the hollow overflow wall 102, which is separated in the lower area by a separating plate 123 which in this example extends vertically in section view.

[0053] As can be seen from the Figure 3In this example, the ring mixing nozzle 121 essentially consists of two sleeves 121a and 121b, which are inserted into one another. The compressed vapor 111 is directed into the outer sleeve 121a, and a second medium 202, for example water, into the inner sleeve 121b. At the front end of the inner sleeve 121b, a mixing chamber 121c is located in the outer sleeve 121a. For example, swirl plates 121d attached to the outside of the front end of the inner sleeve 121b cause the compressed vapor 111 to rotate, thereby increasing the mixing effect in the mixing chamber 121c. The "mixing medium" 204 leaving the mixing chamber can then react further in the transport lines before it enters the next processing step. If the brine 111 and the second medium 202 have different speeds, then the faster medium acts as a pump for the slower medium (ejector effect).

[0054] The ring mixing nozzle 121 generally improves the surface contact between the two media (steam (vapors) and e.g. water) and facilitates the separation of, for example, ammonia (NH 3 ).

[0055] In the upper area 125 in the overflow area 102 (see Fig. 1The uncondensed vapor, enriched with ammonia (NH3), collects and is discharged via line 125a. The reason for the partial non-condensation lies in the excess energy available at the set dew point. A portion of the condensate 126 from the overflow chamber 102 is sprayed into the overflow chamber 103 via line 127 and a spray head 128 in the upper section 129 above a stripping section 130. Simultaneously, fresh steam 132 from the heat exchanger 115 is introduced into the overflow chamber 103 in section 131 below the stripping section 130. The remaining portion of the condensate 126 is fed via line 133 as a second medium to the annular mixing nozzle 121, mixed with the compressed vapor 111, and then returned to the overflow chamber 102.

[0056] The water 128 sprayed into the overflow chamber 103 is purified of ammonia via the stripping section 130 and the live steam 132. The stripping section contains surface-enhancing material (e.g., steel wool), and the ammonia is extracted from the water by the live steam. The ammonia, concentrated in the steam, collects in the upper section 129 and is discharged from there via line 129a. The purified water is conveyed via line 134 to an intermediate storage tank 135 for possible later use. Because part of the condensate 126 from the overflow chamber 102 is guided back into the overflow chamber 102 via the ring mixing nozzle 121, a reaction of at least two stages of the ammonia-containing vapor takes place in the overflow chamber 102, resulting in a further separation of water with low ammonia content, which is then supplied to the spray head 128 via a pump 136 for final ammonia separation.

[0057] The water leaving the internal overflow duct 103 via the line 134 is cleaned by the upstream stripping process in the stripping area 130 to such an extent that it is collected in the water collector 135 and is available for further economic use (for example, steam generation (see lines 206 and 208)).

[0058] Regarding the processes in the overflow walls 102 and 103, it should be added that the ammonia is in equilibrium. It is partially dissolved in water and partially gaseous (together with water vapor and possibly other gases) above the liquid phase and when the liquid phase with dissolved ammonia is separated (see also Figure 6(In the diagram, where the typical operating range of the device is marked), ammonia will again pass from the solution into the gas phase above the liquid during the respective overflow (depending on temperature, pressure, and pH value). To ensure that ammonia remains stable in solution, the equilibrium is used: NH₃ + H₃O⁺ < → NH 4 +< + H₂O.

[0059] The in the Figure 4 embodiment shown (where the Figure 2 (also the sectional view along line AA' shows) of a device 100 differs from the one in the Figure 1The device 100 shown is distinguished, among other things, by the fact that there is no spray head inside the radially inner overflow wall 103. Furthermore, the vapor 111, compressed by the vapor compressor 114, is mixed with a medium described below via a ring mixing nozzle 137 and guided via a line 138 into a lower inner area 139 of the radially outer overflow wall 102, separated in this example by a vertically extending partition plate 123 in cross-sectional view. In the radially outer area 140 of the radially outer overflow wall 102, the vapor is returned or discharged via a stripping section 141 and a line 142. Live steam 132 is fed into the outer area 140 of the radially outer overflow wall 102 in a counterflow flow via a line 143. The live steam can, for example, be directed into the Figures 1 to 3The clean water leaving area 140 is conveyed via line 142 into collector 135 or used for other purposes such as steam generation.

[0060] The excess steam in the upper area 125 of the radial outer overflow wall 102 is mixed with returned water via a line 143a and a further mixing ring nozzle 144 and fed into a lower radial inner area 146 of the radial inner overflow wall 103 separated by a separating plate 145 which extends vertically in sectional view in this example.

[0061] During the Figure 4In the illustrated embodiment, the condensation of the ammonia-containing vapor from the radially inner overflow screen 103 takes place via two condensation stages. In the first stage at a higher temperature (e.g., 50°C), slightly ammonia-containing water is separated, which is then conveyed via the mixing ring nozzle 144 back into the radially inner overflow screen 103 for further NH3 removal. In the second condensation stage (approx. 20°C), the remaining separation takes place with a high ammonia concentration of up to 20%.

[0062] Furthermore, in the Figure 4 In the embodiment shown, excess water from the radial inner overflow chamber 103 is fed back to the radial outer overflow chamber 102 for ammonia separation via the mixing ring nozzle 137.

[0063] In the Figures 1 to 3In the embodiments of the device shown, gaseous ammonia is either condensed out via the second condensation stage after the first condensation stage and collected in an ammonia collector 147, or, for example, mixed with an acid, such as sulfuric acid, in a container 148 to form liquid fertilizer in a container 149 and stored for later use.

[0064] Alternatively, the gaseous ammonia can be directly used for another purpose, such as combustion (see arrow 150).

[0065] In both embodiments of the device, the integration of mixing ring nozzles fundamentally improves the efficiency of ammonia separation.

[0066] By increasing the number of overflow walls (see overflow walls 151 to 154 in the Figure 5 ) and a corresponding increase in the number of ring walls (see ring walls 155 and 156 in the Figure 5) of bell 106, further and possibly more efficient stripping options can be used, e.g., a combination of spraying, mixing, and pressure or temperature changes.

[0067] By increasing the number of overflow walls (see Figure 5 ) the innermost overflow can be used, for example, to cool the purified hot wastewater and thus the energy can be used to preheat the fermentation residues.

[0068] Due to vapor compression, the entire process has a very low energy requirement.

[0069] Furthermore, it should be mentioned that all processes (separation via evaporation, heat recovery via vapor compression, ammonia separation e.g. via stripping, ammonia binding e.g. to fertilizer) are integrated very compactly in one device.

[0070] Various materials, such as steel wool, gravel, spheres, perforated sheets, etc., can be used as surface-enlarging stripping material.

[0071] The separation process can also be used for other wastewater (industrial wastewater, sewage treatment plants, etc.).

[0072] At least in one particular embodiment, the devices can be used to concentrate ammonia and convert it into a useful raw material that can be further processed in industry into, for example, fertilizers, cleaning agents, fuel, etc. Ammonia separation can be carried out economically using this method.

[0073] The device's energy consumption is a fraction of that of conventional dryers, as the heat pump effect is achieved directly through vapor compression, requiring only a pressure increase of approximately 0.3 bar (a dew point increase of approximately 7 °C). This corresponds to a compressor output of approximately 13 kW to evaporate 1 m³ of water (digestate is approximately 93% water) per hour. Using a mechanical compressor, approximately 25 kW of electrical power is required, taking power losses into account. If a combined heat and power (CHP) plant is available, the exhaust gas (approximately 250 kW with a 500 kW electrical CHP unit) can be utilized, and the device could provide an additional 200 kW of residual heat for other processes.

[0074] Furthermore, the separated water has a low nitrite and nitrate content and is otherwise essentially within the limits for drinking water.

[0075] The ammonia content is significantly reduced and can be influenced by the process so that it is within the limits of the wastewater directive.

[0076] Torrefied solids, due to their higher density, are easy to store and transport, and as biochar, they form a valuable, CO2-neutral fuel with a relatively high calorific value. It is used as a fertilizer or soil improver in horticulture and conventional agriculture. Reference symbol list

[0077] 100 Device 101 Container 101a Container bottom 101b Container wall 101c Container lid 101 First container outlet opening 101e Second container outlet opening 101f Insulation 102 Overflow 102a Overflow edge 103 Overflow 103a Overflow edge 104 Feed chamber 105 Ring chamber 106 Bell 106a Bell top 106b Outer wall 106c Bottom 106d Outlet opening 106e Passage opening 107 Filling pipe 107a Bottom 108 Seal 109 Rotary ring 110 Evaporation chamber 111 Vapors 112 First conveying spiral 112a Conveying pipe 113 Pipe 114 Vapor compressor 115 Heat exchanger 116 Exhaust gas 117 Exhaust gas 118 Second conveying spiral 118a Conveying pipe 118b Solids outlet 119 Lock 120 Outlet 121 Ring mixing nozzle 121a Sleeve 121b Sleeve 121c Mixing chamber 121d Swirl plates 122 Pipe 123 Dividing plate 124 Area 125 Upper area 125a Pipe 126 Condensate 127 Pipe 128 Spray head 129 Upper area 129a Pipe 130 Stripping area 131 Area 132 Fresh steam 133 Pipe 134 Pipe 135 Water collector 136 Pump 137 Ring mixing nozzle 138 Pipe 139 Inner area 140 OuterArea 141 Stripping area 142 Pipe 143 Pipe 143a Pipe 144 Mixing ring nozzle 145 Dividing plate 146 Inner area 147 Ammonia collector 148 Tank 149 Liquid fertilizer 150 Arrow 151-154 Overflow 155-156 Ring wall 200 Digestate 202 Second medium 204 Mixing medium 206 Pipe 208 Pipe h102 Height of overflow edge 102a h103 Height of overflow edge 103a L Longitudinal axis M Central axis

Claims

1. Apparatus (100) for treatment of biological materials, especially of digestates (200) of vegetable and animal origin, especially from biogas plants, of liquid manure or of other organic waste products, containing a solids fraction and a liquid fraction, wherein the apparatus comprises: - a separating means for separating water and nitrogen compounds, especially ammonia, from a biological material, wherein the separating means comprises: - a container (101; 148) which is round in plan view having a container floor (101a), a container wall (101b) and a container lid (101c), wherein in the container at least two hollow cylindrical overflow walls (102, 103; 151, 152, 153, 154) are arranged concentrically with the central axis M of the container to form a feed chamber (104) which is round in plan view and at least one outer ring chamber (105), wherein the height h 102, h 103 of the overflow edges (102a, 103a) of the overflow walls (102, 103) decreases from inside to outside from overflow edge to overflow edge, - a rotatable bell (106) arranged concentrically in the container (101; 148) having a bell top surface (106a), wherein the bell is placed over the overflow walls (102, 103; 151-154) and has a cylindrical outer wall (106b) and optionally at least one concentrically arranged radially inner cylindrical ring wall (155, 156) which reaches from above into the at least one ring chamber (105), wherein the bottom surface(s) (106c) of the outer wall (106b) and the optionally present at least one ring wall (155, 156) of the bell (106) terminate(s) above the container floor (101a) and the outer wall (106) and / or the bell top surface (106a) of the bell has / have an upper outlet opening (106d) and the optionally present at least one ring wall of the bell has an upper throughflow opening (106e), wherein the container in its container wall has a first container outlet opening (101d) above the overflow edge (102a) of the radially outer / radially outermost overflow wall (102) and below the at least one upper outlet opening (106d) in the outer wall (106b) of the bell (106) and a second container outlet opening (101e) above the first container outlet opening (101d), wherein the second container outlet opening (101e) is in fluidic communication with the at least one upper outlet opening (106d) in the outer wall (106b) of the bell (106), - a fill pipe (107) which extends from above concentrically with the central axis M of the container (101; 148) through the container lid (101c) and the bell top surface (106a) into the container (101; 148), wherein the bottom surface (107a) of the fill pipe (107) terminates above the container floor (101a) and the fill pipe (107) is, especially fixedly, connected to the bell (106) and is mounted rotatably about its longitudinal axis L in the container lid (101c), - a seal (108) for sealing the fill pipe (107) and the container lid (101c), - a rotary drive for rotating the fill pipe (107) about its longitudinal axis L, and - a heating means for heating the biological material inside the container (101; 148) from inside the hollow overflow walls (102, 103; 151-154) of the container (101), especially to a temperature of about 100°C, especially at an atmospheric pressure of about 1 bar, to produce a liquid phase concentrated with respect to the solids content and a gas phase containing water and nitrogen compounds, especially ammonia, inside the container (101; 148).

2. Apparatus (100) according to Claim 1, wherein said apparatus has a control means for controlling the rotary drive and / or the heating means and / or the filling of the container (101; 148) and / or the discharging of the concentrated liquid phase and / or the gas phase.

3. Apparatus (100) according to Claim 1 or 2, wherein the hollow cylindrical overflow walls (102, 103) are filled with water and steam for heating the biological material inside the container (101; 148).

4. Apparatus (100) according to any of Claims 1 to 3, wherein said apparatus comprises a first conveying means for discharging the concentrated liquid phase which is in fluidic communication with the first container outlet opening (101d).

5. Apparatus (100) according to Claim 4, wherein the first conveying means comprises a conveying screw (112).

6. Apparatus (100) according to Claim 4 or 5, wherein the first conveying means is implemented in addition to the thermal post-drying of the concentrated liquid phase.

7. Apparatus (100) according to either of Claims 5 or 6, wherein said apparatus comprises a torrefaction means arranged downstream of the first conveying means for torrefaction of the predominantly solid product of the post-drying, especially wherein the torrefaction means comprises a second conveying means, especially a conveying screw (118), arranged downstream of the first conveying means.

8. Apparatus (100) according to any of Claims 1 to 7, wherein said apparatus comprises a nitrogen compounds separating means which is in direct or indirect fluidic communication with the second container outlet opening (101e) for separation of nitrogen compounds, for example ammonia or ammonium, from the gas phase.

9. Apparatus (100) according to Claim 8, wherein the nitrogen compounds separating means has a separation means for separating a water fraction by condensation of water from the gas phase in the radially outer or radially outermost overflow wall (102).

10. Apparatus (100) according to Claim 8 or 9, wherein the nitrogen compounds separating means comprises a stripping means for nitrogen compounds stripping in the radially inner overflow wall (103) or in at least one of the radially inner overflow walls.

11. Apparatus (100) according to any of the preceding claims, wherein said apparatus comprises a nitrogen compounds fixing means for producing liquid fertilizer from the separated nitrogen compounds.

12. Apparatus (100) according to any of Claims 1 to 11, wherein said apparatus comprises a discharging means for discharging concentrated nitrogen compounds for further processing.

13. Apparatus (100) according to any of Claims 1 to 12, wherein said apparatus comprises a thermal recovery means for recovering thermal energy from the gas phase.

14. Apparatus (100) according to Claim 13, wherein the thermal recovery means comprises a vapour compressor (114) which is in fluidic communication with the second container outlet opening (101e) for compressing the gas phase.

15. Apparatus (100) according to Claim 14, wherein the thermal recovery means comprises a heat exchanger (115) for operating the vapour compressor (114) which is connected or connectable to an offgas conduit of a block heat and power plant to utilize thermal energy from offgas from block heat and power plants.

16. Apparatus (100) according to Claim 14 or 15, wherein an outflow of the vapour compressor (114) is in fluidic communication with a radially outer lower region inside the radially outer or radially outermost overflow wall (102) for introducing the compressed gas phase.

17. Apparatus (100) according to Claim 16, wherein a mixing nozzle, especially a ring mixing nozzle (137), is connected between the outflow of the vapour compressor (114) and the radially outer or radially outermost overflow wall (102), especially wherein the mixing nozzle has a second inflow which is in or can be brought into fluidic communication with the lower region inside the radially outer or radially outermost overflow wall (102).

18. Process for treatment of biological materials, especially of digestates of vegetable and animal origin, especially from biogas plants, of liquid manure or of other organic waste products, containing a solids fraction and a liquid fraction, using an apparatus according to any of the preceding claims, wherein the process comprises the steps of: - filling the container (101; 148) with a biological material by means of the fill pipe (107), - preferably simultaneously rotating the bell (106), - separating water and nitrogen compounds, especially ammonia, from the biological material in the form of vapour by evaporation, - recovering heat from the vapour by vapour compression, and - separating the nitrogen compounds, especially ammonia, from the compressed vapour by stripping and separation of the water fraction.

19. Process according to Claim 18, further comprising condensing out gaseous nitrogen compounds, especially ammonia, after a first condensation stage for condensation of the vapour containing nitrogen compounds in a second condensation stage.

20. Process according to Claim 19, further comprising subsequently collecting the condensed-out nitrogen compounds, especially ammonia, in a collecting means, especially an ammonia collector.

21. Process according to Claim 19, further comprising mixing the condensed-out nitrogen compounds, especially ammonia, with an acid to afford liquid fertilizer, especially comprising storing the liquid fertilizer for later use.

22. Process according to Claim 18, further comprising condensing the vapour containing nitrogen compounds in a first condensation stage and discharging gaseous nitrogen compounds, especially ammonia, for further processing.