DE102007053212A1 - Drying of solid portions from the separation of fermentation remainders of a biogas plant and/or of liquid manure, comprises supplying an exhaust gas flow into a drying mechanism having the solid portions, and drying the solid portions - Google Patents

Abstract

The method for drying solid portions (2) from the separation of fermentation remainders of a biogas plant and/or from the separation of liquid manure, in a drying plant, comprises supplying an exhaust gas flow (9) from the burning of fermentation gas over an exhaust gas line into a drying mechanism (8) of a drying unit having the solid portions, and partly drying the solid portions in the drying mechanism by heat transmission of the exhaust gas flow on the solid portions. The solid portion of the exhaust gas flow is overflowed and/or flowed through in the drying mechanism. The method for drying solid portions (2) from the separation of fermentation remainders of a biogas plant and/or from the separation of liquid manure, in a drying plant, comprises supplying an exhaust gas flow (9) from the burning of fermentation gas over an exhaust gas line into a drying mechanism (8) of a drying unit having the solid portions, and partly drying the solid portions in the drying mechanism by heat transmission of the exhaust gas flow on the solid portions. The solid portion of the exhaust gas flow is overflowed and/or flowed through in the drying mechanism. A direct heat transmission takes place between the exhaust gas flow and the solid portions. The solid portion is supplied discontinuously to the drying mechanism and/or is exhausted from the drying mechanism. The exhaust gas is mixed with an air flow to the exhaust gas flow, is regulated to 180-195[deg] C and then supplied to the drying mechanism. The solid portion and a partial flow of the dispersion and/or a partial flow of liquid portion (5) present in the solid-liquid separation of the dispersion are supplied to the drying mechanism. The ratio of the solid portion supplied to the drying mechanism is regulated to the partial flow of the dispersion and/or to the partial flow of the liquid portion with respect to the heat energy content of the exhaust gas flow. The drying process of the solid portion is carried out in a multi-stage manner. In a heat carrier (21) downstream to the drying mechanism, a residual heat transmission of the exhaust gas flow is carried out on a further air flow, and in another drying mechanism (25), a heat transmission of the air flow is carried out on the solid portion for the post-drying of the solid portion. An indirect heat transmission takes place between the exhaust gas flow and the further air flow. The exhaust gas flow is filtered and then supplied to the heat carrier. An INDEPENDENT CLAIM is included for a drying plant for drying a solid portion from the separation of fermentation remainders of a biogas plant and/or from the separation of liquid manure.

Description

The The invention relates to a process for drying a solids content from the solid-liquid separation a biological material-containing dispersion in a drying plant, in particular a solid content from the separation of digestate a biogas plant and / or the separation of liquid manure. Furthermore The present invention relates to a drying plant for carrying out the aforementioned method.

Manure accumulates mainly in factory farming in large quantities and consists of a mixture of feces, urine and bedding. The solids and water content of the manure and their composition can vary greatly. The liquid manure is collected in the holdings and, as it is subject to waste regulations and therefore can not be traded as an asset, it is preferably used for its own purposes. However, manure is subject to strict conditions regarding its use as a fertilizer for field management. In nutrient balancing, the phosphorus content of manure is in many cases the limiting factor. The same applies to fermentation residues that are produced, for example, in the fermentation of manure for the production of biogas. In nutrient surplus areas, disposal costs for phosphorus containing dispersions containing a biological material, such as manure and / or fermentation residues, are a factor limiting the economics of biogas plants or new stables, with the high water content of the dispersions in question rendering transport uneconomical in the rule. For example, a biogas plant with a capacity of 500 kW requires around 260 ha of agricultural land to accommodate the amount of phosphorus alone. If it is necessary to dispose of manure and fermentation residues via a so-called Güllebörse, then costs of 7 to 9 EUR / m ^{3 of} manure / digestate are to be estimated.

It Therefore, in the prior art, mechanical separation methods are proposed, to prepare dispersions containing biological material, wherein a dispersion in a solids content and in a liquid portion ge is separated. The separation of manure can, for example, before or after fermentation occur. For this purpose, among others, screw presses in the prior art or decanter centrifuges, wherein the solids content thus obtained enriched with phosphorus-containing components. The liquid phase has a lower phosphorus content and can be used on site be deployed while the solids are used as fertilizer in horticulture, as bedding material or for composting. This is especially for regions with nutrient surplus of considerable importance. It can be increase the accumulation of the solid content with phosphorus, if the Dispersion added prior to mechanical separation flocculant become.

Of the in the mechanical separation of the dispersion obtained solids content contains a residual moisture of up to 80%. Due to the high water content is the removal of the obtained during the mechanical separation Solid fraction from the biogas plant to a recycling center costly. In the prior art, it is therefore proposed that the water content the solids fraction in appropriately trained evaporator devices to evaporate, which requires a lot of energy.

task The present invention is a process and a drying plant for drying a solid fraction in each case of the aforementioned Kind available to make it with energy and cost possible, one from the solid-liquid separation a dispersion containing a biological material Dry solid content, wherein the solids content after drying should have a low residual moisture content.

The The aforementioned object is in a method of the aforementioned Art solved by an exhaust gas flow from the combustion of biogas at least one of the solids content supplied drying device of the drying plant is supplied and that the Solid content in the drying device at least partially by heat transfer is dried by the exhaust stream to the solids content. Device is accordingly in a drying plant of the type mentioned at least a separator for solid-liquid separation of the dispersion in egg NEN solids content and in a liquid content and at least one Drying device provided for drying the solids content, wherein the drying device to an exhaust pipe of an incinerator for biogas connectable is and the solids content by means of a conveyor of the drying device supplied becomes.

The invention is based in particular on the basic idea of utilizing the heat energy contained in the waste gas from the biogas combustion for drying the solids content. The solids content is obtained for example by the separation of digestate of the biogas plant and / or by the separation of manure. In this case, various raw materials, such as biowaste, manure, sewage sludge, fats or plants can be used in a biogas plant. Anaerobic fermentation or decay processes produce biogas, which can be used for decentralized coupled power and heat generation in combined heat and power plants due to the high methane content. The biogas is thereby in a Combustion engine burned the biogas plant, which drives a generator. The electricity thus produced is fed into the grid. The heat contained in the engine cooling water can be recovered in heat exchangers, with some of the heat needed to reach the operating temperature of the fermentation process of 37 ° C or 55 ° C. The excess heat of the engine is used in the art for heating buildings or drying the crop.

at the method according to the invention The dispersion is preferably mechanically in a solid phase and in a liquid Phase separated. You can do this in particular peeler centrifuges, but also decanter centrifuges and screw presses are used. The resulting solids content is in the drying device promoted the drying plant, being the heat energy the exhaust gas is used to the solid content cost and preferably Completely to dry. The inventive method and the drying plant according to the invention allow the residual moisture content in the solids fraction to be 5 to reduce to 15 wt .-%, especially in multi-stage drying. Of the low water content in the dried solid allows one Transport of the solid at low transport costs.

The Drying device is preferably designed as a rotary dryer. It is the case that the Solid content in the drying device during the drying process overflowed by the exhaust stream and / or flows through so that one direct heat transfer takes place between the exhaust stream and the solids content. The solids content is during the drying circulated and intensively mixed, what the heat transfer and evaporation and / or evaporation of moisture contained in the solids content favors. For one intensive upheaval the solids content, the drying device at least one agitator and at least one screw conveyor having a discharge screw exhibit. The discharge screw can be in two different directions be operable, wherein in a running direction dried solid is transported out of the drying device. Will the Discharge screw in a second oppositely directed direction operated, this leads to a revolution the solids content in the drying device. In the agitator can it is a paddle stirrer act with a plurality of staggered Turning vanes, wherein the axis of rotation of the paddle stirrer and the axis of rotation of the Discharge screw can be arranged parallel to each other. at a preferred embodiment the invention provides that the discharge screw in circulate the solids content at a speed of 30 to 70 U / min, in particular of 50 rpm, and the paddle stirrer at a speed of 10 to 30 rpm, in particular of 20 rpm, operate. As a result, the solids content in the drying process intensely mixed, so that the Evaporation or evaporation of moisture promoted and the formation of waterlogging in the solids content is prevented.

Otherwise, will noted that the exhaust gas flow be cooled as needed after drying the solids content can, so it for the separation of water and other volatile components from the Exhaust flow comes through condensation. The separated liquid phase can be used as process water be returned to a biogas plant. Furthermore For example, the liquid phase separated from the exhaust gas stream can be used in a wastewater treatment plant be prepared.

Of the Solid content of the drying device is preferably discontinuous fed and / or discharged discontinuously from the drying device. The Drying of the solid is then batchwise, which is the procedural Reduced effort in the drying of the solids content. Basically it of course also possible, that the Solid content continuously supplied to the drying device, there dried and dried from the drying device dissipated becomes.

at high exhaust gas temperatures, it is inventively provided that the exhaust gas from the biogas combustion before drying the solids content mixed with an air stream and the resulting exhaust stream then the Supplied drying device becomes. For regulating the temperature of the exhaust gas flow is a temperature control device provided, wherein the control of the exhaust gas temperature by supply the air flow to the exhaust gas takes place. The temperature control device is preferably designed such that the inlet temperature of Exhaust gas flow into the drying device between 150 to 200 ° C, preferably between 180 to 195 ° C, is. This can ensure that it during the drying process not to ignite the solid comes in the drying device. Furthermore the addition of ambient air to the exhaust gas serves the purposes of explosion protection.

At high heat energy content of the exhaust gas stream, ie at high exhaust gas temperature and large exhaust gas volume flow, it can be provided that the solids content and a partial flow of the dispersion and / or a partial flow of a liquid fraction obtainable in the solid-liquid separation of the dispersion are fed to the drying device. For example, can not separate digestate or not separated manure are passed directly together with the solids content in the dryer, wherein the evaporation of the liquid portion in the digestate or the slurry, a thermal solid-liquid separation is achieved in the drying device. In order to take account of different heat energy contents of the exhaust gas stream, the ratio of solids supplied to the drying device to the supplied partial stream of the dispersion and / or the partial stream of the liquid fraction can be regulated as a function of the thermal energy content of the exhaust gas stream. It is structurally provided in this connection that the separation device comprises a supply line for the dispersion and a discharge line for the liquid phase and that the supply line and / or the discharge line are connected to the drying device. For example, here a bypass line may be provided which is connected to the supply line on the one hand and the discharge line on the other hand and which makes it possible to pass the dispersion past the separator directly into the discharge line and thus into the drying device. For controlling or regulating the supply of the solids content and / or the dispersion and / or the liquid fraction to the drying device, a control or regulating device is preferably provided, wherein, preferably, the supply in dependence on the heat energy of the exhaust gas stream is controllable. This ensures that the heat energy contained in the exhaust gas can be used to the largest possible extent, which contributes to an increase in the overall efficiency of the gas engine use of biogas.

The Drying of the solids content can be carried out in one or more stages. wherein in particular in multi-stage drying, the residual moisture content of Solids content after the last drying process between 20 to 18 wt .-%, preferably between 5 to 15 wt .-%, can be. In this context, the drying plant at least one further drying device for drying the solids content , wherein, preferably, the further drying device also can be designed as a rotary dryer. In a first drying device The drying plant can heat transfer from the exhaust stream to the solids content for pre-drying the Solids take place. Subsequently, in at least one the heat exchanger downstream heat exchanger a residual heat transfer provided from the exhaust gas stream to another air flow, wherein in the downstream further drying device, a heat transfer from the further air flow on the solids content for post-drying the solids content occurs. The solids content must be from the first drying device to the second drying device promoted what appropriate funding requires.

at the residual heat transfer From the exhaust gas flow to the other air flow, it comes to condensation of liquid Ingredients from the exhaust gas stream, which discharged from the heat exchanger and if necessary, a water treatment must be supplied. The heat transfer between the exhaust stream and the further air flow is preferably carried out indirectly, so that the further air stream is not contaminated with exhaust gas constituents. The further drying device is in the result non-contaminated Ambient air on one opposite increased the ambient air Temperature level supplied. The solids content is in the further drying device of overflowed the further air flow and / or flows through in turn, a direct heat transfer be provided between the further air flow and the solids content can. Can constructively the drying device and the further drying device the same be educated. Due to the same drying equipment the structure of the drying plant is simplified and the effort for maintenance and maintenance of the drying plant reduced. For the rest, can the drying device is also designed as a rotary condensation dryer be.

Of the with water vapor and other volatile Components enriched exhaust gas flow, which after the drying process the solid content of the drying device exits is preferably before entering the for heating the further air flow provided heat exchanger filtered, wherein a suspended matter filter and / or a biofilter provided could be. Also can several filter devices in the flow direction one behind the other be arranged to ensure adequate cleaning of the exhaust gas flow to ensure. A biofilter can ensure that the ammonia concentration in the exhaust gas flow does not exceed the prescribed limits. About that In addition, it is preferably provided that the further air flow, the drying of the solids content, the further drying device flows through then cleaned becomes. You can do this in turn be provided Schwebstoff- and biofilters.

The invention will now be described by way of example with reference to the drying plant shown in the drawing. Moreover, the invention makes it possible, if necessary, to combine the features mentioned in the claims and / or the features disclosed and described with reference to the drawing, even if this is not described in detail. The invention is not limited to the illustrated and described drying system. The above value specifications and the specified intervals cover each values, ie not just the lower limits or, for intervals, the interval limits, without this requiring an explicit mention. In the drawing show

1 a process flow diagram of the process according to the invention for drying a solid fraction from the solid-liquid separation of a dispersion containing biological material using the example of the separation of digestate of a biogas plant,

2 a schematic cross-sectional view of a drying device of in 1 shown drying plant from the side, wherein a solid fraction from the solid-liquid separation of the dispersion is conveyed from a bunker in the drying device, and

3 in the 2 illustrated arrangement of drying device and bunker in a cross-sectional view from above.

In 1 is a drying plant 1 for drying a solids content 2 from the solid-liquid separation of a biological material-containing dispersion 3 wherein it is the dispersion 3 is digestate of a biogas plant, not shown. The dispersion may just as well be liquid manure, for example. For separation of the dispersion 3 is a separator 4 provided, the dispersion 3 in the separator 4 mechanically in the solids content 2 on the one hand and in a liquid fraction 5 on the other hand is separated. At the separator 4 it may preferably be a centrifuge, for example a peeler centrifuge, or a press. From the separator 4 is the solid content obtained in the solid-liquid separation 2 in one in the 2 and 3 schematically illustrated bunker 6 promoted and from there by means of a likewise in the 2 and 3 illustrated conveyor 7 a drying device 8th fed. In the drying device 8th this is the described drying plant 1 around a rotary dryer.

In the drying device 8th becomes the solids content 2 dried, the drying device 8th is connected to an exhaust pipe, not shown, a likewise not shown incinerator for the combustion of biogas. In the drying device 8th becomes the solids content 2 from an exhaust stream 9 overflowed and / or flows through, with a direct heat transfer between the exhaust stream 9 and the solids content 2 he follows. This is the solids content 2 during drying in the drying device 8th circulated. The drying device 8th has a stirrer for this purpose 10 and an operating in two different directions discharge screw 11 on. The agitator 10 has a plurality of mutually offset blade arms 12 on which turn buckets 13 are attached. When turning the blade arms 12 becomes the solids content 2 intensively circulated and mixed. The discharge screw 11 is thereby moved counter to the discharge X, resulting in even better mixing of the solids content 2 in the drying device 8th contributes. The intensive circulation of the solids content 2 in the drying device 8th improves the heat transfer, thereby ensuring that a large part of the in the solid content 2 contained liquid evaporates or evaporates. Is the residual moisture of the solids content 2 Sufficiently dropped, the direction of the discharge screw is 11 conversely, resulting in the discharge of the solids content 2 from the drying device 8th leads. In this context, a corresponding temperature and humidity measurement can be provided. In a preferred embodiment of the invention, the drying device 8th designed for a solids throughput of about 200 to 250 kg / h, with the discharge screw 11 At a speed of about 50 U / min and the agitator is operated at a speed of about 20 U / min. This represents a rapid and largely complete drying of the solids content 2 for sure.

About an unillustrated exhaust stack of the combustion system is exhaust gas 14 taken, which may be provided at high exhaust gas temperatures, an air flow 15 from the environment with the exhaust gas 14 to mix. The thus available exhaust gas flow 9 then preferably has a temperature of about 180 to 195 ° C. The temperature of the solids content 2 before entering the drying device 8th is between 50 to 70 ° C. For controlling the temperature of the exhaust gas flow 9 are in the the exhaust 14 and the airflow 15 leading lines flaps 16 provided, taking over the position of the flaps 16 Influence on the mixing ratio of exhaust gas 14 and airflow 15 can be taken, which ultimately a regulation of the exhaust gas temperature of the exhaust stream 9 allows. This allows the exhaust gas flow 9 be cooled so that it does not ignite the solids during the drying process 2 or even an explosion in the drying device 8th comes. For supplying the exhaust gas flow 9 in the drying device 8th is a fan 17 intended.

The incineration plant can be part of a combined heat and power plant operated with biogas from the fermentation of biomass. The removal of exhaust gas 14 takes place preferably after the exhaust gas has flowed through a heat exchanger of the cogeneration plant, wherein the heat exchanger in the prior art already pre-recovery of heat energy from the exhaust gas see is. The temperature of the exhaust gas 14 After flowing through the heat exchanger of the cogeneration plant is usually between 150 to 200 ° C, so that in the described method, the supply of air flow 15 for temperature regulation of the exhaust gas flow 9 not necessary in every case. The inventive method thus allows the use of the residual heat of the exhaust gas 14 that in the exhaust 14 is still contained after flowing through the heat exchanger of the cogeneration plant and is released in the prior art partly unused with the exhaust gas to the environment. The described method therefore contributes to an increase in the thermal efficiency of the combined heat and power plant.

Contains the exhaust gas flow 9 a very large amount of heat, which may be due to a high exhaust gas temperature and / or a high exhaust gas volume flow, it can be provided that, together with the solids content 2 a partial stream of the dispersion 3 and / or a partial flow of the liquid fraction 5 the drying device 8th be supplied. The drying plant 1 has for this purpose a bypass line, via the means of a valve 18 if necessary, a partial stream of the dispersion 3 to that from the separator 4 withdrawn liquid fraction 5 can be directed. Another valve 19 is provided to an inflow of the dispersion 3 and / or the liquid fraction 5 in the required amount to the drying device 8th to enable. It is understood that a not shown in detail control or Regeleinrich device for controlling or regulating the supply of solids 2 and / or the dispersion 3 and / or the liquid fraction 5 is provided, wherein, preferably, the supply in dependence on the heat energy content of the exhaust gas stream 9 is controllable. Will the dispersion 3 directly into the drying solids content 2 in the drying device 8th introduced, preferably injected, so is by the incipient evaporation of the liquid portion of the dispersion 3 achieved a thermal solid-liquid separation. The supply of the liquid fraction 5 in the drying device 8th is particularly advantageous if the liquid content 5 has a large amount of solids. The not the drying device 8th added liquid content 5 is passed into a collection container, not shown. Due to one in the solid-liquid separation in the separator 4 attained low phosphorus content, the liquid content 5 be applied on site.

The saturated with water vapor exhaust stream 9 gets out of the dryer 8th via a suspended matter filter 20 a heat exchanger 21 fed. The heat exchanger 21 is for heat transfer of residual heat of the exhaust stream 9 on another airflow 22 after flowing through the drying device 8th intended. After flowing through the heat exchanger 21 , in which an indirect heat transfer takes place, the exhaust gas flow 9 with another blower 23 a biofilter 24 supplied, thereby ensuring that the ammonia concentration in the exhaust stream 9 does not exceed the prescribed limits. The exhaust gas flow 9 is then discharged into the environment.

The in the drying device 8th (before) dried solid content 2 is for further drying in a further drying device 25 supported, which requires appropriate funding, not shown. In the further drying device 25 again, it can be a rotary dryer. The drying device 8th and the further drying device 25 may otherwise be the same.

After heating the further air flow 22 in the heat exchanger 21 this one comes with a third blower 26 the further drying device 25 fed. In the further drying device 25 there is a heat transfer from the other air flow 22 on the solids content 2 , the other drying device 25 with a residual moisture content of 5 to 15 wt .-% is removed. The further air flow 22 becomes after flowing through the further drying device 25 in another suspended matter filter 27 and optionally another biofilter 28 cleaned and then discharged into the environment. With the filters 20 and 27 These are self-cleaning and temperature-resistant suspended particle filters. The solids content 2 can be used as fertilizer in horticulture, as bedding material or for composting. Due to the low moisture content of the solids content 2 in the described two-stage drying is otherwise a cost-effective transport of the solids content 2 to the desired location possible.

In the 2 and 3 is the drying device 8th out 1 and the bunker 6 shown in detail. About a material task 29 becomes the solids content 2 in the bunker 6 filled. By means of the conveyor designed as a screw conveyor 7 that drive 30 has, the solids content 2 in a drying chamber 31 the drying device 8th promoted. There, the solids content 2 with the stirrer 10 circulated and with the discharge screw 11 in the dried state from the drying device 8th conveyed away. The discharge screw 11 has a drive 32 and the agitator 10 another drive, not shown. The supply of the exhaust gas flow 9 in the drying device 8th via an inlet area 33 from which a bypass line 34 branches off and below the discharge screw 11 outside the drying device 8th empties. This will become part of the Ab gas stream 9 before entering the drying device 8th towards the discharge screw 11 diverted. The redirected partial flow supports the detachment of solids 2 from the discharge screw 11 after exiting the drying device 8th ,

Claims (24)

Process for drying a solids content ( 2 ) from the solid-liquid separation of a biological material-containing dispersion ( 3 ) in a drying plant ( 1 ), in particular a solids content ( 2 ) from the separation of digestate of a biogas plant and / or from the separation of manure, wherein an exhaust gas stream ( 9 ) from the combustion of biogas via an exhaust pipe at least one of the solids content ( 2 ) having drying device ( 8th ) of the drying plant ( 1 ) and wherein the solids content ( 2 ) in the drying device ( 8th ) at least partially by heat transfer from the exhaust gas stream ( 9 ) on the solids content ( 2 ) is dried. Process according to Claim 1, characterized in that the solids content ( 2 ) from the exhaust stream ( 9 ) in the drying device ( 8th ) is flowed over and / or flows through, with a direct heat transfer between the exhaust gas flow ( 9 ) and the solids content ( 2 ) he follows. Process according to Claim 1 or 2, characterized in that the solids content ( 2 ) during drying in the drying device ( 8th ) is circulated. Method according to one of the preceding claims, characterized in that the solids content ( 2 ) discontinuously the drying device ( 8th ) and / or from the drying device ( 8th ) is discharged. Method according to one of the preceding claims, characterized in that exhaust gas ( 14 ) with a stream of air ( 15 ) to the exhaust stream ( 9 ) and that the exhaust gas stream ( 9 ) of the drying device ( 8th ) is supplied. Method according to one of the preceding claims, characterized in that the temperature of the exhaust gas flow ( 9 ) before entering the drying device ( 8th ) is controlled to a temperature of 150 to 200 ° C, preferably from about 180 to 195 ° C. Method according to one of the preceding claims, characterized in that the solids content ( 2 ) and a substream of the dispersion ( 3 ) and / or a partial stream of one in the solid-liquid separation of the dispersion ( 3 ) available liquid fraction ( 5 ) of the drying device ( 8th ). Method according to claim 7, characterized in that the ratio of the drying device ( 8th ) fed solid fraction ( 2 ) to the supplied substream of the dispersion ( 3 ) and / or to the partial flow of the liquid fraction ( 2 ) as a function of the heat energy content of the exhaust gas stream ( 9 ) is regulated. Method according to one of the preceding claims, characterized in that the drying of the solids content ( 2 ) is carried out in several stages. Method according to one of the preceding claims, characterized in that in a first drying device ( 8th ) a heat transfer from the exhaust gas stream ( 9 ) on the solids content ( 2 ) for predrying the solids content ( 2 ) that in at least one of the drying device ( 8th ) downstream heat exchanger ( 21 ) a residual heat transfer from the exhaust gas flow ( 9 ) to another air stream ( 22 ) and that in at least one further drying device ( 25 ) a heat transfer from the further air flow ( 22 ) on the solids content ( 2 ) for post-drying the solids content ( 2 ) he follows. Method according to claim 10, characterized in that an indirect heat transfer between the exhaust gas flow ( 9 ) and the further air flow ( 22 ) he follows. Process according to Claim 10 or 11, characterized in that the solids content ( 2 ) in the further drying device ( 25 ) of the further air flow ( 22 ) is flowed over and / or flowed through, with a direct heat transfer between the further air flow ( 22 ) and the solids content ( 2 ) he follows. Method according to one of the preceding claims, characterized in that the exhaust gas flow ( 9 ) after passing through the drying device ( 8th ) is filtered, preferably before entering the heat exchanger ( 21 ). Method according to one of the preceding claims 10 to 13, characterized in that the further air flow ( 22 ) after passing through the further drying device ( 25 ) is filtered. Drying plant ( 1 ) for drying a solids content ( 2 ) from the solid-liquid separation of a biological material-containing dispersion ( 3 ), in particular a solids content ( 2 ) from the separation of digestate of a biogas plant and / or from the separation of manure, with little least one separating device ( 4 ) for solid-liquid separation of the dispersion ( 3 ) in a solids content ( 2 ) and a liquid fraction ( 5 ) and with at least one drying device ( 8th ) for drying the solids content ( 2 ), wherein the drying device ( 8th ) is connectable to an exhaust pipe of an incinerator for biogas. Drying plant according to claim 15, characterized in that the drying device ( 8th ) is designed as a rotary dryer. Drying plant according to claim 15 or 16, characterized in that the drying device ( 8th ) at least one agitator ( 10 ) and at least one discharge screw ( 11 ) having screw conveyor, wherein, preferably, the discharge screw ( 11 ) is operable in two different directions. Drying plant according to one of the preceding claims, characterized in that a temperature control device for controlling the temperature of one of the drying device ( 8th ) via the exhaust pipe feedable exhaust gas stream ( 9 ), wherein the regulation of the exhaust gas temperature by supplying an air flow ( 15 ) to the exhaust gas ( 14 ) he follows. Drying plant according to one of the preceding claims, characterized in that the inlet temperature of the exhaust gas stream ( 9 ) into the drying device ( 8th ) between 150 to 200 ° C, preferably between about 180 to 195 ° C. Drying plant according to one of the preceding claims, characterized in that the separating device ( 4 ) a supply line for the dispersion ( 3 ) and a drain line for the liquid phase ( 5 ) and that the supply line and / or the discharge line with the drying device ( 8th ) are connected. Drying plant according to one of the preceding claims, characterized in that a control or regulating device for controlling or regulating the supply of the solids fraction ( 2 ) and / or the dispersion ( 3 ) and / or the liquid fraction ( 5 ) to the drying device ( 8th ), wherein, preferably, the supply in dependence on the thermal energy content of the exhaust gas stream ( 9 ) is controllable. Drying plant according to one of the preceding claims, characterized in that at least one further drying device ( 25 ) for post-drying the solids content ( 2 ), wherein, preferably, the further drying device ( 25 ) is designed as a rotary dryer. Drying plant according to one of the preceding claims, characterized in that at least one heat exchanger ( 21 ) for heat transfer of residual heat of the exhaust gas stream ( 9 ) to another air stream ( 22 ) after flowing through the drying device ( 8th ) is provided. Drying plant according to one of the preceding claims, characterized in that at least one filter device for the exhaust gas flow ( 9 ) and / or the further air flow ( 22 ) are provided.