DE102012012878A1 - Obtaining organic fertilizer, comprises e.g. withdrawing a liquid phase of ammonium and hydrogen sulfide dissolved in an expeller, and dissolving resulting gaseous nitrogen and sulfur compounds in the downstream of fume scrubbers - Google Patents

Abstract

Obtaining organic fertilizer with high nutrient concentration by anaerobic pretreatment of biogenic raw materials and/or waste materials with subsequent solid-liquid phase separation of the resulting digestate, nutrient recovery from the liquid phase with supply for the solid phase and drying the solid phase with final compaction of the dry material, comprises withdrawing the liquid phase of ammonium and hydrogen sulfide dissolved in an expeller, dissolving resulting gaseous nitrogen- and sulfur compounds in the downstream of fume scrubbers in a cooled sulfurous organic acid in the expeller. Obtaining organic fertilizer with high nutrient concentration by anaerobic pretreatment of biogenic raw materials and/or waste materials with subsequent solid-liquid phase separation of the resulting digestate, nutrient recovery from the liquid phase with supply for the solid phase and drying the solid phase with final compaction of the dry material, comprises withdrawing the liquid phase of ammonium and hydrogen sulfide dissolved in an expeller, dissolving resulting gaseous nitrogen- and sulfur compounds in the downstream of fume scrubbers in a cooled sulfurous organic acid in the expeller, discharging a washing liquid, loaded with dissolved ammonium from the fume scrubbers, as a liquid nutrient concentrate and supplying the solid phase from the solid-liquid phase separation, contacting the solid phase of the digestate in an evaporator finely distributed over a period of 0.1-2 seconds with a hot air stream at a temperature of 130-150[deg] C, sucking a dust-air mixture from the evaporator via a dust separation complex, treating a moist air leaving from a dust separation complex before discharge into the environment in the scrubber, and supplying dust of assembly accumulated in the dust separation complex to a classified organic nitrogen-phosphorus-potassium-sulfur-fertilizers. An independent claim is included for an apparatus for obtaining organic fertilizer with high nutrient concentration, comprising an anaerobic system that serves a pre-treatment of the used biogenic raw materials and/or waste materials, a solid-liquid phase separation station that serves a separation of the resulting digestate in the solid phase and the liquid phase, an inhibitor-removal station that serves a recovery of the nitrogen-and sulfur compounds dissolved in the liquid phase, a drying plant, which serves a drying of the solid phase and the liquid nutrient concentrate from the inhibitor-removal station, a fume scrubber that serves the detection of gaseous nitrogen compounds carried in the moist exhaust air of the drying plant, and a compactor- and classifying system that serves the packaging of the nutrient-containing dusts withdrawn from the dust separation complex of the moist exhaust air of the drying plant, where the inhibitor-removal station comprises the expeller equipped with a heating system and a dispensing tube serving a gas delivery, the fume heat exchanger, and the fume scrubbers arranged downstream to a vapors heat exchanger, and the fume scrubber is designed as a trickle apparatus operated with the cooled organic acid. ACTIVITY : Fertilizer. MECHANISM OF ACTION : None given.

Description

The invention relates to a method for obtaining high nutrient organic fertilizers and an arrangement for carrying out the method with the aim of minimizing nutrient losses. Such a technical solution is needed in the material and energetic utilization of biogenic raw and / or waste materials by anaerobic technology.

The fermentation residues from the anaerobic treatment of biogenic raw materials and / or waste materials are known to have, depending on the protein and sulfur contents on the one hand and on the quality and intensity of the anaerobic treatment typical proportions of dissolved ammonium and dissolved hydrogen sulfide. Both substances are extremely beneficial and highly effective plant nutrients for agrochemical applications. By contrast, these substances not only cause economic nutrient losses in the event of unwanted release, but also cause considerable environmental problems because they are considered to be both air and water pollutants. From this point of view, the known technological solutions for the nutrient content and for the provision of processed fermentation residues with a high nutrient concentration differ significantly.

So be in the DE 198 06 089 A1 and DE 198 06 087 A1 Proposals have been made suggesting the addition of mineral rock powders and / or clay minerals for odor retention and incorporation of water-soluble plant nutrients in compounds having reduced water solubility. The additional process steps required for this not only make the entire process more expensive, they also lead to reduced availability of nutrients in the fertilizer produced.

In the DE 198 29 799 C2 describes the incorporation of ammonium from anaerobically treated animal excrements by means of the addition of phosphoric acid and magnesium compounds into sparingly soluble magnesium ammonium phosphate. The lack of this technical solution is both in the use of as a result of the depletion of global inventories increasingly difficult to obtain phosphoric acid as well as the technically complex handling of the nutrient-containing moist precipitates. The DE 10 2005 002 066 B4 contains a technical solution, with the help of which essentially part of the nutrient potential extracted from a dewatered sludge in the form of the phosphate contained and then to be precipitated by the addition of magnesium and calcium compounds. The proposed technical solution aims at the development of only one Närhstoffkomponente under acceptance of the difficult handling requirements for the generated precipitates.

With the in the DE 10 2005 055 310 B4 It is accepted in the technical solution disclosed that the intended aerobic treatment of the process from the anaerobic treatment results in nitrogen losses which are no longer available for plant fertilization. A similar result causes with the DE 10 2007 008 188 A1 announced technical solution by providing the use of ventilated rents for the solid phase treatment.

Also the DE 10 2008 007 296 A1 Proposes the production of a nutrient-containing fertilizer by providing the actual technical scale liquefaction of biogas as a gas mixture of essentially methane and carbon dioxide. Also, the proposed use of phosphoric and / or sulfuric acid and the production of precipitates in the form of ammonium phosphate or ammonium sulfate expensive and complicates the process of maintaining the nutrient potential. In addition, the generated precipitates with modern fertilizer application technology are hardly enforceable in agricultural practice today.

An interesting technical solution describes the DE 10 2009 024 536 A1 , It envisages processing the biogenic substrates both before and after the anaerobic treatment stage in aerobic bioreactors. While the upstream stage should support the hydrolytic process and thus the anaerobic digestion process of the organics used, the downstream aerobic bioreactor is based on the bacterial formation of fats and proteins with the simultaneous use of the nitrogen and sulfur compounds contained in the fermentation residues. In this way, only liquid nutrient concentrates for fertilization purposes should be obtained.

A technical solution that is able to provide the nutrient potential contained in fermentation residues from an anaerobic treatment of biogenic raw and / or waste materials with virtually no loss and without process-external additives in concentrated form has not hitherto been encountered in practice and can also be found in the currently available literature not be removed.

The object of the invention is therefore to overcome the deficiencies of the known prior art. The aim is, on the one hand, an economically feasible application of the thermal energy, which in many cases is sufficiently available, from the energetic utilization of the fuel gases obtained in the anaerobic treatment of the biomass used with the aim of avoiding excessively high moisture contents of the fertilizers produced for storage, transport and storage the agrotechnical application. On the other hand, the in the thermal drying according to the prior art resulting nutrient losses and / or the additional material-consuming process steps are reduced to a minimum. It also includes the task of minimizing the environmental impact of nutrient emissions on the protected assets of soil, air and water.

The object is achieved according to the invention by a method according to claim 1 and by a device according to claim 10. Preferred embodiments of the invention are described in the subclaims.

Thereafter, the digestate from a plant for the anaerobic treatment of biogenic raw and / or waste materials with depending on the quality of the feedstocks contents of phosphorus, potassium, nitrogen, sulfur, calcium and magnesium compounds, first a solid-liquid phase separation fed. Using conventional technical equipment, such as press screw separators and / or decanters, a solid phase having mean dry matter contents of at least 28% and a liquid phase having dry matter contents of not more than 8% are obtained. Since the aim is to obtain the entire nutrient potential contained in the fermentation residues and in the fuel gases obtained during the anaerobic process in the highest possible concentration and in an application form suitable for modern application technology, the plant nutrients should first of all be contained as completely as possible in the solid phase before it is further processed by means of drainage and shaping processes. For this purpose, the sulfur potential discharged in the fuel gas from the anaerobic process is recovered by means of biological gas scrubbing as so-called sulfurous biosic acid. The liquid phase to be recycled back into the process contains dissolved potassium as well as dissolved nitrogen compounds in predominantly ammonium form as well as dissolved sulfur compounds in the form of hydrogen sulphide. The two latter ingredients are considered as inhibitors of the bacterial conversion process from a critical concentration in the fermentation substrate. Therefore, the liquid phase is subjected to nutrient dumping, which primarily relates to the depletion of dissolved ammonium and dissolved hydrogen sulfide. This is achieved by means of a special stripping process in an expeller using circulation gas, for example carbon dioxide, an elevated to about 60 ° C and a temperature lowered to values of 0.8 bar absolute pressure above the liquid phase in the expeller an ammonia - And hydrogen sulfide-containing cycle gas is generated, which at least partially enters a Wrasenwäscher, which is preferably designed as a Rieselkörperwäscher. This Wrasenwäscher the sulfuric bio-acid obtained in the gas desulfurization is supplied as a washing medium. The biosurfactant taken from the scrubber sump is pumped in the circulation and sprayed over the packed packing arranged above the scrubber sump. In this circuit, a heat exchanger is integrated, with the help of which the washing medium is cooled to temperatures of less than 25 ° C. When passing the Füllkörperpackung the majority of the gaseous nitrogen and sulfur compounds entrained by the vapors produced in the expeller is dissolved in the washing medium with a constant increase in its pH. After reaching a selectable saturation level of the washing medium which can be read on the pH reached, it is at least partially removed from the scrubber sump and admixed with the solid phase obtained in the solid-liquid phase separation. The washing medium is then filled to reach the nominal level in the scrubber sump with unloaded biosäure.

Now, the laden with the loaded as the liquid nutrient concentrate laden washing medium from the scrubber sump solid phase fed to a special drying process. The aim of this drying process is to reduce the water content in the drying material to less than 15% while avoiding the release of ammonia from the high-ammonium drying material. This is achieved by the drying material is fed to an evaporator, which is designed as a hot gas flowed through the rotary mill.

• – im vollständigen Erhalt des in den Gärresten einer Anlage zur anaeroben Behandlung von biogenen Roh- und/oder Abfallstoffen verfügbaren Nährstoffpotentials,
• – im Vermeiden des kostenintensiven Einsatzes von zusätzlichen Fremdstoffen in Form von mineralischen oder chemischen Komponenten,
• – im Ausschluss von Umweltbelastungen durch die Emission von Pflanzennährstoffen und
• – im Vereinfachen der Prozessabläufe, verbunden mit Kosteneinsparungen und Ertragsverbesserungen bei der Düngemittelproduktion.

It is well known that ammonium in aqueous solution is increasingly easier to liberate at elevated temperatures and / or elevated pH than ammonia gas. Known plants for the drying of ammonium-containing residues from an upstream anaerobic treatment are environmentally friendly equipment regularly Wrasenbehandlungsanlagen for obtaining ammonia water and / or precipitates in the form of ammonium sulfate or ammonium phosphate, the latter using appropriate mineral acids. Surprisingly, it has now been found that the moisture adhering to the finely divided material to be dried evidently extracts enough heat from the substrate during evaporation that the measurable delivery of ammonia can not yet occur if the heating phase does not exceed a certain period of time. The solution according to the invention makes use of this finding by the found combination of fine comminution and distribution of the solid particles contained in the discontinuous press and / or decanter cake from digestate in hot gases with inlet temperatures between 130 and 150 ° C. and residence times of less than 2 seconds technical realization is based. The dedusting apparatus downstream of the evaporator separate the moist solid-air mixture into a solid phase, which contains, among other things, almost the entire nitrogen inventory of the press cake used. The moist air derived from the dedusting complex already contains no measurable ammonia levels immediately after the dust collectors. As a precaution, this exhaust gas is fed to an exhaust gas scrubber, with the help of which residual dust contents and, in the case of irregularities, also possible contents of volatile nitrogen compounds in the washing medium are bound. Thereafter, the still moist exhaust gas condensate can be withdrawn if necessary, which can also be used to replace the washing medium in the scrubber. In the case of the entry of nitrogen into the washing medium, this can be added to avoid functional impairments of the liquid phase from the phase-separated fermentation residues before the proposed inhibitor release. In this way it is ensured that virtually nutrient losses and thus also uncontrolled nutrient emissions are almost completely avoided. The advantages of the invention over the known prior art are thus summarized

• - the full availability of the nutrient potential available in the digestate of an anaerobic plant for the treatment of biogenic raw and / or waste materials,
• In avoiding the costly use of additional foreign matter in the form of mineral or chemical components,
• - in the absence of environmental pollution from the emission of plant nutrients and
• - Simplify process flows, combined with cost savings and yield improvements in fertilizer production.

embodiment

The invention will be explained in more detail below with an exemplary embodiment.

In the attached drawing show

1 : the schematic representation of the combination of the required process stages;

2 : the schematic representation of the components of the arrangement according to the invention for carrying out the method;

3 : The schematic block diagram of a device for obtaining the nutrient potential from the liquid phase of the digestate of anaerobic treatment of biogenic raw and / or waste materials.

• – Trockenmasseanteil = 13,3% der Originalsubstanz
• – Glühverlust (Organik) = 69,0% der Trockenmasse
• – pH-Wert = 7,6
• – Gesamtstickstoff (als N) = 0,92% der Originalsubstanz
• – Ammoniumstickstoff (als NH₄) = 0,41% der Originalsubstanz
• – Gesamtphosphat (als P₂O₅) = 0,34% der Originalsubstanz
• – Gesamtkalium (als K₂O) = 0,55% der Originalsubstanz

In a plant for the material and energetic utilization of biogenic residues of the food industry has the digestate 2 anaerobic pretreatment 1 the following characteristic values:

• - dry matter content = 13.3% of the original substance
• - loss on ignition (organic) = 69.0% of the dry matter
• - pH = 7.6
• Total nitrogen (as N) = 0.92% of the original substance
• - Ammonium nitrogen (as NH ₄ ) = 0.41% of the original substance
• Total phosphate (as P ₂ O ₅ ) = 0.34% of the original substance
• Total potassium (as K ₂ O) = 0.55% of the original substance

The digestate 2 becomes a solid-liquid phase separation with the aid of a screw extruder 3 subjected. This is a solid phase 4 with a dry matter content of 32% and a liquid phase 5 with a dry matter content of 8.5%. The arrangement for producing an organic NPKS fertilizer 21 (Nitrogen-Phosphorus-Potash-Sulfur-Fertilizer) with high nutrient concentration and to minimize nutrient losses consists of a liquid phase inhibitor plant 5 as well as a plant for drying 6 and for the preparation of the dry product. The Hemmagersentfrachtung takes place in an arrangement consisting of an expeller 7 in which the above-fed liquid phase 5 in the ground area 7.3 withdrawn and in an external circuit 7.1 via a heat exchanger 7.2 to achieve a working temperature in the expeller 7 in the amount of about 60 ° C and then on the container lid 7.4 in the expeller 7 is returned. In the outer cycle 7.1 is a jet pump 7.8 arranged, with the help of a circulation gas flow 7.10 is encouraged. This circulation gas flow 7.10 initially consists of air or carbon dioxide.

The total pressure of the jet pump 7.8 serves to suck the in the expeller 7 resulting vapor containing ammonia and hydrogen sulfide. The expulsion of these vapors in the expeller 7 is promoted by that over that in the exporter 7 up to the height of the drain liquid phase 5 an absolute pressure of <0.95 bar prevails. Furthermore, the release of ammonium and hydrogen sulfide by the heating of the liquid phase is supported up to about 60 ° C. The guided over the outer circuit portion of the liquid phase passes through the container lid 7.4 as a compact jet back into the liquid phase, with additional turbulence in the expeller 7 arises. Finally, the circulation gas stream arrives 7.10 over a dispensing tube 7.6 in the upper area of the expeller 7 located liquid phase 5 , which also promotes obstetrics. The circulation gas flow 7.10 is via a Wrasenwärmetauscher 7.9 directed, with a substantial portion of the entrained heat energy of the expeller 7 sucked nutrient-rich fumes at a temperature of about 60 ° C on the cooled nutrient-poor Wrasenstrom from the Wrasenwäscher 8th is transferred at a temperature of about 25 ° C. The Wrasenwärmetauscher 7.9 downstream is the Wrasenwäscher 8th as Rieselkörperapparat with a scrubber sump 8.3 , a packed bed 8.1 and an external circuit 8.2 the washing liquid 10 , The in the Wrasenwärmetauscher 7.9 cooled to about 35 ° C vapors 7.5 from the expeller 7 be in the Wrasenwäscher 8th above the scrubber sump 8.3 and below the packed bed 8.1 initiated.

The packed bed 8.1 is with washing liquid 10 by wetting it over the outer circulation 8.2 washing liquid 10 from the scrubber sump 8.3 withdrawn, via a liquid cooler 8.4 passed and above the packed bed 8.1 is spent on this. The nutrient-rich vapors pass in countercurrent 7.5 the packed bed 8.1 , wherein in the washing liquid in the form of sulfurous bioacid 9 from biological biogas desulfurization essential parts of the nutrient-rich vapors 7.5 be solved. In the scrubbed sump, the development of the pH value is monitored as a function of the dissolved ammonium and hydrogen sulfide load. Once with a substantial absorption capacity of the washing liquid 10 can no longer be expected, becomes part of the exhausted washing liquid 10 as a liquid nutrient concentrate 11 derived and replaced by fresh bio-acid 9 replaced. The mean temperature is in the Wrasenwäscher 8th kept at about 25 ° C. The recovered liquid nutrient concentrate 11 with considerable levels of nitrogen and sulfur compounds is due to the solid phase produced in the press screw separator 4 sprayed so that the mean dry matter content of the solid phases to be treated 4 drops to about 30%. In the drying plant 6 are next to the hot air generator to provide a hot air stream 12 an evaporator 12 , a dust separation complex 15 for the separation of the dry solids from the generated dust-air mixture 14 in the form of an exhaust air cyclone 16 and a tissue separator 17 with downstream scrubber 18 arranged.

For the assembly of the deposited dusts stands for the compaction 20 a die press and a screen complex 19 ready. The solid phase 4 becomes the evaporator 13 in the form of a rotary mill together with a hot air stream 12 abandoned at a temperature of 135 ° C. The generated moist dust-air mixture 14 will be out of the evaporator within about 400 ms 13 sucked off and first in an exhaust air cyclone in moist exhaust air 15.1 and cyclone dust separated. The humid exhaust air 15.1 then passes into a tissue separator 17 , with whose help separated filter dusts 17.1 be won. The cleaned moist exhaust air 15.1 is a precaution in a fume scrubber 18 treated. Residual dusts and, in the event of a fault, also ammonia components are used here by the washing medium used 18.3 detected. The wet exhaust leaving the fume scrubber 18.1 enters either into the environment or with existing hot water demand via a condenser. The condensate recovered there 18.2 is so unencumbered that it easily as a washing medium 18.3 in the exhaust air scrubber 18 can be used if, for example, the washing medium used 18.3 is overloaded too much and therefore expediently the Hemmstoffentfrachtungsstation must be supplied. The combined cyclone dusts and the separated filter dusts 17.1 are first compacted in the matrix press shaping as a grain and then down to the applicable for the fertilizer application as with conventional technology NPKS fertilizer in a sieve complex 19 classified. The fertilizer produced contains virtually lossless the entire nutrient potential of the biogenic raw and / or waste materials used.

An environmental impact from released plant nutrients can be excluded. Stressful foreign substances are not needed. The moisture content of the fertilizer produced is nearly 90%, which ensures maximum nutrient density and a minimum of unnecessary transport capacity.

LIST OF REFERENCE NUMBERS

1

anaerobic pretreatment

2

digestate

3

Solid-liquid phase separation

4

solid phase

5

liquid phase

6

desiccation

7

expeller

7.1

external circulation

7.2

heat exchangers

7.3

floor area

7.4

container lid

7.5

vapors

7.6

dispensing tube

7.7

Open channel

7.8

jet pump

7.9

Wrasenwärmetauscher

7.10

Circulation gas flow

8th

Wrasenwäscher

8.1

packed bed

8.2

external circulation

8.3

scrubber sump

8.4

Chillers

9

Biosäure

10

washing liquid

11

liquid nutrient concentrate

12

Hot air stream

13

Evaporator

14

Dust-air mixture

15

Staubabscheidekomplex

15.1

moist exhaust air

16

exhaust cyclone

17

Gewebeabscheider

17.1

separated filter dusts

18

fume scrubbers

18.1

moist exhaust gases

18.2

condensate

18.3

wash medium

19

Siebkomplex

20

compacting

21

NPKS fertilizer

QUOTES INCLUDE IN THE DESCRIPTION

This list of the documents listed by the applicant has been generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.

Cited patent literature

• DE 19806089 A1 [0003]
• DE 19806087 A1 [0003]
• DE 19829799 C2 [0004]
• DE 102005002066 B4 [0004]
• DE 102005055310 B4 [0005]
• DE 102007008188 A1 [0005]
• DE 102008007296 A1 [0006]
• DE 102009024536 A1 [0007]

Claims (10)

Process for the recovery of high nutrient organic fertilizers by anaerobic pretreatment ( 1 ) of biogenic raw materials and / or waste with subsequent solid-liquid phase separation ( 3 ) of the fermentation residues ( 2 ), the nutrient recovery from the liquid phase ( 5 ) with feed to the solid phase ( 4 ) and drying ( 6 ) of the solid phase ( 4 ) with final compaction ( 20 ) of the dry material, characterized in that the liquid phase ( 5 ) in an exporter ( 7 ) dissolved ammonium and dissolved hydrogen sulfide is withdrawn, that in the expeller ( 7 ) arising gaseous nitrogen and sulfur compounds in the downstream Wrasenwäscher ( 8th ) in cooled sulfurous bio-acid ( 9 ), that the washing liquid loaded with dissolved ammonium ( 10 ) from the Wrasenwäscher ( 8th ) as a liquid nutrient concentrate ( 11 ) and the solid phase ( 4 ) from the solid-liquid phase separation ( 3 ), that the solid phase ( 4 ) of digestate ( 2 ) in an evaporator ( 13 ) dispersed over a period of between 0.1 and 2 seconds with a hot air stream ( 12 ) is brought into contact with a temperature between 130 and 150 ° C that the dust-air mixture ( 14 ) from the evaporator ( 13 ) via a dust separation complex ( 15 ) is sucked off, that the dust separation complex ( 15 ) leaving moist air before discharging into the environment in a fume scrubber ( 18 ), that in the dust separation complex ( 15 ) dusts of a preparation to be classified organic NPKS = nitrogen (N) phosphorus (P) potassium (K) sulfur (S) fertilizers ( 21 ). Process according to claim 1, characterized in that the liquid phase ( 5 ) the exporter ( 7 ) in the ground area ( 7.3 ), then via an external circuit ( 7.1 ) with integrated heat exchanger ( 7.2 ) and heated to a temperature between 55 and 65 ° C and then the expeller ( 7 ) over the container lid ( 7.4 ) is returned. Method according to one of claims 1 and 2, characterized in that the Wrasentransport from the expeller ( 7 ) to the Wrasenwäscher ( 8th ) via a in the outer circulation line for the liquid phase ( 5 ) on the exporter ( 7 ) arranged jet pump ( 7.8 ) is effected. Method according to one of claims 1 to 3, characterized in that as washing liquid ( 10 ) in the Wrasenwäscher ( 8th ) the biosulphurous sulfuric acid biosulphuric acid ( 9 ) and that the sensible heat of the expeller ( 7 ) to the Wrasenwäscher ( 8th ) transported vapors ( 7.5 ) via a Wrasenwärmetauscher ( 7.9 ) on the the Wrasenwäscher ( 8th ) leaving circulation gas stream ( 7.10 ) is at least partially transmitted. Method according to one of claims 1 to 4, characterized in that the washing liquid ( 10 ) in the outer circuit ( 8.2 ) before re-feeding to the Wrasenwäscher ( 8th ) by means of liquid cooler ( 8.4 ) is cooled to a temperature of less than 25 ° C. Method according to one of claims 1 to 5, characterized in that when exceeding the pH of 2.5 of the washing liquid ( 10 ) in the Wrasenwäscher ( 8th ) the scrubber sump ( 8.3 ) a selectable amount of liquid in the form of a liquid nutrient concentrate ( 11 ) and then the scrubber sump ( 8.3 ) up to the nominal level with fresh bio-acid ( 9 ) is refilled. Process according to claim 1, characterized in that as evaporator ( 13 ) a high-speed rotary mill for comminuting the solid particles of the solid phase ( 4 ) is used to grain sizes of 0.5 mm maximum that as a hot air stream ( 12 ) for heating the evaporator ( 13 ) a mixture of the exhaust gas of a combined heat and power plant and ambient air is used, that the exhaust air scrubber ( 18 ) leaving moist exhaust gases ( 18.1 ) are condensed and the resulting condensate ( 18.2 ) to replace the washing medium ( 18.3 ) in the scrubber ( 18 ) is used. Method according to one of claims 1 to 7, characterized in that when determining ammonium contents in the washing medium ( 18.3 ) of the exhaust air scrubber ( 18 ) the washing medium ( 18.3 ) the liquid phase ( 5 ) in front of the expeller ( 7 ) is added. Process according to claim 1, characterized in that the separated filter dusts ( 17.1 ) by means of granulation, pelleting, briquetting and / or classifying to a low-dust and conventional fertilizer spreadable NPKS fertilizer ( 21 ) with dry matter contents of at least 85%. Apparatus for the production of high nutrient organic fertilizers according to the method of claim 1, consisting of - an anaerobic system used for the pretreatment of the biogenic raw and / or waste materials used, - one of the separation of the accruing digestate ( 2 ) into a solid phase ( 4 ) and into a liquid phase ( 5 ) solid-liquid phase separation station ( 3 ), - one of the recovery in the liquid phase ( 5 ) dissolved nitrogen and sulfur compounds inhibitor Entfrachtungsstation, - one of the drying of the solid phase ( 5 ) and the liquid nutrient concentrates ( 11 ) from the inhibitor-unloading station serving drying plant, - one of the detection of the wet in the exhaust air ( 15.1 ) the drying plant entrained gaseous nitrogen compounds serving exhaust air scrubber ( 18 ) and - one of the packaging in a Staubabscheidekomplex ( 15 ) of the moist exhaust air ( 15.1 ) of the drying plant extracted nutrient-containing dusts compacting and classifying system ( 19 . 20 ), characterized in that the inhibitor deflaking station consists of a distribution lance (19) serving with a heating system and a gassing ( 7.6 ) ( 7 ), a Wrasenwärmetauscher ( 7.9 ) and a this Wrasenwärmetauscher ( 7.9 ) downstream Wrasenwäscher ( 8th ) is that the Wrasenwäscher ( 8th ) as a with cooled bio-acid ( 9 ) operated Rieselkörperapparat is formed and that the serving for drying evaporator ( 13 ) with a hot air stream ( 12 ) or operated with hot exhaust gases grinding unit is.

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