Bioreactor and its applications, method for preparing organic nutrient solution and for storing carbon dioxide

Abstract

The present invention relates to bioreactors (1, 2, 3) and their use for converting organic residues and / or waste into an organic nutrient solution, which, based on the total nitrogen content of the nutrient solution, has a proportion of at least 10% of mineral nitrogen available to plants. The present invention also relates to a method for preparing an organic nutrient solution, to an organic nutrient solution, to the use of an organic nutrient solution as an absorbent for carbon dioxide storage, to an organic nutrient solution as a medium for binding carbon in plants and soil, and to a nutrient production and carbon dioxide storage system.

Description

[0001] The present invention relates to a bioreactor and its use for converting organic residues and / or waste into an organic nutrient solution by means of a reaction vessel, wherein, based on the total nitrogen content of the nutrient solution, the organic nutrient solution has a proportion of at least 10% of mineralized nitrogen that is plant-available, wherein the reaction vessel has a feed line through which a suspension can be introduced into the reaction vessel, and wherein the reaction vessel has a discharge line through which a suspension can be discharged from the reaction vessel.

[0002] The present invention also relates to a method for preparing an organic nutrient solution having a proportion of at least 10% of plant-available nitrogen.

[0003] The present invention further also relates to an organic nutrient solution. In particular, the organic nutrient solution can be an organic plant fertilizer.

[0004] The present invention furthermore relates to the use of an organic nutrient solution as an absorbent for storing preferably COx and / or NOx and / or SOx originating from a gas. In particular, it relates to the use of an organic nutrient solution as an absorbent, for example, in a biogas plant and / or in a central heating plant for carbon dioxide storage.

[0005] Finally, the present invention relates to a nutrient production and carbon dioxide storage system.

[0006] Agriculture has always obtained the nutrients required for plant agricultural production from the utilization and recycling of animal and plant residues and waste. Organic farming designs nitrogen as an important plant nutrient and only allows it to be applied in the organic form of economic / commercial fertilizers, such as manure water, compost, or horn meal fertilizer. Due to the expansion of the organic product market and the increasing specialization of farms, vegetable growers and other farms without livestock are forced to purchase and use organic commercial fertilizers due to the sale and export of biomass and the lack of economic fertilizers. It is precisely in the context of the strong demand for the use of organic fertilizers that there is a considerable proportion of non-mineralized nitrogen that cannot be immediately absorbed by plants.

[0007] Inorganic nitrogen compounds are generally understood to be plant-available nitrogen, i.e., nitrogen that can be directly absorbed by plants. In contrast, organic nitrogen compounds cannot be directly absorbed by plants. The term "plant-available nitrogen" generally refers to nitrogen in the form of ammonium (NH4 + ) and nitrate (NO3).

[0008] Hydroponic, soilless or poor-soil cultivation systems for plants currently use mineral fertilizers or mineral-organic fertilizers (fertilizers that mix mineralized nitrogen compounds from industrial production into organic materials). Pure organic fertilizer materials cannot be used for two reasons. On the one hand, the bacterial soil-plant interactions in such cultivation systems are very limited or not applicable to soilless methods. In addition, mineralized nutrients that can be immediately utilized by plants in the soil cannot be provided in sufficient quantities through bacterial processes that rely on external influences (such as nitrification). Moreover, organic fertilizers cannot achieve the controlled, continuous, and immediate release of nitrogen required by plants, especially in hydroponic cultivation systems.

[0009] Another problem is that the transformation of organic fertilizer materials, such as compost waste, etc., and the associated release of mineralized nitrogen depend on a large number of environmental factors that are difficult to control, such as soil moisture, soil temperature, and organic compounds in the soil at different concentrations. In agricultural applications, this lack of control leads to untimely nitrogen supply and excess / shortage, as well as harmful counter-processes to the economy and environment, such as denitrification.

[0010] Especially for soilless (or poor-soil) hydroponic / aeroponic cultivation systems, plants must be provided with optimally adjusted nutrient solutions because the lack or reduction of soil does not endow the substrate with a buffering function in terms of nutrient and water supply. The use of traditional organic fertilizer materials is not suitable for these systems because the nitrogen in them cannot be or is only insufficiently utilized by plants. In addition, in the case of organic fertilizer materials, due to further degradation or transformation processes, it is impossible to set clear and stable nutrient concentrations in the nutrient solution.

[0011] In addition to the fundamental drawbacks of organic agriculture that abandon the use of industrially obtained mineral nitrogen fertilizers, which may be a basic means to increase yields but are still considered problematic, the demand for nitrogen that can be immediately used by plants, especially in the last third of the growth stage of useful plants, cannot be met in a timely manner by using currently available organic economic fertilizers and organic fertilizers from residues and wastes.

[0012] Since the start of industrialization, the carbon dioxide (CO2) content in the Earth's atmosphere has increased significantly and reached 400 ppm in 2013. In addition to other gases that have an impact on the climate, carbon dioxide also causes global warming through the anthropogenic greenhouse effect. Approximately 18% of global emissions are caused by land use. The problem is that the anaerobic fermentation of organic waste (such as in biogas plants) and the incineration of biogas obtained from biogas plants release CO2.

[0013] Another problem is that fertilizers made from chemicals, minerals, and industrial manufacturing, such as those based on the Haber-Bosch process, are the main source of plant nutrients in global agriculture. The traditionally used organic farmyard manure has led to negative environmental pollution due to its uncontrolled and unmanipulable mineralization and its low utilization rate in the soil, and the usage is decreasing. However, this will trendily reduce soil fertility and the carbon supply required for soil-bacteria interaction.

[0014] Another problem is that fertilizers made from chemicals, minerals, and industrial preparations based on the Haber-Bosch process are the main source of CO2 emissions. Just producing ammonia requires 35.2 GJ of energy, which is equivalent to 840 kg of crude oil per ton of ammonia. Every kilogram of nitrogen (N) releases 2.2 kilograms of CO2.

[0015] The published document ES 2 298 011 A1 describes an aerobic fermentation process in a bioreactor, in which there is a mixture of grains and yeast. A ventilation pipe with a filter is provided at the bottom, and small bubbles are introduced into the bioreactor through this pipe.

[0016] The published document EP 0 486 748 A1 discloses a biofilm reactor for treating organic-polluted wastewater. Biofilm carrier particles are introduced into the reactor, and bacterial particles can adhere to them.

[0017] The document WO 2016 / 050893 A1 discloses the use of biofilm carriers in the anaerobic degradation process, in which a biofilm composed of methanogenic bacteria is provided.

[0018] The published document US 3 779 906 A describes a method for treating wastewater, in which the wastewater is treated in a ventilation chamber for several hours for purification.

[0019] The published document WO 2010 / 003255 A1 discloses a device that can enrich water with oxygen. Then the oxygen-enriched water is introduced into plant cultivation.

[0020] Therefore, the object of the present invention is to separate the carbon dioxide (CO2) gas generated during the anaerobic fermentation of organic residues and waste and / or the carbon dioxide (CO2) gas generated by the combustion of biogas, wash it out from the gas stream, and absorb CO2 in a stable manner.

[0021] According to the present invention, this object is achieved by the features of the following independent technical solutions:

[0022] Solution 1. A method for preparing an organic nutrient solution with a proportion of plant-available mineralized nitrogen in the total nitrogen content of at least 10%, preferably where the nitrate proportion of plant-available mineralized nitrogen is higher than the ammonium proportion, which includes the following steps:

[0023] - In the inoculation step, the carrier unit (10), preferably the carrier unit (10) of the bioreactor (1, 2, 3), is inoculated with an inoculation material containing ammonifying bacteria and / or nitrifying bacteria.

[0024] - On the carrier unit (10), a biofilm (12) with ammonifying bacteria and / or nitrifying bacteria is formed.

[0025] - In the cultivation step, organic residues and / or waste are cultivated together with the biofilm (12), wherein the ammonifying bacteria and / or nitrifying bacteria convert the organic bound nitrogen in the residues and / or waste into mineralized nitrogen.

[0026] - During the implementation of each or all steps, oxygen is introduced into the reaction vessel (5) and / or the carrier unit (10) by means of a ventilation device (8).

[0027] - And then in the carbon dioxide storage step, the organic nutrient solution prepared in the foregoing steps is treated with a carbon dioxide-containing gas such that gaseous carbon dioxide is bound through the organic nutrient solution. And / or

[0028] Variant 2. A bioreactor (1, 2, 3) for converting organic residues and / or waste into an organic nutrient solution, wherein based on the total nitrogen content of the organic nutrient solution, the organic nutrient solution has a proportion of plant-available mineralized nitrogen of at least 10%. The bioreactor has a reaction vessel (5), wherein the reaction vessel (5) has a feed line (6) through which a suspension (4) can be introduced into the reaction vessel (5), and wherein the reaction vessel (5) has a discharge line (7) through which the suspension (4) originating from the reaction vessel (5) can be discharged. The bioreactor (1, 2, 3) has a ventilation device (8) through which oxygen can be introduced into the reaction vessel (5) and the suspension (4) contained therein. In the receiving space (9) of the reaction vessel (5), at least one carrier unit (10) having a breeding area (11) for forming a biofilm (12) of microorganisms is provided, wherein the at least one carrier unit (10) can be rinsed back and forth and / or thoroughly rinsed with the introduced suspension (4) and the introduced oxygen, and the ratio of the surface area to the volume of the carrier unit (10) is greater than the ratio of the surface area to the volume of the receiving space (9). It is characterized in that the ventilation device (8) has a hydrogen peroxide reservoir and at least one catalyst, whereby during ventilation, the hydrogen peroxide flowing out of the hydrogen peroxide reservoir can be converted into or is converted into water and oxygen in a catalytic reaction. And / or

[0029] Variant 3. An organic nutrient solution prepared by the method according to Variant 1 and / or in the bioreactor (1, 2, 3) according to Variant 2, which has a proportion of at least 10% of mineralized nitrogen that is plant - available based on the total nitrogen content of the organic nutrient solution. And / or

[0030] Variant 4. Use of the organic nutrient solution according to Variant 3 as an absorbent for storing COX and / or NOx and / or SOX, wherein the organic nutrient solution is treated with a gas containing COX and / or NOx and / or SOx. And / or

[0031] Variant 5. A nutrient production and carbon dioxide storage system (37), comprising:

[0032] - A fermentation device (38) for producing organic residues and / or waste,

[0033] - Optionally, a combined heat and power plant (39) for burning the biogas produced by the fermentation device (38) to obtain electrical energy and / or heat,

[0034] - A bioreactor (1, 2, 3), in particular the bioreactor according to Variant 2, for converting organic residues and / or waste into an organic nutrient solution, and

[0035] - A carbon dioxide storage device (40) having a carbon dioxide storage space (41), in which at least one scrubber device (42) is provided for carrying out a liquid - gas reaction between the carbon dioxide - containing gas and the organic nutrient solution prepared by the bioreactor (1, 2, 3). And / or

[0036] Variant 6. Use of the organic nutrient solution according to Variant 3, the organic nutrient solution being used as a medium for binding carbon and / or enriching carbon in plants and / or soil.

[0037] In particular, to solve this problem, a bioreactor of the above - mentioned type is proposed, in which the ventilation device has a hydrogen peroxide storage and at least one catalyst, whereby during ventilation, the hydrogen peroxide flowing out of the hydrogen peroxide storage can be converted into water and oxygen in a catalytic reaction. This has the advantage of being able to supply oxygen uniformly in the reaction vessel. Therefore, the liquid contained in the reaction vessel can be particularly well enriched with oxygen. In addition, compared with other ventilation devices, the preparation and maintenance costs of the catalytic conversion of hydrogen peroxide to oxygen are relatively low.

[0038] According to a particularly advantageous design, at least one catalyst can be arranged between the hydrogen peroxide storage and the outlet of the ventilation device. This can better prevent hydrogen peroxide from entering the reaction vessel and being converted into oxygen and water before the outlet of the ventilation device.

[0039] It may be particularly advantageous if at least one catalyst consists of pyrolusite (Braunstein) and / or manganese oxide, in particular manganese dioxide and / or manganite (Manganit).

[0040] It may be particularly suitable if the ventilation device corresponds to the device constructed according to US 4,784,665. The content of US 4,784,665 is hereby incorporated by reference.

[0041] To achieve the above object, a method for preparing an organic nutrient solution is proposed. Based on the total nitrogen content of the organic nutrient solution, the organic nutrient solution has a proportion of at least 10%, in particular at least 25%, preferably at least 50%, more preferably at least 75% of plant-available mineralized nitrogen. Here, it is preferred that the nitrate content of the plant-available mineralized nitrogen is higher than the ammonium content. Here, it is further preferred to use a bioreactor as described and claimed herein.

[0042] The method comprises the following steps:

[0043] - In the inoculation step, the carrier unit is inoculated with an inoculum containing ammonifying bacteria and / or nitrifying bacteria, preferably the carrier unit of a bioreactor as described and / or claimed herein,

[0044] - On the carrier unit, a biofilm with ammonifying bacteria and / or nitrifying bacteria is formed,

[0045] - In the cultivation step, the organic residues and / or wastes are cultivated together with the biofilm, in particular in a reaction vessel, where the ammonifying bacteria and / or nitrifying bacteria convert the organic-bound nitrogen in the residues and / or wastes into mineralized nitrogen,

[0046] - wherein during the implementation of each or all steps, oxygen is introduced into the reaction vessel and / or the carrier unit by means of a ventilation device

[0047] - and wherein then in the carbon dioxide storage step, the organic nutrient solution prepared in the foregoing steps is treated with a carbon dioxide-containing gas, in particular biogas and / or the exhaust gas from a central heating plant, such that gaseous carbon dioxide is bound by the organic nutrient solution. This carbon dioxide storage step can preferably be carried out in a carbon dioxide storage space sealed from the outside.

[0048] By the method according to the invention, not only can an organic nutrient solution with a high proportion of plant-available mineralized nitrogen be prepared. The organic nutrient solution is also treated with carbon dioxide that has hitherto been simply released into the atmosphere, so that the carbon dioxide is absorbed and stored by the nutrient solution. Thus, the nutrient solution provides a better carbon source for the plants fertilized therewith, the soil bacteria and the soil itself. In addition, the climate-damaging gases are prevented from escaping into the atmosphere, but are returned and bound in the cycle.

[0049] CO2 absorption in the organic nutrient solution occurs on cations such as NH4 and potassium. In addition, when added to the soil, on the soil, the organic nutrient solution forms stable carbonates with alkaline earth metals such as magnesium and calcium in the soil. Other alkaline minerals present in the groundwater are neutralized by the bicarbonate HCO3 formed during the absorption process. In the formed organic nutrient solution, plant nutrients are present in a mineralized form that can be directly utilized by plants and are absorbed by the plants. By virtue of this property, these fertilizers can rival the effectiveness of mineral NPK fertilizers and can replace them. Due to their replaceability, the fertilizers have the property of actively restraining carbon dioxide emissions and avoiding additional carbon dioxide emissions.

[0050] The nutrient solution can be preferably concentrated before carbon dioxide storage in a way that reduces the water content. This can be done, for example, by vacuum distillation. Thereby, it is possible to better bind CO2.

[0051] According to a further improvement, it can be designed that during the carbon dioxide storage step, the expansion of the surface of the organic nutrient solution. In particular, this can be achieved by guiding the organic nutrient solution through a scrubber device. The scrubber device can, for example, involve one device selected from the following group or a combination of two or more devices: bubble column reactor, tubular reactor, jet nozzle reactor, stirred tank, thin film reactor, and / or spray tower. With the help of this scrubber device, the surface expansion of the organic nutrient solution is possible, which increases the efficiency of binding CO2 by the organic nutrient solution.

[0052] To achieve the above object, an organic nutrient solution is also proposed, which is prepared by the above method and / or in the above bioreactor and thus has an additional carbon source. It can be particularly preset therein that based on the total nitrogen content of the organic nutrient solution, the organic nutrient solution has a proportion of at least 10%, particularly at least 25%, preferably at least 50%, more preferably at least 75% of plant-available mineralized nitrogen. Preferably, the nitrate content of the plant-available mineralized nitrogen is higher than the ammonium content, more preferably NO3:NH4 + The ratio is at least 2:1, particularly at least 3:1, especially at least 10:1, preferably at least 25:1, more preferably at least 50:1.

[0053] According to a further development, it can be designed that the organic nutrient solution (also referred to as "soiling NRF") has an ammonium content (NH4 + ) of at least 10% of the total nitrogen content of the organic nutrient solution, and / or a potassium content (K + ) of at least 10% of the total solid content of the organic nutrient solution, and / or a calcium content (Ca 2+ ) of at least 5% of the total solid content of the organic nutrient solution, and / or a magnesium content (Mg of at least 1% of the total solid content of the organic nutrient solution+ ), and / or a protein content of at least 15% of the total solids content of the organic nutrient solution. In particular, the pH value of the organic nutrient solution can be at most 7.5, preferably below 7.5, more preferably at most 7.0, more preferably at most 6.5, more preferably at most 6.0. The absorption capacity of the nutrient solution is determined by the molar flow rate of the gas, the absorption efficiency of the gas / liquid reactor system, the volume of the absorbent, and the flow rate. The pH value of the nutrient solution can be regarded as an indicator of CO2 absorption. NH4 + , potassium, calcium, and magnesium ions start to carbonize at a pH value > 7.5 and decrease with the absorption of CO2. For example, as ammonium bicarbonate (NH4HCO3) is formed, the OH concentration decreases, thus causing the pH value to decrease. By absorbing CO2 from the amine group, the number of protons increases, and the pH value decreases.

[0054]

[0055]

[0056] To solve this problem, it is proposed to use the organic nutrient solution described and / or claimed herein and / or prepared by the method described and / or claimed herein and / or prepared in the bioreactor described and / or claimed herein as a storage absorbent for CO X and / or NO X and / or SO X . In particular, it can be designed for use as an absorbent for carbon dioxide storage, for example, in a biogas plant and / or a central heating power plant, where the organic nutrient solution is treated with a gas containing CO X and / or NO X and / or SO X , especially in a closed and / or isolated space, such as a gas containing carbon dioxide, especially biogas and / or exhaust gas from a combustion process, such as exhaust gas from a central heating power plant or exhaust gas from burning fossil fuels. This has the following advantages: gaseous CO X and / or NO X and / or SO X , especially carbon dioxide, is bound by the organic nutrient solution herein. This makes it possible to replace the amine washing based on amine compounds such as monoethanolamine and diethanolamine, which have been most commonly used for storing carbon dioxide and other gases to date. Through this, a particularly environmentally friendly alternative to amine washing can be created.

[0057] To achieve this purpose, a nutrient production and carbon dioxide storage system is also proposed, including:

[0058] - A fermentation device, especially a biogas plant, which is used to produce organic residues and / or wastes,

[0059] - An optional central heating power plant for burning biogas produced by a fermentation device to obtain electrical energy and / or heat,

[0060] - A bioreactor as described and / or claimed herein for converting organic residues and / or waste into an organic nutrient solution, in particular into the nutrient solution as described and / or claimed herein, and

[0061] - A carbon dioxide storage device having a carbon dioxide storage space, preferably a carbon dioxide storage space that can be sealed from the outside, in which at least one scrubber device is provided for performing a liquid-gas reaction between a carbon dioxide-containing gas, in particular biogas and / or the exhaust gas of a central heating power plant (39), and the organic nutrient solution prepared by the bioreactor. This has the advantage of forming a preferably closed gas circuit from which no or almost no carbon dioxide escapes before the carbon dioxide storage step. The carbon dioxide generated as waste during the fermentation process and / or the incineration process can be used by the nutrient production and carbon dioxide storage system to refine the nutrient solution in order to additionally provide a carbon source that is particularly plant-available for the plants to be fertilized, soil bacteria, and the soil itself. Preferably, the fermentation device installed for this purpose and / or, if a central heating power plant is planned, the exhaust gas can be led to the carbon dioxide storage device via at least one gas pipeline. According to a preferred embodiment variant, the bioreactor can also be used as a carbon dioxide storage device. However, the carbon dioxide storage device can also be constructed as a unit independent of the bioreactor. There can preferably be at least one liquid pipeline between the carbon dioxide storage device and the bioreactor so that the organic nutrient solution can be further conducted.

[0062] According to an advantageous embodiment, it can be designed that the carbon dioxide storage space is divided into at least two chambers, the scrubber device is arranged in the first chamber, and the second chamber is designed as a collection chamber for the organic nutrient solution, and the organic nutrient solution is discharged from the first chamber to the second chamber and / or from the second chamber to the first chamber by at least one pumping device. Thus, it is possible to particularly effectively combine the nutrient solution with carbon dioxide.

[0063] As an alternative or supplement, the nutrient production and carbon dioxide storage system can have a concentration device by which the water content of the organic nutrient solution can be reduced. For example, a concentration device can be provided for performing vacuum distillation.

[0064] In particular, it is proposed in the case of a bioreactor of the above type, which has a ventilation device through which oxygen can be introduced into the reaction vessel and the suspension contained therein. In the receiving space of the reaction vessel, at least one carrier unit having a breeding area is provided for forming a biofilm of microorganisms, wherein the at least one carrier unit can be thoroughly rinsed and / or flushed with the introduced suspension and the introduced oxygen, and the surface area to volume ratio of the carrier unit is configured to be greater than the surface area to volume ratio of the receiving space. With the aid of the bioreactor, a biofilm can be formed at a desired position on the breeding area within the receiving space. In this way, ideal growth conditions can be created for ammonifying bacteria and / or nitrifying bacteria in the breeding area. By means of the bioreactor, the required conversion reactions of the microorganisms can be better supported, so that an organic nutrient solution with a higher nitrogen content utilizable by plants can be produced. It can be particularly preferred if the surface area to volume ratio of the carrier unit is designed to be at least eight times the surface area to volume ratio of the receiving space. The ventilation unit can be arranged, for example, to introduce oxygen in the form of air.

[0065] According to an advantageous refinement, at least one carrier unit can be made of one material or a combination of two or more materials selected from plastics (in particular food-neutral plastics), minerals (in particular zeolites) and / or a rubber-plastic mixture. It can be particularly suitable here if the plastic is polypropylene and / or polyethylene and / or rubber, since microorganisms can reproduce particularly well on this plastic and form a biofilm. A polyethylene-rubber mixture is also useful. It is also conceivable to provide a mineral-plastic mixture, in particular a zeolite-plastic mixture.

[0066] It is also particularly advantageous if the breeding area of the carrier unit is at least partially formed in pores and / or chambers. This has the advantage that, in the case of a relatively small external dimension of the carrier unit, the carrier unit has the largest possible surface area for reproduction. The pores and / or the passages leading to the chambers can preferably have a diameter of 10 μm to 100 μm, such that the pores and / or the passages allow the passage and / or penetration of liquids and gases and the penetration and retention of microorganisms. It can be particularly advantageous if the pores are at least partially or mostly permeable, i.e., in particular, the material is designed to have open pores. In this way, particularly good thorough flushing of the suspension can be achieved.

[0067] Alternatively or additionally, according to another advantageous embodiment, it can be designed such that at least one carrier unit is designed to be removable from the reaction vessel, in particular without tools. In particular, the carrier unit can be designed as a replaceable module. This has the advantage that it allows for the quick and easy removal and replacement of the carrier unit from the reaction vessel. Additionally, it is particularly advantageous that guiding means are arranged in the receiving space, by means of which the carrier unit can be introduced into the receiving space in a guided manner, in particular can be pushed or inserted. The position of the carrier unit within the receiving space can thus be defined by the guiding means.

[0068] In order to facilitate the introduction of oxygen into the reaction vessel and better avoid anaerobic reactions, it can be designed that oxygen can be introduced into the reaction vessel and / or at least one carrier unit through a supply line by means of a ventilation device. Here, it is advantageous that the ventilation device has at least one compressor or a gas interface in order to be able to better regulate the gas supply. Preferably, the supply line can be independent of the feed line and the discharge line, so that oxygen and the suspension can be introduced independently of each other. For example, oxygen can also be introduced in the form of air. The advantage is that, in particular, pure oxygen is not introduced, but rather recycled air that can be used in unlimited quantities.

[0069] Alternatively or additionally, the ventilation device is constructed at the bottom of the reaction vessel with a number of ventilation openings, in particular one or the ventilation device made as a ventilation plate as described above. In particular, by means of the ventilation device, a uniform bubble density can be generated within the reaction vessel, preferably within the receiving space, so that particularly uniform ventilation within the reaction vessel becomes possible. The ventilation openings can preferably be arranged to have the same diameter and / or at the same interval from each other. More preferably, the ventilation device can be constructed in a conical shape, so that it is easier to prevent the ventilation openings from being blocked by the settling of solid particles in the suspension.

[0070] In order to achieve particularly good circulation of the suspension within the receiving space, the bioreactor can have a pumping device. The pumping device can, for example, be designed as a centrifugal pump or a circulation pump. Additionally, it is advantageous that the suspension can be pumped into the reaction vessel through the feed line and pumped out of the reaction vessel through the discharge line by means of the pumping device. In order to be able to set different flow rates through the reaction vessel and / or the feed and discharge lines, the pump output of the pumping device can be changed, in particular manually adjustable and / or programmable. Preferably, the pumping device can be used to generate a flow direction of the suspension within the reaction vessel, which flow direction at least partially flows in the opposite direction and / or at least partially flows in the oxygen flow direction. Through this, particularly good mixing of the suspension and oxygen can be achieved. In order to be able to automate the implementation of a multi-step preparation method with the aid of the reactor, the pumping device can preferably be programmed to automatically set a pumping program with a number of sub-steps.

[0071] In order to create ideal growth and / or conversion conditions for microorganisms, the bioreactor can be provided with a heating device by means of which the receiving space of the reaction vessel and / or the suspension in the receiving space of the reaction vessel can be heated to an adjustable temperature. In particular, a temperature of 20 °C to 34 °C can be provided, preferably a temperature of 22 °C to 32 °C.

[0072] For the carrier unit to be easily removable from the bioreactor, according to an advantageous refinement, the reaction vessel has an opening for filling the receiving space of the reaction vessel, and the bioreactor has a closing unit by means of which the opening of the reaction vessel can be closed. The opening of the reaction vessel can preferably be closed by the closing unit in a liquid-tight and / or pressure-resistant manner.

[0073] In order to avoid disruptive external influences on the conversion of organic residues and / or waste into organic nutrient solution, the wall of the reaction vessel and one or the aforementioned closing units can be designed to be opaque. Thereby, the conversion rate can be increased.

[0074] It can also be expedient if the breeding area is hydrophobic.

[0075] In order to make it easier for microorganisms to attach to the breeding area, the breeding area can have a higher roughness than the inner side of the reaction vessel wall.

[0076] In order to provide as large a total breeding area as possible for the reproduction of microorganisms, the bioreactor can have a plurality of carrier units. The carrier units can preferably be designed and / or arranged to be movable relative to each other. The carrier units are preferably arranged loosely in the receiving space. By means of the circulation of the suspension, the carrier units can also be circulated and / or moved by the flow generated thereby. Thereby, the gas exchange and suspension exchange at the carrier units can be improved.

[0077] According to a particularly preferred refinement, a large number of fragments, in particular a large number of flowable fragments made of plastic, can be provided as carrier units, wherein the fragments can be arranged in a disordered manner in the reaction vessel. In particular, the disordered distribution causes the fragments to become entangled with each other. Thus, the breeding areas of the fragments may not adhere to each other and / or may not be sufficiently flushed with oxygen, so that an undesired denitrification process does not occur. It can be particularly preferred if the fragments have one shape or a combination of shapes selected from the group of spiral and / or meandering and / or wavy fragments. This is a particularly good way to prevent the breeding areas of the fragments from adhering to each other or coming into contact with each other.

[0078] The fragments can preferably each have a length of 2 cm to 10 cm and / or a width of 0.5 cm to 1.5 cm and / or a thickness of 50 μm to 500 μm.

[0079] Alternatively or additionally, at least one porous hose can be provided as the carrier unit. In particular, the hose can be arranged transversely or parallel to the flow direction of the oxygen introduced into the reaction vessel and / or transversely or parallel to the flow direction of the suspension introduced into the reaction vessel. This results in particularly good rinsing effect of the hose.

[0080] According to an advantageous refinement, it can be designed that the oxygen can be introduced through the hose or the above-mentioned hose via a supply line. In particular, the supply line can be designed as a bypass gas line, which branches off from the main gas line (preferably leading to a ventilation device or the main gas line of the aforementioned ventilation device). Thus, a particularly good oxygen supply can be provided for the microorganisms breeding on the inner side of the hose wall. The bioreactor preferably has a plurality of carrier units configured as hoses. It can also be designed that the hoses are integrated into a pipeline extending in the receiving space. Such a pipeline can be tied to the feed pipeline and / or the discharge pipeline. Preferably, shut-off valves can be used in the pipeline in the receiving space before and / or after the hose. Thus, the internal pressure of the hose can be increased in a simple manner by closing the shut-off valve arranged behind the hose in the flow direction, whereby the suspension flow can be guided through the holes in the hose for at least a short time. Or by closing the shut-off valve arranged upstream of the hose in the flow direction, the introduction of the suspension into the hose can be prevented.

[0081] According to another advantageous refinement, it can be designed that the carrier unit is designed as zeolite particles. In particular, the zeolite particles can have a particle size of 0.6 mm to 1.0 mm. The zeolite particles and / or another carrier material can preferably be arranged in a collection unit preferably configured as a textile bag and placed in the reaction vessel. Thus, the carrier material can be prevented from being washed into poorly ventilated and / or poorly mixed areas in the receiving space.

[0082] Alternatively or additionally, another ventilation device can be provided on or at the bottom of a collection unit or the aforementioned collection unit, through which oxygen can be introduced into the zeolite particles and / or another carrier unit. The said another ventilation device can preferably be connected to a bypass gas line branching off from the main gas line. Through the said another ventilation device, the zeolite particles and / or other carrier units can be particularly well rinsed with oxygen comprehensively.

[0083] In order to better avoid the sedimentation of solids in the suspension at the bottom of the receiving space, the feed line can lead to the reaction vessel above the discharge line and / or at the same height as the discharge line. Thus, the sinking particles can preferably be introduced into the receiving space higher up and discharged from a lower position in the receiving space. As an alternative or in addition, the bioreactor can have multiple feed lines and / or multiple discharge lines. During the use of the bioreactor, whether a line of the bioreactor serves as a supply line or a discharge line task can preferably be at least partially defined by the adjustable flow direction of the suspension. This allows at least two different flow directions to be preferably set simultaneously within the reaction vessel, where the existing lines can be used as feed or discharge lines according to the flow direction. For example, at least two discharge pipes can lead out from the reaction vessel near the bottom to be able to more effectively discharge the deposited particles and the suspension.

[0084] In order to achieve a particularly good circulation of the suspension within the receiving space of the reaction vessel, at least two suspension flow directions can be set within the reaction vessel and / or within the lines of the biological reaction by means of a pumping device or the aforementioned pumping device. To achieve particularly good circulation, the feed line and the discharge line can alternatively or additionally be separated from each other by a pumping device or the aforementioned pumping device. In particular, the bioreactor can have a suspension circuit including a feed line, a discharge line, a pumping device, and a reaction vessel, such that the suspension can be repeatedly guided through the biofilm within the reaction vessel.

[0085] In order to more easily adjust the suspension flow, a shut-off valve can be provided in the feed line between the reaction vessel and the pumping device, and / or a shut-off valve can be provided in the discharge line between the reaction vessel and a pumping device or the aforementioned pumping device.

[0086] According to an advantageous development of the bioreactor, especially after one or the aforementioned pumping devices and / or before one or the aforementioned shut-off valves, a bypass feed line can branch off from the feed line and connect to the reaction vessel. Thus, the suspension can also be additionally introduced into the reaction vessel through the bypass feed line. Preferably, the bypass supply line can have a shut-off valve. It can also preferably be designed that in the case where the flow direction of the suspension through the pumping device changes, especially reverses, the bypass supply line can be used as a discharge line. Thus, the variability of the flow path can be increased, which results in an even better circulation of the suspension in the reaction vessel.

[0087] This can be particularly advantageous if a biofilm with ammonifying bacteria and / or nitrifying bacteria has colonized the propagation area. Here, for example, it can be designed such that the proportion of ammonifying bacteria and / or nitrifying bacteria in the biofilm is at least 2%, preferably at least 4%, preferably at least 6%, preferably at least 10%, preferably at least 15%, preferably at least 20%, preferably at least 25%, preferably at least 30%, preferably at least 40%, preferably at least 50%, preferably at least 60%, preferably at least 70%, preferably at least 80%, preferably at least 90%, preferably approximately 100%.

[0088] In order to create as large a surface as possible for the propagation of microorganisms, at least one carrier unit can have a plurality of propagation areas, where the propagation areas can be designed to be curved, so as to avoid adhesion and / or abutment of the propagation areas of the carrier unit with each other, and / or adhesion and / or abutment of the propagation areas of different carrier units with each other.

[0089] According to the present invention, the above object is also achieved by the features of the independent method aspect for preparing an organic nutrient solution. In particular, a method for preparing an organic nutrient solution is proposed to achieve the above object, wherein the organic nutrient solution has a proportion of plant-available mineralized nitrogen of at least 10%, in particular at least 25%, preferably at least 50%, more preferably at least 75%, based on the total nitrogen content of the organic nutrient solution. Preferably, the nitrate content in the plant-available mineralized nitrogen is higher than the ammonium content. Here, it can be particularly preferred that in the organic nutrient solution, the NO3:NH4+ ratio is at least 2:1, in particular at least 3:1, in particular at least 10:1, preferably at least 25:1, more preferably at least 50:1. The method here includes the following steps:

[0090] - In the inoculation step, inoculate the carrier unit with inoculation material containing ammonifying bacteria and / or nitrifying bacteria, preferably the carrier unit of the bioreactor as described and claimed herein,

[0091] - Form a biofilm with ammonifying bacteria and / or nitrifying bacteria on the carrier unit,

[0092] - In the cultivation step, cultivate the organic residues and / or wastes together with the biofilm, in particular in a reaction vessel, wherein the ammonifying bacteria and / or nitrifying bacteria convert the organically bound nitrogen in the residues and / or waste materials into mineralized nitrogen.

[0093] For the first time by this method, an organic nutrient solution usable as a plant fertilizer can be produced from organic residues and / or waste. In the case of this method, due to the special method, the proportion of nitrogen available to plants is significantly increased. According to a preferred embodiment, in the case of this nitrogen available to plants, a distinct shift in the ratio of nitrate to ammonium content towards nitrate can also be achieved. Plants are particularly dependent on nitrate, especially in soilless hydroponic systems, because it can be better absorbed. In addition, the odor pollution that often occurs in organic residues and / or waste (which is especially caused by ammonia) can be significantly reduced until the odor in the final organic nutrient solution is completely neutralized.

[0094] According to the present invention, the above object is also achieved by the features of an independent method aspect for preparing a substrate material for plant cultivation. In particular, therefore, a method for preparing a substrate material for cultivating plants is proposed to achieve the above object, which comprises the following steps:

[0095] - In an inoculation step, a carrier unit is inoculated with an inoculation material containing ammonifying bacteria and / or nitrifying bacteria, preferably the carrier unit of a bioreactor according to one of the foregoing aspects.

[0096] - A biofilm with ammonifying bacteria and / or nitrifying bacteria is formed on the carrier unit.

[0097] Using the above method, the carrier unit can thus be inoculated with ammonifying bacteria and / or nitrifying bacteria and the biofilm can grow on the carrier unit thereby. The carrier unit can then be used, for example, in a bioreactor as described and claimed herein, or used as a substrate material as described and claimed herein.

[0098] The following advantageous developments relate to the above two methods.

[0099] In order to be able to achieve particularly good inoculation and / or conversion, the inoculation material and / or organic residues and / or waste can be used in liquid form. Preferably, the inoculation material and / or organic residues and / or waste can be used in the form of a suspension. Thus, particularly good wetting of the carrier unit with the inoculum and / or organic residues and / or waste is possible. In addition, a particularly simple and effective recycling of the organic residues and / or waste is possible. For this purpose, for example, the inoculation material and / or organic residues and / or waste present as solids can be mixed with water to produce a suspension.

[0100] It may be advantageous if the inoculation material or a combination of one or more inoculation materials selected from the group consisting of: compost, especially bark compost, worm excrement, especially earthworm excrement, soil, especially field soil is used. In addition to ammonifying bacteria and / or nitrifying bacteria, these inoculation materials also contain mucus and / or protein substances, which can accelerate the formation of the biofilm on the carrier unit and stabilize the biofilm. In principle, worm excrement living in the soil is suitable because they are rich in ammonifying bacteria and / or nitrifying bacteria.

[0101] According to a particularly advantageous embodiment, the proportion of organic material in the organic residues and / or waste can be 5% to 60%.

[0102] Alternatively or additionally, the carbon / nitrogen ratio of the organic residues and / or waste can be 11 or less. When the value is higher than 11, the conversion rate will decrease.

[0103] It is also advantageous if the total nitrogen content based on the total weight of the organic residues and / or waste is at least 0.3%.

[0104] It can be further designed that, based on the total content of plant-available nitrogen in the organic residues and / or waste, the proportion of nitrogen bound to nitrate is less than the proportion of nitrogen bound to ammonium. This proportion can be changed by the method so that most of what exists is nitrate rather than ammonium.

[0105] In order to create ideal growth conditions for ammonifying bacteria and / or nitrifying bacteria, individual or all method steps can be carried out at a temperature, especially a constant temperature, of 20°C to 34°C, preferably 22°C to 32°C.

[0106] In order to prevent anaerobic denitrifying bacteria from carrying out an undesired denitrification process and to adequately supply oxygen to aerobic ammonifying bacteria and / or nitrifying bacteria, oxygen can be introduced into the reaction vessel and / or the carrier unit when carrying out individual or all steps.

[0107] In order to better prevent anaerobic bacteria from multiplying during the inoculation step, the inoculation material can be circulated during the inoculation step. Especially by pumping the inoculation material multiple times and / or in different flow directions through a preferably closed loop in which a carrier unit is arranged. In particular, the inoculation material and part of the biofilm fixed on the carrier unit can be torn off by circulation and reattached at another position. This tearing off and reattaching promotes bacterial growth.

[0108] Alternatively or additionally, the organic residues and / or waste can be circulated during the cultivation step to better prevent the occurrence of solid precipitation and anaerobic degradation processes. Especially the organic residues and / or waste can be pumped multiple times and / or in different flow directions through a preferably closed loop in which a carrier unit is arranged.

[0109] In order to further improve the transformation efficiency of bacteria, the inoculation step can be divided into a first stage of continuous aeration and / or circulation and a second stage of discontinuous aeration and / or circulation. Preferably, an aeration pause and / or a circulation pause can be carried out during the second stage, especially for 30 to 50 minutes per hour.

[0110] It can also be expedient if the inoculation step and the cultivation step are carried out in different reaction vessels. Preferably, the reaction vessel used in the inoculation step can have a smaller volume than the reaction vessel used in the cultivation step.

[0111] It can be further designed that the cultivation step has an ammonification step and / or a nitrification step, wherein during the ammonification step the organically bound nitrogen from organic residues and / or waste is converted into ammonium groups by the ammonifying bacteria of the biofilm, and / or wherein during the nitrification step the ammonium groups are converted into nitrates by the nitrifying bacteria in the biofilm. Depending on the organic residues and / or waste materials used and the initial proportion of plant-available nitrogen they have, sometimes only one nitrification step can be designed. In particular, the cultivation step can be carried out until the organic nutrient solution contains more nitrates than ammonium groups, preferably until the NO3:NH4 + ratio is at least 2:1, especially at least 3:1, preferably at least 10:1, preferably at least 25:1, more preferably at least 50:1. In order to determine the proportion of plant-available nitrogen, the measurement step can preferably be carried out regularly or continuously. Measurement methods known to those skilled in the art for determining nitrate and / or ammonium concentration and / or total nitrogen concentration can be used.

[0112] According to a particularly advantageous improvement, at least one porous hose (especially a porous rubber-plastic hose) can be used as the carrier unit, wherein oxygen and the inoculation material and / or oxygen and residues and / or waste are introduced into the hose at different times. Here, it is preferably possible to vary the internal pressure of the hose during the inoculation step and / or the cultivation step, especially by increasing the flow rate of the inoculation material and / or residues and / or waste through the hose over a period of time, and / or by increasing the volumetric flow rate of oxygen through the hose over a period of time. The porous hose form of the carrier unit has the advantage of generating a relatively large reproduction area for the microorganisms. Especially due to the open-pore structure, the suspension flowing through the hose can also be discharged through the pores penetrating the hose wall. Thus, on the one hand, particularly good inoculation of the entire reproduction area is possible, and in addition, particularly good supply of oxygen and nutrients to the biofilm bacteria is possible. In particular, the hose can be designed to be flexible, i.e., stretchable, which has the advantage that the pore diameter can be enlarged when the pressure inside the hose increases. Thus, an increased flow rate through the pores can be achieved at least for a short time, for example in order to also achieve better circulation of the suspension inside the hose.

[0113] In order to achieve particularly good wetting of the carrier material, the carrier unit can be completely immersed in the inoculation material during the inoculation step, and / or the carrier unit can be completely immersed in the residues and / or waste during the cultivation step.

[0114] The present invention also relates to an organic nutrient solution, in particular an organic plant fertilizer, prepared by the methods as described and claimed herein and / or in the bioreactors as described and claimed herein. Based on the total nitrogen content of the organic nutrient solution, it has a proportion of at least 10%, in particular at least 25%, preferably at least 50%, more preferably at least 75% of plant-available mineralized nitrogen. Preferably, the nitrate content of the plant-available mineralized nitrogen is higher than the ammonium content. Further preferably, in the organic nutrient solution, the NO3:NH4 + ratio is at least 2:1, in particular at least 3:1, especially at least 10:1, preferably at least 25:1, more preferably at least 50:1. The advantage of the organic nutrient solution is that, compared with industrially produced mineral fertilizers, it can also be used in organic agriculture. An organic plant fertilizer with such a high nitrogen mineralization rate made entirely from organic residues and / or waste is hitherto unknown.

[0115] Preferably, the organic nutrient solution is a liquid fertilizer.

[0116] In order for the organic nutrient solution to be used in organic agriculture, the plant-available mineralized nitrogen must be completely or substantially converted from organically bound nitrogen and / or the organic nutrient solution does not contain industrially produced mineral fertilizers. Industrially produced mineral fertilizers include, for example, mineral salts obtained by chemical or physical treatment from raw materials mainly mined in mining, especially nitrogen fertilizers of non-organic origin. The organic residues and / or waste used as starting materials for preparing the organic nutrient solution can include, for example, plant and / or animal waste, fermentation residues, especially from biogas plants, manure water, sewage, farm manure, and organic secondary raw materials from the food and consumer and feed industries.

[0117] The present invention further relates to a substrate material for cultivating plants with an ammonifying bacteria and / or nitrifying bacteria biofilm, which is prepared by the methods as described and claimed herein and / or by the bioreactors as described and claimed herein. The carrier unit preferably can have pores and / or chambers with a diameter of 10 μm to 100 μm.

[0118] According to an advantageous improvement of the substrate material, the carrier unit can be designed as a porous tube. The carrier unit can preferably be designed as a hose made of a plastic-rubber mixture. Here, referring to the implementation of the carrier unit of the bioreactor, it can also be useful for the substrate material.

[0119] According to another advantageous refinement of the substrate material, the carrier unit can be made of minerals, in particular of zeolites. In particular, the carrier unit can be designed as zeolite granules. Zeolites are particularly suitable as soil aids because, based on their porous structure, they have a particularly large surface area composed of an inner surface and an outer surface, which can be used as a breeding area. Thus, despite the relatively large breeding area, zeolites require relatively little space.

[0120] In order to be able to better protect plants in contact with or cultivated in the vicinity of the substrate material from nutrient and / or water deficiencies, the carrier unit can have a sponge effect, by means of which the substrate material can store liquids. This can be achieved, for example, by the carrier unit being at least partially made of a foam material, in particular of a foamed plastic.

[0121] The invention also relates to the use of ammonifying bacteria and / or nitrifying bacteria in the form of a biofilm on the carrier unit, in particular in the bioreactors as described and claimed herein, for converting organic residues and / or waste into an organic nutrient solution, which, based on the total nitrogen content of the nutrient solution, has a proportion of at least 10%, in particular at least 25%, preferably at least 50%, more preferably at least 75% of plant-available mineralized nitrogen, in particular by carrying out the method as described and claimed herein. Here, it is preferred that in the final organic nutrient solution NO3:NH4 + is at least 2:1, in particular at least 3:1, especially at least 10:1, preferably at least 25:1, more preferably at least 50:1.

[0122] The invention also relates to the use of the organic nutrient solution as described and claimed herein for fertilizing plants, in particular for fertilizing plants grown according to organic farming standards. Compared to conventional organic plant fertilizers, the organic nutrient solution can better compensate for soil leaching occurring in the last third of crop growth.

[0123] According to an advantageous embodiment, the organic nutrient solution can be used in a hydroponic system, in particular in a soilless and / or poor-soil hydroponic system. Compared to other pure organic plant fertilizers, the organic nutrient solution is also suitable for soilless and / or poor-soil cultivation systems because the proportion of plant-available nitrogen, in particular plant-available nitrates, is significantly higher than that of conventional organic plant fertilizers.

[0124] The invention further relates to the use of the substrate material as described and claimed herein in plant cultivation. In particular for cultivating useful plants. Preferably, the substrate material can be mixed with the arable soil, in particular as a soil aid. In particular, it can be mixed under the soil of the field. This makes it possible to accelerate the ammonification and / or nitrification conversion processes occurring naturally in the soil. Thus, the organically bound nitrogen in the soil can be converted more quickly into plant-available nitrogen. This increases the fertility of natural soil and increases crop yields.

[0125] Alternatively or additionally, it can be designed that the substrate material serves as an anchoring material, especially in a hydroponic system. Thus, when the required soil is not available or is insufficient in form, the substrate material can be used so that plants can be fixed thereon.

[0126] According to a preferred refinement, plants can be in direct contact at least in part through their roots with the outside of the carrier unit of the substrate material. In particular, an organic nutrient solution can be guided through the carrier unit, especially the organic nutrient solution as described and claimed herein. Preferably, the organic nutrient solution can then diffuse and / or be extruded from the inside of the carrier unit to the outside of the carrier unit through holes in the inner wall of the carrier. This can provide particularly good nutrient supply for plants. For example, the carrier unit can be placed in arable land. In addition, as described above, the carrier unit can also be used in this form in poor soil or soil-free systems.

[0127] According to a particularly preferred refinement, plants can be in direct contact at least in part through their roots with the outside of the carrier unit of the substrate material, wherein the organic residues and / or waste are guided through the carrier unit, wherein the residues and / or waste are converted into mineralized nitrogen by bacteria of a biofilm, wherein the mineralized nitrogen diffuses and / or is extruded from the inside of the carrier unit to the outside of the carrier unit through holes in the carrier unit wall, and wherein the plant roots in at least partial contact with the outside of the carrier unit absorb the mineralized nitrogen available to the plants. Thus, the organic residues and / or waste can be directly used for supplying plants without prior separate conversion into an organic nutrient solution. It has surprisingly been shown that plants are sufficiently supplied with nitrogen due to the effective conversion of organically bound nitrogen into plant-available nitrogen by the biofilm on the carrier unit.

[0128] The invention also relates to a kit consisting of a bioreactor as described and claimed herein, and an inoculation material for inoculating the carrier unit and for forming a biofilm having ammonifying bacteria and / or nitrifying bacteria.

[0129] The invention also relates to a kit consisting of a carrier unit and an inoculation material for inoculating the carrier unit and for forming a biofilm having ammonifying bacteria and / or nitrifying bacteria, especially for carrying out the method as described and claimed herein, and / or in a bioreactor as described and claimed herein, and / or for the use as described and claimed herein.

[0130] The present invention further relates to the use of an organic nutrient solution as described herein and / or claimed herein and / or prepared by a method as described herein and / or claimed herein and / or prepared in a bioreactor as described herein and / or claimed herein, for use as a medium for binding and / or enriching carbon in plants and / or soil, preferably by means of alkaline earth metals present in the soil and / or by means of alkaline minerals in groundwater and weathering of topsoil minerals.

[0131] The present invention will now be explained in more detail on the basis of specific embodiments, but is not limited to these embodiments. Further embodiments result from combinations of the features of one or more of the aforementioned technical solutions with one another and / or combinations of the features of one or more of the specific embodiments. Specific embodiments

[0132] 1. Embodiment

[0133] Implementation of the method for preparing an organic nutrient solution, using the bioreactor as described and claimed herein in the following examples.

[0134] In the receiving space of the reaction vessel, first fermentation residues (obtained from the fermentation of biowaste) are added, the biowaste consisting of separately collected private household waste (92%), vegetable materials from food, consumer goods and feed production, vegetable materials from horticulture and landscaping, from forestry, fats and fat residues, which have a small proportion of plant-available nitrogen (less than 1%).

[0135] Alternatively or additionally, fermented beet molasses (distillers' grains) can be added as residues from the food and feed industries, which have an available nitrogen proportion of less than 0.5%.

[0136] As described above, inoculation of the carrier units is carried out separately in the first container.

[0137] Then, 200 grams of inoculated plastic carrier material with an estimated plastic contact area of 1.76 square meters is added in pieces to the second container and filled with 720 milliliters of organic liquid fermentation residues and 11 liters of water.

[0138] The fermentation residues have the following composition:

[0139] 0.46% total nitrogen N

[0140] 0.18% ammonium nitrogen N

[0141] 0.12% total phosphate P2O5

[0142] 0.42% total potassium oxide K2O

[0143] 0.0029% total zinc Zn

[0144] Minor components:

[0145] 0.11% of MgO in total magnesium oxide

[0146] 0.04% of S (sulfur)

[0147] 0.66% of CaO in basic active ingredients

[0148] 6.41% of organic matter

[0149] Bulk density 1040 kg / m 3

[0150] pH value 8.4

[0151] The total nitrogen in the initial solution was calculated to be 294 mg / l. The fermentation residue material introduced together with 11 liters of water had the initial values (measured using MQuant test strips from Merck KgaA, 64271 Darmstadt, Germany): TM Measured):

[0152] pH = 7.4

[0153] NH4 = 200 mg / l corresponding to NH4-N = 155 mg / l

[0154] NO3 = 0 mg / l

[0155] During the cultivation step, the liquid was heated to 25°C and air was blown in for 6 minutes per hour, 14 hours a day. This corresponds to a total air volume of 25.2 m 3 per day.

[0156] After 5 days, the NO3 value was 250 ml / l (corresponding to 56 ml / l of NO3-N), while the NH4 value had dropped to 90 ml / l (corresponding to 70 ml / l of NH4-N). After 9 days, the NO3 value reached a maximum of 1000 ml / l (226 ml / l of NO3-N), and the NH4 value was 15 ml / l (12 ml / l of NH4-N). At this time, 81% (238 mg / l) of the total nitrogen contained in the starting solution was present in a plant-available form. The nitrogen was present in a NO3 to NH4 ratio of 50:1. In the initial solution, 39% of the total nitrogen was present directly plant-available as 100% NH4.

[0157] In Central Europe, depending on temperature and soil moisture, the annual average mineralization rate of organic nitrogen in the soil is approximately 1 - 2%. At a mineralization rate of 2%, the 294 ml / l of total nitrogen in the soil would mineralize at a rate of 5.88 ml / l per year. After 9 days, 0.145 ml / l was mineralized. Compared to soil mineralization, this use results in a mineralization rate more than 1500 times higher.

[0158] 2. Embodiment

[0159] In this case, distillers' grains are used as organic residues and / or waste.

[0160] The inoculated plastic carrier material weighing 150 g with an estimated plastic contact area of 1.32 square meters was added in pieces to a second container, and the container was filled with 60 ml of distillers' grains and 93 liters of water.

[0161] The distillers' grains have the following composition:

[0162] 4.5% N total nitrogen

[0163] 0.5% N available nitrogen

[0164] 6% K2O total potassium oxide

[0165] Minor components:

[0166] 1.5% S water-soluble sulfur

[0167] 2.5% Na water-soluble sodium

[0168] 48% organic matter

[0169] Density 1360 kg / m 3

[0170] The total nitrogen was calculated to be 40 ml / l. The distillers' grains introduced together with 93 liters of water had the following initial values (measured using MQuant test strips from Merck KgaA, 64271 Darmstadt, Germany):

[0171] pH = 6.8

[0172] NH4 = 20 mg / l corresponding to NH4-N = 16 mg / l

[0173] NO3 = 5 mg / l corresponding to NO3-N = 1.2 mg / l

[0174] During the cultivation step, the liquid was heated to 25 °C and air was blown in for 10 minutes per hour, 14 hours per day. This corresponds to a total air volume of 42 cubic meters per day.

[0175] After 5 days, the NH4 value was 45 ml / l (corresponding to 35 ml / l of NH4-N), and the maximum value was 80 ml / l (corresponding to 62 ml / l of NH4-N) after 9 days. After 9 days, the NO3 value was 3 ml / l and increased to a maximum of 240 ml / l (50 ml / l of NO3-N) on the 11th day. At this time, the NH4 value was 8 ml / l (6 ml / l of NH4-N).

[0176] At this time, 140%*(56 ml / l) of the total nitrogen contained in the starting solution exists in a form available to plants. The nitrogen exists in a ratio of NO3 to NH4 of 8:1. In the initial solution, 11% of the total nitrogen exists directly available to plants in a ratio of NO3 to NH4 of 1:10.

[0177] In Central Europe, depending on temperature and soil moisture, the annual average mineralization rate in the soil is approximately 1 - 2% of the organic nitrogen. When the mineralization rate is 2%, it is calculated that 40 ml / l of the total nitrogen in the soil will mineralize at a rate of 0.8 ml / l per year. 0.02 ml / l is mineralized after 9 days. Compared with soil mineralization, this use results in a mineralization rate more than 2500 times higher.

[0178] *Total nitrogen was determined by the Kjeldahl method. The nitrogen contained in the protein content was largely determined, and the nitrogen content fluctuations depending on the amino acid composition were not considered here. It can be seen from this that the actual nitrogen content in the starting material is higher than the value determined by Kjeldahl analysis.

[0179] 3. Embodiment

[0180] A porous hose is used as the carrier material.

[0181] Fermentation residues (obtained from the fermentation of biowaste) are introduced through an inoculation carrier unit in the form of a hose. The biowaste consists of separately collected private household waste (92%), vegetable materials from food, consumer goods, and feed production, vegetable materials from horticulture and landscaping, and forestry, fats and fat residues, and it has a small proportion of nitrogen available to plants (less than 1%).

[0182] Alternatively or supplementally, fermented beet molasses (distillers' grains), which is a residue of the food and feed industries, with a proportion of available nitrogen less than 0.5%, can be introduced through an inoculation carrier unit in the form of a hose.

[0183] A nutrient solution with immediately plant-available mineralized N flows out separately over the pores of the carrier unit in the form of a hose and is absorbed by the plant roots in contact with the substrate as an immediately plant-available mineral nutrient solution.

[0184] For this purpose, 720 ml of liquid organic fermentation residues and 13 liters of water are injected.

[0185] The fermentation residues have the following composition:

[0186] 0.46% N total nitrogen

[0187] 0.18% N ammonia nitrogen

[0188] 0.12% P2O5 total phosphate

[0189] 0.42% total potassium oxide as K2O

[0190] 0.0029% total zinc as Zn

[0191] Minor components:

[0192] 0.11% total magnesium oxide as MgO

[0193] 0.04% sulfur as S

[0194] 0.66% basic active ingredient as CaO

[0195] 6.41% organic matter

[0196] Bulk density 1040 kg / m 3

[0197] pH value 8.4

[0198] The total nitrogen in this initial solution was calculated to be 251 ml / l. The introduced fermented residue material had the following initial values (measured using MQuant test strips from Merck KgaA, 64271 Darmstadt, Germany):

[0199] pH = 7.2

[0200] NH4 = 180 ml / l corresponding to 140 ml / l of NH4-N

[0201] NO3 = 0 ml / l

[0202] Three days later, when measuring the liquid (A) collected by dripping and the outer surface (B) of the inoculated carrier unit in the form of a hose, the following values were obtained:

[0203] <![CDATA[NO3(NO3-N)mg / l]]> <![CDATA[NH4(NH4-N)mg / l]]> <![CDATA[NO3:NH4]]> A 40(9) 190(148) 1:4.75 B 300(69) 50(34) 6:1

[0204] And after 5 days:

[0205]

[0206]

[0207] When an uninoculated hose-shaped carrier unit was supplied in parallel with the starting solution, the A and B measurement results obtained after 3 days and 5 days were the starting values.

[0208] 4. Embodiment

[0209] 25 ml of organic distillers' grains and 10 liters of water were injected through the inoculated carrier unit in the form of a hose.

[0210] The distillers' grains had the following composition:

[0211] 4.5% Total Nitrogen (N)

[0212] 0.5% Available Nitrogen (N)

[0213] 6% Total Potassium Oxide (K2O)

[0214] Minor Components:

[0215] 1.5% Water-Soluble Sulfur (S)

[0216] 2.5% Water-Soluble Sodium (Na)

[0217] 48% Organic Matter

[0218] Density 1360 kg / m 3

[0219] The total nitrogen in this initial solution was calculated to be 153 ml / l. The distillers' grains introduced together with 10 liters of water showed the following initial values (measured using MQuant test strips from Merck KgaA, Darmstadt, Germany, 64271):

[0220] pH = 6.5

[0221] NH4 = 15 ml / l corresponding to 12 ml / l of NH4-N

[0222] NO3 = 0 ml / l

[0223] When measuring the liquid (A) collected by dripping and the outer surface (B) of the inoculated carrier unit in the form of a hose after 1 day, the following values were obtained:

[0224] <![CDATA[NO3(NO3-N)mg / l]]> <![CDATA[NH4(NH4-N)mg / l]]> <![CDATA[NO3:NH4]]> A 35(27) 5(4) 7:1 B 35(27) 5(4) 7:1

[0225] After 7 days:

[0226]

[0227]

[0228] After 14 days

[0229] <![CDATA[NO3(NO3-N)mg / l]]> <![CDATA[NH4(NH4-N)mg / l]]> <![CDATA[NO3:NH4]]> A 20(5) 150(117) 1:7.5 B 400(92) 70(55) 5.7:1

[0230] When the carrier unit in the form of an uninoculated hose was supplied in parallel with the starting solution, the A and B measurement results obtained after 1, 7, and 14 days were the initial values.

[0231] 5. Embodiment

[0232] Zeolite particles were used as the carrier unit.

[0233] The inoculated zeolite particles are mixed into the growing soil. Fermentation residues (obtained from the fermentation of biowaste) are added to the zeolite - soil mixture, said biowaste consisting of separately collected private household waste (92%), vegetable materials from food, consumer goods, and feed production, vegetable materials from horticulture and landscaping, from forestry, fats and fat residues, and having a small proportion of plant - available nitrogen (less than 1%).

[0234] Alternatively or additionally, fermented beet molasses (vinasse) as residues from the food and feed industry can be added to the zeolite - soil mixture, said vinasse having an available nitrogen proportion of less than 0.5%.

[0235] 400 grams of inoculated zeolite particles with an estimated contact area of 21.6 square meters are added to a second container and filled with 440 ml of organic liquid fermentation residues and 28 liters of water.

[0236] The fermentation residues have the following composition:

[0237] 0.46% N total nitrogen

[0238] 0.18% N ammonia nitrogen

[0239] 0.12% P2O5 total phosphate

[0240] 0.42% K2O total potassium oxide

[0241] 0.0029% Zn total zinc

[0242] Minor components:

[0243] 0.11% MgO total magnesium oxide

[0244] 0.04% S sulfur

[0245] 0.66% CaO basic active ingredient

[0246] 6.41% organic matter

[0247] Bulk density 1040 kg / m 3

[0248] pH value 8.4

[0249] Thus, the total nitrogen in the initial solution is calculated to be 74 ml / l. The fermentation residue material introduced together with 28 liters of water has the initial values (measured using MQuant test strips from Merck KgaA, 64271 Darmstadt, Germany):

[0250] pH = 7.4

[0251] NH4 = 80 ml / l corresponds to 56 ml / l of NH4-N

[0252] NO3 = 5 ml / l corresponds to 1 ml / l of NO3-N

[0253] After 5 days, the NO3 value was 75 ml / l (corresponding to 17 ml / l of NO3-N), and the NH4 value had dropped to 5 ml / l (corresponding to 4 ml / l of NH4-N). At this time, 28% (21 ml / l) of the total nitrogen contained in the starting solution was present in a plant-available form. The nitrogen was present in a NO3 to NH4 ratio of 15:1. In the initial solution, 77% of the total nitrogen was present in a NO3 to NH4 ratio of 1:16. Description of the Drawings

[0254] The present invention will be described in more detail below with reference to the accompanying drawings.

[0255] Show:

[0256] Figure 1 Shows a first implementation variant of a bioreactor, which has a plurality of plastic fragments wound together to form a ball as a carrier unit,

[0257] Figure 2 Shows a second implementation variant of a bioreactor, which has a plurality of carrier units constructed of zeolite particles, which are arranged in a textile bag in the receiving space of the bioreactor,

[0258] Figure 3 Shows a third implementation variant of a bioreactor, which has three carrier units respectively constructed of porous hoses, parallel to each other, and connected to a pipeline in the receiving space,

[0259] Figure 4 Shows a general schematic diagram of an implementation variant of a nutrient preparation and carbon dioxide storage system,

[0260] Figure 5 Shows a schematic diagram of a possible implementation variant of a carbon dioxide storage device having two chambers,

[0261] Figure 6 Shows an experimental setup of a plurality of parallel carbon dioxide storage devices, which contain as absorbents for CO2 storage A) concentrated nutrient solution, B) nutrient solution, or C) water as a reference,

[0262] Figure 7 is Figure 6 The result of the experiment shown, where A) concentrated nutrient solution is represented by a narrow dashed line, B) nutrient solution is represented by a wide dashed line, and C) water is represented by a solid line.

[0263] In Figures 1 to 3In it, three different exemplary embodiments of a bioreactor are shown, which are each labeled as 1, 2, or 3 as a whole. The bioreactors 1, 2, and 3 are configured to convert organic residues and / or waste into an organic nutrient solution having a relatively high proportion of plant-available mineral nitrogen.

[0264] By means of the bioreactors 1, 2, and 3, a method for preparing an organic nutrient solution can thus be implemented, wherein based on the total nitrogen content of the nutrient solution, the proportion of plant-available nitrogen is at least 10%. In addition, in the plant-available mineral nitrogen, the nitrate content should be higher than the ammonium content.

[0265] The bioreactors 1, 2, and 3 have a reaction vessel 5, which is connected to a feed line 6 and a discharge line 7. The suspension 4 can be introduced into the reaction vessel through the feed line 6, and the suspension can be discharged again through the discharge line 7 after passing through the reaction vessel 5.

[0266] The bioreactors 1, 2, and 3 have a ventilation device 8 through which oxygen can be introduced into the reaction vessel 5 preferably in the form of air. In Figures 1 to 3 the illustrated embodiment, the ventilation device 8 has a compressor 17. Oxygen in the form of air can be introduced into the reaction vessel 5 via the supply line 16 by the compressor 17.

[0267] The main difference between the three bioreactors 1, 2, and 3 lies in different carrier units 10, which are each arranged in the receiving space 9 of the reaction vessel 5. The carrier units 10 are arranged in the receiving space 9 in such a way that the carrier units 10 can be thoroughly rinsed by the suspension 4 introduced via the feed line 6. The suspension 4 can be, for example, the organic residues and / or waste as described above, and / or the organic inoculum material as described above. In addition, the carrier units 10 are also arranged in such a way that the oxygen introduced by means of the ventilation device 8 preferably surrounds and flushes the carrier units 10 substantially on all sides.

[0268] The carrier units 10 have a particularly large surface area relative to their volume. The surface of the carrier units 10 is herein configured as a breeding area 11 for forming a biofilm 12, which biofilm 12 consists at least in part of ammonifying bacteria and / or nitrifying bacteria. Therefore, the breeding area 11 is configured to be, for example, rougher than the inner side of the reaction vessel wall. Thus, the microorganisms of the biofilm 12 can adhere particularly well to the breeding area 11 and grow thereon. This enables ammonifying bacteria and / or nitrifying bacteria to form the biofilm 12 substantially on the breeding area 11, because ideal growth conditions can be created here.

[0269] Figures 1 to 3 The carrier units 10 of the various exemplary embodiments in are made in part of different materials or combinations of multiple materials.

[0270] Figure 1 The carrier unit 10 of the bioreactor 1 therein is made of plastic fragments 13. For example, when processing plastic blanks, these fragments 13 may occur as waste products. It may be particularly advantageous if the fragments are made of thermoplastics such as polypropylene and / or polyethylene. Here, a plurality of the fragments 13 are arranged in a disordered manner within the receiving space 9 of the reaction vessel 5. As a result, the fragments 13 are suitably entangled with one another. Since the fragments 13 have curved propagation regions 11 (which may be produced, for example, by the meandering and / or helical and / or undulating forms of the fragments 13), individual fragments 13 can be prevented from adhering to one another or lying against one another in a simple manner. Adhesion or lying against one another is disadvantageous because gas exchange and / or thorough rinsing can no longer be ensured, and as a result, a biofilm of anaerobic bacteria can form. This can precisely lead to undesired effects, especially the occurrence of the denitrification process.

[0271] In Figure 2 the case of the bioreactor 2, the carrier unit 10 is designed as zeolite granules 14. In order to be able to prevent the granules 14 from depositing in poorly flowing or poorly ventilated regions of the receiving space 9, the carrier unit 10 constructed of the granules 14 is arranged in a collecting unit 27 designed as a textile bag. The collecting unit 27 can be fixed in the receiving space by means of a suspension device. Another ventilation device 28 can supply oxygen via a bypass gas line 25, which is arranged within the collecting unit 27. In addition, a feed line 6 extending inside the reaction vessel 5 leads into the collecting unit 27 and ends there, so that the suspension 4 can be directly introduced into the collecting unit 27. The collecting unit 27 has an open-pored design such that the suspension can drain from the collecting unit 27 into the receiving space 9. The bypass gas line 25 branches off from a main gas line 26 connected to the ventilation device 8. Thus, oxygen can be introduced into the receiving space 9 at two different locations without a second compressor 17.

[0272] Figure 3 The bioreactor 3 therein has three carrier units 10 each designed as a porous hose 15, which are integrated parallel to one another in a pipeline system within the receiving space 9. The hoses 15 are each connected to the feed line 6 and a gas supply line 16 designed as a bypass gas line 25. Thus, in particular, the suspension 4 and oxygen can be introduced into the hoses 15 at different times. In order to prevent oxygen or the suspension 4 from being introduced into one or more of the hoses 15, a shut-off valve 34 is arranged in front of each hose 15 in the direction of the inflowing feed line 6.

[0273] In order to be able to increase the internal pressure of the hose 15 or hoses 15, especially independently of other hoses 15, another shut-off valve 35 is provided behind each hose 15 in the flow direction of the suspension 4. By blocking the shut-off valve 35, it is possible to prevent the suspension from escaping from the hose 15 through the discharge line 7 extending within the receiving space 9. The suspension 4 can thus enter the receiving space 9 through the holes in the hose wall. Since the hose 15 is preferably designed to be stretchable, the holes in the hose wall can be enlarged by increasing the pressure inside the hose 15. The bioreactor 3 has an additional discharge line 7 through which the suspension 4 can be discharged from the receiving space 9 in the case where the first discharge line 7 is closed.

[0274] The ventilation device 8 has a ventilation plate 19 which is arranged on the bottom 18 of the reaction vessel 5 of the bioreactors 1, 2, 3. The ventilation plate 19 is connected to the compressor 17 via a supply line 16, especially the main gas line 26. The ventilation plate 19 has a plurality of evenly distributed ventilation openings 20 through which oxygen can flow into the suspension 4.

[0275] Each of the bioreactors 1, 2, 3 has a pumping device 21 which can in particular be designed as a centrifugal pump or a circulation pump. By means of the pumping device 21, the suspension 4 can be pumped into the reaction vessel 5 through the feed line 6 and sucked out of the reaction vessel 5 through the discharge line 7.

[0276] The bioreactors 1, 2, 3 thus have a suspension circuit 29 composed of the supply line 6, the discharge line 7 and the reaction vessel 5, through which the suspension 4 can be circulated by means of the pumping device 21. The pumping device 21 is arranged such that the flow direction of the suspension inside the reaction vessel 5 and / or in the lines of the bioreactors 1, 2, 3 can be reversed. In combination with a plurality of shut-off valves 30, 31, 34, 35, the flow direction inside the reaction vessel 5 can be set and changed.

[0277] For example, as Figures 1 to 3 shown, a bypass feed line 32 can branch off from the feed line 6 and lead to the receiving space 9 of the reaction vessel 5. If the flow direction of the suspension is reversed, one of the feed lines 6 among the plurality of feed lines 6 can be converted into a discharge line 7 and / or the bypass feed line 32 can be converted into a discharge line 7. The function of each line thus depends on the flow direction of the suspension 4 predetermined by means of the pumping device 21. Generally speaking, however, the supply line 6 leads to the receiving space 9 of the reaction vessel 5 above the discharge line 7 or at least at the same height as the discharge line 7. Better circulation of the suspension inside the reaction vessel 5 can thus be achieved.

[0278] In order to be able to conveniently remove the carrier unit 10 from the receiving space 9, the bioreactors 1, 2, 3 have an opening 23 on the upper side of the reaction vessel 5. By means of a closing unit 24 designed as a lid, this opening 23 can be closed in a liquid-tight and / or pressure-resistant manner when using the bioreactors 1, 2, 3.

[0279] The bioreactor 1 has a diverter unit 36 at the upper third of the receiving space 9, through which the suspension 4 can be divided into a plurality of individual jets. In this way, on the one hand, solids adhering to each other can be broken up, and on the other hand, additional aeration of the suspension can be achieved. The diverter unit 36 can be designed, for example, as a partition plate. In addition, the diverter unit 36 can also be combined with Figure 2 and 3 other implementation variants or the features of the foregoing technical solutions.

[0280] The bioreactors 1, 2, 3 also have a heating device 22, by means of which the receiving space 9 and / or the suspension 4 accommodated therein can be heated to a desired temperature.

[0281] From Figure 3 it can be seen that a shut-off valve 33 can be designed to be provided in the bypass gas pipeline 25. This can prevent oxygen from being introduced into the receiving space 9 of the reaction vessel 5, but at the same time ventilation can be carried out through the ventilation plate 19.

[0282] In order to produce the biofilm 12 from at least partially ammonifying bacteria and / or nitrifying bacteria, a suspension is made from the granular organic inoculum with water. For example, worm excrement or worm soil can be used as the inoculation material. Other possible inoculation materials have been described in detail above. In principle, it can be said that, in principle, all organic substances containing soil bacteria that decompose proteins are suitable as inoculation materials.

[0283] For optimal biofilm formation, the inoculation material is brought into contact with the carrier material by circulation and by turbulent air inflation. The organic inoculation material has an increased concentration of soil bacteria, mucus and other proteins, as well as inorganic minerals, to which dead bacterial material adheres. These components, on the one hand, support the adhesion of the bacteria contained on the carrier unit 10, thus supporting the formation of the biofilm. In addition, they also serve as nutrients for the bacteria. As a result, a carrier unit 10 with a diverse, qualitatively and quantitatively variable and modifiable bacterial cultivation is produced, and the bacterial cultivation consists of a variety of soil bacteria including ammonifying bacteria and nitrifying bacteria.

[0284] After the biofilm 12 has formed on the carrier element 10, the carrier material can be removed from the first reaction vessel 5 and transferred to another reaction vessel 5. The conversion of the organic residues and / or waste into an organic nutrient solution can then be carried out with the aid of the biofilm. However, it is also conceivable to carry out the inoculation step and the cultivation step in the same reaction vessel 5. It is recommended to remove the inoculation material from the reaction vessel 5 before adding the organic residues and / or waste.

[0285] The present invention also relates in particular to a bioreactor 1, 2, 3 and its use, which are used to convert organic residues and / or waste into an organic nutrient solution, which has a proportion of at least 10% of plant-available mineralized nitrogen, based on the total nitrogen content of the nutrient solution, and the bioreactor has a reaction container 5, wherein the reaction container 5 has a feed line 6, through which a suspension 4 can be introduced into the reaction container 5, and the reaction container 5 has a discharge line 7, through which the suspension 4 can be discharged from the reaction container 5, and the bioreactor has a ventilation device 8, which is used for ventilation of the suspension 4 and / or a carrier unit 10 arranged in the reaction container 5, wherein the carrier unit 10 has at least one internal and external breeding area 11, on which ammonifying bacteria and / or nitrifying bacteria can breed in a biofilm 12.

[0286] Figure 4 A nutrient production and carbon dioxide storage system 37 is shown, which has a fermentation device 38 for producing biogas and organic residues and / or waste, a central heating power plant 39 for burning the biogas produced by the fermentation device 38 to obtain electrical energy and / or heat, bioreactors 1, 2, 3 for converting organic residues and / or waste into an organic nutrient solution, and a carbon dioxide storage device 40 having a carbon dioxide storage space 41 (preferably a carbon dioxide storage space 41 in which the carbon can be sealed from the outside), wherein at least one scrubber device 42 is arranged, which is configured to carry out a liquid-gas reaction between a carbon dioxide-containing gas (in particular, biogas and / or exhaust gas from the central heating power plant 39) and the organic nutrient solution produced by the bioreactors 1, 2, 3.

[0287] The carbon dioxide produced by the fermentation process in the fermentation device 38 can be introduced into the carbon dioxide storage device 40 through a pipeline 43 designed as a gas pipeline. The organic residues and wastes (fermentation residues) are introduced from the fermentation device 38 into the bioreactors 1, 2, 3 as raw materials for preparing an organic nutrient solution. The biogas produced in the fermentation device 38 can be burned by means of a central heating power plant 39. The carbon dioxide produced in the process is also sent to the carbon dioxide storage device 40.

[0288] The organic nutrient solution prepared from residues and waste (fermentation residues) in bioreactors 1, 2, and 3 is then transported from said bioreactors 1, 2, and 3 via pipeline 43 to the carbon dioxide storage space 41. There, the organic nutrient solution is mixed with the carbon dioxide-containing gas from fermentation device 38 and the central heating power plant 39.

[0289] Figure 5 Shows the process of the organic nutrient solution storing CO2 in the carbon dioxide storage device 40.

[0290] The carbon dioxide storage space 41 of the carbon dioxide storage device 40 is divided into two chambers 44, 45. The organic nutrient solution can be pumped back and forth between chambers 44, 45 by a pumping device 46. The scrubber device 42 is arranged in the first chamber 44. This can be designed, for example, as a bubble column reactor, a tubular reactor, a jet nozzle reactor, a stirred tank, a thin film reactor, and / or a spray tower. Establishing as large an interface as possible between the organic nutrient solution and the gas is crucial for improving CO2 binding.

[0291] Figure 6 The carbon dioxide storage devices 40 in [context not clear] are all constructed in the same way to create uniform experimental conditions. From Figure 7 It can be seen that for the same treatment duration, the concentrated nutrient solution gives the best results. Most of its CO2 / liquid volume can be bound.

[0292] Composition of samples A (concentrated nutrient solution), B (nutrient solution), and C (reference = water):

[0293]

[0294]

[0295] The gas mixture from the internal combustion engine exhaust is supplied to the carbon dioxide storage devices A, B, and C for about 10 minutes, and then these channels are sealed airtight. The CO2 content is measured at the start of the scrubber function and then after 1, 2, 3, and 4 hours. A measuring instrument (testo330-2LX; flue gas analyzer from Testo SE and Co KGaA, Lenzkirch) determines the proportion of CO2 in the gas mixture.

[0296] The experimental results can be obtained from the following table and Figure 7 the relevant charts in [context not clear].

[0297] Test results

[0298]

[0299] At the start of the test series, the CO2 concentration was approximately 30 times higher than the 0.038% CO2 concentration in air.

[0300] After 4 hours of cycling, the absorbent liquid in scrubbers A, B, and C was measured and the following measurements were obtained:

[0301] Scrubber A with concentrated soilingNRCO2capF

[0302] pH <![CDATA[NH4 mg / l*]]> <![CDATA[NO3 mg / l*]]> <![CDATA[CaCO3 mg / l*]]> K mg / l* 6.4 20 1750 200 125

[0303] * Measured using test stick MQuant. from Merck KGaA, Darmstadt; concentration determined by visually comparing the reaction zone of the test stick with the area on the color scale

[0304] Scrubber B with soilingNRCO2capF

[0305] pH <![CDATA[NH4 mg / l*]]> <![CDATA[NO3 mg / l*]]> <![CDATA[CaCO3 mg / l*]]> K mg / l* 5.3 5 450 120 170

[0306] * Measured using test stick MQuant. from Merck KGaA, Darmstadt; concentration determined by visually comparing the reaction zone of the test stick with the area on the color scale

[0307] Scrubber C with water

[0308] pH <![CDATA[NH4 mg / l*]]> <![CDATA[NO3 mg / l*]]> <![CDATA[CaCO3 mg / l*]]> K mg / l* 6 0 3 130 0

[0309] * Measured using test stick MQuant. from Merck KGaA, Darmstadt; concentration determined by visually comparing the reaction zone of the test stick with the area on the color scale

[0310] Particularly good CO2 storage can be achieved with concentrated nutrient solution (A) and nutrient solution (B).

[0311] The present invention is also suitable for binding and / or as an absorbent for COx, NOx, and SOx from fermentation gases, and combustion gases generated in the production and combustion of biogas and the combustion of fossil fuels.

[0312] Therefore, the system is particularly suitable for performing the methods described and / or claimed herein for preparing organic nutrient solutions and / or for carbon dioxide storage.

[0313] List of reference numerals

[0314] 1, 2, 3 Bioreactor

[0315] 4 Suspension

[0316] 5 Reaction vessel

[0317] 6 Feed line

[0318] 7 Discharge pipeline

[0319] 8 Ventilation device

[0320] 9 Receiving space

[0321] 10 Carrier unit

[0322] 11 Reproduction area

[0323] 12 Biofilm

[0324] 13 Debris

[0325] 14 Particles

[0326] 15 Hose

[0327] 16 Air supply pipeline

[0328] 17 Compressor

[0329] 18 Soil reaction vessel

[0330] 19 Ventilation plate

[0331] 20 Ventilation hole

[0332] 21 Pumping device

[0333] 22 Heating device

[0334] 23 Opening

[0335] 24 Sealing unit

[0336] 25 Bypass ventilation pipeline

[0337] 26 Main ventilation pipeline

[0338] 27 Collection unit

[0339] 28 Enhanced ventilation device

[0340] 29 Suspension circulation

[0341] 30 Stop valve

[0342] 31 Stop valve

[0343] 32 Bypass feed pipeline

[0344] 33 Stop valve (air)

[0345] 34 Stop valve in reaction vessel

[0346] 35 Stop valve in reaction vessel

[0347] 36 Diverter unit

[0348] 37 Nutrient production and carbon dioxide storage - systems

[0349] 38 Fermentation devices, in particular biogas plants

[0350] 39 Central heating plants

[0351] 40 Carbon dioxide storage devices

[0352] 41 Carbon dioxide storage chambers

[0353] 42 Scrubber devices

[0354] 43 Pipelines

[0355] 44 Scrubber device chambers

[0356] 45 Collection chambers

[0357] 46 Pumping devices

[0358] 47 Carbon dioxide measuring devices

Claims

1. A method for preparing an organic nutrient solution having a proportion of plant-available mineralized nitrogen of at least 10% based on the total nitrogen content of the organic nutrient solution, comprising the following steps: - In an inoculation step, inoculate a carrier unit (10) with an inoculation material containing ammonifying bacteria and / or nitrifying bacteria, - On the carrier unit (10), form a biofilm (12) having ammonifying bacteria and / or nitrifying bacteria, - In a cultivation step, cultivate organic residues and / or wastes together with the biofilm (12), wherein the ammonifying bacteria and / or nitrifying bacteria convert the organically bound nitrogen in the residues and / or wastes into mineralized nitrogen, - Wherein during the implementation of each or all steps, oxygen is introduced into the reaction vessel (5) and / or the carrier unit (10) by means of a ventilation device (8), - And wherein then in a carbon dioxide storage step, the organic nutrient solution prepared by the foregoing steps is treated with a carbon dioxide-containing gas such that gaseous carbon dioxide is bound through the organic nutrient solution.

2. The method according to claim 1, characterized in that, In the carbon dioxide storage step, surface expansion of the organic nutrient solution is carried out.

3. The method according to claim 1, wherein The nitrate proportion of the plant-available mineralized nitrogen is higher than the ammonium proportion.

4. The method according to claim 1, wherein The carrier unit (10) is a bioreactor (1, 2, 3).

5. The method according to claim 2, wherein In the carbon dioxide storage step, surface expansion of the organic nutrient solution is carried out by guiding the organic nutrient solution through a scrubber device.

6. A bioreactor (1, 2, 3) for implementing the method according to any one of claims 1 to 5, which is used to convert organic residues and / or waste into an organic nutrient solution. Based on the total nitrogen content of the organic nutrient solution, the organic nutrient solution has a proportion of plant-available mineralized nitrogen of at least 10%. The bioreactor has a reaction vessel (5), wherein the reaction vessel (5) has a feed line (6) through which a suspension (4) can be introduced into the reaction vessel (5), and wherein the reaction vessel (5) has a discharge line (7) through which the suspension (4) originating from the reaction vessel (5) can be discharged. The bioreactor (1, 2, 3) has a ventilation device (8) through which oxygen can be introduced into the reaction vessel (5) and the suspension (4) contained therein. In the receiving space (9) of the reaction vessel (5), at least one carrier unit (10) having a propagation area (11) for forming a microbial biofilm (12) is provided, wherein the at least one carrier unit (10) can be rinsed back and forth and / or thoroughly rinsed with the introduced suspension (4) and the introduced oxygen, and the surface area to volume ratio of the carrier unit (10) is greater than the surface area to volume ratio of the receiving space (9), characterized in that, The ventilation device (8) has a hydrogen peroxide reservoir and at least one catalyst, whereby during ventilation, hydrogen peroxide flowing out of the hydrogen peroxide reservoir can be converted into or is converted into water and oxygen in a catalytic reaction.

7. The bioreactor (1, 2, 3) according to claim 6, characterized in that, At least one catalyst is arranged between the hydrogen peroxide reservoir and the outlet of the ventilation device (8).

8. The bioreactor (1, 2, 3) according to claim 6, characterized in that, The at least one catalyst is pyrolusite and / or manganese oxide.

9. The bioreactor (1, 2, 3) according to claim 8, characterized in that, The at least one catalyst is manganese dioxide and / or manganite.

10. An organic nutrient solution prepared by the method according to any one of claims 1 to 5 and / or in a bioreactor (1, 2, 3) according to any one of claims 6 to 9, having a proportion of plant-available mineralized nitrogen of at least 10% based on the total nitrogen content of the organic nutrient solution.

11. The organic nutrient solution according to claim 10, characterized in that, The organic nutrient solution is an organic plant fertilizer.

12. The organic nutrient solution according to claim 10, characterized in that, The nitrate proportion of the plant-available mineralized nitrogen is higher than the ammonium proportion.

13. The organic nutrient solution according to claim 10, characterized in that, In the organic nutrient solution, the ratio of NO3:NH4 + is at least 2:

1.

14. The organic nutrient solution according to any one of claims 10 to 13, characterized in that, The organic nutrient solution has an ammonium content of at least 10% of the total nitrogen content of the organic nutrient solution, and / or a potassium content of at least 10% of the total solid content of the organic nutrient solution, and / or a calcium content of at least 5% of the total solid content of the organic nutrient solution, and / or a magnesium content of at least 1% of the total solid content of the organic nutrient solution, and / or a protein content of at least 15% of the total solid content of the organic nutrient solution.

15. The organic nutrient solution according to claim 14, characterized in that, The pH value of the organic nutrient solution is at most 7.

5.

16. Use of the organic nutrient solution according to any one of claims 10 to 15 as an absorbent for storing CO X and / or NO x and / or SO X wherein the organic nutrient solution is treated with a gas containing CO X and / or NOx and / or SOx.

17. A nutrient production and carbon dioxide storage system (37), comprising: - A fermentation device (38) for producing organic residues and / or wastes, - Optionally, a combined heat and power plant (39) for burning the biogas produced by the fermentation device (38) to obtain electrical energy and / or heat, - A bioreactor (1, 2, 3) according to any one of claims 6 to 9, for converting organic residues and / or waste into an organic nutrient solution, and - A carbon dioxide storage device (40) having a carbon dioxide storage space (41), wherein at least one scrubber device (42) is provided for performing a liquid-gas reaction between a carbon dioxide-containing gas and the organic nutrient solution prepared by the bioreactor (1, 2, 3).

18. The nutrient generation and carbon dioxide storage system (37) according to claim 17, characterized in that, The carbon dioxide storage space (41) is divided into at least two chambers (44, 45), wherein the scrubber device (42) is arranged in the first chamber (44), and the second chamber (45) is configured as a collection chamber for the organic nutrient solution, and the organic nutrient solution can be pumped from the first chamber (44) into the second chamber (45) and / or from the second chamber (45) into the first chamber (44) by at least one pumping device (46).

19. Use of an organic nutrient solution according to any one of claims 10 to 15, wherein the organic nutrient solution is used as a medium for binding and / or enriching carbon in plants and / or soil.

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