INTEGRATED ORGANOMINERAL FERTILIZER PRODUCTION SYSTEM AND METHOD IN BIOGAS SYSTEMS

Abstract

It relates to an organomineral fertilizer production system (A) that includes at least one anaerobic digester (1) enabling the production of biogas and digestate by anaerobic fermentation of organic raw materials. Figure 1

Description

1 TARIFF INTEGRATED ORGANOMINERAL FERTILIZER PRODUCTION IN BIOGAS SYSTEMS SYSTEM AND METHOD TECHNICAL FIELD This invention is used in renewable energy and biogas production facilities to implement "zero waste and The invention relates to an integrated system based on a "fully closed loop". Specifically, it concerns biogas. production, obtained from Power-to-Gas (P2G) systems and anaerobic digestion 10 It is related to the technical fields of digestate processing. More specifically, the invention concerns the sulfur gases separated during biogas treatment and Electrolyzer-derived oxygen is used in the enrichment of the digestate, and The waste heat released as a result of the Sabatier reaction is used in drying the digestate. an integrated biogas and organomineral fertilizer production system, which was evaluated and It is related to the method. PREVIOUS TECHNIQUE In biogas plants, methane is produced as a result of the anaerobic decomposition of organic matter. and biogas containing carbon dioxide, along with digestate containing a high percentage of water, are obtained. In current practices, hydrogen sulfide (H₂S) in biogas is removed. Sulfur compounds are used biologically or in other ways to make the gas usable. They are removed by chemical desulfurization methods. Oxygen or air 25 In assisted biological desulfurization methods, the oxidation of H₂S is a known process. Although it is an application, its primary purpose is the purification of biogas. The digestate obtained from anaerobic digestion can also be used as fertilizer. This is known from previous techniques. In order to reduce the high water content of the digestate, 30 Mechanical separation, evaporation, filtration, and drying processes can be applied; Additionally, sulfates and similar mineral compounds are used to increase nutritional value. Organomineral fertilizers can be prepared by adding them externally. With this... 2 These processes together lead to additional chemical and / or energy needs. It can open. In power-to-gas systems, hydrogen and oxygen are produced through electrolysis, and The resulting hydrogen is then subjected to a Sabatier reaction with carbon dioxide to produce synthetic 5. Methane production is known. High levels of methane are released during the Sabatier reaction. applications for recovering a certain amount of heat for various purposes It is available. However, with the current technique, the sulfurous gases separated during biogas treatment are 10 The digestate is converted into sulfate form using oxygen obtained from the electrolyzer. by transforming and thus enriching the digestate in situ, Sabatier waste heat obtained from the reaction is enriched within the same process. The need for an integrated system that enables the use of digestate in drying. It is located. 15 Patent document number EP3150569A1 describes the process of anaerobic digestion. making the obtained digestate suitable for horticultural applications It describes a method. The document basically explains the pasteurization of the digestate, mechanical removal of water, filtration and, if necessary, deodorization 20 a fertilizer whose particle size has been reduced and made easier to use by means of processing. The aim is to obtain the product. Additionally, the resulting solid product is to be pelletized. or pulverization is also explained. Publication number EP3150569A1 The patent document focuses solely on the physical processing of the digestate. The document describes the chemical enrichment of digestate, biogas treatment 25 utilization of process by-products or Sabatier electrolyzer any technique for integrating processes within the same system There is no teaching or motivation involved. Patent document number EP3814300 describes the production of organic fertilizers from zeolite, leonardite and various 30 It has controlled release properties due to being mixed with mineral raw materials. This document describes the process of obtaining organomineral fertilizer. The document also mentions sulfate content. external addition of compounds such as potassium sulfate, magnesium sulfate, or zinc sulfate This is achieved by adding sulfate from the outside. In the present invention, however, instead of adding sulfate from the outside, 3 H₂S separated from biogas is mixed with O₂ obtained from the electrolyzer in the digestate. It is converted into sulfate. Additionally, the EP3814300 features an electrolyzer for biogas. a process in which the treatment and Sabatier waste heat are integrated into digestate drying It does not have a structure. In conclusion, an innovative solution that will provide improvement in this technical field. The need to develop the approach has arisen. A BRIEF DESCRIPTION OF THE INVENTION The present invention eliminates the aforementioned disadvantages and the related technical to bring new advantages to the field, an organomineral fertilizer production system and It is related to the method. The main purpose of the invention is to process H₂S-containing gases separated during biogas treatment, 15 Sulfate is added to the digestate using O₂ obtained from the electrolyzer. conversion and thus the addition of sulfate-containing chemicals from the outside obtaining sulfate-enriched organomineral fertilizer without the need for it to provide. Another aim of the invention is to utilize O₂, which is formed as a byproduct in the electrolysis process. The aim is to enable its evaluation in the digestate enrichment process. Another aim of the invention is to utilize the waste heat released during the Sabatier reaction. By using it in drying the digestate, the energy requirement of the process is reduced by 25%. The aim is to ensure its reduction. Another purpose of the invention is to utilize biogas production, electrolysis, methanization, and digestion. By-products and waste streams generated in processing processes act as inputs to each other. The aim is to establish a closed-loop process structure in which it is used. 30 Another objective of the invention is the storage of the digestate by reducing its water content. and to ensure the production of dry organomineral fertilizer that is easy to transport. 4 Another objective of the invention is to introduce water separated from the digestate into the system as a process input. The aim is to reduce fresh water consumption by feeding it back into the body. Another aim of the invention is to digest sulfur compounds before their release into the atmosphere. The aim is to reduce process emissions by keeping them contained. 5 Another aim of the invention is to replace air with pure oxygen in the digestate enrichment process. nitrogen compounds resulting from the entrainment of inert gases through their use The aim is to prevent losses and preserve the nitrogen content of the fertilizer. All the purposes mentioned above and those that will emerge from the detailed explanation below. The present invention aims to achieve anaerobic processing of organic raw materials. at least one anaerobic system that enables the production of biogas and digestate through fermentation. It is an organomineral fertilizer production system that includes a digester. Accordingly, the aforementioned System feature; 15  H₂S originating from the anaerobic digester and in the resulting biogas. a process that separates sulfur compounds and enriches the separated sulfur compounds. at least one sulfur separator that conveys it to the tank,  At least one electrolyzer that produces hydrogen and oxygen by electrolysis of water, 20  associated with the electrolyzer and separating the obtained hydrogen and oxygen from each other, at least one gas that delivers at least some of the separated oxygen to the enrichment tank separator,  Liquid digestate from the anaerobic digester, H₂S from the sulfur separator by bringing into contact with sulfur compounds from the source and oxygen from the gas separator 25 The conversion of H₂S-derived sulfur to sulfate and the sulfate breakdown of the digestate. at least one enrichment tank that enables its enrichment,  as a result of the reaction of hydrogen and carbon dioxide obtained from the electrolyzer At least one Sabatier reactor that enables the production of synthetic methane and heat,  At least one heat exchanger that recovers the heat released in the Sabatier reactor, 30  at least one of the following reduces the water content of the digestate coming from the enrichment tank mechanical separator and  The solid digestate obtained from the mechanical separator is released in the Sabatier reactor. a dryer that uses the heat generated and recovered via a heat exchanger to dry at least It includes a drying unit. A preferred configuration of the invention involves the gas separator enriching pure oxygen. 5 It has an oxygen outlet to feed the tank from the bottom. Another preferred configuration of the invention involves water present in the gas stream. It must contain at least one moisture separator for separation. Another preferred configuration of the invention is that the aforementioned moisture separator separates the moisture. It is related to the electrolyzer in terms of feeding water back to the electrolyzer. All the purposes mentioned above and those that will emerge from the detailed explanation below. The present invention aims to achieve anaerobic processing of organic raw materials. organomineral fertilizer from the digestate obtained as a result of fermentation It is an organomineral fertilizer production method aimed at producing this type of fertilizer. Accordingly, the word the subject of the method's characteristics; i. H₂S derived from biogas obtained as a result of anaerobic fermentation Separation of sulfur compounds, 20 ii. Obtaining hydrogen and oxygen through electrolysis of water, iii. at least a portion of the oxygen obtained as a result of electrolysis must be present in the aforementioned Feeding liquid digestata with H₂S-derived sulfur compounds, iv. In the digestate, sulfur derived from H₂S is converted to sulfate, and then sulfate is formed. Obtaining enriched digestate, 25 v. Hydrogen obtained as a result of electrolysis with carbon dioxide Sabatier Synthetic methane and heat are obtained by subjecting it to a reaction. vi. Mechanical dewatering of sulfate-enriched digestate and vii. During the Sabatier reaction of the digestate from which the water has been mechanically separated The drying steps using the recovered heat generated are 30 It includes. 6 A preferred configuration of the invention is obtained in step 3 as a result of electrolysis. A portion of the pure oxygen obtained is transferred to the enrichment tank containing the liquid digestate. It is controlled feeding from below. Another preferred configuration of the invention is, in step 4, sulfur derived from H₂S 5 conversion to sulfate, sulfur naturally present in the digestate biological oxidation carried out by oxidizing microorganisms (OMIs) chemical reaction between H₂S dissolved in liquid phase and oxygen This is achieved through the combined use of oxidation processes. Another preferred configuration of the invention is, in step 4, sulfur derived from H₂S. Its conversion to sulfate occurs within a pH range of 6.5-8.5 and a temperature range of 25-45°C. It is the realization of. Another preferred configuration of the invention is, in step 4, sulfur derived from H₂S 15 Its conversion to sulfate occurs within a pH range of 7.2-8.2 and a temperature range of 30-38°C. It is the realization of. Another preferred configuration of the invention is the Sabatier reaction in step v. the heat released during this process is recovered through a heat exchanger and returned 20 At least some of the heat gained is used in drying the digestate in step VII. It is the use of. BRIEF DESCRIPTION OF THE FIGURE Figure 1 shows the integrated biogas and organomineral fertilizer production system that is the subject of this invention. A schematic view is provided. REFERENCE NUMBERS GIVEN IN THE FIGURE A: Organomineral fertilizer production system 1. Anaerobic digester 2 Sulfur separator 3 Sabatier reactors 7 4 Heat exchanger Moisture Separator 6 Electrolyzers 7 Gas separator 8 Enrichment tanks 5 9 Mechanical separator Drying unit DETAILED DESCRIPTION OF THE INVENTION This detailed description describes the organomineral fertilizer production system (A) that is the subject of the invention. only aimed at a better understanding of the subject, with no limiting effects. This is explained with examples that will not create a problem. The subject of the invention is an organomineral fertilizer production system (A); basically an anaerobic 15 digester (1), a sulfur separator (2), an electrolyzer (6), a gas separator (7) and a It contains an enrichment tank (8). Obtained from the anaerobic digester (1) When the biogas is conveyed to the sulfur separator (2), the separated sulfur compounds are enriched. Hydrogen and oxygen obtained in the electrolyzer (6) are directed to the tank (8). In the gas separator (7) they are separated from each other and at least some of the separated oxygen is 20 It is fed into the enrichment tank (8). Thus, sulfur compounds and oxygen, The digestate is brought together in the enrichment tank (8) where the digestate is located. It is enriched with sulfate. Organomineral fertilizer production system (A) also includes a Sabatier reactor (3), a heat 25 exchanger (4), a moisture separator (5), a mechanical separator (9) and a drying unit (10) It contains. Hydrogen obtained in the electrolyzer (6) is transferred to the Sabatier reactor (3) heat released during the Sabatier reaction is transferred to the heat exchanger (4) It is recovered by means of digestate coming out of the enrichment tank (8). It is passed through a mechanical separator (9) and the resulting solid digestate is recovered 30 It is dried in the drying unit (10) where heat is used. 8 Anaerobic digester (1) Anaerobic digester (1), organic raw materials under anaerobic conditions that it is fermented by means of microorganisms and that this fermentation As a result, raw biogas containing methane and carbon dioxide, as well as digestate, are obtained. It is a unit. The raw biogas obtained from the anaerobic digester (1) contains sulfur 5 The compounds are sent to a sulfur separator (2) for separation. Anaerobic The digestate obtained as a result of decomposition is used as organomineral fertilizer in the system. It constitutes the organic-based raw material for its production. Sulfur separator (2) 10 The sulfur separator (2) removes H₂S from the raw biogas coming from the anaerobic digester (1). It enables the separation of sulfur compounds from the gas stream. Sulfur The sulfur compounds separated in the separator (2) are not released into the atmosphere or disposed of. Instead of being processed, the biogas is sent to the enrichment tank (8). Thus, the biogas The sulfurous stream formed during the purification process contains 15% sulfate in the digestate. It is converted into a process input used in enrichment. The said flow, directed from the sulfur separator (2) to the enrichment tank (8), is H₂S ammonia separated during biogas treatment in addition to sulfur compounds from natural sources It can also contain nitrogenous compounds such as 20. Sabatier reactor (3) The Sabatier reactor (3) converts hydrogen and carbon dioxide obtained from the electrolyzer (6) It is the unit where synthetic methane and water are obtained by reacting them. Sabatier The reaction occurs exothermically, and a high 25 is obtained as a result of the reaction. High-quality heat is released. This released heat is expelled from the system. instead of being recovered by means of a heat exchanger (4), especially the digestate It is used in drying. The Sabatier reactor (3) is a nickel (Ni) based fixed-bed reactor in a preferred configuration. It contains a catalyst. Hydrogen and carbon dioxide fed into the reactor are converted into methane. in accordance with the reaction, at an approximate H₂ / CO₂ molar ratio of 4:1 It is possible to operate the Sabatier reactor (3) under pressure. In a sample application, the reactor inlet pressure is 10 atm and the outlet pressure is 9.6 atm. 9 The gas stream containing carbon dioxide fed into the Sabatier reactor (3) is approximately 40°C, Hydrogen, on the other hand, can be fed at a temperature of approximately 80°C and an exothermic reaction occurs. As a result, the temperature inside the reactor reaches approximately 426.85°C. Heat exchanger (4) 5 Heat exchanger (4), exothermic reaction taking place in Sabatier reactor (3). the resulting heat is recovered and the system is able to use it as needed. It ensures that the heat is transferred to its components. Some of the recovered heat is used anaerobically. While it can be used in the thermostatic control of the digester (1), its main part is mechanical. To dry the solid digestate coming out of the separator (9), it is sent to the drying unit (10). is being transferred. Moisture separator (5) Moisture separator (5) removes water from the gas stream in the system. It ensures separation. The water separated in the moisture separator (5) is discharged outside the system. instead, to meet at least part of the electrolyzer's (6) water requirement to the system It is fed back. Thus, water is recovered within the system. is being carried out. Electrolyzer (6) 20 Electrolyzer (6) by electrolysis of water using preferably renewable energy. It produces hydrogen and oxygen. The hydrogen and oxygen formed in the electrolyzer (6), They are sent to the gas separator (7) to be separated from each other. Hydrogen Sabatier used in the reaction; at least one of the pure oxygens, a byproduct of electrolysis part of it is enriched into the enrichment tank (8) 25 for the purpose of enriching the digestate. is sent away. Thus, the oxygen produced in the electrolysis process is sent as a separate waste or Instead of being discarded as an unused byproduct, it can be used as organomineral fertilizer. It is integrated into the production process. Gas separator (7) 30 The gas separator (7) separates the streams of hydrogen and oxygen coming from the electrolyzer (6). It enables the separation of hydrogen. The separated hydrogen is sent to the Sabatier reactor (3), pure oxygen. At least a portion of it is directed to the enrichment tank (8). Enrichment Oxygen that is not used in the process is removed from the system and used for other purposes. can be evaluated. Enrichment tank (8) Enrichment tank (8) contains the liquid digestate obtained as a result of anaerobic digestion, 5 Sulfurous stream from H₂S originating from sulfur separator (2) and from gas separator (7) It is a closed tank where it is brought together with pure oxygen. In the enrichment tank (8), the conversion of sulfur compounds into sulfate, one another through supporting biochemical and chemical mechanisms 10 This is carried out in the biochemical mechanism, naturally within the digestate. The sulfur-oxidizing microorganisms (SOBs) present in the system absorb the pure oxygen supplied to it. by using it to metabolize H₂S and make sulfur available to plants. It enables the conversion to sulfate (SO₄²⁻) form. However, the pure oxygen supplied from the electrolyzer (6) is used as an oxidizer in the tank. It creates an environment. The contact of H₂S dissolved in the liquid phase with oxygen. The resulting chemical oxidation also contributes to sulfate formation. This allows biological and chemical oxidation to be carried out together. external sulfate-containing chemical substance or external bacterial culture added 20 The digestate is enriched with sulfate without any intervention. Conversion of H₂S to sulfate; H₂S + 2O₂ → SO₄²⁻ + 2H⁺ 25 It takes place in accordance with the reaction. Provided to the enrichment tank (8) oxygen amount, stoichiometric oxygen required for the conversion of H₂S to sulfate. The amount can be determined to be above a certain level. Thus, H₂S turns into sulfate. An oxygen-rich reaction environment is provided for the transformation. 30 Enrichment tank (8), continuous flow mixing in a preferred configuration. It is structured as a reactor (CSTR). Pure oxygen is continuously injected into the tank. Liquid-gas mass transfer is achieved through feeding; gas diffusion and sulfur 11 Conversion of H₂S to sulfate as a result of the activity of oxidizing microorganisms. This is done simultaneously throughout the process flow. Therefore, the system The study does not depend on a specific batch reaction time; the conversion is continuous. This can be accomplished within the process flow. Using pure oxygen instead of air in the enrichment tank (8) also It contributes to the preservation of nitrogenous compounds found in the digestate. With air... The high amount of inert nitrogen gas present in the aeration carried out is released from the tank. During the discharge process, volatile ammonia may be transferred to the gas phase. By using pure oxygen, this gas stripping effect is reduced, and digestat 10 The nitrogen compounds present are kept in the liquid phase. Additionally, sulfur... The flow directed from the separator (2) to the enrichment tank (8) contains H₂S as well. Ammonia can also be recovered from the digestate. Thus, the digestate is reduced in sulfate. In addition to enrichment, it also involves preserving the nitrogen content and returning it to the system. The retention of nitrogen compounds in the digestate is facilitated by the addition of ammonia. 15 a contribution is being made. Mechanical separator (9) The mechanical separator (9) collects the sulfate-enriched from the enrichment tank (8). It removes a significant portion of the water from the digestate and reduces the solid content to 20%. This ensures the production of an enhanced digestate. At least some of the separated water, water is returned to the system to meet the water needs of the electrolyzer (6). can be fed, and the solid digestate is sent to the drying unit to be dried (10) is being transferred. Drying unit (10) The drying unit (10) reduces the moisture content of the solid digestate coming from the mechanical separator (9). It ensures the reduction of the thermal energy required in the drying process. A small portion of it is released in the Sabatier reactor (3) and via the heat exchanger (4) This is provided from the recovered heat. Thus, the waste heat of the Sabatier reaction is 30 It is integrated into the drying stage of the organomineral fertilizer production process. The starting digest obtained from the anaerobic digester (1) has a high water content. It contains approximately 86.5% water by volume, in a sample application. 12 After the enrichment process, the solid digestate coming out of the mechanical separator (9) It contains approximately 70-80% moisture. This solid digestate is called Sabatier. In the drying unit (10) where the thermal energy recovered from the reactor (3) is used By drying, the moisture content of the final product is reduced to 15-20%. Thus... Dry 5 with increased solid content, easier to store and transport. Organomineral fertilizer is obtained. How the System Works In the organomineral fertilizer production system, (A) primarily organic raw materials It is fed into an anaerobic digester (1) and subjected to anaerobic fermentation. 10 The raw biogas obtained as a result of fermentation is fed into a sulfur separator (2) The biogas is sent through a process where sulfur compounds originating from H₂S are separated. The separated sulfur stream is sent to the enrichment tank (8), while the cleaned gas stream It is directed to the methanization portion of the system. On the other hand, the water recovered within the system is fed to the electrolyzer (6) and Hydrogen and pure oxygen are obtained as a result of the electrolysis of water. Hydrogen and Oxygen is separated from each other in the gas separator (7). Hydrogen is sent to the Sabatier reactor (3) During the process, the portion of pure oxygen required for enrichment is transferred to the enrichment tank. (8) is nourished. 20 In the enrichment tank (8), the liquid digestate contains H₂S supplied from the sulfur separator (2). The sulfur stream and pure oxygen supplied from the electrolyzer (6) are combined. H₂S is converted into sulfur sulfate through biochemical and chemical oxidation. It is converted and retained in the digestate, and the sulfate-enriched digestate 25 is obtained. The enriched digestate is sent to a mechanical separator (9) where a significant amount of water content is reduced. A portion is removed. The solid digestate obtained as a result of mechanical separation. It is sent to the drying unit (10). 30 In parallel, the hydrogen obtained from the electrolyzer (6) is mixed with carbon dioxide. Synthetic methane is obtained by feeding it into the Sabatier reactor (3). The heat released in the reaction is recovered by means of a heat exchanger (4) and 13 It is mainly transferred to the drying unit (10). Thus, from biogas treatment the resulting sulfurous stream, oxygen obtained from electrolysis, and Sabatier The heat obtained from the reaction is different from the same organomineral fertilizer production process. It is evaluated in stages. A Sample Application of the Invention In a sample application of the invention, 2500 kg / hour of fertilizer is fed into the anaerobic digester (1) and 500 kg / hour of straw is fed. The raw materials in question are processed using an anaerobic digester. (1) It is mixed and fermented for 26 days. Fermentation During this process, microorganisms break down organic matter, resulting in the release of CO₂ and 10⁻¹⁰. Approximately 1080 kg / hour of crude biogas containing methane is obtained. The resulting crude biogas is sent to the sulfur separator (2) and the H₂S in the gas is removed. Sulfur compounds from the source are separated. The separated sulfur compounds are released into the atmosphere. 15 without being discarded, to be used later in the enrichment of the digestate. It is sent to the enrichment tank (8). In the example application, sulfur is separated from biogas by means of a sulfur separator (2). The sulfur gas flow directed to the enrichment tank (8) is 5.63 kg / hour H₂S It contains. In addition, approximately 20 dissolved in the liquid digestate. There is 1.00 kg / hour of H₂S, and the total H₂S reaching the enrichment tank (8) The amount is approximately 6.63 kg / hour. On the other hand, in the electrolyzer (6), as a result of the electrolysis of the water fed back into the system H₂ and O₂ are produced. The produced hydrogen and oxygen gases are separated by means of a gas separator (7) 25 They are separated from each other. The resulting hydrogen is sent to the Sabatier reactor (3), Approximately 20 kg / hour of pure oxygen is added to the liquid digestate at a controlled flow rate. It is injected into the enrichment tank (8) from the bottom of the tank. Oxygen obtained from electrolysis is not used in the enrichment process. The rest is obtained from the system. 30 The total H₂S entering the enrichment tank (8) is approximately 0.195 kmol / hour, or 6.63 kg / hour. This corresponds to the amount of H₂S. The conversion of H₂S to sulfate; 14 H₂S + 2O₂ → SO₄²⁻ + 2H⁺ This occurs in accordance with the reaction, and the amount of H₂S in question is converted into sulfate. Approximately 12.48 kg / hour of O₂ is required for its conversion, on a stoichiometric basis. By feeding approximately 20 kg / hour of O₂ into the enrichment tank (8), stoichiometric 5 Oxygen is supplied at approximately 60% above the oxygen requirement. H₂S / O₂ mass ratio The feed ratio is approximately 1 / 3. Thus, the conversion of H₂S to sulfate occurs. A reaction environment with excess oxygen is created. In the enrichment tank (8), the liquid obtained as a result of anaerobic digestion is 10 digestate, sulfurous stream from H₂S origin from sulfur separator (2) and gas separator (7) are combined with the incoming pure oxygen. The enrichment process combines them. through supporting biochemical and chemical mechanisms is being carried out. Naturally occurring sulfur-oxidizing microorganisms in the digestate. (SOB) metabolizes H₂S using pure oxygen fed into the system, and It enables the conversion of sulfur into sulfate (SO₄²⁻) form. In addition, the liquid The chemical reaction that occurs when dissolved H₂S comes into contact with pure oxygen. Oxidation also contributes to sulfate formation. Thus, external sulfur 20 or without adding external bacterial culture with a sulfate-containing chemical substance A sulfate-enriched digestate is obtained. Enrichment tank (8), a continuous flow stirred reactor in the example application. It is operated as (CSTR). Continuous supply of pure oxygen into the tank is required. 25 Liquid-gas mass transfer is achieved in this way; gas diffusion and sulfur oxidizing The conversion of H₂S to sulfate through the activity of microorganisms throughout the process flow. They are carried out simultaneously. The process in the enrichment tank (8) is carried out in the pH range of 6.5-8.5 and the temperature range of 25-45°C for 30 This is carried out preferably at a pH of 7.2-8.2 and a temperature of 30-38°C. is maintained. These operating conditions are derived from the anaerobic digester (1). the natural buffering capacity of the digestate and its thermal stability within the process It is protected by means of... Using pure oxygen instead of air in the enrichment tank (8), digestat It also contributes to the preservation of nitrogen compounds within it. With air During the aeration process, a large amount of inert gas flow exits the tank. During this process, volatile ammonia may be transferred to the gas phase, while pure 5 The use of oxygen reduces the gas stripping effect. Example In practice, the flow is directed from the sulfur separator (2) to the enrichment tank (8) Approximately 5.47 kg / hour of NH₃ is recovered into the system. Thus, sulfate In addition to enrichment, retention of nitrogen compounds in the liquid phase. It is supported. 10 The sulfate-enriched digestate coming out of the enrichment tank (8) is mechanically processed. The initial digestate coming out of the anaerobic digester (1) is sent to the separator (9). It is in liquid form and consists of approximately 86.5% water by its total mass. Mechanical As a result of the separation, most of the water in the digestate is removed, and sample 15 In practice, approximately 2000 kg / hour of water is recovered. The separated water is returned to the system. while being fed, the water content reduced solid digestate drying unit (10) is being sent. In parallel, the hydrogen obtained in the electrolyzer (6) is transferred to the Sabatier reactor (3) 20 It is sent here and reacted with CO₂ to produce synthetic methane and water. In the example application, the Sabatier reactor (3) is a nickel (Ni) based fixed bed reactor. It contains a catalyst. The Sabatier reactor receives approximately 704.26 kg / hour of CO₂. 130.28 kg / hour of H₂ is being fed. These amounts are approximately 16 respectively. This corresponds to 65 kmol / hour CO₂ and 65 kmol / hour H₂, approximately 4:1 H₂ / CO₂. It provides a molar feed rate. The inlet pressure of the Sabatier reactor (3) is approximately The outlet pressure is approximately 9.6 atm. The water fed into the Sabatier reactor (3) The gas stream containing carbon dioxide is at a temperature of approximately 40°C, while hydrogen is at a temperature of approximately 80°C. It is fed into the reactor. As a result of the exothermic methane reaction, the reactor The operating temperature inside reaches approximately 426.85°C. 30 A high amount of heat is released during the Sabatier reaction, and the aforementioned Heat is recovered via a heat exchanger (4). In the system, Sabatier The high-temperature thermal energy resulting from the reaction is utilized. 16 and approximately 1200 kW after meeting the facility's own thermal needs. Thermal power is being recovered. Some of the recovered heat is thermostatically controlled by the anaerobic digester (1). used, the main part of which is the solid digestate coming out of the mechanical separator (9) 5 It is transferred to the drying unit (10) for drying purposes. From the mechanical separator (9) The solid digestate coming out contains approximately 70-80% moisture, from the Sabatier reactor (3) drying the final product by using the recovered thermal energy and moisture The percentage of solids is reduced to approximately 15-20%. In this way, the solid matter content is... Increased dry organomineral fertilizer, which is easier to store and transport, is obtained. 10 is being done. The water separated in the moisture separator (5) and the water separated from the digestate in the mechanical separator (9) a small portion of it is used to meet the water needs of the electrolyzer (6). It is fed back into the system. Thus, the 15 separated during the purification of biogas is recovered. Sulfur compounds derived from H₂S are used in sulfate enrichment of digestate and in electrolysis. The pure oxygen obtained during the oxidation of H₂S, obtained during electrolysis In the production of synthetic methane, the hydrogen produced is released during the Sabatier reaction. The heat generated is used in drying the digestate, and the water separated during the process is reused. By being evaluated in the electrolysis process, an integrated organomineral fertilizer production 20 The process is being carried out. The scope of protection of the invention is set out in the claims attached hereto and is strictly limited to these. The detailed explanation cannot be limited to the examples given. Because in technology... an expert, without deviating from the main theme of the invention, will do what is described above. 25 It is clear that similar structures can emerge in light of this.

Claims

17 REQUESTS 1. Obtaining biogas and digestate through anaerobic fermentation of organic raw materials. an organomineral containing at least one anaerobic digester (1) that enables it to be processed The fertilizer production system is (A), and its characteristic is; 5  H₂S in the biogas obtained in relation to the anaerobic digester (1) at least one sulfur separator (2) that separates sulfur compounds from the source,  at least one electrolyzer that produces hydrogen and oxygen by electrolysis of water (6),  related to the electrolyzer (6) and separate the obtained hydrogen and oxygen from each other at least one gas separator (7), 10  Liquid digestate from the anaerobic digester (1) is passed through the sulfur separator (2) incoming H₂S-derived sulfur compounds and gas separator (7) by bringing it into contact with oxygen, H₂S-derived sulfur is converted into sulfate. the most effective way to convert and enrich the digestate with sulfate a small enrichment tank (8), 15  Reaction of hydrogen and carbon dioxide obtained from the electrolyzer (6) resulting in at least one that produces synthetic methane and heat. Sabatier reactor (3),  At least one heat recovery system that recovers the heat released in the Sabatier reactor (3) modifier (4), 20  Reduce the water content of the digestate coming from the enrichment tank (8) by at least a mechanical separator (9) and  Solid digestate obtained from the mechanical separator (9) in the Sabatier reactor (3) heat released and recovered by means of heat exchanger (4) It must contain at least one drying unit (10) that dries using 25 2. The organomineral fertilizer production system (A) according to claim 1 is characterized by; gas. from the bottom of the enrichment tank (8) of pure oxygen from the separator (7) at least one oxygen tank that provides its feed and is associated with the enrichment tank (8). It has an exit. 30 3. Organomineral fertilizer production system (A) according to claim 1, its characteristic is; gas At least one moisture separator (5) for separating the water in the stream It includes. 18 4. The organomineral fertilizer production system (A) according to claim 3 is characterized as follows: The mentioned moisture separator (5) returns the separated water to the electrolyzer (6). It is related to the electrolyzer (6) for its feeding.

5. The organomineral fertilizer production system (A) according to claim 1 has the following characteristics: 5 enrichment tank (8), a continuous flow stirred reactor (CSTR) It is the fact that.

6. Obtained as a result of anaerobic fermentation of organic raw materials. an organomineral fertilizer for the production of organomineral fertilizer from digestate 10 It is a production method, and its characteristic is; i. H₂S from biogas obtained as a result of anaerobic fermentation Separation of sulfur compounds from various sources, ii. Obtaining hydrogen and oxygen through electrolysis of water, iii. at least a portion of the oxygen obtained as a result of electrolysis, 15 liquid digestata along with the aforementioned H₂S-derived sulfur compounds nutrition, iv. In the digestate, sulfur derived from H₂S is converted to sulfate. Obtaining sulfate-enriched digestate, v. Hydrogen obtained as a result of electrolysis with carbon dioxide Sabatier 20 Synthetic methane and heat are obtained by subjecting it to a reaction. vi. at least some of the water in the sulfate-enriched digestate mechanical separation and vii. During the Sabatier reaction of the digestate from which the water has been mechanically separated The drying steps using the recovered heat released are 25 It includes.

7. This is a method of producing organomineral fertilizer according to claim 6, and its characteristic is; iii. In this step, at least some of the pure oxygen obtained as a result of electrolysis Controlled 30 from the bottom of the enrichment tank (8) where the liquid digestate is located It is nutrition in this way.

8. This is a method of producing organomineral fertilizer according to claim 6, and its characteristic is; iv. In this step, the conversion of H₂S-derived sulfur to sulfate occurs in the digestate. 19 naturally occurring sulfur-oxidizing microorganisms (SOBs) dissolved in liquid phase by biological oxidation carried out by The chemical oxidation of H₂S with oxygen together It is achieved through the use of...

9. This is a method of producing organomineral fertilizer according to claim 6, and its characteristic is; iv. In the next step, the conversion of H₂S-derived sulfur to sulfate takes place at a pH of 6.5-8.5 and 25- It is carried out within a temperature range of 45°C.

10. This is a method of producing organomineral fertilizer according to claim 9, and its characteristic is; iv. 10 In the next step, the conversion of H₂S-derived sulfur to sulfate occurs at a pH of 7.2-8.2 and 30- It is carried out within a temperature range of 38°C.

11. This is a method of producing organomineral fertilizer according to claim 6, and its characteristic is; v. In step 15, the heat released during the Sabatier reaction is transferred to a heat exchanger. (4) recovery and at least part of the recovered heat vii. The next step is its use in drying the digestate.

12. This is a method of producing organomineral fertilizer according to claim 6, and its characteristic is; iv. In step 20, the oxygen supplied for the conversion of H₂S-derived sulfur to sulfate is 20. the amount of stoichiometric oxygen required for the conversion of H₂S to sulfate It is the amount being above the limit.

13. This is a method of producing organomineral fertilizer according to claim 6, and its characteristic is; vi. at least some of the water mechanically separated in step 1, 25 in step ii. It is the feedback used in the electrolysis process.

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