A system for reducing organic waste and increasing biogas production, combined with a hydrothermal carbonization device that improves energy efficiency

Abstract

A system for reducing organic waste and increasing biogas production combined with a hydrothermal carbonization device with improved energy consumption efficiency is disclosed. According to one aspect of the present invention, the system for reducing organic waste and increasing biogas production includes: a storage tank for receiving and storing organic waste; an anaerobic digestion tank for receiving the organic waste from the storage tank to digest the organic matter and produce biogas; a dehydrator for primary dehydration of the organic waste discharged from the anaerobic digestion tank; a hydrothermal carbonization device for receiving the dehydrated organic waste and hydrothermal carbonization; and a filter press for secondary dehydration of the hydrothermal carbonization product discharged from the hydrothermal carbonization device.

Description

[Technical Field]

[0001] The present invention relates to a system for reducing organic waste and increasing biogas production, which is combined with a hydrothermal carbonization device and has improved energy consumption efficiency. [Background technology]

[0002] The material described in this section merely provides background information for the present invention and does not constitute prior art.

[0003] Due to regulatory reforms such as the ban on direct landfilling and ocean dumping of organic waste, there has been a surge in interest in reducing, recycling, and using organic waste to produce biogas.

[0004] Anaerobic digestion is a treatment method that is very suitable for reducing and stabilizing organic waste, and in particular, the methane (CH4) gas produced during the anaerobic digestion process can be used as an alternative energy source. Therefore, anaerobic digestion is an environmentally friendly process and is very useful for treating organic waste.

[0005] However, the digestate that has undergone anaerobic digestion still contains biomass produced in the anaerobic digester, and such biomass has limitations in weight reduction using mechanical dehydration due to internal water within cells and interstitial water between cells.

[0006] In relation to reducing the volume of sludge, there has been recent interest in applying additional volume reduction processes to treat biomass produced in digesters, with the application of hydrothermal carbonization, which uses high temperatures and high pressures, being particularly widespread. However, because this process uses high-temperature thermal energy, efforts are underway to maximize its utilization while conserving energy, as well as to address operational issues that may arise due to the high pressure. Summary of the Invention [Problem to be solved by the invention]

[0007] One embodiment of the present invention aims to provide a system for reducing organic waste and increasing biogas production, which minimizes the amount of sludge ultimately generated and reduces the cost of final organic waste treatment by connecting a hydrothermal carbonization device with improved energy consumption efficiency to the downstream of an anaerobic digester.

[0008] One object of one embodiment of the present invention is to provide a system for reducing organic waste and increasing biogas production, which can increase biogas production by returning the supernatant liquid generated when anaerobic digestion sludge undergoes a hydrothermal carbonization reaction and a dewatering process using a filter press to an anaerobic digestion tank.

[0009] One embodiment of the present invention is an organic waste reduction system that improves the energy consumption efficiency of a hydrothermal carbonization device, and has the objective of providing a system for reducing organic waste and increasing biogas production that reuses thermal energy within the system, thereby reducing the energy consumption of the system.

[0010] Another object of one embodiment of the present invention is to provide a system for reducing organic waste and increasing biogas production that can reduce the impact load imposed on a treatment system to which the digestion supernatant is connected. [Means for solving the problem]

[0011] According to one aspect of the present invention, there is provided a system for reducing organic waste and increasing biogas production that is combined with a hydrothermal carbonization device, the system comprising: a storage tank into which organic waste is introduced and stored; an anaerobic digestion tank into which the organic waste from the storage tank is introduced to digest the organic matter and produce biogas; a dehydrator that performs primary dehydration of the organic waste discharged from the anaerobic digestion tank; a hydrothermal carbonization device into which the dehydrated organic waste is introduced and hydrothermally carbonized; and a filter press that performs secondary dehydration of the hydrothermal carbonization product discharged from the hydrothermal carbonization device.

[0012] According to one aspect of the present invention, the hydrothermal carbonization apparatus includes: a preheating tank into which the organic waste discharged from the dehydrator is introduced and preheated; a plurality of hydrothermal carbonization reactors into which the preheated organic waste from the preheating tank is applied and hydrothermally carbonized in a predetermined environment; a pressure reduction tank into which all of the products hydrothermally carbonized in each hydrothermal carbonization reactor, excluding some of the gaseous components, are introduced, where the gaseous components are separated from the non-gaseous components, and the gaseous components are discharged to the preheating tank and the remaining products are discharged; a steam purification tank into which some of the gaseous components of the products hydrothermally carbonized in any one of the hydrothermal carbonization reactors are introduced, where the gaseous components are separated from the liquid components, and the gaseous components are discharged to another hydrothermal carbonization reactor and the liquid components are discharged to the pressure reduction tank; a heat exchanger into which the hydrothermal carbonized products discharged from the pressure reduction tank are introduced, where they are cooled to a predetermined temperature, and then supplied to the filter press; and a control unit that controls the operation of each component within the hydrothermal carbonization apparatus.

[0013] According to one aspect of the present invention, each hydrothermal carbonization reactor performs the same process to hydrothermally carbonize organic waste, but performs different operations at different times.

[0014] According to one aspect of the present invention, the control unit is characterized in that when the pressure due to the gas components in any one of the hydrothermal carbonization reactors is equal to or greater than a predetermined reference value, the control unit controls the discharge of a portion of the gas components into the steam purification tank.

[0015] According to one aspect of the present invention, the preset environment has a pressure of 5 to 64 bar and a temperature of 150 to 280°C.

[0016] According to one aspect of the present invention, the hydrothermal carbonization apparatus further includes an ejector that injects steam flowing in from the outside and gas components separated and discharged in the steam purification tank into any one of the hydrothermal carbonization reactors.

[0017] According to one aspect of the present invention, the heat exchanger is characterized in that the heated cooling water generated by cooling the hydrothermal carbonized product is merged into a boiler that supplies steam to the hydrothermal carbonization device, or into the feedwater for a boiler that heats the anaerobic digestion tank, thereby reducing energy consumption.

[0018] According to one aspect of the present invention, the filter press is characterized in that the supernatant liquid discharged during dehydration of the hydrothermal carbonization product is discharged into the storage tank so that it can be used for anaerobic digestion.

[0019] According to one aspect of the present invention, the organic waste is selected from the group consisting of thickened sludge generated in sewage and wastewater treatment equipment, food waste, food wastewater, livestock manure sludge, and mixtures of any one or more of these.

[0020] According to one aspect of the present invention, the organic waste reduction and biogas production system further includes a digestion supernatant treatment device, which removes nitrogen components from the supernatant discharged from the dehydrator.

[0021] According to one aspect of the present invention, the digestion supernatant treatment device includes a partial nitritation reaction tank into which the digestion supernatant is introduced to perform partial nitritation; an AOB granule production tank into which sludge with reduced settling property present in the partial nitritation reaction tank is introduced to produce ammonium oxidizing bacteria (AOB) granules; an intermediate storage tank into which treated water from the partial nitritation reaction tank is introduced and stored while solids are precipitated and removed from the treated water; and an anammox reaction tank that receives treated water from the intermediate storage tank and removes nitrogen components through an anaerobic ammonium oxidation (anammox) reaction. [Effects of the Invention]

[0022] As described above, according to one aspect of the present invention, digested sludge that has undergone anaerobic digestion is solubilized using hydrothermal treatment in a subsequent stage and dehydrated using a filter press, which has the advantage of reducing the energy consumption for subsequent drying or the treatment costs for final disposal.

[0023] According to one aspect of the present invention, there is an advantage in that the thermal energy generated in the hydrothermal carbonization device can be reused in the organic waste reduction and biogas production increase system, thereby improving the energy consumption efficiency of the system.

[0024] Furthermore, according to one aspect of the present invention, there is an advantage in that the impact load imposed on the processing system to which the digestion supernatant is connected can be reduced. [Brief explanation of the drawings]

[0025] [Figure 1] 1 is a diagram showing a process flow of an organic waste reduction and biogas production system combined with a hydrothermal carbonization device according to an embodiment of the present invention. FIG. [Figure 2] 1 is a diagram showing the configuration of a hydrothermal carbonization apparatus according to one embodiment of the present invention. [Figure 3] FIG. 2 is a diagram illustrating the operation sequence of a hydrothermal carbonization reactor according to one embodiment of the present invention. [Figure 4] FIG. 2 is a diagram showing the operation sequence of each hydrothermal carbonization reactor according to one embodiment of the present invention. [Figure 5] FIG. 2 is a diagram showing the operation sequence of a hydrothermal carbonization apparatus according to one embodiment of the present invention. [Figure 6] FIG. 2 is a diagram showing the operation sequence of a hydrothermal carbonization apparatus according to one embodiment of the present invention. [Figure 7] FIG. 2 is a diagram showing the operation sequence of a hydrothermal carbonization apparatus according to one embodiment of the present invention. [Figure 8] FIG. 2 is a diagram showing the operation sequence of a hydrothermal carbonization apparatus according to one embodiment of the present invention. [Figure 9] FIG. 2 is a diagram showing the operation sequence of a hydrothermal carbonization apparatus according to one embodiment of the present invention. [Figure 10]FIG. 2 is a diagram showing the operation sequence of a hydrothermal carbonization apparatus according to one embodiment of the present invention. [Figure 11] FIG. 2 is a diagram showing the configuration of a hydrothermal carbonization apparatus according to another embodiment of the present invention. [Figure 12] 1 is a diagram showing the configuration of a digestion supernatant treatment device according to an embodiment of the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0026] Although the present invention can be implemented in various forms and in various embodiments, specific embodiments will be illustrated in the drawings and described in detail. However, it should be understood that this is not intended to limit the present invention to the specific embodiments, but rather to include all modifications, equivalents, or alternatives that fall within the spirit and technical scope of the present invention. Similar reference numerals are used to refer to similar components throughout the drawings.

[0027] Terms such as "first," "second," "A," and "B" may be used to describe various components, but the components should not be limited by these terms. These terms are used only to distinguish one component from another. For example, a first component may be referred to as a "second component," and similarly, a second component may be referred to as a "first component," without departing from the scope of the present invention. The term "and / or" includes a combination of multiple related listed items or any item of multiple related listed items.

[0028] When a component is said to be "coupled" or "connected" to another component, it should be understood that it may be directly coupled or connected to the other component, but that there may be other components in between. In contrast, when a component is said to be "directly coupled" or "directly connected" to another component, it should be understood that there are no other components in between.

[0029] The terms used in this application are merely used to describe specific embodiments and are not intended to limit the present invention. A singular expression includes a plural expression unless the context clearly indicates otherwise. In this application, it should be understood that terms such as "comprise" or "have" do not preclude the possibility of the presence or addition of features, numbers, steps, operations, components, parts, or combinations thereof described in the specification.

[0030] Unless otherwise defined, all terms used herein, including technical or scientific terms, have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.

[0031] Terms defined in commonly used dictionaries should be construed to have a meaning consistent with the meaning they have in the context of the relevant art, and should not be construed in an idealized or overly formal sense unless expressly defined in this application.

[0032] Furthermore, the configurations, processes, steps, or methods included in the embodiments of the present invention may be shared within the scope of not being technically inconsistent with each other.

[0033] FIG. 1 is a diagram showing a system for reducing organic waste and increasing biogas production, which is combined with a hydrothermal carbonization apparatus according to one embodiment of the present invention.

[0034] As shown in the figure, an organic waste reduction and biogas production system 100 (hereinafter abbreviated as "system 100") combined with a hydrothermal carbonization apparatus according to one embodiment of the present invention includes a first storage tank 110, an anaerobic digester 120, a second storage tank 130, a dehydrator 140, a cake storage tank 150, a hydrothermal carbonization apparatus 160, a filter press 170, and a digestion supernatant treatment device 180.

[0035] The first storage tank 110 receives organic waste delivered from outside and the supernatant discharged from the filter press 170 , and stores them until they are poured into the anaerobic digestion tank 120 .

[0036] On the other hand, the organic waste delivered from the outside can be selected from the group consisting of thickened sludge generated in sewage treatment plants, pretreated food waste, food wastewater and livestock manure, and mixtures thereof. Such organic waste may be subjected to additional pretreatment before flowing into the first storage tank 110 for effective anaerobic digestion in the subsequent stage.

[0037] For example, sludge generated in a sewage treatment plant can be transported to the first storage tank 110 after being concentrated through a thickener to a total solids (TS) concentration of about 4-5%. Food waste can be transported to the first storage tank 110 after indigestible components are removed through crushing, separation by specific gravity, and fine crushing, and after being crushed to an appropriate size for digestion. Livestock manure sludge can be transported to the first storage tank 110 after impurities are removed. In addition, when two or more types of organic waste are mixed and treated, each type of waste can be pretreated separately and then mixed in the first storage tank 110, but the pretreatment method for the organic waste is not limited to this.

[0038] The anaerobic digestion tank 120 receives and digests a mixture of organic waste and the supernatant liquid from the filter press 170 from the first storage tank 110. In this way, the anaerobic digestion tank 120 reduces and stabilizes the organic waste, and produces gaseous products (biogas) and digested sludge.

[0039] The anaerobic digester 120 generates biogas from organic waste and decomposes organic matter through the action of anaerobic microorganisms. The biogas generated in the anaerobic digester 120 is used to generate electricity through a biogas purification facility or is reused as thermal energy. The digested sludge generated in the anaerobic digester 120 is discharged to the second storage tank 130.

[0040] The second storage tank 130 receives the digested sludge generated in the anaerobic digestion tank 120 and temporarily stores it before it is subjected to primary dehydration in the dehydrator 140. The second storage tank 130 can also receive excess sludge discharged from the downstream digestion supernatant treatment device 180 and store it there until it is discharged together with the digested sludge to the dehydrator 140.

[0041] The dewatering machine 140 receives the mixture of digested sludge and excess sludge from the second storage tank 130 and performs primary water removal. The dewatering machine 140 separates the sludge mixture into dewatered cake and supernatant liquid, and discharges the cake to the cake storage tank 150 and the supernatant liquid to the digested supernatant liquid treatment device 180.

[0042] The dehydrator 140 is a mechanical dehydrator, and may be, for example, a centrifugal dehydrator. The organic waste (sludge) that has been primarily dehydrated in the dehydrator 140 has a moisture content of approximately 78%. The organic waste that has been primarily dehydrated in the dehydrator 140 is discharged to the hydrothermal carbonization device 160, where post-treatment (hydrothermal carbonization) is carried out to reduce the amount of organic waste.

[0043] The supernatant liquid is discharged from the dehydrator 140 to a digestion / elution liquid treatment device 180, which performs post-treatment to remove nitrogen components from the supernatant liquid, as will be described later.

[0044] The cake storage tank 150 receives the organic waste that has been primarily dewatered by the dehydrator 140 and temporarily stores it before it is transported to the hydrothermal carbonization device 160.

[0045] The hydrothermal carbonization device 160 receives the organic waste from the cake storage tank 150 , hydrothermally carbonizes (HTC) the organic waste, and discharges the hydrothermal carbonization product to the filter press 170 .

[0046] In hydrothermal carbonization, when the temperature of a closed reactor is raised by an external heat source in a closed system, hot water in the range of 150-280°C decomposes some of the organic matter in the solid material, allowing the carbonization reaction to proceed without evaporation of water. During this process, decarboxylation and dehydration reactions are induced, increasing the energy density of the solid fuel through carbon fixation, and hydrophobicity improves dehydration.

[0047] The hydrothermal carbonization unit 160 processes organic waste at a preset temperature and pressure, destroying the cell walls of the waste and expelling the internal water, thereby improving the dehydration of the waste and breaking down high molecular weight substances into low molecular weight substances. Therefore, the hydrothermal carbonization of organic waste further improves the moisture removal rate in the subsequent filter press 170.

[0048] The specific configuration and operation sequence of the hydrothermal carbonization device 160 will be described later with reference to FIGS.

[0049] The filter press 170 receives the hydrothermal carbonization product discharged from the hydrothermal carbonization device 160 and separates it into solid and liquid. The filter press 170 discharges the supernatant liquid into the first storage tank 110 and the dewatered cake for final disposal.

[0050] Depending on the disposal method, the dehydrated cake discharged from the filter press 170 may be used as fuel after drying or may be transported to an external site for outsourced processing. The moisture content of the dehydrated cake discharged from the filter press 170 is 45% or less.

[0051] The filter press 170 performs dewatering by pressure filtration and pressure bonding, and has the advantages of being easily installed in a small footprint and achieving a lower moisture content than a typical mechanical dewatering machine.

[0052] The filter press 170 is operated in a batch mode, and operates in the following order: feeding the target material, primary solid-liquid separation by pressure filtration, dewatering by high-pressure squeegeeing, and detaching the separated cake. In this case, a separate storage tank (not shown) may be included between the hydrothermal carbonization apparatus 160 and the filter press 170 to feed the hydrothermal carbonized product into the filter press 170.

[0053] As mentioned above, filter presses can achieve the lowest moisture content among conventional mechanical dewatering devices. Generally, when dewatering sludge (with a moisture content of about 80%) that has undergone primary dewatering using only a filter press, the moisture content of the discharged dewatered cake remains at 55-65%.

[0054] However, the system 100 sequentially arranges a hydrothermal carbonization device 160 and a filter press 170 to hydrothermally carbonize the organic waste that has undergone anaerobic digestion, improving its dehydration and reducing its volume. As a result, the final dehydrated cake discharged from the system 100 has a moisture content of 45% or less. As a result, the organic waste reduction and biogas production system 100 can reduce the amount of waste discharged by 75% or more.

[0055] As described above, in the system 100, the anaerobic digestion sludge is hydrothermally carbonized, converting high molecular weight organic substances into low molecular weight organic substances, thereby improving the dewaterability and biodegradability of the waste. Therefore, the supernatant discharged from the solid-liquid separation process in the filter press 170 contains a large amount of biodegradable dissolved organic substances.

[0056] This supernatant is returned to the first storage tank 110 and used again for digestion in the anaerobic digestion tank 120. By performing the digestion process, the amount of biogas produced in the anaerobic digestion tank 120 can be increased by 20% or more compared to when the supernatant is not returned.

[0057] The digested sludge treatment device 180 receives the supernatant liquid obtained by the primary dewatering of mixed sludge such as digested sludge in the dehydrator 140, removes nitrogen components from the supernatant liquid, and discharges treated water. The treated water discharged from the digested sludge treatment device 180 can be treated separately at a later stage or can be treated in conjunction with another water treatment device such as a sewage treatment device.

[0058] As described above, the system 100 recovers the supernatant from the filter press 170 and converts it into biogas in the anaerobic digestion tank 120. Therefore, the supernatant generated in the dehydrator 130 downstream of the anaerobic digestion tank 120 contains a low concentration of organic matter and a high concentration of nitrogen components.

[0059] The nitrogen components in the supernatant liquid can affect the quality of the treated water from the wastewater treatment equipment when the supernatant liquid is treated in conjunction with a wastewater treatment equipment, making direct discharge difficult. Therefore, the digestion supernatant liquid treatment equipment 180 removes nitrogen from the supernatant liquid and returns or discharges the treated water to the wastewater treatment equipment.

[0060] In addition, the digestion supernatant treatment device 180 discharges excess sludge during the nitrogen treatment process of the supernatant, and the excess sludge from the digestion supernatant treatment device 180 is collected again in the second storage tank 130 and reprocessed in the dehydrator 140 and hydrothermal carbonization device 160.

[0061] The specific configuration of the digestion / elution liquid treatment device 180 will be described later with reference to FIG.

[0062] As described above, by sequentially arranging a hydrothermal carbonization apparatus 160 and a filter press 170 downstream of the anaerobic digestion tank 120, the moisture content of the dehydrated cake discharged from the system 100 can be reduced to 45% or less (35 to 45%).

[0063] Typically, the moisture content of the primarily dewatered sludge discharged from the sewage treatment process is 80% or more, and a large amount of heat energy is consumed to reduce the moisture content of the sludge to 10% or less using only a dryer. However, System 100 produces dewatered cake with a moisture content of 45% or less, thereby significantly reducing the amount of heat energy consumed to dry the dewatered cake.

[0064] Furthermore, the system 100 returns the supernatant discharged from the filter press 170 to the anaerobic digester 120 to use as an additional organic matter source for biogas production, thereby increasing the amount of biogas generated in the anaerobic digester 120 by 20% or more compared to when anaerobic digestion is performed alone.

[0065] In other words, the system 100 destroys biologically difficult-to-decompose substances in the hydrothermal carbonization device 160, and returns the organic substances with improved biodegradability to the upstream anaerobic digestion tank 120, thereby making it possible to improve the amount of biogas produced in the anaerobic digestion tank 120 compared to general anaerobic digestion systems (anaerobic digestion-only treatment).

[0066] In addition, the system 100 further includes a digestion supernatant treatment device 180, which treats the supernatant containing high concentrations of nitrogen components generated through the anaerobic digestion tank 120, thereby minimizing the impact on the quality of treated water from the sewage treatment device in which the supernatant is treated.

[0067] FIG. 2 is a diagram showing the configuration of a hydrothermal carbonization apparatus 160 according to one embodiment of the present invention.

[0068] Referring to FIG. 2, a hydrothermal carbonization apparatus 160 according to one embodiment of the present invention includes a preheating tank 210, a transfer pump 215, a plurality of hydrothermal carbonization reactors 220, a pressure reducing tank 230, a steam purification tank 240, a heat exchanger 250, and a control unit (not shown).

[0069] The preheating tank 210 preheats the organic waste to be treated by receiving it from the cake storage tank 150. The hydrothermal carbonization reactor 220, which will be described later, hydrothermally carbonizes the organic waste under relatively high temperature and pressure conditions. This requires the consumption of a relatively large amount of thermal energy, but to prevent this, the preheating tank 210 is placed before the hydrothermal carbonization reactor 220 in the treatment process to preheat the organic waste to be carbonized.

[0070] The preheating tank 210 does not receive heat energy (mainly in the form of steam) from a separate heat source, but instead receives gas components separated in the decompression tank 230 (described below). The gas components separated in the decompression tank 230 have a constant temperature. Rather than being discharged (vented) to the outside, the gas components separated in the decompression tank 230 are returned to the preheating tank 210 and used for preheating. This allows the preheating tank 210 to preheat the incoming organic waste using the gas components separated in the decompression tank 230 without the need for heat energy from a separate heat source, thereby minimizing energy consumption.

[0071] The transfer pump 215 transfers the organic waste stored in the cake storage tank 150 to the preheating tank 210. The transfer pump 215 is controlled by a control unit (not shown) in conjunction with the operating sequence of the hydrothermal carbonization device 160 in order to transfer the organic waste from the cake storage tank 150 to the preheating tank 210 at a constant rate.

[0072] The hydrothermal carbonization reactor 220 receives preheated organic waste from the preheating tank 210 and hydrothermally carbonizes it. The hydrothermal carbonization reactor 220 hydrothermally carbonizes the organic waste, allowing the organic waste to be smoothly dehydrated in the filter press 170 and finally disposed of (dried or outsourced).

[0073] The hydrothermal carbonization reactor 220 operates as shown in FIG.

[0074] FIG. 3 is a diagram illustrating the operation sequence of the hydrothermal carbonization reactor 220 according to one embodiment of the present invention.

[0075] Referring to FIG. 3, preheated organic waste is first introduced into the hydrothermal carbonization reactor 220. Once the organic waste is introduced, a predetermined environment must be created in the hydrothermal carbonization reactor 220 to allow the hydrothermal carbonization reaction to occur. The predetermined environment may be a pressure of 5 to 64 bar, more specifically, approximately 10 to 40 bar, and a temperature of 150 to 280°C, more specifically, 180 to 250°C to improve the decomposition ability of the organic waste. At this time, thermal energy (steam) is applied from an external heat source to ensure that the hydrothermal carbonization reactor 220 maintains the predetermined temperature environment. Once the predetermined environment, particularly the temperature condition, is established by sufficient temperature rise, the hydrothermal carbonization reaction occurs within the hydrothermal carbonization reactor 220. The hydrothermal carbonization reaction proceeds for a predetermined time (e.g., several tens of minutes). After the reaction is completed, some of the gaseous components of the product are discharged to the steam purification tank 240, and all remaining components are discharged to the vacuum tank 230. The hydrothermal carbonization reactor 220 operates in this manner to hydrothermally carbonize the organic waste.

[0076] Referring again to FIG. 2, the hydrothermal carbonization reactor 220 may be implemented in multiple units. After the hydrothermal carbonization reaction is completed in one of the hydrothermal carbonization reactors 220, a portion of the gaseous components of the product is discharged to the steam purification tank 240. As described above, the gaseous components separated in the pressure reduction tank 230 flow into the preheating tank 210, while the steam purification tank 240, described below, also separates liquid components that may be contained in the gaseous components (steam), similar to the pressure reduction tank 230. The gaseous components separated in the steam purification tank 240 flow into other hydrothermal carbonization reactors 220 to assist in the temperature composition for hydrothermal carbonization. This is possible because the multiple hydrothermal carbonization reactors 220a-220d each operate as shown in FIG. 4.

[0077] FIG. 4 is a diagram showing the operation sequence of each hydrothermal carbonization reactor according to one embodiment of the present invention.

[0078] Each of the hydrothermal carbonization reactors 220a to 220d operates as described with reference to Fig. 3, with a time lag between them. For example, as shown in Fig. 4, when the hydrothermal carbonization reactor 220a has begun the process of receiving organic waste from the preheating tank 210 and raising its temperature, the hydrothermal carbonization reactor 220b can finally begin receiving organic waste from the preheating tank 210. The hydrothermal carbonization reactor 220c can begin receiving organic waste from the preheating tank 210 at the time when the hydrothermal carbonization reactor 220a begins hydrothermal carbonization of the organic waste, and the hydrothermal carbonization reactor 220d can begin receiving organic waste from the preheating tank 210 at the time when the product of the completed reaction is discharged to the outside. When operating in this manner, as described above, the purified gas component (steam) discharged from any one of the hydrothermal carbonization reactors 220 can flow into another hydrothermal carbonization reactor that is being heated, thereby reducing the amount of thermal energy consumed for heating.

[0079] Referring again to FIG. 2, the hydrothermal carbonization reactor 220 can secure a portion of the heat required for the hydrothermal carbonization reaction from the gas components generated in other hydrothermal carbonization reactors 220, thereby minimizing wasted energy and reducing energy consumption for heating.

[0080] The hydrothermal carbonization reactor 220 includes an internal pressure sensor, and under the control of a control unit (not shown), separates and discharges a portion of the gaseous components of the product of the hydrothermal carbonization reaction to the steam purification tank 240. The hydrothermal carbonization reactor 220 senses the pressure inside the reactor and separates and discharges all remaining gaseous components to the steam purification tank 240, except for an amount sufficient to preheat the preheating tank 210 (by being separated in the pressure reduction tank 230 and returned to the preheating tank 210). By performing pressure sensing, the hydrothermal carbonization reactor 220 precisely discharges the remaining amount other than that required for preheating to the steam purification tank 240, enabling the temperature of other hydrothermal carbonization reactors to be raised. Conventionally, the entire amount was discharged to the pressure reduction tank 230, and even if all the gaseous components were returned to the preheating tank and used for preheating, more than the amount required for preheating was returned, so the remaining gaseous components used for preheating were all discharged and discarded.

[0081] Alternatively, the hydrothermal carbonization reactor 220 senses its internal pressure to determine whether there is an abnormally excessive amount of gaseous components inside the reactor or whether excessive steam is being introduced from outside. If the pressure inside the reactor due to the gaseous components exceeds a preset reference value, the hydrothermal carbonization reactor 220, under the control of a control unit (not shown), discharges all of the gaseous components into the steam purification tank 240 until the pressure falls below the reference value. By discharging a certain amount of the gaseous components into the steam purification tank 240, the hydrothermal carbonization reactor 220 prevents the risk of explosion of the hydrothermal carbonization reactor and can recover heat that can be used to heat other hydrothermal carbonization reactors.

[0082] The depressurization tank 230 receives most of the products generated upon completion of the hydrothermal carbonization reaction in the hydrothermal carbonization reactor 220 and separates them into gaseous components and non-gaseous hydrothermal carbonization products. Among the products generated by the hydrothermal carbonization reaction, only the non-gaseous hydrothermal carbonization products (e.g., in a slurry state) correspond to the components that are dehydrated by the filter press 170, while the gaseous components correspond to components unrelated to dehydration. Therefore, the depressurization tank 230 separates the gaseous components from the products so that they can be used for preheating. The depressurization tank 230 has a pressure that is relatively lower than that of the hydrothermal carbonization reactor 220. The depressurization lowers the temperature of the products, and components with lower boiling points (lower than the temperature inside the depressurization tank) remain in a gaseous state, while components with higher boiling points (higher than the temperature inside the depressurization tank) liquefy into a liquid product. In this way, the decompression tank 230 generates a pressure difference with the hydrothermal carbonization reactor 220, converting certain components into non-gaseous products and the remaining components into a gaseous state. The decompression tank 230 returns the separated gaseous components to the preheating tank 210 and discharges the remaining hydrothermal carbonization products to the heat exchanger 250 for post-treatment.

[0083] The steam purification tank 240 receives a portion of the gaseous components discharged from the hydrothermal carbonization reactor 220 and purifies the liquid components. Because the hydrothermal carbonization reactor 220 is under relatively high pressure, even if only the gaseous components are discharged from the reactor 220, they may be completely converted into liquid components after discharge, or the gaseous components may be discharged at high pressure and the liquid components may be discharged together. Therefore, the steam purification tank 240 separates the gaseous and liquid components and sends the liquid components to the reduced pressure tank 230, while the gaseous components are sent to another hydrothermal carbonization reactor into which preheated organic waste is input. The steam purification tank 240 separates the gaseous and liquid components from the product as follows.

[0084] Components other than gaseous components of the products generated in the hydrothermal carbonization reactor 220 correspond to components that have already undergone the hydrothermal carbonization reaction. If these components are fed back into the hydrothermal carbonization reactor for further hydrothermal carbonization, it would be inefficient and wasteful in terms of energy consumption. Furthermore, when organic waste is fed from the preheating tank 210 to a specific hydrothermal carbonization reactor 220, an appropriate amount is fed to ensure smooth hydrothermal carbonization in the hydrothermal carbonization reactor 220. If products other than gaseous components generated in other hydrothermal carbonization reactors flow into the corresponding hydrothermal carbonization reactor, more than the appropriate amount will flow into the corresponding hydrothermal carbonization reactor. This will result in an inefficient hydrothermal carbonization reaction and excessive consumption of thermal energy. To prevent this problem, the steam purification tank 240 separates the liquid and gaseous components from the products discharged from the hydrothermal carbonization reactor 220 and transports them to different locations.

[0085] The steam purification vessel 240 may be realized in any shape or structure as long as it can separate the gas component and the liquid component.

[0086] The heat exchanger 250 lowers the temperature of the hydrothermal carbonization product discharged from the reduced pressure tank 230 to adjust it to the preset operating temperature of the filter press 170 applied in the subsequent stage.

[0087] The heat exchanger 250 circulates cooling water and exchanges heat with the high-temperature hydrothermal carbonization product to lower the temperature of the hydrothermal carbonization product. Since the temperature of the hydrothermal carbonization product discharged from the reduced pressure tank 230 is about 100°C, the heat exchanger 250 lowers the temperature of the hydrothermal carbonization product to about 60°C, which is within the appropriate temperature range of the filter press 170, and then supplies the hydrothermal carbonization product to the filter press 170.

[0088] Meanwhile, the cooling water heated by heat exchange with the high-temperature hydrothermal carbonization product can be recovered in an external heat source (boiler) to supply thermal energy (steam) to the hydrothermal carbonization reactor 220. That is, the heated cooling water is merged with the boiler water for steam generation, thereby reducing the energy consumed for steam generation.

[0089] The heated cooling water discharged from heat exchanger 250 may be combined with the water supply to a boiler (not shown) for heating anaerobic digestion tank 120. This reduces the energy consumption of the boiler for heating anaerobic digestion tank 120. Similarly, the heated cooling water may be recycled as heat exchange water for maintaining a preset operating temperature of anammox reactor 1250 (described below).

[0090] As described above, the thermal energy generated in the hydrothermal carbonization device 160 can be recovered in various ways within the system 100. Therefore, all of the thermal energy generated in the hydrothermal carbonization device 160 is reused, thereby improving the energy consumption efficiency of the system 100.

[0091] A control unit (not shown) controls the operation of each component in the hydrothermal carbonization apparatus 160.

[0092] A control unit (not shown) controls the transfer pump 215 so that the organic waste to be treated flows into the preheating tank 210. To this end, the preheating tank 210 may include a water level gauge, and the control unit (not shown) controls the pump so that if the water level in the preheating tank 210 is below a preset water level, the waste from the cake storage tank 150 is introduced into the preheating tank 210, and if the water level is above the preset water level, the introduction of the waste is stopped.

[0093] A control unit (not shown) can control the decompression tank 230 so that the gas components separated in the decompression tank 230 are returned to the preheating tank 210 in order to preheat the organic waste.

[0094] A control unit (not shown) controls the organic waste preheated in the preheating tank 210 to be transported to a hydrothermal carbonization reactor (e.g., 220a). After being transported, the control unit (not shown) causes steam from an external heat source and gas components (steam) separated from the products in another hydrothermal carbonization reactor (e.g., 220c) to flow into the hydrothermal carbonization reactor 220a so that a hydrothermal carbonization reaction can occur in the hydrothermal carbonization reactor 220a. This causes a hydrothermal carbonization reaction to occur in the hydrothermal carbonization reactor 220a.

[0095] At this time, the control unit (not shown) determines whether the pressure inside the hydrothermal carbonization reactor 220a is below a preset reference value. If the pressure inside the hydrothermal carbonization reactor 220a is below the preset reference value, this corresponds to a situation in which the hydrothermal carbonization reaction is proceeding normally. In contrast, if the pressure inside the hydrothermal carbonization reactor 220a exceeds the preset reference value, this corresponds to a situation in which an abnormally large amount of gas components has been generated or excessive steam has been introduced from the outside, potentially causing an abnormality in the reactor 220. In response, the control unit (not shown) discharges the gas components into the steam purification tank 240 until the pressure falls below the preset reference value. In this way, the control unit (not shown) resolves the abnormality inside the hydrothermal carbonization reactor 220a.

[0096] When the hydrothermal carbonization reaction has progressed for a preset time in the hydrothermal carbonization reactor 220a, the control unit (not shown) discharges a portion of the gaseous components to the steam purification tank 240 and all remaining products to the pressure reduction tank 230. At this time, when discharging the gaseous components, the control unit (not shown) discharges all of the gaseous components except for the amount that is separated in the pressure reduction tank 230 and sufficient to preheat the organic waste in the preheating tank 210 to the steam purification tank 240. As a result, the remaining gaseous components other than those required for preheating are not discharged to the outside and can all be used to heat other hydrothermal carbonization reactors, maximizing energy efficiency.

[0097] The control unit (not shown) controls the pressure reducing tank 230 to separate the gaseous components from the non-gaseous hydrothermal carbonization products, and controls the tank 230 to discharge the gaseous components to the preheating tank 210 and the remaining hydrothermal carbonization products to the heat exchanger 250 for anaerobic digestion.

[0098] At the same time, the remaining hydrothermal carbonization reactors 220b to 220d are controlled in parallel to operate in order. The process by which the control unit (not shown) controls the operation of each hydrothermal carbonization reactor will be described later with reference to FIGS.

[0099] By controlling each component in this manner using a control unit (not shown), the thermal energy applied from the external heat source can be minimized by recycling the thermal energy source to the maximum extent possible without wasting any thermal energy.

[0100] 5 to 10 are diagrams showing the operation sequence of an organic waste treatment apparatus according to an embodiment of the present invention, which show in detail the process in which organic waste is introduced into the hydrothermal carbonization apparatus 160 and treated.

[0101] Referring to FIG. 5, organic waste is (first) introduced into the preheating tank 210 and preheated under the control of a control unit (not shown).

[0102] Referring to FIG. 6, the preheated organic waste flows into one hydrothermal carbonization reactor 220a and is (initially) heated by receiving thermal energy (in the form of steam) from an external heat source.

[0103] 7, if no particular abnormality occurs in the hydrothermal carbonization reactor 220a, the hydrothermal carbonization reactor 220a is separated in the pressure reduction tank 230 under the control of a control unit (not shown), and the remaining gas components other than the amount sufficient to preheat the organic waste in the preheating tank 210 are discharged to the steam purification tank 240, and all remaining products are discharged to the pressure reduction tank 230. If the internal pressure of the hydrothermal carbonization reactor 220a exceeds a preset reference value, the hydrothermal carbonization reactor 220a discharges the gas components to the steam purification tank 240 and all remaining products to the pressure reduction tank 230 until the internal pressure drops below the preset reference value.

[0104] Referring to FIG. 8, organic waste flows into the preheating tank 210 and is preheated by the gas component returned from the decompression tank 230, and the preheated organic waste flows into the hydrothermal carbonization reactor 220c.

[0105] 9, the liquid component separated in the steam purification tank 240 flows into the reduced pressure tank 230, and the gas component flows into the hydrothermal carbonization reactor 220c. At the same time, thermal energy (in the form of steam) is applied from an external heat source, causing the temperature of the hydrothermal carbonization reactor 220c to rise.

[0106] When gas components and thermal energy are applied to the hydrothermal carbonization reactor 220c, the gas components are applied first, followed by the application of energy from the external heat source. The external heat source that applies thermal energy to the hydrothermal carbonization reactor has a relatively high pressure. On the other hand, the steam purification tank 240 has a relatively low pressure. Therefore, if both are applied to the hydrothermal carbonization reactor 220c simultaneously, the pressure difference can cause a problem in which the gas components cannot be completely applied to the hydrothermal carbonization reactor 220c in the steam purification tank 240. Furthermore, there is a possibility that the thermal energy (steam) applied to the hydrothermal carbonization reactor 220c from the outside may be discharged toward the steam purification tank 240. To prevent this, the gas components are applied to the hydrothermal carbonization reactor 220c first from the steam purification tank 240, and then the thermal energy (steam) from the external heat source is applied to the hydrothermal carbonization reactor 220c. This allows for the complete addition of all components to the hydrothermal carbonization reactor.

[0107] Referring to FIG. 10, the decompression tank 230, under the control of a control unit (not shown), transfers the hydrothermal carbonization products other than the separated gaseous components to the heat exchanger 250, and returns the separated gaseous components to the preheating tank 210 to provide the thermal energy required for preheating.

[0108] As the gas components separated in the steam purification tank 240 flow into the hydrothermal carbonization reactor 220c, the amount of heat energy applied from the external heat source is reduced by the amount of the gas components. In this way, the hydrothermal carbonization reaction proceeds in the heated hydrothermal carbonization reactor 220c, and the processes of Figures 7 to 10 are repeated again to complete the treatment.

[0109] FIG. 11 is a diagram showing a hydrothermal carbonization apparatus according to another embodiment of the present invention.

[0110] Referring to FIG. 11, a hydrothermal carbonization apparatus 160 according to another embodiment of the present invention may further include an ejector 1110 in addition to the configuration of the hydrothermal carbonization apparatus 160 according to an embodiment of the present invention.

[0111] The ejector 1110 is provided on a thermal energy supply path that supplies thermal energy (in the form of steam) to a specific hydrothermal carbonization reactor 220 from the steam purification tank 240 and an external heat source to raise the temperature of the hydrothermal carbonization reactor 220.

[0112] The ejector 1110 simultaneously injects the gas components separated in the steam purification vessel 240 and the thermal energy applied from the external heat source into a specific hydrothermal carbonization reactor 220 regardless of the pressure difference.

[0113] As described above, the external heat source has a relatively very high pressure, while the steam purification tank 240 has a relatively very low pressure. Therefore, when both are simultaneously applied to the hydrothermal carbonization reactor 220, the pressure difference may prevent all gas components from the steam purification tank 240 from being applied to the hydrothermal carbonization reactor 220. In fact, a problem may occur in which the thermal energy applied from the external heat source is discharged to the steam purification tank 240.

[0114] To prevent such problems, the ejector 1110 is disposed at the point where the path for applying thermal energy from an external heat source and the path for applying gas components from the steam purification tank 240 to the reactor 220 join together.

[0115] The ejector 1110 receives the steam and gas components provided to each path, allowing each component to be applied to the hydrothermal carbonization reactor 220 regardless of the pressure difference. Furthermore, the ejector 1110 allows the gas components discharged from the steam purification tank 240 along with the steam injected from the external heat source to be applied to the hydrothermal carbonization reactor 220 due to the pressure of the steam. Therefore, the ejector 1110 not only prevents the gas components from the hydrothermal carbonization reactor 220 from being discharged to the steam purification tank 240, but also increases the discharge rate of the gas components from the steam purification tank 240.

[0116] When the ejector 1110 is included, the operation of the hydrothermal carbonization apparatus 160 in FIG. 9 described above is as follows.

[0117] The liquid component separated in the steam purification tank 240 flows into the reduced pressure tank 230, and the gas component flows into the hydrothermal carbonization reactor 220c. At the same time, steam is applied from an external heat source, and the temperature of the hydrothermal carbonization reactor 220c increases.

[0118] Since the ejector 1110 is located at the confluence of the supply path of the external heat source and the gas component supply path of the steam purification tank 240, the gas components and the steam supplied from the outside can be injected into the hydrothermal carbonization reactor 220c as soon as they are generated, regardless of the order. In addition, the ejector 1110 allows the gas components to be supplied to the hydrothermal carbonization reactor 220c more quickly, increasing the temperature rise rate of the reactor.

[0119] FIG. 12 is a diagram showing the configuration of a digestion lysate treatment apparatus according to one embodiment of the present invention.

[0120] Referring to FIG. 12, the digestion supernatant treatment device 180 includes a flow rate adjustment tank 1210 , a partial nitritation reaction tank 1220 , an AOB granule production tank 1230 , an intermediate storage tank 1240 , and an anammox reaction tank 1250 .

[0121] The flow rate adjustment tank 1210 receives the digested supernatant liquid discharged from the dehydrator 140 and stores it therein until it is introduced into the partial nitritation reaction tank 1220 .

[0122] The partial nitritation reaction tank 1220 receives the digested supernatant from the flow rate adjustment tank 1210 and oxidizes a portion (approximately half) of the ammonia nitrogen contained in the supernatant to nitrite nitrogen using ammonium oxidation bacteria (AOB) granules (hereinafter referred to as "AOB granules"). The partial nitritation reaction tank 1220 receives the AOB granules produced by the AOB granule production tank 1230 from the AOB granule production tank 1230. The partial nitritation reaction tank 1220 uses the inflowing AOB granules to oxidize a portion of the ammonia nitrogen in the supernatant to nitrite nitrogen. The partial nitritation reaction tank 1220 continues the partial nitritation reaction until the ratio of ammonia nitrogen to nitrite nitrogen reaches 1:1.32. In the partial nitritation reaction tank 1220, the AOB granules predominate and nitritation is carried out. After the partial nitritation reaction has progressed in the partial nitritation reaction tank 1220, AOB granules are precipitated, and the treated water (supernatant) other than the AOB granules is discharged to the intermediate storage tank 1240, while sludge that does not settle well is returned to the AOB granule production tank 1230. By using AOB granules, the partial nitritation reaction tank 1220 can ensure improved treatment efficiency and shorten the settling time.

[0123] The AOB granule production tank 1230 receives poorly sedimenting sludge from the partial nitritation reaction tank 1220, produces AOB granules, and supplies them back to the partial nitritation reaction tank 1220. By repeating this process, the partial nitritation reaction tank 1220 can maintain granules and perform stable partial nitritation.

[0124] The AOB granule production tank 1230 can use, but is not limited to, an airlift type reactor (not shown) in order to effectively produce granules.

[0125] The intermediate storage tank 1240 receives treated water from the partial nitritation reaction tank 1220 and temporarily stores it therein before it is supplied to the anammox reaction tank 1250 .

[0126] The intermediate storage tank 1240 stores the treated water discharged from the partial nitritation reaction tank 1220 and supplies the treated water that has been nitritated to correspond to the flow to the downstream anammox reaction tank 1250, which is operated in a continuous flow mode.

[0127] Sludge can be formed by the precipitation of solids in the treated water stored in the intermediate storage tank 1240. The sludge formed in the intermediate storage tank 1240 is collected again in the second storage tank 130.

[0128] The anammox reactor 1250 receives the partially nitritized treated water from the intermediate storage tank 1240 to remove nitrogen, and the treated water is treated in conjunction with a sewage and wastewater treatment facility.

[0129] The Anammox reactor 1250 contains Anaerobic Ammonium Oxidizing Bacteria (AnAOB), which use nitrite as an electron acceptor to convert ammonia in the treated water into nitrogen gas, thereby removing nitrogen. The related chemical formula is as follows:

[0130] 1.0NH4 + +1.32NO2 - +0.066HCO3 - +0.13H + →1.02N2+0.26NO3 - +0.066CH2O 0.5 N 0.15 +2.03H2O

[0131] The anammox reactor 1250 may be, but is not limited to, a completely mixed fluidized bed deposition reactor (not shown).

[0132] The above description merely illustrates the technical concept of the present embodiment, and various modifications and variations may be made by a person skilled in the art without departing from the essential characteristics of the present embodiment. Therefore, the present embodiment is intended to illustrate, not limit, the technical concept of the present embodiment, and the scope of the technical concept of the present embodiment is not limited by such an embodiment. The scope of protection of the present embodiment should be interpreted according to the following claims, and all technical concepts within the scope equivalent thereto should be interpreted as being included in the scope of the present embodiment.

[0133] CROSS-REFERENCE TO RELATED APPLICATION *This patent application claims priority under 35 U.S.C. § 119(a) to patent application serial number 10-2022-0101222, filed in Korea on August 12, 2022, the entire contents of which are incorporated herein by reference. This patent application also claims priority to countries other than the United States for the same reasons as above, the entire contents of which are incorporated herein by reference.

Claims

1. a storage tank into which organic waste is introduced and stored; an anaerobic digestion tank into which the organic waste from the storage tank is introduced to digest the organic matter and generate biogas; a dehydrator that performs primary dehydration of the organic waste discharged from the anaerobic digestion tank; a hydrothermal carbonization device into which the dehydrated organic waste is introduced and hydrothermally carbonized; a filter press for secondary dehydration of the hydrothermal carbonization product discharged from the hydrothermal carbonization apparatus; A system for reducing organic waste and increasing biogas production, which is combined with a hydrothermal carbonization device, comprising:

2. The hydrothermal carbonization apparatus is a preheating tank into which the organic waste discharged from the dehydrator is introduced and preheated; a plurality of hydrothermal carbonization reactors to which the preheated organic waste from the preheating tank is applied and hydrothermal carbonization is performed in a predetermined environment; a pressure-reducing tank into which all of the products hydrothermally carbonized in each hydrothermal carbonization reactor, excluding some of the gaseous components, are introduced, the gaseous components are separated from the non-gaseous components, and the gaseous components are discharged into the preheating tank and the remaining products are discharged; a steam purification tank into which a portion of the gas component of the product hydrothermally carbonized in any one of the hydrothermal carbonization reactors is introduced, which separates the gas component from the liquid component, and which discharges the gas component to the other hydrothermal carbonization reactor and the liquid component to the reduced pressure tank; a heat exchanger into which the hydrothermal carbonization product discharged from the decompression tank is introduced, cooled to a predetermined temperature, and then supplied to the filter press; The system for reducing organic waste and increasing biogas production combined with the hydrothermal carbonization device of claim 1, further comprising a control unit for controlling the operation of each component within the hydrothermal carbonization device.

3. The system for reducing organic waste and increasing biogas production combined with a hydrothermal carbonization device as described in claim 2, characterized in that each hydrothermal carbonization reactor hydrothermally carbonizes organic waste through the same process and performs different operations at different times.

4. The control unit A system for reducing organic waste and increasing biogas production combined with a hydrothermal carbonization device as described in claim 3, characterized in that when the pressure due to gas components in any one of the hydrothermal carbonization reactors is equal to or greater than a predetermined reference value, a portion of the gas components is controlled to be discharged to the steam purification tank.

5. The preset environment is: The system for reducing organic waste and increasing biogas production combined with the hydrothermal carbonization device according to claim 4, characterized in that it has a pressure of 5 to 64 bar and a temperature of 150 to 280°C.

6. The hydrothermal carbonization apparatus is The organic waste reduction and biogas production system combined with a hydrothermal carbonization device according to claim 2, further comprising an ejector that injects steam flowing in from the outside and gas components separated and discharged in the steam purification tank into any one of the hydrothermal carbonization reactors.

7. The heat exchanger comprises: The system for reducing organic waste and increasing biogas production combined with a hydrothermal carbonization device as described in claim 2, characterized in that the heated cooling water generated by cooling the hydrothermal carbonization product is combined with a boiler that supplies steam to the hydrothermal carbonization device or with the feed water of a boiler that heats the anaerobic digestion tank, thereby reducing energy consumption.

8. The filter press is The system for reducing organic waste and increasing biogas production combined with a hydrothermal carbonization device as described in claim 1, characterized in that the supernatant discharged during dehydration of the hydrothermal carbonization product is discharged into the storage tank and used for anaerobic digestion.

9. The organic waste reduction and biogas production system combined with a hydrothermal carbonization device according to claim 1, wherein the organic waste is selected from the group consisting of concentrated sludge generated in a sewage treatment device, pretreated food waste, food wastewater, livestock manure, and a mixture of any one or more of these.

10. The organic waste reduction and biogas production system includes:

2. The system for reducing organic waste and increasing biogas production combined with a hydrothermal carbonization device according to claim 1, further comprising a digestion supernatant treatment device for removing nitrogen components from the supernatant discharged from the dehydrator.

11. The digestion supernatant treatment device comprises: a partial nitritation reaction tank into which the digestion supernatant is introduced and which performs partial nitritation; an AOB granule production tank into which sludge with reduced settling property present in the partial nitritation reaction tank is introduced to produce ammonium oxidizing bacteria (AOB) granules; an intermediate storage tank into which treated water from the partial nitritation reaction tank flows and is stored while solids are precipitated and removed from the treated water; and an Anammox reaction tank that receives treated water from the intermediate storage tank and removes nitrogen components through an anaerobic ammonium oxidation (Anammox) reaction.

11. The system for reducing organic waste and increasing biogas production combined with a hydrothermal carbonization device according to claim 10.

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