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

Background Art

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

[0003] Due to institutional reforms such as the prohibition of direct landfill and ocean dumping of organic waste, there has been a rapid increase in interest in reducing, recycling organic waste, and producing biogas using organic waste.

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

[0005] However, the digestate after anaerobic digestion still contains biomass generated in the anaerobic digester, and such biomass has limitations in weight reduction using mechanical dehydration by internal water in cells, interstitial water between cells, etc.

[0006] Regarding such sludge weight reduction, recently, attention has been paid to applying additional reduction treatments to process the biomass generated in the digester. In particular, the application of hydrothermal carbonization using high temperature and high pressure has been expanding. However, since high-temperature heat energy is used, attempts are being made to maximize its usability while conserving energy and to complement operational problems that may occur due to high pressure.

Summary of the Invention

Problems 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 can reduce the amount of sludge generated and lower the final treatment costs of organic waste by linking a hydrothermal carbonization device with improved energy consumption efficiency downstream of an anaerobic digester.

[0008] One objective 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 eluate generated from anaerobic digestion sludge through a hydrothermal carbonization reaction and dehydration process by a filter press to an anaerobic digester.

[0009] One embodiment of the present invention is an organic waste reduction system that improves the energy consumption efficiency of a hydrothermal carbonization apparatus, and aims to provide an organic waste reduction and biogas production increase system that reduces the energy consumption of the system by reusing thermal energy within the system.

[0010] Furthermore, one objective of one embodiment of the present invention is to provide an organic waste reduction and biogas production increase system that can reduce the impact load placed on the processing system through which the digested and detached liquid is connected. [Means for solving the problem]

[0011] According to one aspect of the present invention, a system for reducing organic waste and increasing biogas production is provided, which is a hydrothermal carbonization apparatus that includes a storage tank for receiving and storing organic waste, an anaerobic digester for receiving the organic waste from the storage tank, digesting the organic matter and generating biogas, a dewatering machine for primary dewatering the organic waste discharged from the anaerobic digester, a hydrothermal carbonization apparatus for receiving the dewatered organic waste and hydrothermally carbonizing it, and a filter press for secondary dewatering the hydrothermal carbonization product discharged from the hydrothermal carbonization apparatus.

[0012] According to one aspect of the present invention, the hydrothermal carbonization apparatus includes a preheating tank into which organic waste discharged from the dewatering machine is introduced and preheated; a plurality of hydrothermal carbonization reactors to which the preheated organic waste from the preheating tank is applied and hydrothermally carbonized in a preset environment; a vacuum tank into which all of the hydrothermally carbonized products from each hydrothermal carbonization reactor are introduced, except for a portion of the gaseous component, to separate the gaseous component from the non-gas component, and to which the gaseous component is discharged to the preheating tank and the remaining products are discharged; a steam purification tank into which a portion of the gaseous component from the hydrothermally carbonized products from any one of the hydrothermal carbonization reactors is introduced, to which the gaseous component is separated from the liquid component, and to which the gaseous component is discharged to the other hydrothermal carbonization reactor and the liquid component is discharged to the vacuum tank; a heat exchanger into which the hydrothermal carbonization products discharged from the vacuum tank are introduced, cooled to a preset temperature, and then supplied to the filter press; and a control unit that controls the operation of each component in the hydrothermal carbonization apparatus.

[0013] According to one aspect of the present invention, each hydrothermal carbonization reactor hydrothermally carbonizes organic waste through the same process, and then 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 gaseous components in any one of the hydrothermal carbonization reactors exceeds a preset reference value, it controls the discharge of a portion of the gaseous components to the steam purification tank.

[0015] According to one aspect of the present invention, the preset environment is characterized by having 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 gaseous components separated and discharged in the steam purification tank into one of the hydrothermal carbonization reactors.

[0017] According to one aspect of the present invention, the heat exchanger is characterized in that it reduces energy consumption by combining the heated cooling water generated by cooling the hydrothermally carbonized product with the boiler that supplies steam to the hydrothermally carbonized apparatus, or by combining it with the feedwater for the boiler that heats the anaerobic digester.

[0018] According to one aspect of the present invention, the filter press is characterized in that it discharges the eluate produced during the dehydration of the hydrothermal carbonization product into the storage tank for use in anaerobic digestion.

[0019] According to one aspect of the present invention, the organic waste is selected from the group consisting of concentrated sludge generated in a lower wastewater treatment device, food waste, food wastewater, livestock manure sludge, and a mixture of one or more of these.

[0020] According to one aspect of the present invention, the organic waste reduction and biogas production increase system further includes a digestion desorbed liquid treatment device, characterized in that it removes nitrogen components from the desorbed liquid discharged from the dewatering machine.

[0021] According to one aspect of the present invention, the digestion detachment treatment apparatus is characterized by comprising: a partial nitrite reaction tank into which the digestion detachment is introduced and partial nitrite is performed; an AOB granule generation tank into which sludge with reduced settling properties present in the partial nitrite reaction tank is introduced and ammonium oxidizing bacteria (AOB) granules are produced; an intermediate storage tank into which the treated water from the partial nitrite reaction tank is introduced and stored, while solid matter is precipitated and removed from the treated water; and an Anammox reaction tank that receives the treated water from the intermediate storage tank and removes nitrogen components by an anaerobic ammonium oxidation (Anammox) reaction. [Effects of the Invention]

[0022] As described above, according to one aspect of the present invention, by solubilizing digested sludge that has undergone anaerobic digestion by hydrothermal treatment and dehydrating it with a filter press, there is an advantage in that the energy consumption for subsequent drying or the treatment cost for final disposal can be reduced.

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

[0024] Also, according to one aspect of the present invention, there is an advantage in that the shock load imposed on the treatment system with which the digestion desorption liquid is associated can be reduced.

Brief Description of the Drawings

[0025] [Figure 1] It is a diagram showing a process diagram of a system for reducing organic waste and increasing biogas production, to which a hydrothermal carbonization apparatus according to an embodiment of the present invention is coupled. [Figure 2] It is a diagram showing the configuration of a hydrothermal carbonization apparatus according to an embodiment of the present invention. [Figure 3] It is a diagram showing the operation sequence of a hydrothermal carbonization reactor according to an embodiment of the present invention. [Figure 4] It is a diagram showing the operation sequence of each hydrothermal carbonization reactor according to an embodiment of the present invention. [Figure 5] It is a diagram showing the operation sequence of a hydrothermal carbonization apparatus according to an embodiment of the present invention. [Figure 6] It is a diagram showing the operation sequence of a hydrothermal carbonization apparatus according to an embodiment of the present invention. [Figure 7] It is a diagram showing the operation sequence of a hydrothermal carbonization apparatus according to an embodiment of the present invention. [Figure 8] It is a diagram showing the operation sequence of a hydrothermal carbonization apparatus according to an embodiment of the present invention. [Figure 9] It is a diagram showing the operation sequence of a hydrothermal carbonization apparatus according to an embodiment of the present invention. [Figure 10]This figure shows the operation sequence of a hydrothermal carbonization apparatus according to one embodiment of the present invention. [Figure 11] This figure shows the configuration of a hydrothermal carbonization apparatus according to another embodiment of the present invention. [Figure 12] This figure shows the configuration of a digestion and desorption liquid processing device according to one embodiment of the present invention. [Modes for carrying out the invention]

[0026] While the present invention can be modified in various ways and have many embodiments, specific embodiments are illustrated and described in detail in the drawings. However, it should be understood that this does not intend to limit the present invention to specific embodiments, but rather includes all modifications, equivalents, or substitutions that fall within the spirit and technical scope of the invention. Similar reference numerals have been used for similar components in the illustration of each drawing.

[0027] Terms such as First, Second, A, B, etc., can be used to describe a variety of components, but the components should not be limited by such terms. The terms are used solely for the purpose of distinguishing one component from another. For example, the First component may be named the Second component, and similarly, the Second component may be named the First component, without departing from the scope of the invention. The terms and / or include combinations of multiple related descriptions or any one of multiple related descriptions.

[0028] When it is mentioned that one component is “linked” or “connected” to another component, it must be understood that it is directly linked to the other component, or may be connected, but other components may exist in between. Conversely, when it is mentioned that one component is “directly linked” or “directly connected” to another component, it must be understood that there are no other components in between.

[0029] The terms used in this application are used solely to describe specific embodiments and are not intended to limit the invention. Singular expressions include plural expressions unless the context clearly indicates otherwise. It should be understood that in this application, terms such as “includes” or “having” do not preemptively exclude the possibility of the presence or addition of features, figures, stages, actions, components, parts, or combinations thereof as described in the specification.

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

[0031] Terms as defined in commonly used dictionaries should be interpreted to have meanings consistent with their meanings in the context of the relevant technology, and not in an ideal or overly formal sense unless explicitly defined in this application.

[0032] Furthermore, the various configurations, processes, steps, or methods included in each embodiment of the present invention can be shared to the extent that they are not technically contradictory.

[0033] Figure 1 shows a system for reducing organic waste and increasing biogas production, which incorporates 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 increase system 100 (hereinafter abbreviated as "system 100") that incorporates a hydrothermal carbonization device according to one embodiment of the present invention includes a first storage tank 110, an anaerobic digester 120, a second storage tank 130, a dewaterer 140, a cake storage tank 150, a hydrothermal carbonization device 160, a filter press 170, and a digestion eluent treatment device 180.

[0035] The first storage tank 110 receives organic waste brought in from outside and desorbed liquid discharged from the filter press 170, and stores them until they are transferred to the anaerobic digester 120.

[0036] On the other hand, organic waste brought in from outside can be selected from the group consisting of concentrated sludge generated in the lower wastewater treatment system, pre-treated food waste, food wastewater and livestock manure, and mixtures thereof. Such organic waste may undergo further pre-treatment before flowing into the first storage tank 110 for effective anaerobic digestion in the subsequent stage.

[0037] For example, sludge generated in the lower wastewater treatment system can be transported to the first storage tank 110 after being concentrated through a concentrator to a total solids concentration (TS) of approximately 4-5%. Food waste can be transported to the first storage tank 110 after being crushed, separated by specific gravity, and finely crushed to remove indigestible components and then crushed to an appropriate size for digestion. In the case of livestock manure sludge, it can be transported to the first storage tank 110 after the removal of impurities. Furthermore, when two or more types of organic waste are mixed and treated, each type of waste can be pretreated individually before being mixed in the first storage tank 110, but the pretreatment method for organic waste is not limited to this.

[0038] The anaerobic digester 120 receives the organic waste from the first storage tank 110 and the waste mixed with the liquid eluent from the filter press 170, and digests it. In this way, the anaerobic digester 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 through the action of anaerobic microorganisms, decomposing organic matter. The biogas generated in the anaerobic digester 120 is used to produce electricity or reused as thermal energy after passing through a biogas purification facility. The digested sludge generated in the anaerobic digester 120 is discharged into the second storage tank 130.

[0040] The second storage tank 130 receives the digested sludge generated in the anaerobic digester 120 and temporarily stores it until it is dewatered in the dewatering machine 140. The second storage tank 130 can also receive excess sludge discharged from the subsequent digested sludge treatment device 180 and store it until it is discharged together with the digested sludge to the dewatering machine 140.

[0041] The dewatering machine 140 receives the mixture of digested sludge and excess sludge from the second storage tank 130 and removes the water in the first stage. The dewatering machine 140 separates the sludge mixture into a dewatered cake and a detached liquid, discharging the cake to the cake storage tank 150 and the detached liquid to the digested detached liquid treatment device 180.

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

[0043] Furthermore, the leached liquid is discharged from the dewatering machine 140 to the digested leached liquid processing device 180, which will be described later. The digested leached liquid processing device 180 then performs post-processing to remove nitrogen components from the leached liquid.

[0044] The cake storage tank 150 receives organic waste that has been dewatered in the dewatering machine 140 and temporarily stores it until it is transported to the hydrothermal carbonization unit 160.

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

[0046] Hydrothermal carbonization is a closed-system reactor where an external heat source raises the reactor temperature, causing some of the organic matter in the solid material to decompose in hot water between 150 and 280°C, allowing the carbonization reaction to proceed without water evaporation. This process induces decarboxylation and dehydration reactions, leading to carbon fixation, which increases the energy density of the solid fuel, and also improves dehydration through hydrophobicity.

[0047] The hydrothermal carbonization apparatus 160 improves the dewatering of organic waste by breaking down the cell walls of the waste and draining internal water under preset temperatures and pressures, thereby breaking down high molecular weight substances into low molecular weight substances. Therefore, the hydrothermal carbonization treatment of organic waste further improves the water removal rate in the subsequent filter press 170.

[0048] The specific configuration and operating sequence of the hydrothermal carbonization apparatus 160 will be described later with reference to Figures 2-11.

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

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

[0051] The filter press 170 performs dewatering using a pressure filtration and compression method, and has the advantages of being easy to install in a small area and achieving a lower moisture content compared to general mechanical dewatering machines.

[0052] The filter press 170 operates in batch mode, following the sequence of inputting the material, primary solid-liquid separation by pressurized filtration, dewatering by high-pressure squeegeeing, and removal of the separated cake. At this time, a separate storage tank (not shown) may be included between the hydrothermal carbonization apparatus 160 and the filter press 170 to input 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 machines. Generally, when dewatering sludge (with a moisture content of around 80%) that has been primarily dewatered using only a filter press, the moisture content of the discharged dewatered cake remains at around 55-65%.

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

[0055] As mentioned above, in system 100, anaerobic digestion sludge undergoes hydrothermal carbonization, converting high molecular weight organic substances into low molecular weight organic substances, while simultaneously improving the dewatering and biodegradability of the waste. Therefore, the eluate discharged during the solid-liquid separation process of the filter press 170 contains a large amount of biodegradable dissolved organic substances.

[0056] This eluate is returned to the first storage tank 110 and used again for digestion in the anaerobic digester 120. Digestion increases the biogas production of the anaerobic digester 120 by more than 20% compared to when the eluate is not returned.

[0057] The digestion sludge treatment device 180 receives the sludge obtained by the dewatering machine 140 from the mixed sludge such as digestion sludge, removes nitrogen components from the sludge, and discharges treated water. The treated water discharged from the digestion sludge treatment device 180 can be further processed in a later stage or treated in conjunction with other water treatment devices such as a lower wastewater treatment device.

[0058] As mentioned above, system 100 recovers the eluate from the filter press 170 and converts it into biogas in the anaerobic digester 120. Therefore, the eluate generated in the dewatering machine 130 downstream of the anaerobic digester 120 contains low concentrations of organic matter and high concentrations of nitrogen components.

[0059] The nitrogen component in the eluent can affect the treated water quality of the lower wastewater treatment system if the eluent is treated in conjunction with the lower wastewater treatment system, and direct discharge is not easy. Therefore, the digested eluent treatment system 180 removes nitrogen from the eluent and returns the treated water to the lower wastewater treatment system or discharges it.

[0060] Furthermore, the digestion sludge treatment device 180 discharges excess sludge during the nitrogen treatment of the sludge, but the excess sludge from the digestion sludge treatment device 180 is recovered again in the second storage tank 130 and reprocessed in the dewatering machine 140 and the hydrothermal carbonization device 160.

[0061] The specific configuration of the digestion and desorption fluid processing device 180 will be described later in Figure 12.

[0062] As described above, by sequentially arranging a hydrothermal carbonizer 160 and a filter press 170 downstream of the anaerobic digester 120, the system 100 can reduce the moisture content of the dewatered cake discharged from the system 100 to 45% or less (35-45%).

[0063] Typically, the moisture content of the primary dewatered sludge discharged in the lower wastewater treatment process is 80% or more, and a large amount of thermal energy is consumed to reduce the moisture content of the sludge to 10% or less using only a dryer. However, since system 100 produces a dewatered cake with a moisture content of 45% or less, the amount of thermal energy consumed to dry the dewatered cake can be significantly reduced.

[0064] Furthermore, since system 100 returns the eluate discharged from the filter press 170 to the anaerobic digester 120 and uses it as an additional organic matter source for biogas production, the amount of biogas generated in the anaerobic digester 120 can be increased by more than 20% compared to when anaerobic digestion is performed alone.

[0065] In other words, system 100 can improve the biogas production of the anaerobic digester 120 compared to a general anaerobic digestion system (anaerobic digestion alone) by destroying biologically recalcitrant substances in the hydrothermal carbonization device 160 and returning the organic substances, whose biodegradability has improved, back to the preceding anaerobic digester 120.

[0066] Furthermore, the system 100 further includes a digestion eluent treatment device 180, which treats the eluent containing high concentrations of nitrogen components generated after passing through the anaerobic digester 120, thereby minimizing the impact on the treated water quality of the downstream wastewater treatment device to which the eluent is treated in conjunction.

[0067] Figure 2 shows the configuration of a hydrothermal carbonization apparatus 160 according to one embodiment of the present invention.

[0068] Referring to Figure 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 reduced pressure tank 230, a steam purification tank 240, a heat exchanger 250, and a control unit (not shown).

[0069] The preheating tank 210 is preheated by receiving the organic waste to be processed 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 high pressure conditions. Therefore, a relatively large amount of thermal energy must be consumed, but to prevent this, the preheating tank 210 is placed before the hydrothermal carbonization reactor 220 in the processing process to preheat the organic waste to be carbonized.

[0070] The preheating tank 210 does not receive thermal energy (mainly in the form of steam) from another heat source, but rather receives gaseous components separated in the depressurized tank 230, which will be described later. The gaseous components separated in the depressurized tank 230 have a constant temperature. Rather than being discharged (vented) to the outside, the gaseous components separated in the depressurized tank 230 are returned to the preheating tank 210 and used for preheating. As a result, the preheating tank 210 can preheat the incoming organic waste using the gaseous components separated in the depressurized tank 230 without needing to receive thermal energy from another heat source, thereby minimizing energy consumption.

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

[0072] The hydrothermal carbonization reactor 220 is subjected to hydrothermal carbonization of organic waste that has been preheated from the preheating tank 210. By hydrothermally carbonizing the organic waste, the hydrothermal carbonization reactor 220 enables the organic waste to be smoothly dewatered by the filter press 170 and then disposed of in its final form (drying or outsourced treatment).

[0073] The hydrothermal carbonization reactor 220 operates as shown in Figure 3.

[0074] Figure 3 shows the operation sequence of a hydrothermal carbonization reactor 220 according to one embodiment of the present invention.

[0075] Referring to Figure 3, first, preheated organic waste is introduced into the hydrothermal carbonization reactor 220. Once the organic waste is introduced, a pre-set environment must be created in the hydrothermal carbonization reactor 220 so that the hydrothermal carbonization reaction can occur. The pre-set environment may be a pressure of 5 to 64 bar, more specifically around 10 to 40 bar, and a temperature of 150 to 280°C, more specifically 180 to 250°C to improve the decomposition of the organic waste. At this time, thermal energy (steam) is applied from an external heat source so that the hydrothermal carbonization reactor 220 can maintain the pre-set temperature environment. Once the pre-set environment is established, in particular, when sufficient heating occurs and the temperature conditions are met, the hydrothermal carbonization reaction occurs in the hydrothermal carbonization reactor 220. The hydrothermal carbonization reaction proceeds for a pre-set time (for example, several tens of minutes), and after the reaction is complete, some of the gaseous components of the product are discharged to the steam purification tank 240, and all of the remaining components are discharged to the reduced pressure tank 230. The hydrothermal carbonization reactor 220 operates in this manner to hydrothermally carbonize organic waste.

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

[0077] Figure 4 shows the operating sequence of each hydrothermal carbonization reactor according to one embodiment of the present invention.

[0078] Each hydrothermal carbonization reactor 220a to 220d operates as described with reference to Figure 3, with a time difference between them. For example, as shown in Figure 4, when hydrothermal carbonization reactor 220a enters the process of raising the temperature by introducing organic waste from the preheating tank 210, hydrothermal carbonization reactor 220b can finally begin introducing organic waste from the preheating tank 210. Hydrothermal carbonization reactor 220c can begin introducing organic waste from the preheating tank 210 at the same time that hydrothermal carbonization reactor 220a begins hydrothermal carbonization of the organic waste, and hydrothermal carbonization reactor 220d can begin introducing organic waste from the preheating tank 210 at the time when the completed reaction product is being discharged to the outside. When operating in this manner, as described above, the gaseous components (steam) discharged and purified from one of the hydrothermal carbonization reactors 220 can flow into the other hydrothermal carbonization reactor that is being heated, thereby reducing the amount of thermal energy consumed for heating.

[0079] Referring again to Figure 2, the hydrothermal carbonization reactor 220 can obtain a portion of the heat required for the hydrothermal carbonization reaction from the gaseous components produced 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 products from 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, excluding the amount sufficient to preheat the preheating tank 210 (which is separated in the vacuum tank 230 and returned to the preheating tank 210). By performing pressure sensing, the hydrothermal carbonization reactor 220 accurately discharges only the amount necessary for preheating to the steam purification tank 240, enabling the heating of other hydrothermal carbonization reactors. Conventionally, the entire amount was discharged to the vacuum tank 230, and even if all the gaseous components were returned to the preheating tank and used for preheating, more than the amount necessary for preheating was returned, so all remaining gaseous components used for preheating were discharged and discarded.

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

[0082] The reduced pressure tank 230 receives most of the products generated after the hydrothermal carbonization reaction is completed in the hydrothermal carbonization reactor 220, separating the gaseous components from the non-gas hydrothermal carbonization products. Of the products generated in the hydrothermal carbonization reaction, only the non-gas hydrothermal carbonization products (e.g., in slurry form) are dehydrated by the filter press 170, while the gaseous components are unrelated to dehydration. Therefore, the reduced pressure tank 230 separates the gaseous components from the products so that these components can be separated and used for preheating. The reduced pressure tank 230 has a relatively lower pressure than the hydrothermal carbonization reactor 220. The reduced pressure lowers the temperature of the products, so that components with boiling points lower than the temperature in the reduced pressure tank remain in a gaseous state, and components with boiling points higher than the temperature in the reduced pressure tank liquefy into liquid products. In this way, the reduced pressure tank 230 creates a pressure difference with the hydrothermal carbonization reactor 220, converting certain components into non-gas products and the remaining components into a gaseous state. The reduced pressure 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 purifies the liquid component by introducing a portion of the gaseous component discharged from the hydrothermal carbonization reactor 220. Because the hydrothermal carbonization reactor 220 is under relatively high pressure, even if only the gaseous component is discharged from the reactor 220, it will all be generated as a liquid component after discharge, or the liquid component can be discharged together with the gaseous component at high pressure. For this reason, the steam purification tank 240 separates the gaseous and liquid components, transferring the liquid component to the reduced pressure tank 230 and the gaseous component to another hydrothermal carbonization reactor into which the preheated organic waste flows. The separation of the gaseous and liquid components from the product by the steam purification tank 240 is as follows.

[0084] The non-gas components of the products generated in the hydrothermal carbonization reactor 220 correspond to components that have already undergone the hydrothermal carbonization reaction. If such components are introduced back into the hydrothermal carbonization reactor and undergo the reaction again, it would be inefficient and a waste of energy. Furthermore, when organic waste is introduced from the preheating tank 210 to a specific hydrothermal carbonization reactor 220, an appropriate amount is introduced to ensure that the hydrothermal carbonization reaction proceeds smoothly in the hydrothermal carbonization reactor 220. At this time, if non-gas components of the products generated in other hydrothermal carbonization reactors flow into the hydrothermal carbonization reactor, an amount exceeding the appropriate amount will flow into that reactor. This causes an inefficient hydrothermal carbonization reaction and leads to the consumption of more thermal energy than necessary. To prevent such problems, the steam purification tank 240 separates the liquid and gaseous components in the products discharged from the hydrothermal carbonization reactor 220 and transports each to different configurations.

[0085] The steam purification tank 240 can be implemented in any form or structure as long as it can separate the gaseous and liquid components.

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

[0087] The heat exchanger 250 lowers the temperature of the hydrothermal carbonization product by circulating cooling water and exchanging heat with the high-temperature hydrothermal carbonization product. Since the temperature of the hydrothermal carbonization product discharged from the reduced pressure tank 230 is at approximately 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 for the filter press 170, before supplying the hydrothermal carbonization product to the filter press 170.

[0088] On the other hand, the cooling water, which has been heated by heat exchange with the high-temperature hydrothermal carbonization product, can be recovered and used as an external heat source (boiler) to supply thermal energy (steam) to the hydrothermal carbonization reactor 220. In other words, by combining the heated cooling water with the water for the steam generation boiler, the energy consumed for steam generation is reduced.

[0089] Furthermore, the heated cooling water discharged from the heat exchanger 250 may be combined with the feedwater for a boiler (not shown) used to heat the anaerobic digester 120. In this case, the energy consumption of the boiler used to heat the anaerobic digester 120 is reduced. Similarly, the heated cooling water may be recirculated as heat exchange water to maintain a preset operating temperature for the Anammox reaction tank 1250, which will be described later.

[0090] Thus, the thermal energy generated in the hydrothermal carbonization unit 160 can be recovered within the system 100 using various methods. Therefore, by reusing all the thermal energy generated in the hydrothermal carbonization unit 160, the energy consumption efficiency of the system 100 is improved.

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

[0092] A control unit (not shown) controls the transport pump 215 so that organic waste to be processed flows into the preheating tank 210. For this purpose, the preheating tank 210 may include a water level gauge, and the control unit (not shown) controls the system to introduce waste from the cake storage tank 150 into the preheating tank 210 if the water level in the preheating tank 210 is below a preset level, and to interrupt the introduction of waste if the water level is above the preset level.

[0093] A control unit (not shown) can control the vacuum tank 230 to return the gaseous components separated in the vacuum tank 230 to the preheating tank 210 in order to preheat the organic waste.

[0094] A control unit (not shown) controls the transport of organic waste preheated in the preheating tank 210 to a hydrothermal carbonization reactor (e.g., 220a). After transport, the control unit (not shown) introduces steam from an external heat source and gaseous components (steam) separated from the product in another hydrothermal carbonization reactor (e.g., 220c) 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 standard value. If the pressure inside the hydrothermal carbonization reactor 220a is below the preset standard value, it corresponds to a situation where the hydrothermal carbonization reaction is proceeding without any abnormalities. On the other hand, if the pressure inside the hydrothermal carbonization reactor 220a exceeds the preset standard value, it corresponds to a situation where there is an abnormally large amount of gaseous components, or where excessive steam is introduced from the outside, potentially causing abnormalities in the reactor 220. In this case, the control unit (not shown) discharges the gaseous components into the steam purification tank 240 until the pressure falls below the preset standard value. In this way, the control unit (not shown) resolves the abnormality inside the hydrothermal carbonization reactor 220a.

[0096] When the hydrothermal carbonization reaction proceeds for a predetermined 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 of the remaining products to the vacuum tank 230. At this time, when discharging the gaseous components, the control unit (not shown) discharges all but the amount separated in the vacuum tank 230 and sufficient to preheat the organic waste in the preheating tank 210 to the steam purification tank 240. In this way, the remaining gaseous components, other than those necessary for preheating, are not discharged to the outside and can all be used to heat other hydrothermal carbonization reactors, thereby maximizing energy efficiency.

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

[0098] Simultaneously, the remaining hydrothermal carbonization reactors 220b to 220d are controlled in parallel to operate in sequence. The process by which the control unit (not shown) controls the operation of each hydrothermal carbonization reactor will be described later with reference to Figures 5 to 10.

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

[0100] Figures 5-10 show the operation sequence of an organic waste treatment device according to one embodiment of the present invention. Figures 5-10 show in detail the process by which the hydrothermal carbonization device 160 receives and treats organic waste.

[0101] Referring to Figure 5, the control unit (not shown) controls the flow of organic waste into the preheating tank 210 (first) for preheating.

[0102] Referring to Figure 6, the preheated organic waste flows into one hydrothermal carbonization reactor 220a, where it receives thermal energy (in the form of steam) from an external heat source (first) and its temperature rises.

[0103] Referring to Figure 7, if no special abnormality occurs in the hydrothermal carbonization reactor 220a, the hydrothermal carbonization reactor 220a is separated in the vacuum tank 230 by the control unit (not shown), and any remaining gaseous components other than those 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 vacuum tank 230. If the internal pressure of the hydrothermal carbonization reactor 220a exceeds a preset standard value, the hydrothermal carbonization reactor 220a will continue to discharge gaseous components to the steam purification tank 240 and all remaining products to the vacuum tank 230 until the internal pressure drops below the preset standard value.

[0104] Referring to Figure 8, the preheating tank 210 receives organic waste and is preheated by gaseous components returned from the reduced pressure tank 230, and the preheated organic waste flows into the hydrothermal carbonization reactor 220c.

[0105] Referring to Figure 9, the liquid components separated in the steam purification tank 240 flow into the reduced pressure tank 230, and the gaseous components flow into the hydrothermal carbonization reactor 220c. Simultaneously, thermal energy (in the form of steam) is applied from an external heat source, causing the hydrothermal carbonization reactor 220c to heat up.

[0106] At this time, when gaseous components and thermal energy are applied to the hydrothermal carbonization reactor 220c, the gaseous components are applied preferentially, and then energy from an external heat source is applied. The external heat source that applies thermal energy to the hydrothermal carbonization reactor has a relatively very high pressure. On the other hand, the steam purification tank 240 has a relatively very low pressure. As a result, when both are applied to the hydrothermal carbonization reactor 220c simultaneously, a problem arises in which the gaseous components in the steam purification tank 240 cannot be completely applied to the hydrothermal carbonization reactor 220c due to the pressure difference. Moreover, a problem may occur in which the thermal energy (steam) applied to the hydrothermal carbonization reactor 220c from the outside is instead discharged to the steam purification tank 240. To prevent this, gaseous components are preferentially applied to the hydrothermal carbonization reactor 220c from the steam purification tank 240, and then thermal energy (steam) from an external heat source is applied to the hydrothermal carbonization reactor 220c. This allows all components to be completely supplied to the hydrothermal carbonization reactor.

[0107] Referring to Figure 10, the reduced pressure tank 230, under the control of a control unit (not shown), transmits 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, providing the thermal energy necessary for preheating.

[0108] As the gaseous components separated in the steam purification tank 240 flow into the hydrothermal carbonization reactor 220c, the amount of thermal energy applied from the external heat source can be reduced by the amount of gaseous components. In this way, the hydrothermal carbonization reaction proceeds in the heated hydrothermal carbonization reactor 220c, and the process shown in Figures 7-10 is repeated, making the material treatable.

[0109] Figure 11 shows a hydrothermal carbonization apparatus according to another embodiment of the present invention.

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

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

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

[0113] As mentioned above, the external heat source has a relatively very high pressure. On the other hand, the steam purification tank 240 has a relatively very low pressure. As a result, when both are applied to the hydrothermal carbonization reactor 220 simultaneously, the pressure difference may prevent the gaseous components from the steam purification tank 240 from being completely supplied to the hydrothermal carbonization reactor 220, and may even cause the thermal energy supplied from the external heat source to be discharged into the steam purification tank 240.

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

[0115] The ejector 1110 applies steam and gaseous components supplied to each path, ensuring that each component is applied to the hydrothermal carbonization reactor 220 regardless of the pressure difference. Furthermore, the ejector 1110 allows gaseous components discharged from the steam purification tank 240 together with the steam injected from an external heat source to be applied to the hydrothermal carbonization reactor 220. Thus, the ejector 1110 not only prevents gaseous components from being discharged from the hydrothermal carbonization reactor 220 into the steam purification tank 240, but can also improve the discharge rate of gaseous components from the steam purification tank 240.

[0116] When the ejector 1110 is included, the operation of the hydrothermal carbonizer 160 in Figure 9 described above is as follows:

[0117] The liquid components separated in the steam purification tank 240 flow into the reduced pressure tank 230, and the gaseous components flow into the hydrothermal carbonization reactor 220c. Simultaneously, steam is applied from an external heat source, causing the hydrothermal carbonization reactor 220c to heat up.

[0118] Since the ejector 1110 is located at the confluence of the supply path for the external heat source and the supply path for the gaseous components of the steam purification tank 240, the gaseous 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. Furthermore, the ejector 1110 allows the gaseous components to be supplied to the hydrothermal carbonization reactor 220c more rapidly, increasing the heating rate of the reactor.

[0119] Figure 12 shows the configuration of a digestion and desorption liquid processing apparatus according to one embodiment of the present invention.

[0120] Referring to Figure 12, the digestion and desorption treatment apparatus 180 includes a flow rate adjustment tank 1210, a partial nitrite reaction tank 1220, an AOB granule generation tank 1230, an intermediate storage tank 1240, and an anammox reaction tank 1250.

[0121] The flow rate adjustment tank 1210 receives the digested sludge discharged from the dewatering machine 140 and stores it until it is introduced into the partial nitrite reaction tank 1220.

[0122] The partial nitrite reaction tank 1220 receives digestion eluate from the flow rate adjustment tank 1210 and uses ammonium oxidizing bacteria (AOB) granules (hereinafter abbreviated as "AOB granules") to oxidize a portion (about half) of the ammoniacal nitrogen contained in the eluate to nitrite nitrogen. The partial nitrite reaction tank 1220 receives AOB granules produced by the AOB granule generation tank 1230. The partial nitrite reaction tank 1220 uses the incoming AOB granules to oxidize a portion of the ammoniacal nitrogen in the supplied eluate to nitrite nitrogen. The partial nitrite reaction tank 1220 continues the partial nitrite reaction until the ratio of ammoniacal nitrogen to nitrite nitrogen becomes 1:1.32. In the partial nitrite reaction tank 1220, AOB granules become dominant and nitrification takes place. The partial nitrite reaction tank 1220 carries out the partial nitrite reaction, then precipitates the AOB granules. The treated water (supernatant) is discharged to the intermediate storage tank 1240, and any sludge with poor sedimentation properties is returned to the AOB granule generation tank 1230. By using AOB granules, the partial nitrite reaction tank 1220 can ensure improved treatment efficiency and shorten the precipitation time.

[0123] The AOB granule generation tank 1230 receives poorly precipitated sludge from the partial nitrite reaction tank 1220, generates AOB granules, and supplies these granules back to the partial nitrite reaction tank 1220. By repeating this process, the partial nitrite reaction tank 1220 can maintain the granules and perform stable partial nitrification.

[0124] The AOB granule generating tank 1230 may, but is not limited to, use an air-lift type reactor (not shown) to effectively generate granules.

[0125] The intermediate storage tank 1240 receives treated water from the partial nitrite reactor 1220 and temporarily stores it before supplying it to the anammox reactor 1250.

[0126] The intermediate storage tank 1240 stores treated water discharged from the partial nitrification reactor 1220 and supplies nitrified treated water in accordance with the flow of the subsequent continuous-flow anammox reactor 1250.

[0127] Solid matter settles in the treated water stored in the intermediate storage tank 1240, forming sludge. The sludge formed in the intermediate storage tank 1240 is then recovered and transferred to the second storage tank 130.

[0128] The Anammox reaction tank 1250 receives partially nitrified treated water from the intermediate storage tank 1240 to remove nitrogen, and then the treated water is treated in conjunction with the wastewater treatment system.

[0129] The AnamoX 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 - +0.066 HCO3 - +0.13H + →1.02N2+0.26NO3 - +0.066CH2O 0.5 N 0.15 +2.03H2O

[0131] The Anammox reactor 1250 may be carried out in a fully mixed fluid-bed reactor (not shown), but is not limited thereto.

[0132] The above description is merely an example illustrating the technical concept of this embodiment, and a person with ordinary skill in the art to which this embodiment belongs could make various modifications and variations without departing from the essential characteristics of this embodiment. Therefore, this embodiment is for illustrative purposes only, not to limit the technical concept of this embodiment, and the scope of the technical concept of this embodiment is not limited by such an embodiment. The scope of protection of this embodiment should be interpreted in accordance with the following claims, and all technical concepts within an equivalent scope should be interpreted as being included in the scope of rights of this embodiment.

[0133] CROSS-REFERENCE TO RELATED APPLICATION *This patent application claims priority under Section 119(a) of the United States Patent Act (35 U.S.SC § 119(a)) to Patent Application No. 10-2022-0101222 filed in Korea on 12 August 2022, and all its contents are incorporated into this patent application as references. In addition, this patent application also claims priority in countries other than the United States for the same reasons as above, and all its contents are incorporated into this patent application as references.

Claims

1. A storage tank into which organic waste is introduced and stored, An anaerobic digester into which organic waste from the aforementioned storage tank is introduced to digest organic matter and generate biogas, A dewatering machine for primary dewatering of organic waste discharged from the anaerobic digester, A hydrothermal carbonization apparatus into which the dewatered organic waste is introduced and subjected to hydrothermal carbonization, A filter press for secondary dewatering of the hydrothermal carbonization product discharged from the hydrothermal carbonization apparatus, Includes, The aforementioned hydrothermal carbonization apparatus is A preheating tank into which organic waste discharged from the aforementioned dewatering machine is introduced and preheated, Multiple hydrothermal carbonization reactors to which preheated organic waste from the aforementioned preheating tank is applied and hydrothermally carbonized in a predetermined environment, A vacuum tank receives all of the hydrothermally carbonized product from each hydrothermal carbonization reactor, excluding a portion of the gaseous component, to separate the gaseous component from the non-gas component, and discharges the gaseous component to the preheating tank and the remaining product. A steam purification tank is provided, into which a portion of the gaseous component of the product produced by hydrothermal carbonization in one of the hydrothermal carbonization reactors is introduced to separate the gaseous component from the liquid component, and the gaseous component is discharged to another hydrothermal carbonization reactor, and the liquid component is discharged to the vacuum tank. A heat exchanger into which hydrothermal carbonization products discharged from the aforementioned depressurized tank are introduced and cooled to a predetermined temperature before being supplied to the filter press, A control unit that controls the operation of each component within the hydrothermal carbonization apparatus. A system for reducing organic waste and increasing biogas production, characterized by the inclusion of a hydrothermal carbonization device.

2. A system for reducing organic waste and increasing biogas production, comprising hydrothermal carbonization apparatuses according to claim 1, characterized in that each hydrothermal carbonization reactor hydrothermally carbonizes organic waste through the same process, and performs different operations with a time difference between them.

3. The control unit, A system for reducing organic waste and increasing biogas production, which is coupled with a hydrothermal carbonization apparatus according to claim 2, characterized in that if the pressure due to gaseous components in any one of the hydrothermal carbonization reactors exceeds a preset standard value, the system controls the discharge of a portion of the gaseous components to the steam purification tank.

4. The aforementioned pre-configured environment is A system for reducing organic waste and increasing biogas production, which is combined with the hydrothermal carbonization apparatus according to claim 3, characterized by having a pressure of 5 to 64 bar and a temperature of 150 to 280°C.

5. The aforementioned hydrothermal carbonization apparatus is A system for reducing organic waste and increasing biogas production, comprising a hydrothermal carbonization apparatus according to claim 1, further comprising an ejector for injecting steam flowing in from the outside and gaseous components separated and discharged in the steam purification tank into one of the hydrothermal carbonization reactors.

6. The heat exchanger is, The hydrothermal carbonization apparatus described in claim 1 is combined with an organic waste reduction and biogas production system, characterized in that the heated cooling water generated by cooling the hydrothermal carbonized product is combined with a boiler that supplies steam to the hydrothermal carbonization apparatus, or with feedwater for a boiler that heats the anaerobic digester, thereby reducing energy consumption.

7. The aforementioned filter press is A system for reducing organic waste and increasing biogas production, which is combined with the hydrothermal carbonization apparatus according to claim 1, characterized in that the desorbed liquid discharged during the dewatering of the hydrothermal carbonization product is discharged into the storage tank and used for anaerobic digestion.

8. The organic waste reduction and biogas production increase system for hydrothermal carbonization according to claim 1, characterized in that the organic waste is selected from the group consisting of concentrated sludge generated in the lower wastewater treatment device, pre-treated food waste, food wastewater, livestock manure, and mixtures of one or more of these.

9. The aforementioned system for reducing organic waste and increasing biogas production is A system for reducing organic waste and increasing biogas production, further comprising a digestion desorbing liquid treatment device, characterized in that it removes nitrogen components from the desorbing liquid discharged from the dewatering machine, and is combined with the hydrothermal carbonization apparatus according to claim 1.

10. The digestion and desorbed liquid processing apparatus is, A partial nitrite reaction tank into which the liquid discharged from the dewatering machine is introduced and partial nitrite is carried out, An AOB granule production tank is used to generate ammonium oxidizing bacteria (AOB) granules by introducing sludge with reduced settling properties present in the partial nitrite reaction tank, An intermediate storage tank that receives and stores treated water from the partial nitrite reaction tank, while removing solid matter by sedimentation from the treated water, An Anammox reactor receives treated water from the aforementioned intermediate storage tank and removes nitrogen components by an anaerobic ammonium oxidation (Anammox) reaction. A system for reducing organic waste and increasing biogas production, characterized by comprising the hydrothermal carbonization apparatus according to claim 9.

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