Wet garbage hydrothermal resource processing system and method

Abstract

The present invention relates to a wet garbage hydrothermal resource treatment system and method in the field of organic waste treatment technology, comprising a slurry mixing tank, a screw pump, a centrifuge, a liquid storage tank, and a primary treatment subsystem; the primary treatment subsystem comprises a first reactor, a first flash separator, a second reactor, and a heater, the first reactor and the second reactor being connected via the first flash separator, the heater being used to heat the first reactor and the second reactor respectively, the screw pump being used to pump the wet garbage in the slurry mixing tank into the first reactor and the second reactor respectively, the centrifuge receiving the materials in the first reactor and the second reactor and separating them into liquid material and solid material, the liquid material being transported to the liquid storage tank, and the solid material being transported to an external device. The present invention recovers energy by adopting a flash evaporation switching method, thereby improving energy utilization and shortening heating time, thereby solving the problem of high energy consumption existing in the devices of the prior art.

Description

Technical Field

[0001] The present invention relates to the technical field of organic waste treatment, and in particular to a wet garbage hydrothermal resource treatment system and method. Background Art

[0002] At present, the main methods for treating wet garbage are processing into organic fertilizer, landfilling, fermentation to generate biogas, and incineration. Among them, landfilling is difficult to extract, collect and treat pollutants such as leachate and biogas generated by garbage piles, which not only causes serious pollution to the surrounding environment, but also poses a safety hazard and seriously affects the image of the town. Incineration of garbage is prone to produce toxic gases such as dioxins, which pollute the air and produce odors, causing serious impacts on the surrounding environment.

[0003] The technology of treating domestic waste using the hydrothermal method is very suitable for treating this type of urban domestic waste. It is a fast, efficient and environmentally friendly waste treatment technology. The hydrothermal treatment process, also known as hydrothermal oxidation (HTO), is a very effective chemical oxidation technology, especially suitable for the treatment of toxic and organic waste. The hydrothermal method is a method of oxidizing and decomposing dissolved and suspended organic matter or reducing inorganic matter in the waste in the aqueous phase with air or other oxidants under high temperature and high pressure, significantly removing COD (chemical oxygen demand), BOD (biochemical oxygen demand), SS (sulfide), etc. The reaction is carried out in the hot water phase, which is a characteristic of this method.

[0004] During the development of the present invention, the inventors discovered that the prior art suffers from at least the following problems: high energy consumption and insufficient waste reduction. For example, publication number CN108380636A discloses a continuous pilot plant for treating domestic waste using a hydrothermal method. The plant comprises an engine, a raw material tank, a slurry pump, a preheater, an oxidant pump, an oxidant storage tank, a filter, a solid-liquid separator, a cooler, and a reactor, as well as a control and connection mechanism. This plant suffers from high energy consumption and insufficient waste reduction. Summary of the Invention

[0005] In view of the defects in the prior art, the purpose of the present invention is to provide a wet garbage hydrothermal resource treatment system and method.

[0006] According to the present invention, a wet garbage hydrothermal resource processing system includes a slurry mixing tank, a screw pump, a centrifuge, a liquid storage tank and a primary processing subsystem;

[0007] The primary processing subsystem includes a first reactor, a first flash separator, a second reactor, and a heater. The first reactor and the second reactor are connected through the first flash separator. The heater is used to heat the first reactor and the second reactor respectively. The slurry mixing tank is used to store wet garbage after sorting, crushing, pulping, and emulsification. The screw pump is used to pump the wet garbage in the slurry mixing tank into the first reactor and the second reactor respectively. The centrifuge receives the materials in the first reactor and the second reactor and separates the materials into liquid material and solid material. The liquid material is transported to the liquid storage tank, and the solid material is transported to external equipment.

[0008] When the first reactor is heated and pressurized and maintained at a constant temperature and pressure for a predetermined time, the slurry mixing pipe transports the wet garbage to the second reactor through the screw pump, and before the first reactor is unloaded, heat energy is transported to the second reactor through the first flash separator to preheat the wet garbage in the second reactor; when the second reactor is heated and pressurized and maintained at a constant temperature and pressure for a predetermined time, the slurry mixing tank pumps the wet garbage into the first reactor from which the material has been unloaded through the screw pump, and before the second reactor is unloaded, heat energy is transported to the first reactor through the first flash separator to preheat the wet garbage in the second reactor, and the cycle is repeated in sequence.

[0009] In some embodiments, the primary processing subsystem further includes a feed balancing tank, which is in communication with the first flash separator and is used to maintain a pressure and temperature balance between the first reactor and the second reactor.

[0010] In some embodiments, a heat preservation cavity is provided on the outer peripheral surface of the slurry mixing tank, the feed balancing tank is connected to the heat preservation cavity, and the steam in the feed balancing tank is passed into the heat preservation cavity to heat the slurry mixing tank.

[0011] In some embodiments, an oil-water separator is further included. The liquid material in the liquid storage tank enters the oil-water separator and is separated into water and liquid fertilizer. The liquid fertilizer is sent to the next-level processing subsystem.

[0012] In some embodiments, a secondary processing subsystem is further included, which includes a second flash separator, a steam compressor and a heat exchanger. The second flash separator is connected to the oil-water separator and receives the liquid fertilizer. The second flash separator transmits steam to the heat exchanger through the steam compressor. The condensed water discharged from the heat exchanger enters an external water tank. The concentrated liquid fertilizer from the second flash separator and the heat exchanger is discharged to external equipment.

[0013] In some embodiments, the second flash separator is in communication with the heat-insulating chamber, and excess steam in the heat-insulating chamber enters the second flash separator.

[0014] In some embodiments, the secondary treatment subsystem further comprises a third flash separator, wherein an inlet of the third flash separator is in communication with the second flash separator, and an outlet of the third flash separator is in communication with the steam compressor.

[0015] The present invention also provides a method for hydrothermal resource recovery treatment of wet garbage, which uses the wet garbage hydrothermal resource recovery treatment system, including a flash evaporation switching step and a multi-stage distillation step;

[0016] The flash switching step comprises:

[0017] A1, pumping the sorted, crushed, pulped and emulsified wet garbage into the pulp mixing tank through an emulsification pump;

[0018] A2, pumping the wet garbage in the slurry mixing tank into the first reactor through the screw pump;

[0019] A3, starting the heater to heat the first reactor, and simultaneously supplying air into the first reactor through an air compressor to pressurize the first reactor, and maintaining the first reactor at a predetermined temperature and predetermined pressure for a predetermined time;

[0020] A4, while performing step A3, pumping the wet garbage in the slurry mixing tank into the second reactor through the screw pump;

[0021] A5: After the first reactor is maintained at a constant temperature and pressure for a predetermined time, the valves connecting the first flash separator to the first reactor and the second reactor are opened. The heat energy in the first reactor is transferred to the second reactor through flash evaporation in the first flash separator, thereby heating the wet garbage in the second reactor.

[0022] A6, after the temperature and pressure in the first reactor drop to predetermined values, the discharge valve of the first reactor is opened, and the material in the first reactor is conveyed into the centrifuge, where it is separated into liquid material and solid material. The liquid material is conveyed to the liquid storage tank, and the solid material is conveyed to an external device;

[0023] A7, heating the second reactor with the heater and simultaneously supplying air into the second reactor with an air compressor to pressurize the second reactor, wherein the second reactor is maintained at a predetermined temperature and a predetermined pressure for a predetermined time;

[0024] A8, while carrying out step A7, pumping the wet garbage in the slurry mixing tank into the first reactor through the screw pump;

[0025] A9: After the second reactor is maintained at a constant temperature and pressure for a predetermined period of time, the valves connecting the first flash separator to the first reactor and the second reactor are opened. The heat energy in the second reactor is transferred to the first reactor through flash evaporation in the first flash separator, thereby heating the wet garbage in the first reactor.

[0026] A10. After the temperature and pressure in the second reactor drop to predetermined values, the discharge valve of the second reactor is opened. The material in the second reactor is transported to the centrifuge, where it is separated into liquid and solid materials. The liquid material is transported to the liquid storage tank, and the solid material is transported to an external device. A11. Repeat steps A1-A10.

[0027] The multi-stage distillation step comprises:

[0028] B1, transporting the liquid material in the liquid storage tank to an oil-water separator, separating the liquid material into water and liquid fertilizer through the oil-water separator, and transporting the liquid fertilizer to the second flash separator for flash separation;

[0029] B2, flash separation in the second flash separator to form steam and concentrated liquid fertilizer, the steam is fed into the heat exchanger through the steam compressor, and the concentrated liquid fertilizer is discharged from the discharge port of the second flash separator to an external device;

[0030] B3, the heat exchanger converts the steam into condensed water and concentrated liquid fertilizer through heat exchange, the condensed water is discharged into the external water tank, and the concentrated liquid fertilizer is transported to the external equipment.

[0031] In some embodiments, step A5 and / or step A9 further include a temperature and pressure balance step, wherein the temperature and pressure balance step is as follows: the first flash separator and the feed balance tank transmit steam so that the temperature and pressure of the first reactor and the second reactor are balanced during feeding.

[0032] In some embodiments, step B2 further includes a steam redistillation step, and the steam distillation step is as follows: the steam generated in the feed balancing tank is passed into the insulation chamber of the slurry mixing tank to preheat the slurry mixing tank, and then the excess steam is passed through a pipeline into the second flash separator for distillation.

[0033] Compared with the prior art, the present invention has the following beneficial effects:

[0034] 1. The present invention recovers energy by adopting a double-kettle periodic heating and flash evaporation switching method, thereby improving energy utilization and shortening heating time, thereby solving the problem of high energy consumption in the devices in the prior art.

[0035] 2. The present invention provides a feed balance tank, which can not only maintain the pressure and temperature balance of the first reactor and the second reactor while feeding, but also use excess steam to heat the seasoning tank, further improving energy utilization.

[0036] 3. The present invention forms a multi-effect distillation treatment system by setting up a secondary treatment subsystem. The liquid fertilizer produced by the hydrothermal process is treated by the technical process of multi-effect distillation, thereby solving the problems of deoiling and desalting and achieving the effect of reducing the amount of fertilizer. BRIEF DESCRIPTION OF THE DRAWINGS

[0037] Other features, objects and advantages of the present invention will become more apparent upon reading the detailed description of non-limiting embodiments with reference to the following drawings:

[0038] Figure 1 A schematic diagram of a process for implementing the present invention;

[0039] Figure 2 This is a flow chart of another implementation method of an embodiment of the present invention. DETAILED DESCRIPTION

[0040] The present invention will be described in detail below with reference to specific embodiments. The following examples will help those skilled in the art to further understand the present invention, but are not intended to limit the present invention in any form. It should be noted that, for those skilled in the art, several changes and improvements can be made without departing from the scope of the present invention. These all fall within the scope of protection of the present invention.

[0041] Example 1

[0042] This embodiment provides a wet garbage hydrothermal resource processing system, such as Figure 1 As shown, it includes a slurry mixing tank 1, a screw pump 2, a centrifuge 3, a liquid storage tank 4 and a primary treatment subsystem 5, wherein the primary treatment subsystem 5 includes a first reactor 51, a first flash separator 52, a second reactor 53 and a heater 54.

[0043] The slurry mixing tank 1 is used to store wet garbage that has been sorted, crushed, pulped and emulsified. The emulsified wet garbage can be pumped into the slurry mixing tank 1 through an emulsification pump. The inlet of the screw pump 2 is connected to the outlet of the slurry mixing tank 1, and the outlet of the screw pump 2 is connected to the inlet of the first reactor 51 and the inlet of the second reactor 53 through pipelines. The emulsified wet garbage in the slurry mixing tank 1 is pumped into the first reactor 51 and the second reactor 53 respectively by the screw pump 2, and the process of the screw pump 2 pumping the wet garbage in the slurry mixing tank 1 into the first reactor 51 and the second reactor 53 is independent and can be pumped in simultaneously or separately. The first flash separator 52 is connected to the first reactor 51 and the second reactor 53 respectively through pipelines. The heat energy within the first reactor 51 and the second reactor 53 is transferred to each other through the first flash separator 52. That is, the heat energy within the first reactor 51 is transferred to the second reactor 53 through the first flash separator 52, or the heat energy within the second reactor 53 is transferred to the first reactor through the first flash separator 52. The heater 54 can be an electric heating furnace with thermal oil, and is used to heat the first reactor 51 and the second reactor 53, respectively. The centrifuge 3 can be a horizontal spiral centrifuge. The inlet of the centrifuge 3 is connected to the discharge port of the first reactor 51 and the discharge port of the second reactor 53 via pipelines. The outlet of the centrifuge 3 is connected to the liquid storage tank 4 via a pipeline. The liquid material generated by the centrifugal force of the centrifuge 3 is transported to the liquid storage tank 4.

[0044] The working principle of this embodiment is as follows: the emulsified wet garbage is pumped into the slurry mixing tank 1 via an emulsification pump. First, a portion of the wet garbage in the slurry mixing tank 1 is pumped into the first reactor 51 using the screw pump 2. The heater 54 is turned on to heat the first reactor 51. Simultaneously, the first reactor 51 is pressurized using the air compressor. When the first reactor 51 is heated and pressurized to 200°C and 2.0 MPa, the temperature and pressure are stopped and maintained at this temperature and pressure for approximately one hour. While the first reactor 51 is heated and pressurized and maintained at a constant temperature and pressure for a predetermined time, the wet garbage in the slurry mixing tank 1 is pumped into the second reactor 53 using the screw pump 2. After the wet waste in the first reactor 51 completes its reaction at constant temperature and pressure for a predetermined period of time, the valves connecting the first and second reactors 51 and 53 to the first flash separator 52 are opened, transferring the heat energy from the first reactor 51 to the second reactor 53 through the first flash separator 52. At this point, the wet waste in the second reactor 53 has been pumped in, and the wet waste in the second reactor 53 is preheated through the heat transfer. After the temperature in the first reactor 51 drops to 115°C and the pressure reaches room temperature, the discharge valve of the first reactor 51 is opened, and the material in the first reactor 51 is transferred to the centrifuge 3. The centrifugal force of the centrifuge 3 separates the material into liquid and solid materials. The solid material, which is humic acid organic fertilizer, is discharged to external equipment for further processing. The liquid material is discharged through a pipeline into the liquid storage tank 4 for further processing.

[0045] While the first reactor 51 is being discharged, the heater 54 heats the second reactor 53, which is simultaneously pressurized by an air compressor. When the third reactor 53 reaches 200°C and 2 MPa, the temperature and pressure increase ceases and are maintained at this temperature and pressure for approximately one hour. While the third reactor 53 is being heated and pressurized and maintained at this constant temperature and pressure for a predetermined time, the screw pump 2 pumps the emulsified wet waste into the emptied first reactor 51. Once the wet waste in the third reactor 53 has completed its reaction at this constant temperature and pressure for a predetermined time, the valves connecting the first and second reactors 51 and 53 to the first flash separator 52 are opened, transferring the heat energy from the second reactor 53 to the first reactor 51 through the first flash separator 52. At this point, the wet waste in the first reactor 51 has been completely pumped in, and the transferred heat energy preheats the wet waste in the first reactor 51. After the temperature in the third reactor 53 reaches 115°C and the pressure reaches room temperature, the discharge valve of the second reactor 51 is opened and the material in the second reactor is discharged into the centrifuge 3. Similarly, the centrifuge 3 separates the material into liquid material and solid material. The liquid material is discharged into the liquid storage tank 4 through a pipeline, and the solid material is humic acid organic fertilizer, which is discharged into external equipment for separate processing.

[0046] In this embodiment, the first reactor 51 and the second reactor 53 adopt the above-mentioned alternating heating and temperature raising method and transfer the heat energy to each other through the first flash separator 52 to circulate the wet garbage, that is, the double-reactor periodic heating and flash switching method are used to recover energy, which improves the energy utilization rate and shortens the heating time, thereby solving the problem of high energy consumption existing in the device of the prior art.

[0047] Furthermore, an oil-water separator 6 is included, the inlet of which is connected to the outlet of the liquid storage tank 4. After receiving the liquid material in the liquid storage tank 4, the oil-water separator 6 separates the liquid material into water and liquid fertilizer. The water is pumped into the water tank through a pumping mechanism for centralized biochemical treatment, and the liquid fertilizer is discharged to the next level treatment system for further treatment.

[0048] Example 2

[0049] This embodiment 2 is formed on the basis of embodiment 1. By setting up a feed balance tank, it can not only maintain the pressure and temperature balance of the first reactor and the second reactor while feeding, but also use the excess steam to heat the seasoning tank, further improving the energy utilization rate. Specifically:

[0050] like Figure 1As shown, the primary treatment subsystem 5 also includes a feed balancing tank 55. An outlet of the first flash separator 52 is connected to the inlet of the feed balancing tank 55. The feed balancing tank 55 is used to accommodate excess steam in the first flash separator 52. The feed balancing tank 55 can also replenish steam in the first flash separator 52 to achieve a balance in pressure and temperature between the first reactor 51 and the second reactor 53 during the feeding process.

[0051] Furthermore, the outer surface of the seasoning tank 1 is provided with an insulation chamber (not shown). This insulation chamber can be formed by applying a layer of sealed insulation material to the outer wall of the seasoning pipe 1. An outlet of the feed balancing tank 55 communicates with the insulation chamber, through which steam is transferred to the insulation chamber, thereby preheating the emulsified wet waste in the seasoning tank 1, further improving energy utilization and reducing energy consumption.

[0052] Example 3

[0053] Example 3 is formed on the basis of Example 1 or 2. By setting up a secondary treatment subsystem, a multi-effect distillation treatment system is formed. The liquid fertilizer produced by the hydrothermal process is treated by the multi-effect distillation technology, solving the problems of deoiling and desalting, and achieving the effect of reducing the amount of fertilizer. Specifically:

[0054] like Figure 1-2 As shown, the secondary processing subsystem 7 includes a second flash separator 71, a steam compressor 72, and a heat exchanger 73. An inlet of the second flash separator 71 is connected to the liquid fertilizer discharge port of the oil-water separator 6. A steam outlet of the second flash separator 71 is connected to the steam compressor 72, which transports steam to the heat exchanger 73. After the liquid fertilizer in the oil-water separator 6 is discharged into the second flash separator 71, it continues to undergo flash separation in the second flash separator 71. The separated water vapor is transported to the heat exchanger 73 via the steam compressor 72, while the concentrated material is discharged through the discharge port to external equipment for further processing. After heat exchange in the heat exchanger 73, most of the steam turns into condensed water. The condensed water is pumped into a water tank for biochemical treatment. The remaining small amount of concentrated liquid fertilizer is also discharged to external equipment for further processing. Preferably, two or more heat exchangers 73 can be designed in parallel to improve efficiency.

[0055] Furthermore, the secondary processing subsystem 7 also includes a third flash separator 74 (which is connected to the oil-water separator to further introduce liquid fertilizer). The inlet of the third flash separator 74 is connected to the steam outlet of the second flash separator 71, and the steam outlet of the third flash separator 74 is connected to the steam compressor 72. At this time, the steam flashed and separated in the second flash separator 71 enters the third flash separator 74 and undergoes another flash separation. After that, the steam passes through the steam compressor 72 and is discharged into the heat exchanger 73. This improves energy utilization efficiency and further enhances the concentration and reduction of liquid materials.

[0056] In some preferred embodiments, the second flash separator 71 may be connected to the insulation chamber of the slurry mixing tank 1, and excess steam in the insulation chamber may enter the second flash separator 71, thereby further improving energy utilization efficiency.

[0057] Multi-stage distillation, also known as multi-effect distillation, is a heat exchange system composed of multiple evaporators connected in series. The principle of a multi-effect evaporator is to connect multiple evaporators in series, with the secondary steam from the previous evaporator serving as the heating steam for the next evaporator. The heating steam for the next evaporator is then used in the heating chamber of the next evaporator, which is the condenser of the previous evaporator. To evaporate the same amount of water, the amount of raw steam required using a multi-effect system is much smaller than that required using a single-effect system. In a multi-effect evaporation system, the operating pressure and boiling point of each effect decrease sequentially. The secondary steam from the first effect serves as the heating steam for the next effect, meaning the heating chamber of the next effect is equivalent to the condenser of the secondary steam from the previous effect. Only raw steam is consumed during the process, thus improving steam utilization.

[0058] The multi-stage distillation subsystem in this embodiment adopts a parallel feeding evaporation process. The so-called parallel feeding evaporation process means that the flow direction of the solution and steam is the same, and both flow from the first stage to the last stage in sequence, which is called the parallel feeding method. In the parallel feeding evaporation process, the transportation of the solution between the effects can utilize the pressure difference between the effects without the need for pumping. At the same time, when the solution of the previous effect flows into the effect with lower temperature and pressure, evaporation (flash evaporation) will occur, thereby generating a portion of secondary steam. This operation is simple and the process conditions are stable. After distillation, the separated liquid, in addition to the concentrated liquid fertilizer, is separated into grease and salt due to the different specific gravities of the liquids. The liquid fertilizer is also concentrated to 10% of the original amount and is filled as concentrated liquid humic acid organic fertilizer. After the multi-effect distillation, the steam is condensed and the water is introduced into a biochemical water treatment device for water treatment and discharged after meeting the standards.

[0059] Example 4

[0060] This embodiment 4 is a method for treating wet garbage by hydrothermal resource utilization based on embodiment 3, which adopts a wet garbage hydrothermal resource utilization treatment system, such as Figure 1-2 As shown, it includes a flash switching step and a multi-stage distillation step;

[0061] The flash switching steps include:

[0062] A1, pumping the sorted, crushed, pulped and emulsified wet garbage into the slurry mixing tank 1 through the emulsification pump;

[0063] A2, pumping the wet garbage in the slurry mixing tank 1 into the first reaction kettle 51 through the screw pump 2;

[0064] A3, starting the heater 54 to heat the first reactor 51, and simultaneously sending air into the first reactor 51 through the air compressor to pressurize the first reactor 51, and maintaining the first reactor 51 at a predetermined temperature and predetermined pressure for a predetermined time;

[0065] A4, while carrying out step A3, pump the wet garbage in the slurry mixing tank 1 into the second reactor 52 through the screw pump 2;

[0066] A5: After the first reactor 51 is maintained at a constant temperature and pressure for a predetermined period of time, the valves connecting the first flash separator 52 to the first reactor 51 and the second reactor 53 are opened. The heat energy in the first reactor 51 is transferred to the second reactor 52 through flash evaporation in the first flash separator 52, thereby heating the wet garbage in the second reactor 52.

[0067] A6: After the temperature and pressure in the first reactor 51 drop to predetermined values, the discharge valve of the first reactor 51 is opened, and the material in the first reactor 51 is conveyed to the centrifuge 3. The centrifuge 6 separates the material into liquid and solid materials. The liquid material is conveyed to the liquid storage tank 4, and the solid material is conveyed to an external device.

[0068] A7, heating the second reactor 53 by the heater 54, and simultaneously supplying air into the second reactor 53 by the air compressor to pressurize the second reactor 53, and maintaining the second reactor 53 at a predetermined temperature and predetermined pressure for a predetermined time;

[0069] A8: While carrying out step A7, the wet garbage in the slurry mixing tank 1 is pumped into the first reaction kettle 51 by the screw pump 2;

[0070] A9: After the second reactor 53 is maintained at a constant temperature and pressure for a predetermined period of time, the valves connecting the first flash separator 52 to the first reactor 51 and the second reactor 53 are opened. The heat energy in the second reactor 53 is transferred to the first reactor 51 through flash evaporation in the first flash separator 52, thereby heating the wet garbage in the first reactor 51.

[0071] A10: After the temperature and pressure in the second reactor 53 drop to predetermined values, the discharge valve of the second reactor 53 is opened. The material in the second reactor 53 is conveyed to the centrifuge 3, where it is separated into liquid and solid materials by the centrifuge 6. The liquid material is conveyed to the liquid storage tank 4, and the solid material is conveyed to an external device.

[0072] A11, repeat steps A1-A10.

[0073] Preferably, step A5 and / or step A9 further include a temperature and pressure balance step, which is: the first flash separator 52 and the feed balance tank 55 transmit steam so that the temperature and pressure of the first reactor 51 and the second reactor 52 are kept balanced during feeding.

[0074] The multi-stage distillation steps include:

[0075] B1, the liquid material in the liquid storage tank 4 is transported to the oil-water separator 6, the liquid material is separated into water and liquid fertilizer by the oil-water separator 6, and the liquid fertilizer is transported to the second flash separator 71 for flash separation;

[0076] B2, flash separation in the second flash separator 71 forms steam and concentrated liquid fertilizer, the steam is sent to the heat exchanger 71 through the steam compressor 72, and the concentrated liquid fertilizer is discharged from the discharge port of the second flash separator 71 to external equipment;

[0077] B3, the heat exchanger 73 converts the steam into condensed water and concentrated liquid fertilizer through heat exchange. The condensed water is discharged into the external water tank, and the concentrated liquid fertilizer is transported to the external equipment.

[0078] Preferably, step B2 also includes a steam redistillation step, and the steam distillation step is as follows: the steam generated in the feed balance tank 55 is passed into the insulation chamber of the slurry mixing tank 1 to preheat the slurry mixing tank 1, and the excess steam is passed through a pipeline into the second flash separator 71 for distillation.

[0079] In the description of this application, it should be understood that the terms "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inside", "outside", etc., indicating the orientation or position relationship, are based on the orientation or position relationship shown in the accompanying drawings, and are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on this application.

[0080] The above describes specific embodiments of the present invention. It should be understood that the present invention is not limited to the specific embodiments described above, and those skilled in the art may make various changes or modifications within the scope of the claims, which do not affect the essence of the present invention. The embodiments of this application and the features in the embodiments may be combined with each other in any manner unless there is a conflict.

Claims

1. A wet garbage hydrothermal resource treatment system, characterized in that: It comprises a slurry mixing tank (1), a screw pump (2), a centrifuge (3), a liquid storage tank (4) and a primary processing subsystem (5); The primary treatment subsystem (5) includes a first reactor (51), a first flash separator (52), a second reactor (53) and a heater (54). The first reactor (51) and the second reactor (53) are connected through the first flash separator (52). The heater (54) is used to heat the first reactor (51) and the second reactor (53) respectively. The pulping tank (1) is used to store wet garbage after sorting, crushing, pulping and emulsification. The screw pump (2) is used to pump the wet garbage in the pulping tank (1) into the first reactor (51) and the second reactor (53) respectively. The centrifuge (7) receives the materials in the first reactor (51) and the second reactor (53) and separates the materials into liquid materials and solid materials. The liquid materials are transported to the liquid storage tank (4), and the solid materials are transported to external equipment. When the first reactor (51) is heated and pressurized and maintained at a constant temperature and pressure for a predetermined time, the slurry mixing pipe (1) transports the wet garbage to the second reactor (53) through the screw pump (2), and before the first reactor (51) is unloaded, heat energy is transported to the second reactor (53) through the first flash separator (52) to preheat the wet garbage in the second reactor (53); when the second reactor (5) is heated and pressurized and maintained at a constant temperature and pressure for a predetermined time, the slurry mixing tank (1) pumps the wet garbage into the first reactor (3) from which the material has been unloaded through the screw pump (2), and before the second reactor (5) is unloaded, heat energy is transported to the first reactor (3) through the first flash separator (4) to preheat the wet garbage in the second reactor (53), and the cycle continues in sequence; The primary treatment subsystem (5) further comprises a feed balancing tank (55), the feed balancing tank (55) being in communication with the first flash separator (52), and the feed balancing tank (55) being used to maintain a pressure and temperature balance between the first reactor (51) and the second reactor (53); The outer peripheral surface of the slurry mixing tank (1) is provided with a heat preservation cavity, the feed balance tank (55) is communicated with the heat preservation cavity, and the steam in the feed balance tank (55) is passed into the heat preservation cavity to heat the slurry mixing tank (1); It also includes an oil-water separator (6), wherein the liquid material in the liquid storage tank (4) enters the oil-water separator (6) and is separated into water and liquid fertilizer, and the liquid fertilizer is sent to the next-level processing subsystem; The invention also includes a secondary processing subsystem (7), wherein the secondary processing subsystem (7) includes a second flash separator (71), a steam compressor (72) and a heat exchanger (73). The second flash separator (71) is connected to the oil-water separator (6) and receives the transported liquid fertilizer. The second flash separator (71) transports steam to the heat exchanger (73) through the steam compressor (72). The condensed water discharged from the heat exchanger (73) enters an external water tank. The concentrated liquid fertilizer from the second flash separator (71) and the heat exchanger (73) is discharged to an external device.

2. The wet garbage hydrothermal resource treatment system according to claim 1 is characterized in that: The second flash separator (71) is in communication with the heat preservation chamber, and excess steam in the heat preservation chamber enters the second flash separator (71).

3. The wet garbage hydrothermal resource processing system according to claim 1 is characterized in that: The secondary treatment subsystem (7) further comprises a third flash separator (74), the inlet of the third flash separator (74) being connected to the second flash separator (71), and the outlet of the third flash separator (74) being connected to the steam compressor (72).

4. A method for hydrothermal resource recovery of wet garbage, characterized in that: The wet garbage hydrothermal resource treatment system according to claim 1 includes a flash evaporation switching step and a multi-stage distillation step; The flash switching step comprises: A1, pumping the wet garbage that has been sorted, crushed, pulped and emulsified into the pulp mixing tank (1) through an emulsification pump; A2, pumping the wet garbage in the slurry mixing tank (1) into the first reaction kettle (51) through the screw pump (2); A3, starting the heater (54) to heat the first reactor (51), and simultaneously sending air into the first reactor (51) through an air compressor to pressurize the first reactor (51), and maintaining the first reactor (51) at a predetermined temperature and a predetermined pressure for a predetermined time; A4, while carrying out step A3, pumping the wet garbage in the slurry mixing tank (1) into the second reaction kettle (52) through the screw pump (2); A5, after the first reactor (51) is kept at a constant temperature and pressure for a predetermined time, the valves of the first flash separator (52), the first reactor (51), and the second reactor (53) are opened, and the heat energy in the first reactor (51) is transferred to the second reactor (52) by flash evaporation through the first flash separator (52), thereby heating the wet garbage in the second reactor (52); A6, after the temperature and pressure in the first reactor (51) drop to predetermined values, the discharge valve of the first reactor (51) is opened, and the material in the first reactor (51) is transported to the centrifuge (3), and the material is separated into liquid material and solid material by the centrifuge (6), the liquid material is transported to the liquid storage tank (4), and the solid material is transported to an external device; A7, heating the second reactor (53) by the heater (54), and simultaneously sending air into the second reactor (53) by an air compressor to pressurize the second reactor (53), and maintaining the second reactor (53) at a predetermined temperature and a predetermined pressure for a predetermined time; A8, while carrying out step A7, pumping the wet garbage in the slurry mixing tank (1) into the first reactor (51) through the screw pump (2); A9, after the second reactor (53) is kept at a constant temperature and pressure for a predetermined time, the valves of the first flash separator (52) and the first reactor (51) and the second reactor (53) are opened, and the heat energy in the second reactor (53) is transferred to the first reactor (51) through flash evaporation in the first flash separator (52), thereby heating the wet garbage in the first reactor (51); A10, after the temperature and pressure in the second reactor (53) drop to predetermined values, the discharge valve of the second reactor (53) is opened, and the material in the second reactor (53) is transported to the centrifuge (3), and the material is separated into liquid material and solid material by the centrifuge (6), the liquid material is transported to the liquid storage tank (4), and the solid material is transported to an external device; A11, repeat steps A1-A10. The multi-stage distillation step comprises: B1, transporting the liquid material in the liquid storage tank (4) to the oil-water separator (6), separating the liquid material into water and liquid fertilizer through the oil-water separator (6), and transporting the liquid fertilizer to the second flash separator (71) for flash separation; B2, flash separation in the second flash separator (71) to form steam and concentrated liquid fertilizer, the steam is sent into the heat exchanger (71) through the steam compressor (72), and the concentrated liquid fertilizer is discharged from the discharge port of the second flash separator (71) to an external device; B3, the heat exchanger (73) converts the steam into condensed water and concentrated liquid fertilizer through heat exchange, the condensed water is discharged into the external water tank, and the concentrated liquid fertilizer is transported to the external equipment.

5. The method for hydrothermal resource recovery of wet garbage according to claim 4, characterized in that: Said step A5 and / or step A9 also includes a temperature and pressure balance step, wherein said temperature and pressure balance step is as follows: the first flash separator (52) and the feed balance tank (55) transmit steam so that the temperature and pressure of the first reactor (51) and the second reactor (52) are kept balanced during feeding.

6. The method for hydrothermal resource recovery of wet garbage according to claim 4 or 5, characterized in that: The step B2 also includes a steam redistillation step, wherein the steam distillation step is as follows: the steam generated in the feed balance tank (55) is passed into the insulation chamber of the slurry mixing tank (1) to preheat the slurry mixing tank (1), and the excess steam is passed through a pipeline into the second flash separator (71) for distillation.

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