A method and system for separating all components of organic waste

Abstract

This invention provides a method and system for the complete separation of organic waste components. The method innovatively adopts a separation-then-conversion approach, abandoning the previous integrated mixing treatment method. It separates all components in stages and designs a conversion path for each component, maximizing the utilization of waste value. The system comprises a pretreatment module, an air-assisted dynamic filtration module, a sedimentation-emulsification flocculation-demulsification and reduction module, an oil-water separation module, a fermentation tank, and a purification tank, all connected in sequence. Through the coordinated operation of the various mechanical structures, the system separates waste into high-purity oil, water, and solid phases, providing high-quality raw materials for subsequent diversified high-value conversion pathways such as oil-to-biodiesel, starch-to-sugar lactic acid, and cellulose-to-ethanol production.

Description

Technical Field

[0001] This invention relates to the field of waste treatment and resource utilization technology, and in particular to a method and system for separating all components of organic waste. Background Technology

[0002] With the acceleration of urbanization, organic waste accounts for 50%-70% of the total amount of household waste in cities. Due to its high water content, rich organic matter content, and easy decomposition and odor, it has become a difficult point in waste sorting and treatment.

[0003] Existing organic waste treatment technologies mainly fall into three categories: anaerobic fermentation for biogas production, aerobic composting, and incineration for power generation. Among these, anaerobic fermentation is currently the most widely used technology. Its typical process involves crushing and homogenizing the waste before it directly enters an anaerobic digester for biotransformation, where microorganisms convert the organic matter into biogas and biogas residue. However, these technologies all employ a "holistic treatment" model, treating organic waste as a single unit without separating its different components. Some improved processes add simple pressure filtration or centrifugal solid-liquid separation after pretreatment, but this only achieves coarse separation and does not provide fine grading of the components.

[0004] Existing technologies generally suffer from problems such as incomplete component separation, large loss of organic matter, low oil recovery rate, poor impurity removal efficiency, and low resource utilization rate. They cannot achieve efficient and accurate separation of all components in organic waste, such as biodegradable organic matter, waste oil, and filter residue, nor can they meet the requirements for the coordinated treatment of organic waste reduction, harmlessness, and resource utilization.

[0005] Therefore, developing a new technology that can efficiently process, recycle, recycle, integrate processes, and increase the value of all components of organic waste has become an urgent technical problem to be solved in this field. Summary of the Invention

[0006] In view of the shortcomings of the prior art described above, the purpose of this invention is to provide a method and system for the complete separation of organic waste components, in order to solve the problems in the prior art.

[0007] To achieve the above and other related objectives, the present invention provides a method for the complete separation of organic waste components, comprising the following steps: 1) The waste is crushed, homogenized, and acidified, and then filtered to obtain filter residue I and filtrate I; filter residue I is returned to be homogenized, acidified, and filtered at least twice to obtain first filter residue and filtrate II; filtrate I and filtrate II are combined to obtain first filtrate. 2) The first filter residue is further compressed to obtain the second filter residue and the second filtrate; 3) The first filtrate is allowed to stand and settle. The filtrate separates into a first solid phase precipitate, a first aqueous phase, and a first oil phase. The first oil phase is filtered to obtain large-particle-size free oil and small-particle-size emulsified oil and dispersed oil mixed in the first aqueous phase. 4) Add emulsifier / flocculator to the small-particle-size emulsified oil and dispersed oil mixed with the first aqueous phase to achieve emulsification and flocculation equilibrium, thus obtaining the second solid phase precipitate and the second aqueous phase containing emulsified oil droplets; 5) Add a demulsifier to the second aqueous phase containing emulsified oil droplets to demulsify, filter, and obtain an oil-water mixture and solid particles; 6) Add a reducing agent to the oil-water mixture for reduction, and then perform at least one oil-water separation to separate the emulsified oil, dispersed oil, and aqueous phase; also add a reducing agent to the solid particles for reduction. 7) The second filtrate from step 2), the large-particle-size free oil from step 3), and the emulsified and dispersed oil from step 6) are purified to prepare biodiesel. 8) The second filter residue from step 2), the first solid phase precipitate from step 3), the second solid phase precipitate from step 4), and the reduced solid particles from step 6) are subjected to a fermentation process to prepare ethanol and / or lactic acid; the aqueous phase from step 6) is subjected to an alcohol precipitation and fermentation process in sequence to prepare lactic acid and / or pectin.

[0008] The present invention also provides a treatment system for the complete separation of organic waste components, the system comprising a pretreatment module, an air-assisted dynamic filtration module, a sedimentation-emulsification flocculation-demulsification and reduction module, an oil-water separation module, a fermentation tank and a purification tank connected in sequence; The pretreatment module includes a crushing unit and a homogenizing acidification unit connected in sequence. The crushing unit is provided with a waste inlet, and the homogenizing acidification unit is provided with an acid feed inlet, a filter cake discharge outlet, and a slurry discharge outlet. The filter cake discharge outlet is connected to a filter cake compression mechanism, which is connected to a fermentation tank and a purification tank respectively. The air-assisted dynamic filtration module includes an air-assisted plate, an air-assisted cylinder, and a piston backflushing mechanism arranged sequentially from top to bottom. The air-assisted plate is located at the top of the air-assisted cylinder, and the lower surface of the air-assisted plate is a pressing surface with a uniform airflow distribution structure. The air-assisted plate is adapted to be connected to an external air pump. The inlet of the air-assisted cylinder is connected to the slurry outlet. A filter screen assembly is located at the bottom of the air-assisted cylinder. A slurry return port is located above the filter screen assembly and on the bottom side of the air-assisted cylinder. The slurry return port is connected to the inlet of the homogenization acidification unit. The piston backflushing mechanism includes an adjustable backflushing piston plate located below the air-assisted cylinder. The backflushing piston plate is adapted to be connected to an external water pump. In the closed state, it is adapted to spray water to backflush and clean the filter screen assembly. In the open state, it is adapted to discharge the filtrate passing through the filter screen assembly into the sedimentation-emulsification flocculation-demulsification and reduction module. The sedimentation-emulsification-flocculation-demulsification and reduction module includes a sedimentation tank, an emulsification tank, a demulsification tank, and a reduction tank connected in sequence; the sedimentation tank is connected to the bottom of the backflushing piston plate, and the sedimentation tank, emulsification tank, and reduction tank are also connected to the fermentation tank respectively; The oil-water separation module includes at least one buffer tank and at least one separation tank connected together. The buffer tank is connected to a reduction tank. The separation tank includes an aqueous phase outlet and an oil phase outlet. The oil phase outlet is connected to a purification tank, and the aqueous phase outlet is connected to a fermentation tank.

[0009] As described above, the organic waste complete component separation method and treatment system of the present invention have the following beneficial effects: The organic waste separation method of the present invention pioneers a path of separation followed by conversion, abandoning the previous integrated mixing treatment method. It separates all components in stages and designs a conversion path for each component to maximize the utilization of waste value.

[0010] The system of this invention, through the coordinated work of the preceding and following mechanical structures, separates waste into high-purity oil phase, aqueous phase and solid phase, providing high-quality raw materials for subsequent diversified high-value conversion pathways such as oil to biodiesel, starch sugar to lactic acid, and cellulose to ethanol. Attached Figure Description

[0011] Figure 1 This is a schematic diagram of the overall system for the complete separation of organic waste components according to the present invention.

[0012] Figure 2 This is a schematic diagram of the air-assisted dynamic filtration module in the system of the present invention.

[0013] Figure 3 This is a schematic diagram of the deformable membrane mechanism in the system of the present invention in a non-operating state.

[0014] Figure 4 This is a schematic diagram of the filter state of the deformable membrane mechanism in the system of the present invention. Figure 5 This is a schematic diagram of the membrane frame in the deformable membrane mechanism of the present invention.

[0015] Figure 6 This is a schematic diagram of the suction cup of the first siphon mechanism in the system of the present invention.

[0016] Explanation of icon numbers 10 Preprocessing Module 20. Air-assisted dynamic filtration module 30 Sedimentation-Emulsification-Flocculation-Demulsification and Reduction Module 40 Oil-water separation module 50 fermentation tanks 60 purification pools 11 Crushing Unit 12 Homogenization Acidification Units 111 Garbage Inlet 121 Acid feed port 122 Filter residue discharge port 21 Air-assisted plate 22 Piston recoil mechanism 222 Recoil Piston Plate 23. Air-assisted cylinder 231 Liftable Filter Assembly 232 Slurry return port 31 Settling tank 311 First oil phase discharge outlet 312 First aqueous phase discharge outlet 313 First solid phase outlet 314 Deformable Membrane Mechanism 3141 Density Sensor 3142 membrane frame 3142a Polygonal Frame 3142b guide rail 3142c slider 3143 Main body of the sliding group 3144 Inflatable Retractable Ring 3145 gasket 3146 Circular Support 3147 Membrane 315 First Siphon Mechanism 3151 Suction Port 3152 Suction Cup 32 Emulsifying Tank 321 Emulsifier feed port 322 Second aqueous phase discharge outlet 323 Second solid phase outlet 324 Second Siphon Mechanism 33 Broken Milk Jars 331 Demulsifier Inlet 34 First Reduction Vessel 35 Second Reduction Vessel 36. Membrane filtration system 41 First Buffer Box 42 Coarse Separation Box 421 Third aqueous phase discharge outlet 422 Second oil phase discharge port 43 Second Buffer Box 44 Finely separated phases 441 Fourth aqueous phase discharge outlet 442 Third oil phase discharge port Detailed Implementation

[0017] The following specific examples illustrate the implementation of the present invention. Those skilled in the art can easily understand other advantages and effects of the present invention from the content disclosed in this specification. The present invention can also be implemented or applied through other different specific embodiments, and various details in this specification can also be modified or changed based on different viewpoints and applications without departing from the spirit of the present invention.

[0018] In this invention, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a mechanical connection, an electrical connection, or a communication connection; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components, unless otherwise explicitly limited. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0019] In this invention, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, a feature defined with "first" or "second" may explicitly or implicitly include one or more of that feature. Terms such as "length," "width," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," and "outer," indicating orientation or positional relationships, are based on the orientation or positional relationships shown in the accompanying drawings and are only for the convenience of describing the invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of the invention.

[0020] When a numerical range is disclosed herein, the range is considered continuous and includes the minimum and maximum values ​​of the range, as well as every value between the minimum and maximum values. Furthermore, when the range refers to an integer, it includes every integer between the minimum and maximum values ​​of the range. Additionally, when multiple ranges are provided to describe a feature or characteristic, the ranges may be combined. In other words, unless otherwise specified, all ranges disclosed herein should be understood to include any and all subranges to which they are included. For example, a specified range from “1 to 10” should be considered to include any and all subranges between the minimum value 1 and the maximum value 10. Exemplary subranges of the range 1 to 10 include, but are not limited to, 1 to 6.1, 3.5 to 7.8, 5.5 to 10, etc.

[0021] Furthermore, it should be understood that the existence of other method steps before or after the combined steps, or the insertion of other method steps between these explicitly mentioned steps, does not preclude the existence of other method steps before or after the combined steps, or the insertion of other method steps between these explicitly mentioned steps, unless otherwise stated. It should also be understood that the combined connection relationship between one or more devices / apparatus mentioned in this invention does not preclude the existence of other devices / apparatus before or after the combined devices / apparatus, or the insertion of other devices / apparatus between these explicitly mentioned devices / apparatus, unless otherwise stated. Moreover, unless otherwise stated, the numbering of each method step is merely a convenient tool for identifying each method step, and not for limiting the order of the method steps or limiting the scope of the invention. Changes or adjustments to their relative relationships, without substantially altering the technical content, should also be considered within the scope of the invention.

[0022] Please refer to the accompanying drawings. It should be noted that the illustrations provided in this embodiment are only schematic representations of the basic concept of the present invention. Therefore, the drawings only show the components related to the present invention and are not drawn according to the actual number, shape and size of the components in the actual implementation. In the actual implementation, the form, quantity and proportion of each component can be arbitrarily changed, and the layout of the components may also be more complex.

[0023] The first aspect of this invention provides a method for separating all components of organic waste, comprising the following steps: 1) The waste is crushed, homogenized, and acidified, and then filtered to obtain filter residue I and filtrate I; filter residue I is returned to be homogenized, acidified, and filtered at least twice to obtain first filter residue and filtrate II; filtrate I and filtrate II are combined to obtain first filtrate. 2) The first filter residue is further compressed to obtain the second filter residue and the second filtrate; 3) The first filtrate is allowed to stand and settle. The filtrate separates into a first solid phase precipitate, a first aqueous phase, and a first oil phase. The first oil phase is filtered to obtain large-particle-size free oil and small-particle-size emulsified oil and dispersed oil mixed in the first aqueous phase. 4) Add emulsifier / flocculator to the small-particle-size emulsified oil and dispersed oil mixed with the first aqueous phase to achieve emulsification and flocculation equilibrium, thus obtaining the second solid phase precipitate and the second aqueous phase containing emulsified oil droplets; 5) Add a demulsifier to the second aqueous phase containing emulsified oil droplets to demulsify, filter, and obtain an oil-water mixture and solid particles; 6) Add a reducing agent to the oil-water mixture for reduction, and then perform at least one oil-water separation to separate the emulsified oil, dispersed oil, and aqueous phase; also add a reducing agent to the solid particles for reduction. 7) The second filtrate from step 2), the large-particle-size free oil from step 3), and the emulsified and dispersed oil from step 6) are purified to prepare biodiesel. 8) The second filter residue from step 2), the first solid phase precipitate from step 3), the second solid phase precipitate from step 4), and the reduced solid particles from step 5) are subjected to a fermentation process to prepare ethanol and / or lactic acid; the aqueous phase from step 6) is subjected to an alcohol precipitation and fermentation process in sequence to prepare lactic acid and / or pectin.

[0024] In some embodiments of the present invention, the acidification in step 1) is achieved by controlling the pH to 3.90–4.10 using an acetic acid solution. For example, the pH is 3.90–4.00 or 4.00–4.10. The concentration of the acetic acid is 0.3 mol / L–0.7 mol / L. For example, it is 0.3 mol / L–0.4 mol / L, 0.4 mol / L–0.5 mol / L, 0.5 mol / L–0.6 mol / L, or 0.6 mol / L–0.7 mol / L.

[0025] In some embodiments of the present invention, the acidification temperature in step 1) is 75-85°C. For example, it is 75-77°C, 77-79°C, 79-80°C, 80-82°C, 82-84°C, or 84-85°C. At this temperature, the oil precipitation rate is relatively high. Through homogenous acidification, starch, cellulose, and oil in the waste can be fully separated.

[0026] In some embodiments of the present invention, the filtration in step 1) uses a 200-mesh filter.

[0027] In some embodiments of the present invention, the filter membrane used for filtering the first oil phase in step 3) is a PAN membrane (polyacrylonitrile).

[0028] In some embodiments of the present invention, the emulsifier in step 4) is Tween / Span, and the flocculant is PAC / PAM. PAC: polyaluminum chloride; PAM: polyacrylamide.

[0029] In some embodiments of the present invention, the amount of emulsifier added in step 4) relative to the volume ratio of the filtrate after homogenization and acidification filtration (Tween:Span:Slurry) is (1~3)×10⁻⁶. -3 : (3~7.5)×10 -4 1. This invention uses 10% Tween and 10% Span. The Tween used in this invention is Tween-80. The Span used in this invention is Span-80.

[0030] The volume ratio of the flocculant added in step 4) to the filtrate after homogenization and acidification is PAC:PAM:slurry (1.3~10)×10. -3 : (2.5~20)×10 -3 1. In this invention, 1% PAC and 0.1% PAM are used.

[0031] In this invention, after initial separation by sedimentation, the aqueous phase still contains residual emulsified oil, dispersed oil, and a small amount of solid particles. To achieve precise phase separation of oil and solids, the inventors adjusted the type of surfactant added (single reagent / compound), the compound ratio, and the total amount added, and simultaneously matched the synergistic addition of PAC and PAM. That is, by controlling the amount of emulsifier and flocculant, the inventors ensured that as many solid particles (starch / cellulose) as possible precipitated during the emulsification and flocculation process, and that as many emulsified oils and dispersed oils as possible were emulsified, without being entrained by solid particles and settling. This ensured that under different material characteristics, the emulsification-flocculation dynamic balance was always maintained in the tank, maximizing the goal of oil droplet emulsification remaining in the aqueous phase and solid particle flocculation and sedimentation.

[0032] In some embodiments of the present invention, the demulsifier in step 5) is a Fenton reagent.

[0033] In some embodiments of the present invention, the filter membrane used in step 5) is a PTFE membrane (polytetrafluoroethylene).

[0034] In some embodiments of the present invention, the reducing agent in step 6) is sodium sulfite.

[0035] In some embodiments of the present invention, the fermentation process in step 8) includes the following steps: adding amylase to convert starch into glucose glycogen, filtering, adding lactic acid bacteria to the filtrate for fermentation to prepare lactic acid, and using co-culture to prepare ethanol from the filter residue. The co-culture can be performed using existing technology. The co-culture method in this invention is not specifically limited; for example, it could be (Wang Bohan, Cui Jinna, et al. Magnetic nano-iron enhanced multi-strain co-fermentation of cellulose to prepare fuel ethanol [J]. Applied Chemical Industry, 2025). Those skilled in the art can choose according to the actual situation.

[0036] A second aspect of the present invention provides a treatment system for the complete separation of organic waste components, such as... Figure 1 and Figure 2 As shown, the system includes a pretreatment module 10, an air-assisted dynamic filtration module 20, a sedimentation-emulsification flocculation-demulsification and reduction module 30, an oil-water separation module 40, a fermentation tank 50, and a purification tank 60 connected in sequence. The pretreatment module 10 includes a crushing unit 11 and a homogenization and acidification unit 12 connected in sequence. The crushing unit 11 is provided with a waste inlet 111, and the homogenization and acidification unit 12 is provided with an acid feed inlet 121, a filter cake discharge outlet 122, and a slurry discharge outlet. The filter cake discharge outlet 122 is connected to a filter cake compression mechanism, which is connected to a fermentation tank 50 and a purification tank 60 respectively. The air-assisted dynamic filtration module 20 includes an air-assisted plate 21, an air-assisted cylinder 23, and a piston backflushing mechanism 22 arranged sequentially from top to bottom. The air-assisted plate 21 is located at the top of the air-assisted cylinder 23. The lower surface of the air-assisted plate 21 is a pressing surface with a uniform airflow distribution structure. The air-assisted plate is adapted to communicate with an external air pump. The inlet of the air-assisted cylinder 23 is connected to the slurry outlet. A filter assembly 231 is provided at the bottom of the air-assisted cylinder 23. Above the filter assembly 231 and the air-assisted cylinder 23... The bottom side is provided with a slurry return port, which is connected to the inlet of the homogenization acidification unit 12. The piston backflushing mechanism 22 includes a backflushing piston plate 222 that is adjustable to open and close located below the air-assisted cylinder 23. The backflushing piston plate 222 is adapted to be connected to an external water pump. In the closed state, it is adapted to spray water to backflush and clean the filter screen assembly 231. In the open state, it is adapted to discharge the filtrate passing through the filter screen assembly 231 into the sedimentation-emulsification flocculation-demulsification and reduction module 30. The sedimentation-emulsification-flocculation-demulsification and reduction module 30 includes a sedimentation tank 31, an emulsification tank 32, a demulsification tank 33, and a reduction tank connected in sequence; the sedimentation tank 31 is connected to the bottom of the backflushing piston plate 222, and the sedimentation tank 31, the emulsification tank 32, and the reduction tank are also connected to the fermentation tank 50 respectively; The oil-water separation module 40 includes at least one buffer tank and at least one separation tank connected together. The buffer tank is connected to a reduction tank. The separation tank includes an aqueous phase outlet and an oil phase outlet. The oil phase outlet is connected to a purification tank 60, and the aqueous phase outlet is connected to a fermentation tank 50.

[0037] In some embodiments of the present invention, the filter cake compression mechanism includes a filtrate outlet and a filter cake outlet. The filtrate outlet is connected to a purification tank 60, and the filter cake outlet is connected to a fermentation tank 50. The liquid deeply compressed by the filter cake compression mechanism enters the purification tank 60 for purification to produce biodiesel. The remaining filter residue solids are used to produce ethanol through co-cultivation. The filter cake compression mechanism in the present invention can be a plate and frame filter press.

[0038] In some embodiments of the present invention, the settling tank 31 includes a first oil phase outlet 311, a first aqueous phase outlet 312 and a first solid phase outlet 313. The first oil phase outlet 311 is connected to the purification tank 60, the first aqueous phase outlet 312 is connected to the emulsification tank 32, and the first solid phase outlet 313 is connected to the fermentation tank 50.

[0039] In a preferred embodiment of the present invention, the settling tank 31 is further provided with a deformable membrane mechanism 314, which is connected to the first oil phase outlet 311 and is suitable for discharging large-particle-size free oil. In this invention, the free oil has a particle size > 100 μm. Preferably, the particle size of the free oil is 200 μm.

[0040] In a preferred embodiment of the present invention, such as Figure 1 and Figures 3-4 As shown, the settling tank 31 has a slide rail that can move up and down on its inner wall. The deformable membrane mechanism 314 includes a density sensor 3141, a membrane frame 3142, a sliding body 3143, an inflatable telescopic ring 3144, a gasket 3145, a ring support 3146, and a membrane body 3147. The sliding body 3143 is slidably connected to the slide rail on the settling tank 31. The sliding body 3143 is provided with an air pump connection port. The density sensor 3141 is located on the top of the sliding body 3143. The membrane frame 3142 includes a polygonal frame 3142a, several guide rails 3142b, and a slider 3142c embedded in each guide rail and slidable along the guide rail axis. The gasket 3145 is sleeved on the polygonal frame 3142a. The guide rail 3142b is a hollow tubular structure. One end of the guide rail 3142b is connected to the air pump connection port, and the other end is connected to the polygonal frame 3142a. The membrane 3147 is cylindrical. Both ends of the membrane 3147 are fixedly connected to the inner side of the inflatable retractable ring 3144 and the slider 3142c, respectively. The membrane 3147 at the end of the slider 3142c extends and connects to the first grease phase outlet 311. The ring bracket 3146 is fixed below the sliding body 3143. The inflatable retractable ring 3144 is located at the end of the ring bracket 3146. The inflatable retractable ring 3144 has an inflation port, which is connected to the air pump connection port. The air pump connection port is adapted to connect to an external air pump.

[0041] The system is also equipped with a PLC control system, and the density sensor 3141, the sliding block body 3143, and the external air exchange pump are respectively connected to the PLC control system.

[0042] The gasket 3145 is an integral structure with an internal pipe and several pipe openings, each of which is connected to the guide rail 3142b.

[0043] like Figure 5 As shown, the guide rails 3142b do not intersect except at the starting point, and each vertex of the polygonal frame 3142a must be connected to a guide rail 3142b.

[0044] In this invention, the circular bracket 3146 and the inflatable retractable circular ring 3144 can serve as the support structure for the deformable membrane mechanism 314.

[0045] The inflatable retractable ring 3144 of this invention can be adapted to tanks of different diameters simply by adjusting its inflation volume using an air pump. Inflation or deflation allows the diameter (including the inner and outer diameters) of the inflatable retractable ring 3144 to expand or contract. The increase in the inner diameter simultaneously causes the membrane 3147 attached to it to unfold. In the deflated state, the membrane 3147 attached to the inflatable retractable ring 3144 is tightened, facilitating filtration. In the inflated state, the inflatable retractable ring 3144 expands, increasing its inner diameter and causing the membrane 3147 to unfold, facilitating the discharge of large-particle free oil that has been filtered out.

[0046] In a preferred embodiment of the present invention, the settling tank 31 is provided with a first siphon mechanism 315, which is connected to a first aqueous phase outlet 312 and is suitable for discharging the aqueous phase and small-particle-size emulsified oil and dispersed oil. In this invention, the first siphon mechanism 315 can be a water pump and several pipes connected to the water pump, with each pipe end connected to a suction cup 3152 containing several suction ports 3151, such as... Figure 6 As shown. The dispersed oil in this invention has a particle size of 1~100μm. Preferably, the particle size of the dispersed oil is 50μm. The emulsified oil in this invention has a particle size of 0.5~15μm. Preferably, the particle size of the emulsified oil is 5μm.

[0047] In some embodiments of the present invention, the emulsifying tank 32 includes an emulsifier feed port 321, a second aqueous phase outlet 322 and a second solid phase outlet 323, wherein the second aqueous phase outlet 322 is connected to the demulsifying tank 33 and the second solid phase outlet 323 is connected to the fermentation tank 50.

[0048] In a preferred embodiment of the present invention, the emulsifying tank 32 is provided with a second siphon mechanism 324, which is connected to a second aqueous phase outlet 322 and is suitable for discharging an aqueous phase containing emulsified oil droplets. The structure of the second siphon mechanism 324 is the same as that of the first siphon mechanism 315.

[0049] In some embodiments of the present invention, the demulsifier tank 33 includes a demulsifier inlet 331.

[0050] In some embodiments of the present invention, a membrane filtration mechanism 36 is provided between the demulsifying tank 33 and the reduction tank. The reduction tank includes a first reduction tank 34 and a second reduction tank 35. The second deformable membrane mechanism 36 is adapted to pass the membrane filtrate into the first reduction tank 34 and to pass the membrane filter residue into the second reduction tank 35. The second reduction tank 35 is connected to the fermentation tank 50.

[0051] The membrane filtration mechanism 36 described in this invention uses a PTFE membrane.

[0052] In a preferred embodiment of the present invention, both the first reduction tank 34 and the second reduction tank 35 are provided with a reducing agent feeding port 345.

[0053] In a preferred embodiment of the present invention, the first reduction tank 34 is connected to the oil-water separation module 40.

[0054] In some embodiments of the present invention, the oil-water separation module 40 includes a first buffer tank 41, a coarse separation tank 42, a second buffer tank 43, and a fine separation phase 44 connected in sequence. The first buffer tank 41 is connected to a reduction tank, and the coarse separation tank 42 and the fine separation phase 44 are both connected to a purification tank 60.

[0055] In a preferred embodiment of the present invention, the coarse separation tank 42 includes a third aqueous phase outlet 421 and a second oil phase outlet 422. The third aqueous phase outlet 421 is connected to a second buffer tank 43, and the second oil phase outlet 422 is connected to a purification tank 60.

[0056] In a preferred embodiment of the present invention, the finely separated phase 44 includes a fourth aqueous phase outlet 441 and a third oil phase outlet 442, the third oil phase outlet 442 being connected to a purification tank 60, and the fourth aqueous phase outlet 441 being connected to a fermentation tank 50.

[0057] In some embodiments of the present invention, the separation chamber is provided with a double-membrane slit separation mechanism, which is suitable for oil-water separation.

[0058] In a preferred embodiment of the present invention, the dual membranes in the dual-membrane slit separation mechanism are a hydrophilic membrane and a hydrophobic membrane, which are arranged in parallel, forming a slit between the two membranes for oil-water separation. In this invention, the dual-membrane slit separation mechanism can be (Yang Haocheng, Xu Zhikang. Hydrophilic / Hydrophobic Dual-Membrane Slit: A New Technology for Simultaneous Oil-Water Recovery in Oil-Water Emulsions [J]. Science Bulletin, 2024, 69(35): 5063-5064). Those skilled in the art can choose according to the actual situation.

[0059] In a preferred embodiment of the present invention, the width of the slit is 3.5 to 4.5 mm. For example, it is 3.5 to 3.7 mm, 3.7 to 3.9 mm, 3.9 to 4.0 mm, 4.0 to 4.2 mm, 4.2 to 4.4 mm, or 4.4 to 4.5 mm. In a preferred embodiment of the present invention, the width of the slit is 4 mm.

[0060] The present invention will be further described in detail below with reference to specific embodiments. The described embodiments are only for explaining the present invention and are not intended to limit the scope of protection of the present invention. Unless otherwise specified, the equipment used in the following embodiments is conventional equipment in the art; unless otherwise specified, the reagents used are commercially available products or prepared by conventional methods in the art. Items not described in detail in the following embodiments can be achieved using conventional experimental methods in the art.

[0061] Example 1 The method for separating all components will be described in detail below with reference to the accompanying drawings.

[0062] First, such as Figure 1 , Figure 2 As shown, after the organic waste is crushed in the crushing unit 11, it enters the homogenization and acidification unit 12. Acetic acid solution is added through the acid feed port 121 to control the pH to 3.90~4.10 and homogenize at 80°C. Then, the slurry is discharged into the air-assisted cylinder 23 through the slurry discharge port. The air-assisted plate 21 is connected to the air pump, and at the same time, the backflush piston plate 222 below is opened. The air pump applies a uniform air wall downward through the air-assisted plate 21, squeezing the slurry towards the filter screen assembly 231 for pressure filtration. The filtrate flows to the settling tank 31, and the filter residue remains on the filter screen assembly 231. After the filter press is completed, the air pump is turned off, and the backwash piston plate 22 is closed. The backwash piston plate 222 is connected to an external water pump, which sprays high-intensity water through the piston on the backwash piston plate 222 onto the filter screen assembly 231 for high-pressure water backwashing, achieving self-cleaning of the filter screen assembly 231. The filter residue is broken up and the slurry formed with the water is returned to the homogenization and acidification unit 12 through the slurry return port 232 for further treatment. While ensuring that the residue on the filter screen is thoroughly cleaned and unblocked, it is remixed and homogenized, and then subjected to dynamic filtration again with the next batch of organic waste, realizing the material circulation of organic waste filter residue. Through several dynamic filtration cycles, it is ensured that as much starch as possible in the waste is broken up and enters the filtrate. After the final return to the homogenization and acidification unit 12, the first filter residue is discharged through the filter residue discharge port 122. The first filter residue is then deeply compressed in the filter cake compression mechanism to obtain the second filter residue and the second filtrate. At this point, most of the components in the first filter residue have been acidified and dissolved into the second filtrate, and the starch has been broken down as much as possible and entered into the second filtrate. The second filtrate is discharged into the purification tank 60. The remaining components are mostly cellulose (such as lignin) that is difficult to acidify and large-diameter oil droplets that have not been homogenized and dispersed, which constitute the second filter residue and are discharged into the fermentation tank 50.

[0063] Then, as Figure 1 , Figures 3-5As shown, the first filtrate flowing to the settling tank 31 is allowed to settle and separate into three phases: a first solid phase, a first aqueous phase, and a first oil phase. The deformable membrane mechanism 314 is controlled by a PLC control system, which controls the sliding body 3143 to slide from bottom to top on the slide rail on the settling tank 31 at a speed of 0.5 mm / s. During this process, the density sensor 3141 (pressure sensor) on the sliding body monitors the liquid pressure at a fixed position at regular intervals (1 second). After detecting the abrupt change point, the sliding body 3143 returns to the midpoint between the previous point and the previous point, locates the interface between the oil phase and the aqueous phase, and transmits the signal to the PLC control system, which drives the slider to slide up and down on the tank to move to the oil-water two-phase interface. The PLC control system starts the external air pump, which inputs positive pressure to the guide rail 3142b, pushing the embedded slider 3142c to slide axially along the guide rail to the intersection of the polygonal frame 3142a and the gasket 3145. The membrane 3147 unfolds into an annular surface, ensuring that the membrane 3147 accurately corresponds to the preset position of the (aqueous phase, liquid phase) interface, completing the initial debugging of the device. The density sensor 3141 is activated to detect the density change of the oil-water mixture in the settling tank 31 in real time, accurately locate the oil-water interface, and transmit the signal to the PLC control system. The PLC control system drives the sliding body 3143 to slide up and down to the interface, and then the membrane 3147 unfolds. The first siphon mechanism 315 at the bottom of the settling tank 31 is activated. The first siphon mechanism 315 draws the aqueous phase into the emulsification tank 32 through the suction port 3151 of the suction cup 3152, using the siphon effect to achieve... The first aqueous phase and the first oily phase undergo liquid-liquid phase separation. Simultaneously, large-particle free oil in the first oily phase is retained, while small-particle emulsified and dispersed oils are mixed into the first aqueous phase via membrane 3147 and sent to emulsification tank 32. Throughout the process, the membrane position remains unaffected by liquid disturbance. Then, air is introduced into the aerated retractable ring 3144, causing it to expand. Simultaneously, the increased inner diameter of the ring expands the membrane 3147 connected to its inner side, facilitating the discharge of the large-particle free oil intercepted by the membrane 3147 into purification tank 60. After the operation is completed, the PLC control system switches the air pump to negative pressure mode, retracting the slider along the guide rail axially and causing the edges of membrane 3147 to retract. Simultaneously, the air pump releases air from the aerated retractable ring 3144, causing it to shrink to its initial state, and the bottom first solid phase precipitate is discharged into fermentation tank 50.

[0064] After that, as Figure 1 , Figure 6As shown, an emulsifier / flocculator is added to the emulsification tank 32 to maximize the emulsification of oil droplets, which remain in the aqueous phase, while solid particles flocculate and settle, resulting in a second aqueous phase and a second solid phase. The second siphon mechanism 324 is activated to pump the second aqueous phase into the demulsification tank 33, while the second solid phase is discharged into the fermentation tank 50. Fenton's reagent is added to the demulsification tank 33 to oxidize the Tween / Span emulsifier. After a certain period, ensuring that the amount of Tween / Span minimizes damage to the PTFE membrane of the membrane filtration mechanism 36, filtration is performed. The small amount of solid particles obtained from the filtration is collected in the second reduction tank 35, reduced, and then sent to the fermentation tank 50. The filtered oil-water mixture is sent to the first reduction tank 34, reduced with sodium sulfite, and then enters the oil-water separation module 40 for separation.

[0065] Finally, as Figure 1 As shown, the reduced oil-water mixture sequentially passes through a first buffer tank 41, a coarse separation tank 42, a second buffer tank 43, and a fine separation phase 44, employing a staged filtration method. Both the coarse separation tank 42 and the fine separation phase 44 utilize a double-membrane slit separation mechanism. The coarse separation tank 42 has a larger membrane pore size, primarily filtering coarse oil (some relatively large dispersed oil droplets). The coarse oil enters the purification tank 60. The aqueous phase is transported via the second buffer tank 43 to the fine separation tank 44 for secondary filtration. The fine separation tank 44 has a smaller membrane pore size and a slower filtration speed, but it can filter even smaller oil droplets emulsified in the aqueous layer, achieving extremely fine separation of the aqueous layer substances. The oil filtered out by the fine separation phase 44 enters the purification tank 60. The aqueous phase is first transported to an alcohol precipitation tank for an alcohol precipitation reaction, separating pectin and glycogen. Functional pectin is produced from the pectin, and the glycogen is then transported to the fermentation tank 50 for fermentation to produce lactic acid.

[0066] Therefore, this invention effectively overcomes the various shortcomings of the prior art and has high industrial application value.

[0067] The above embodiments are merely illustrative of the principles and effects of the present invention and are not intended to limit the invention. Any person skilled in the art can modify or alter the above embodiments without departing from the spirit and scope of the present invention. Therefore, all equivalent modifications or alterations made by those skilled in the art without departing from the spirit and technical concept disclosed in the present invention should still be covered by the claims of the present invention.

Claims

1. A method for separating all components of organic waste, characterized in that, Includes the following steps: 1) The waste is crushed, homogenized, and acidified, then filtered to obtain filter residue I and filtrate I; Filter residue I is returned to undergo at least two homogenization, acidification, and filtration processes to obtain first filter residue and filtrate II. Filtrate I and filtrate II are combined to obtain first filtrate. 2) The first filter residue is further compressed to obtain the second filter residue and the second filtrate; 3) The first filtrate is allowed to stand and settle. The filtrate separates into a first solid phase precipitate, a first aqueous phase, and a first oil phase. The first oil phase is filtered to obtain large-particle-size free oil and small-particle-size emulsified oil and dispersed oil mixed in the first aqueous phase. 4) Add emulsifier / flocculator to the small-particle-size emulsified oil and dispersed oil mixed with the first aqueous phase to achieve emulsification and flocculation equilibrium, thus obtaining the second solid phase precipitate and the second aqueous phase containing emulsified oil droplets; 5) Add a demulsifier to the second aqueous phase containing emulsified oil droplets to demulsify, filter, and obtain an oil-water mixture and solid particles; 6) Add a reducing agent to the oil-water mixture for reduction, and then perform at least one oil-water separation to separate the emulsified oil, dispersed oil, and aqueous phase; also add a reducing agent to the solid particles for reduction. 7) The second filtrate from step 2), the large-particle-size free oil from step 3), and the emulsified and dispersed oil from step 6) are purified to prepare biodiesel. 8) The second filter residue from step 2), the first solid phase precipitate from step 3), the second solid phase precipitate from step 4), and the reduced solid particles from step 6) are subjected to a fermentation process to prepare ethanol and / or lactic acid; the aqueous phase from step 6) is subjected to an alcohol precipitation and fermentation process in sequence to prepare lactic acid and / or pectin.

2. The method for separating all components of organic waste according to claim 1, characterized in that, It also includes at least one of the following features: 11) The acidification described in step 1) is performed by controlling the pH to 3.90~4.10 using an acetic acid solution; 12) The acidification temperature described in step 1) is 75~85℃; 13) The filtration described in step 1) uses a 200-mesh filter; 31) The filter membrane used for filtering the first oil phase in step 3) is a PAN membrane; 41) The emulsifier mentioned in step 4) is Tween / Span, and the flocculant is PAC / PAM; 51) The demulsifier mentioned in step 5) is Fenton's reagent; 52) The filter membrane used in step 5) is a PTFE membrane; 61) The reducing agent mentioned in step 6) is sodium sulfite.

3. The method for separating all components of organic waste according to claim 1, characterized in that, The fermentation process described in step 8) includes the following steps: adding amylase to convert starch into glucose glycogen, filtering, adding lactic acid bacteria to the filtrate for fermentation to prepare lactic acid, and using a co-culture method to prepare ethanol from the filter residue.

4. A system for the complete separation of organic waste components, characterized in that, The system includes a pretreatment module (10), an air-assisted dynamic filtration module (20), a sedimentation-emulsification flocculation-demulsification and reduction module (30), an oil-water separation module (40), a fermentation tank (50), and a purification tank (60) connected in sequence. The pretreatment module (10) includes a crushing unit (11) and a homogenization acidification unit (12) connected in sequence. The crushing unit (11) is provided with a waste inlet (111), and the homogenization acidification unit (12) is provided with an acid feed inlet (121), a filter cake discharge outlet (122), and a slurry discharge outlet. The filter cake discharge outlet (122) is connected to a filter cake compression mechanism, which is connected to a fermentation tank (50) and a purification tank (60). The air-assisted dynamic filtration module (20) includes an air-assisted plate (21), an air-assisted cylinder (23), and a piston backflushing mechanism (22) arranged sequentially from top to bottom. The air-assisted plate (21) is located at the top of the air-assisted cylinder (23). The lower surface of the air-assisted plate (21) is a pressing surface with a uniform airflow distribution structure. The air-assisted plate is suitable for communication with an external air pump. The inlet of the air-assisted cylinder (23) is connected to the slurry outlet. A filter assembly (231) is provided at the bottom of the air-assisted cylinder (23). Above the filter assembly (231) and the air-assisted cylinder (22) 3) The bottom side is provided with a slurry return port (232), which is connected to the inlet of the homogenization acidification unit (12). The piston backflushing mechanism (22) includes a backflushing piston plate (222) that can be adjusted to open and close, located below the air-assisted cylinder (23). The backflushing piston plate (222) is suitable to be connected to an external water pump. When closed, it is suitable to spray water to backflush and clean the filter assembly (231). When open, it is suitable to discharge the filtrate passing through the filter assembly (231) into the sedimentation-emulsification flocculation-demulsification and reduction module (30). The sedimentation-emulsification-flocculation-demulsification and reduction module (30) includes a sedimentation tank (31), an emulsification tank (32), a demulsification tank (33), and a reduction tank connected in sequence; the sedimentation tank (31) is connected to the bottom of the backflushing piston plate (222), and the sedimentation tank (31), the emulsification tank (32), and the reduction tank are also connected to the fermentation tank (50) respectively; The oil-water separation module (40) includes at least one buffer tank and at least one separation tank connected together. The buffer tank is connected to a reduction tank. The separation tank includes an aqueous phase outlet and an oil phase outlet. The oil phase outlet is connected to a purification tank (60), and the aqueous phase outlet is connected to a fermentation tank (50).

5. The organic waste complete component separation treatment system according to claim 4, characterized in that, It also includes at least one of the following features: A1) The filter cake compression mechanism includes a filtrate outlet and a filter cake outlet, wherein the filtrate outlet is connected to a purification tank (60) and the filter cake outlet is connected to a fermentation tank (50). A2) The settling tank (31) includes a first oil phase outlet (311), a first aqueous phase outlet (312) and a first solid phase precipitate outlet (313). The first oil phase outlet (311) is connected to the purification tank (60), the first aqueous phase outlet (312) is connected to the emulsification tank (32), and the first solid phase precipitate outlet (313) is connected to the fermentation tank (50). A3) The emulsifying tank (32) includes an emulsifying / flocculating agent feed port (321), a second aqueous phase outlet (322) and a second solid phase outlet (323). The second aqueous phase outlet (322) is connected to the demulsifying tank (33), and the second solid phase outlet (323) is connected to the fermentation tank (50). A4) The demulsifier tank (33) includes a demulsifier inlet (331); A5) A membrane filtration mechanism (36) is provided between the demulsifying tank (33) and the reduction tank. The reduction tank includes a first reduction tank (34) and a second reduction tank (35). The membrane filtration mechanism (36) is adapted to pass the membrane filtrate into the first reduction tank (34) and to pass the membrane filter residue into the second reduction tank (35). The first reduction tank (34) is connected to the oil-water separation module (40), and the second reduction tank (35) is connected to the fermentation tank (50). A6) The oil-water separation module (40) includes a first buffer tank (41), a coarse separation tank (42), a second buffer tank (43) and a fine separation phase (44) connected in sequence. The first buffer tank (41) is connected to a reduction tank, and the coarse separation tank (42) and the fine separation phase (44) are both connected to a purification tank (60).

6. The organic waste complete component separation treatment system according to claim 5, characterized in that, It also includes at least one of the following features: A21) The settling tank (31) is also provided with a deformable membrane mechanism (314), which is connected to the first oil phase outlet (311) and is suitable for discharging large-particle-size free oil. A22) The settling tank (31) is provided with a first siphon mechanism (315), which is connected to the first aqueous phase outlet (312) and is suitable for discharging aqueous phase and small particle size emulsified oil and dispersed oil; A31) The emulsifying tank (32) is provided with a second siphon mechanism (324), which is connected to the second aqueous phase outlet (322) and is suitable for discharging the second aqueous phase containing emulsified oil droplets; A51) Both the first reduction tank (34) and the second reduction tank (35) are equipped with a reducing agent feeding port (345); A61) The coarse separation tank (42) includes a third aqueous phase outlet (421) and a second oil phase outlet (422). The third aqueous phase outlet (421) is connected to the second buffer tank (43), and the second oil phase outlet (422) is connected to the purification tank (60). A62) The finely separated phase (44) includes a fourth aqueous phase outlet (441) and a third oil phase outlet (442). The third oil phase outlet (442) is connected to the purification tank (60), and the fourth aqueous phase outlet (441) is connected to the fermentation tank (50) through the alcohol precipitation tank.

7. The organic waste complete component separation treatment system according to claim 6, characterized in that, It also includes at least one of the following features: (A211) The settling tank (31) has a slide rail that can move up and down on its inner wall. The deformable membrane mechanism (314) includes a density sensor (3141), a membrane frame (3142), a slide body (3143), an inflatable telescopic ring (3144), a gasket (3145), a ring bracket (3146), and a membrane body (3147). The slide body (3143) is slidably connected to the slide rail on the settling tank (31). The slide body (3143) is provided with an air pump connection port. The density sensor (3141) is located on the top of the slide body (3143). The membrane frame (3142) includes a polygonal frame (3142a), several guide rails (3142b), and a slider (3142c) embedded in each guide rail and slidable along the guide rail axis. The gasket (3145) is sleeved on the polygonal frame (3142a). 142a) Around the perimeter, the guide rail (3142a) is a hollow tubular structure. One end of the guide rail (3142b) is connected to the air pump connection port, and the other end is connected to the polygonal frame (3142a). The membrane (3147) is cylindrical. The two ends of the membrane (3147) are fixedly connected to the inner side of the inflatable retractable ring (3144) and the slider (3142c) respectively. The membrane (3147) at the end of the slider (3142c) extends and connects to the first grease phase outlet (311). The ring bracket (3146) is fixed below the sliding body (3143). The inflatable retractable ring (3144) is located at the end of the ring bracket (3146). The inflatable retractable ring (3144) is provided with an air inlet. The air inlet is connected to the air pump connection port. The air pump connection port is suitable for connecting to an external air pump. A221) The first siphon mechanism (315) includes a water pump and several pipes connected to the water pump, and each pipe end is connected to a suction cup (3152) containing several suction ports (3151).

8. The organic waste complete component separation treatment system according to claim 4, characterized in that, The separation chamber is equipped with a double-membrane slit separation mechanism, which is suitable for oil-water separation.

9. The organic waste complete component separation treatment system according to claim 8, characterized in that, The dual-membrane slit separation mechanism consists of a hydrophilic membrane and a hydrophobic membrane, which are arranged in parallel, forming a slit between them for oil-water separation.

10. The organic waste complete component separation treatment system according to claim 9, characterized in that, The width of the slit is 3.5 to 4.5 mm; preferably, the width of the slit is 4 mm.

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