An organic solid waste treatment system and a treatment method thereof

Abstract

The present application relates to the technical field of organic solid waste resource processing, and discloses an organic solid waste processing system and a processing method thereof, wherein the organic solid waste processing system comprises: a mixing device for mixing solid residues discharged by a low-temperature oil magnetic cracking device with azeotrope; a multi-stage distillation column for thermally distilling and separating components with different boiling point ranges; a crystallization inhibitor spraying device for spraying a crystallization inhibitor to the inner wall of the multi-stage distillation column and the surface of the inner component of the multi-stage distillation column during distillation, so as to inhibit the adhesion of tar polymerization products; and a gradient condensation trap array for multi-stage condensation and trapping of distilled steam. The organic solid waste processing system and the processing method thereof improve the separation efficiency of components with different boiling points through cooperation of the multi-stage distillation column and the gradient condensation trap array, and realize anti-coking in the whole process through the crystallization inhibitor spraying device, thereby reducing the cleaning frequency of the equipment.

Description

Technical Field

[0001] This invention relates to the technical field of resource utilization of organic solid waste, and in particular to an organic solid waste treatment system and its treatment method. Background Technology

[0002] Low-temperature oil magnetic pyrolysis technology, as a method for treating organic solid waste, can convert oily waste into recyclable oil and gas resources, and has significant application prospects in reducing environmental pollution and promoting resource recycling. However, after the pyrolysis process, a certain amount of solid residue will still remain in the system. The solid residue has a complex composition, containing not fully pyrolyzed long-chain organic matter, as well as inert substances and metal compounds.

[0003] Currently, the main methods for treating solid residues are simple incineration or direct landfill, which fail to effectively recover the potential combustible components and valuable ingredients, and pose a risk of secondary pollution.

[0004] Because the components in the solid residue have a wide range of boiling points and large differences in volatility, it is difficult to achieve accurate separation of different components using a single distillation method. This can easily lead to problems such as the loss of low-boiling-point substances due to entrainment, low recovery rate of medium-boiling-point oils and waxes, and difficulty in converting high-boiling-point tar substances. In addition, during the heating process, tar substances are prone to polymerization and coking, causing equipment blockage, and overlapping contamination between fractions often occurs, affecting separation purity and system stability. Summary of the Invention

[0005] Therefore, the purpose of this invention is to overcome the problems of complex composition and wide boiling point distribution of solid residues generated after processing organic solid waste by existing low-temperature oil magnetic pyrolysis technology, making precise separation difficult. Simultaneously, it addresses the issue that unsaturated hydrocarbons in tar-like substances are prone to free radical polymerization during heating distillation, forming coke deposits on the inner wall of the equipment and causing blockages. This invention proposes an organic solid waste treatment system and method. Through the combination of multi-stage distillation towers and gradient condenser arrays, the separation efficiency of components with different boiling points is improved. A crystallization inhibitor spraying device forms an inhibitor coating before distillation, providing an anti-coking foundation for subsequent distillation. Inhibitor powder is continuously sprayed during distillation to achieve full-process anti-coking, reducing the frequency of equipment cleaning.

[0006] To address the aforementioned technical problems, the present invention provides an organic solid waste treatment system, comprising:

[0007] A mixing device is used to mix the solid residue discharged from the low-temperature oil magnetic pyrolysis equipment with an azeotropic agent to reduce the apparent boiling point of tar-like substances.

[0008] A multi-stage distillation column, connected to the mixing device, includes a low-boiling-point section, a medium-boiling-point section, and a high-boiling-point section, used for heating and distilling components with different boiling point ranges to separate them.

[0009] A crystallization inhibitor spraying device is connected to the multi-stage distillation column and is used to spray crystallization inhibitors onto the inner wall of the multi-stage distillation column and the surface of the components inside the multi-stage distillation column during the distillation process to inhibit the adhesion of tar polymerization products.

[0010] A gradient condenser array is connected to the outlets of each boiling point fraction of the multi-stage distillation column to perform multi-stage condensation and collection of the distilled vapor.

[0011] Preferably, the mixing device has a first air outlet and a first feed inlet at the top; the mixing device has a material distributor, a ceramic packing layer and a gas distributor arranged sequentially from top to bottom; and the mixing device has a first air inlet and a first discharge outlet at the bottom.

[0012] The material distributor includes a rotary spreading disc, which is located below the first feed inlet and is used to evenly spread solid residue.

[0013] The gas distributor includes an annular jet pipe connected to the first air inlet, and the annular jet pipe is provided with multiple upward jet holes for uniformly spraying azeotropic agent vapor.

[0014] The ceramic packing layer includes multiple stacked Raschig rings to increase the contact area and contact time between solid residues and azeotropic vapors.

[0015] Preferably, the multi-stage distillation column is provided with a second feed inlet at the top, and the second feed inlet is connected to the first discharge outlet;

[0016] The multi-stage distillation column is provided with the following sections from top to bottom: a low-boiling point section, a medium-boiling point section, and a high-boiling point section; each boiling point section is provided with a fraction outlet; each boiling point section is provided with multiple layers of trays, and heating coils are provided between adjacent trays to control the temperature of the corresponding boiling point section.

[0017] The multi-stage distillation tower is equipped with a second discharge port at the bottom, which is used to discharge components with a boiling point higher than 450°C for subsequent solidification treatment.

[0018] Preferably, the crystallization inhibitor spraying device includes a coating mechanism and a powder spraying mechanism;

[0019] The coating mechanism includes multiple sets of annular spray pipes, each set of annular spray pipes being respectively installed at the top of the multi-stage distillation column, the low-boiling point section, the medium-boiling point section, and the high-boiling point section; each annular spray pipe is equipped with multiple rotatable nozzles for spraying the inhibitor suspension onto the inner wall of the multi-stage distillation column and the surface of the heating coil.

[0020] The powder spraying mechanism includes a first nozzle group, a second nozzle group, a third nozzle group, and a fourth nozzle group; wherein, the first nozzle group is located at the top of the multi-stage distillation column with the nozzles facing downwards; the second nozzle group is located between the trays in the low-boiling-point section with the nozzles horizontally positioned; the third nozzle group is located between the trays in the medium-boiling-point section with the nozzles horizontally positioned; and the fourth nozzle group is located on one side of the heating coil in the high-boiling-point section with the nozzles facing the heating coil.

[0021] Preferably, the gradient condensation trap array includes a first condensation structure, a second condensation structure, and a third condensation structure;

[0022] Each condensation structure includes a primary condensation trap, a secondary condensation trap, and a tertiary condensation trap connected in series.

[0023] The first-stage condenser of the first condensing structure is connected to the outlet of the low-boiling-point fraction; the first-stage condenser of the second condensing structure is connected to the outlet of the medium-boiling-point fraction; and the first-stage condenser of the third condensing structure is connected to the outlet of the high-boiling-point fraction.

[0024] Both the first-stage condenser of the first condensing structure and the first-stage condenser of the second condensing structure are equipped with a first reflux pipe. One end of each first reflux pipe is connected to the liquid collection tank outlet of the corresponding first-stage condenser, and the other end of the first reflux pipe is connected to the upper reflux port of the high-boiling point section of the multi-stage distillation column.

[0025] The third reflux pipe is provided in the three-stage condenser of the third condensing structure. One end of the third reflux pipe is connected to the liquid collection tank outlet of the three-stage condenser of the third condensing structure, and the other end of the third reflux pipe is connected to the upper reflux port of the middle boiling point section of the multi-stage distillation column.

[0026] Both the first and second condensing structures have a second reflux pipe in their three-stage condenser traps. One end of each second reflux pipe is connected to the outlet of the liquid collection tank of the corresponding three-stage condenser trap, and the other end of the second reflux pipe is connected to the upper reflux port of the low-boiling point section of the multi-stage distillation column.

[0027] The primary condenser of the third condensation group is equipped with a slag discharge pipeline for collecting components with boiling points higher than 450°C for subsequent solidification treatment.

[0028] On the other hand, the present invention provides a method for treating organic solid waste using an organic solid waste treatment system, comprising:

[0029] Before starting the multi-stage distillation column, an inhibitor coating is formed on the inner wall of the multi-stage distillation column and the surface of the heating coil.

[0030] The solid residue is mixed with the azeotropic agent vapor in a countercurrent manner to obtain a first mixture;

[0031] Start the multi-stage distillation column and sequentially distill the first mixture in the low-boiling-point section, the medium-boiling-point section, and the high-boiling-point section of the multi-stage distillation column.

[0032] During the distillation process, inhibitor powder is continuously sprayed into the multi-stage distillation tower;

[0033] The steam from the outlets of the low-boiling-point, medium-boiling-point, and high-boiling-point fractions was subjected to a three-stage gradient condensation process. Components with different boiling ranges were separated and collected through gradient condensation: components with boiling points in the range of 80℃ to 150℃ were classified as light oil products, components with boiling points in the range of 150℃ to 280℃ were classified as medium oil products, and components with boiling points in the range of 280℃ to 450℃ were classified as heavy tar products.

[0034] Preferably, the method for forming the inhibitor coating includes: spraying an inhibitor suspension onto the inner wall of a multi-stage distillation column and the surface of a heating coil, then raising the temperature inside the multi-stage distillation column to 150°C to 200°C and maintaining the temperature to dry, thereby forming an inhibitor suspension and an inhibitor coating; wherein the concentration of the inhibitor suspension is 10wt% to 15wt%; and the thickness of the inhibitor coating is 50 micrometers to 100 micrometers.

[0035] The first mixture has an apparent boiling point of 50°C to 80°C, and the azeotropic agent content in the first mixture is 5wt% to 8wt%; wherein the azeotropic agent is tetrahydronaphthalene.

[0036] Preferably, the temperature control range of the low boiling point section is 80°C to 150°C, used to separate components with boiling points in the range of 80°C to 150°C;

[0037] The temperature control range of the intermediate boiling point range is 150°C to 280°C, which is used to separate components with boiling points in the range of 150°C to 280°C.

[0038] The temperature control range of the high boiling point section is 280℃ to 450℃, which is used to separate components with boiling points in the range of 280℃ to 450℃.

[0039] The amount of the inhibitor powder injected is 0.5% to 1% of the mass of the first mixture.

[0040] Preferably, the three-stage gradient condensation treatment of the steam from the low-boiling-point, medium-boiling-point, and high-boiling-point fraction outlets includes:

[0041] The vapor from the low-boiling-point fraction outlet is sequentially passed through a primary condenser at 70℃±5℃ to collect heavy components with boiling points above 150℃, through a secondary condenser at 40℃±5℃ to collect light oil products with boiling points in the range of 80℃ to 150℃, and through a tertiary condenser at 5℃±5℃ to collect extremely light components with boiling points below 80℃.

[0042] The vapor from the mid-boiling point fraction outlet is sequentially passed through a primary condenser at 140℃±5℃ to collect heavy components with boiling points above 280℃, through a secondary condenser at 80℃±5℃ to collect medium-quality oil products with boiling points in the range of 150℃ to 280℃, and through a tertiary condenser at 20℃±5℃ to collect light components with boiling points below 150℃.

[0043] The vapor from the high-boiling-point fraction outlet is sequentially passed through a primary condenser at 260℃±5℃ to collect components with boiling points above 450℃, through a secondary condenser at 180℃±5℃ to collect heavy tar products with boiling points in the range of 280℃ to 450℃, and through a tertiary condenser at 100℃±5℃ to collect medium-boiling-point components with boiling points below 280℃.

[0044] Preferably, the three-stage gradient condensation treatment of the steam from the low-boiling-point, medium-boiling-point, and high-boiling-point fraction outlets includes:

[0045] The heavy components that are captured by the first-stage condenser in the low-boiling-point section of the multi-stage distillation column are returned to the high-boiling-point section for secondary distillation, while the light components that are captured by the third-stage condenser in the low-boiling-point section of the multi-stage distillation column are returned to the low-boiling-point section for secondary distillation.

[0046] The heavy components, which are captured by a primary condenser in the middle boiling point section of the multi-stage distillation column, are returned to the high boiling point section for secondary distillation. The light components, which are captured by a tertiary condenser in the middle boiling point section of the multi-stage distillation column, are returned to the low boiling point section for secondary distillation.

[0047] The light components captured by the three-stage condenser in the high-boiling-point section of the steam are returned to the middle-boiling-point section of the multi-stage distillation column for secondary distillation.

[0048] Compared with the prior art, the above-described technical solution of the present invention has the following advantages:

[0049] The organic solid waste treatment system of the present invention improves the separation efficiency of components with different boiling points by combining multi-stage distillation towers with gradient condenser arrays; by using a crystallization inhibitor spraying device, an inhibitor coating is formed before distillation, providing an anti-coking basis for subsequent distillation; and inhibitor powder is continuously sprayed during the distillation process to achieve anti-coking throughout the process, reducing the frequency of equipment cleaning.

[0050] The organic solid waste treatment system of this invention involves pre-coating the inner wall of a multi-stage distillation tower with an inhibitor coating before distillation to form an initial anti-adhesion barrier and delay the coking initiation time. The solid residue is then mixed with azeotropic agent vapor in a counter-current manner to lower the apparent boiling point of the tar, thereby reducing the polymerization rate. During distillation, inhibitor powder is continuously sprayed to dynamically replenish the protective layer, reducing the coking rate of the heating coils and the frequency of equipment cleaning, thus extending the operating cycle. This invention improves the purity and yield of light oil, medium oil, and heavy tar products through the synergistic effect of three-stage temperature gradient distillation (80℃ to 150℃, 150℃ to 280℃, 280℃ to 450℃) and three-stage gradient condensation (capturing heavy components, collecting products, and capturing light components). Attached Figure Description

[0051] To make the content of this invention easier to understand, the invention will be further described in detail below with reference to specific embodiments and accompanying drawings.

[0052] Figure 1 This is a schematic diagram of an organic solid waste treatment system according to an embodiment of the present invention.

[0053] Figure 2 This is a schematic flowchart of a method for treating organic solid waste in a preferred embodiment of the present invention.

[0054] Explanation of reference numerals in the accompanying drawings: 1. Mixing device; 11. First gas outlet; 12. First feed inlet; 13. Material distributor; 14. Ceramic packing layer; 15. Gas distributor; 16. First discharge outlet; 2. Multistage distillation column; 21. Second discharge outlet; 22. Low boiling point section; 23. Medium boiling point section; 24. High boiling point section; 25. Distillate outlet; 26. Tray; 27. Heating coil; 31. Annular spray pipe; 32. Spray nozzle; 33. First nozzle group; 4. Gradient condenser array; 41. First-stage condenser; 42. Second-stage condenser; 43. Third-stage condenser; 44. Liquid collection tank outlet; 45. Heat exchanger. Detailed Implementation

[0055] The present invention will be further described below with reference to the accompanying drawings and specific embodiments, so that those skilled in the art can better understand and implement the present invention. However, the embodiments described are not intended to limit the present invention.

[0056] Example 1: This example discloses an organic solid waste treatment system.

[0057] refer to Figure 1 The organic solid waste treatment system of this embodiment includes: a mixing device 1, a multi-stage distillation tower 2, a crystallization inhibitor injection device, and a gradient condenser array 4.

[0058] In application, the low-temperature oil magnetic pyrolysis equipment performs low-temperature oil magnetic pyrolysis on the solid portion of pretreated organic solid waste, generating pyrolysis gas and solid residue. Pretreatment of organic solid waste includes sorting, crushing, drying, and three-phase separation using existing technologies, which will not be elaborated here.

[0059] The mixing device 1 in this embodiment is used to mix the solid residue discharged from the low-temperature oil magnetic pyrolysis equipment with an azeotropic agent to reduce the apparent boiling point of tar-like substances.

[0060] During application, the mixing device 1 is kept under a slightly positive pressure, for example, 0.05 MPa to 0.1 MPa. The mixing device 1 is made of a corrosion-resistant material.

[0061] The mixing device 1 in this embodiment is provided with a first air outlet 11 and a first feed inlet 12 at the top.

[0062] The first feed inlet 12 is connected to the solid residue outlet of the low-temperature oil magnetic pyrolysis equipment. Furthermore, the output end of the first feed inlet 12 is equipped with a first feed valve for adjusting the feed rate.

[0063] The first outlet 11 is used to discharge unliquefied gas from the mixing device 1. Furthermore, the first outlet 11 is connected to a first collecting device, which contains a condenser.

[0064] The mixing device 1 in this embodiment is provided with a first air inlet and a first discharge outlet 16 at the bottom.

[0065] The first discharge port 16 is used to discharge the mixture inside the mixing device 1. Furthermore, the first discharge port 16 is provided with a first discharge valve at its output end for adjusting the discharge speed.

[0066] The first air inlet is used to charge the azeotropic agent vapor into the mixing device 1. Further, the first air inlet is connected to the azeotropic agent storage tank and the vaporizer; the azeotropic agent is heated and vaporized in the vaporizer and then enters the mixing device 1 through the first air inlet. Even further, the azeotropic agent can be tetrahydronaphthalene, and the liquid tetrahydronaphthalene is heated to 220°C to 250°C in the vaporizer to vaporize.

[0067] In this embodiment, the mixing device 1 is provided with a material distributor 13, a ceramic packing layer 14, and a gas distributor 15 from top to bottom.

[0068] The material distributor 13 includes a rotating spreading disc, which is positioned below the first feed inlet 12 to evenly spread solid residue. In application, the rotating spreading disc has multiple spreading holes with a diameter of 5mm to 10mm. In practical applications, the rotating spreading disc rotates at a speed of 10rpm / min to 30rpm / min, evenly spreading the solid residue into a curtain-like pattern to prevent localized accumulation.

[0069] The gas distributor 15 includes an annular jet pipe connected to the first air inlet. Further, the diameter of the annular jet pipe matches the inner diameter of the mixing device 1. Even further, the annular jet pipe has multiple upward-facing jet holes for uniformly injecting azeotropic agent vapor upwards. The distance between adjacent jet holes is 100 mm to 150 mm; the diameter of each jet hole is 3 mm to 5 mm.

[0070] The ceramic packing layer 14 comprises multiple stacked Raschig rings to increase the contact area and contact time between solid residues and azeotropic agent vapors. Further, the ceramic packing layer 14 comprises 2 to 3 stacked Raschig rings, each layer having a height of 0.5 m to 1.0 m.

[0071] In this embodiment, the multi-stage distillation column 2 is connected to the mixing device 1 and includes a low-boiling-point section 22, a medium-boiling-point section 23 and a high-boiling-point section 24, which are used to separate components with different boiling point ranges by heating and distillation.

[0072] In application, the multistage distillation column 2 is operated under a slightly positive pressure, such as 0.05 MPa to 0.1 MPa, or at atmospheric pressure. The multistage distillation column 2 is made of corrosion-resistant material.

[0073] In practical applications, the height of the multi-stage distillation column 2 is 8m to 15m, and the diameter is 0.8m to 2.0m.

[0074] In this embodiment, the multi-stage distillation column 2 is provided with a second feed inlet at the top, and the second feed inlet is connected to the first discharge outlet 16.

[0075] When applied, the solid residue mixed with the azeotropic agent enters the multi-stage distillation column 2, where the lighter components move upward and the heavier components move downward.

[0076] In this embodiment, the multi-stage distillation column 2 is provided with the following sections from top to bottom: a low-boiling-point section 22, a medium-boiling-point section 23, and a high-boiling-point section 24.

[0077] In application, each boiling point segment is equipped with a distillation outlet 25 to draw steam into the gradient condenser array 4. In practical applications, each boiling point segment is equipped with multiple layers of trays 26, such as valve trays 26, to provide a gas-liquid contact surface, allowing for liquid crossflow and gas rise. Furthermore, the spacing between each layer of trays 26 is 300mm to 500mm. In actual implementation, heating coils 27 are installed between adjacent trays 26 to control the temperature of the corresponding boiling point segment: the temperature of the low boiling point segment 22 is (80, 150°C); the temperature of the medium boiling point segment 23 is (150, 280°C); and the temperature of the high boiling point segment 24 is (280, 450°C).

[0078] In this embodiment, the multi-stage distillation column 2 is provided with a second discharge port 21 at the bottom for discharging components with boiling points higher than 450°C for subsequent solidification treatment. Furthermore, a second discharge valve is provided at the output end of the second discharge port 21 for adjusting the discharge rate.

[0079] In this embodiment, the crystallization inhibitor spraying device is connected to the multi-stage distillation column 2 and is used to spray crystallization inhibitor onto the inner wall of the multi-stage distillation column 2 and the surface of the internal components of the multi-stage distillation column 2 during the distillation process to inhibit the adhesion of tar polymerization products.

[0080] In application, the crystallization inhibitor injection device includes a coating mechanism and a powder spraying mechanism. The coating mechanism forms an inhibitor coating on the inner wall of the multi-stage distillation column 2 and the surface of the heating coil 27 before startup. The powder spraying mechanism continuously sprays inhibitor powder into the multi-stage distillation column 2 during the distillation process.

[0081] The coating mechanism in this embodiment includes multiple sets of annular spray pipes 31, which are used to spray the inhibitor suspension onto the inner wall of the multi-stage distillation column 2 and the surface of the heating coil 27 to form an inhibitor coating.

[0082] In application, each group of annular spray pipes 31 is respectively installed at the top of the multi-stage distillation column 2, the low-boiling point section 22, the medium-boiling point section 23, and the high-boiling point section 24. For example, the first annular spray pipe 31 is installed at the top of the multi-stage distillation column 2; the second annular spray pipe 31 is installed at the low-boiling point section 22; the third annular spray pipe 31 is installed at the medium-boiling point section 23; and the fourth annular spray pipe 31 is installed at the high-boiling point section 24.

[0083] In practical applications, the annular spray pipe 31 connects the suspension storage tank and the high-pressure delivery pump, and each set of annular spray pipes 31 is equipped with multiple rotatable nozzles 32. The high-pressure delivery pump pressurizes the zinc borate aqueous suspension stored in the suspension storage tank to 0.5MPa to 1.0MPa and then delivers it to each rotatable nozzle 32. Furthermore, each set of annular spray pipes 31 is equipped with 5 to 10 rotatable nozzles 32 to achieve 360° uniform spraying.

[0084] The powder spraying mechanism of this embodiment includes a first nozzle group 33, a second nozzle group, a third nozzle group, and a fourth nozzle group.

[0085] In application, each nozzle group is connected to a powder storage device, which stores inhibitor powder with a particle size of 10 μm to 20 μm. Furthermore, each nozzle group comprises 4 to 6 nozzles arranged in a ring.

[0086] In practical applications, the inhibitor powder is mixed with compressed nitrogen and injected into the multi-stage distillation column 2 through nozzles. The injected inhibitor powder moves with the airflow and comes into contact with the rising tar vapor. The powder coats the surface of the tar droplets, forming a lubricating layer. Even if the tar droplets condense and aggregate, the resulting particles are loosely coated with powder, rather than dense tar deposits adhering to the wall. Simultaneously, some powder deposits on the wall surface to repair any peeling inhibitor coating.

[0087] In actual implementation, the first nozzle group 33 is located at the top of the multi-stage distillation column 2 with downward-facing nozzles, causing the inhibitor powder to move downwards and come into countercurrent contact with the rising steam. The second nozzle group is located between the trays 26 in the low-boiling-point section 22 with horizontally positioned nozzles to cover the area of ​​tray 26. The third nozzle group is located between the trays 26 in the medium-boiling-point section 23 with horizontally positioned nozzles to cover the area of ​​tray 26. The fourth nozzle group is located on one side of the heating coil 27 in the high-boiling-point section 24 with nozzles facing the heating coil 27.

[0088] In this embodiment, the gradient condenser array 4 is connected to the boiling point fraction outlets 25 of the multi-stage distillation column 2, respectively, for multi-stage condensation and collection of the distilled steam.

[0089] In application, the gradient condensation trap array 4 includes a first condensation structure, a second condensation structure, and a third condensation structure, and each condensation structure includes a first-stage condensation trap 41, a second-stage condensation trap 42, and a third-stage condensation trap 43 connected in series. Furthermore, each condensation trap includes a heat exchanger 45, which stores a heat-conducting medium.

[0090] The first-stage condenser 41 of the first condensing structure is connected to the fraction outlet 25 of the low-boiling-point section 22; the first-stage condenser 41 of the second condensing structure is connected to the fraction outlet 25 of the medium-boiling-point section 23; and the first-stage condenser 41 of the third condensing structure is connected to the fraction outlet 25 of the high-boiling-point section 24.

[0091] The liquid collection tank outlets 44 of the secondary condenser traps 42 of the first condensing structure, the second condensing structure, and the third condensing structure are respectively connected to the corresponding product collection devices.

[0092] The outer side of the primary condenser 41 of the third condensing group is covered with a heat insulation layer. At the same time, the liquid collection tank outlet 44 of the primary condenser 41 of the third condensing group is connected to the slag discharge pipeline to discharge the collected components with boiling points higher than 450°C for subsequent solidification treatment.

[0093] The top of the three-stage condenser trap 43 in the third condensation structure is provided with an exhaust port for discharging uncondensed gases such as nitrogen. Furthermore, the exhaust port is connected to an external gas processing device.

[0094] In practical applications, both the first-stage condenser 41 of the first condensing structure and the first-stage condenser 41 of the second condensing structure are equipped with a first reflux pipe. One end of each first reflux pipe is connected to the liquid collection tank outlet 44 of the corresponding first-stage condenser 41, and the other end of the first reflux pipe is connected to the upper reflux port of the high-boiling point section 24 of the multi-stage distillation column 2.

[0095] Both the first condensing structure and the second condensing structure have a second reflux pipe in the three-stage condensing trap 43. One end of each second reflux pipe is connected to the liquid collection tank outlet 44 of the corresponding three-stage condensing trap 43, and the other end of the second reflux pipe is connected to the upper reflux port of the low boiling point section 22 of the multi-stage distillation column 2.

[0096] The third condenser structure has a third reflux pipe inside the three-stage condenser trap 43. One end of the third reflux pipe is connected to the liquid collection tank outlet 44 of the three-stage condenser trap 43 of the third condenser structure, and the other end of the third reflux pipe is connected to the upper reflux port of the middle boiling point section 23 of the multi-stage distillation column 2.

[0097] In actual implementation, in the first condensation structure, the temperature of the heat-conducting medium flowing through the primary condenser 41 is 70℃±5℃, causing heavy components in the steam with a boiling point greater than 150℃ to condense into liquid, and the condensate drips into the bottom collection tank; uncondensed steam with a boiling point less than or equal to 150℃ enters the secondary condenser 42. The temperature of the heat-conducting medium flowing through the secondary condenser 42 is 40℃±5℃, causing components in the steam with a boiling point in the range of 80℃ to 150℃ to condense into liquid, and the condensate drips into the bottom collection tank for collection as light oil products; uncondensed steam with a boiling point less than 80℃ enters the tertiary condenser 43. The temperature of the heat-conducting medium flowing through the tertiary condenser 43 is 5℃±5℃, causing light components in the steam with a boiling point less than 80℃ to condense into liquid, and the condensate drips into the bottom collection tank.

[0098] In the second condensation structure, the temperature of the heat-conducting medium flowing through the primary condenser 41 is 140℃±5℃, causing heavy components in the steam with a boiling point greater than 280℃ to condense into liquid, and the condensate drips into the bottom collection tank; uncondensed steam with a boiling point less than or equal to 280℃ enters the secondary condenser 42. The temperature of the heat-conducting medium flowing through the secondary condenser 42 is 80℃±5℃, causing components in the steam with a boiling point in the range of 150℃ to 280℃ to condense into liquid, and the condensate drips into the bottom collection tank for collection as medium-quality oil products; uncondensed steam with a boiling point less than 150℃ enters the tertiary condenser 43. The temperature of the heat-conducting medium flowing through the tertiary condenser 43 is 20℃±5℃, causing light components in the steam with a boiling point less than 150℃ to condense into liquid, and the condensate drips into the bottom collection tank.

[0099] In the third condensation structure, the heat transfer medium temperature of the primary condenser 41 is 260℃±5℃, causing heavy components in the steam with a boiling point greater than 450℃ to condense and settle, and then be discharged through the slag discharge pipeline for solidification treatment; uncondensed steam with a boiling point less than or equal to 450℃ enters the secondary condenser 42. The heat transfer medium temperature of the secondary condenser 42 is 180℃±5℃, causing components in the steam with a boiling point in the range of 280℃ to 450℃ to condense into liquid, and the condensate drips into the bottom collection tank for collection as heavy tar product; uncondensed steam with a boiling point less than 280℃ enters the tertiary condenser 43. The heat transfer medium temperature of the tertiary condenser 43 is 100℃±5℃, causing light components in the steam with a boiling point less than 280℃ to condense into liquid, and the condensate drips into the bottom collection tank.

[0100] Example 2: Based on Example 1, this example discloses a treatment method for an organic solid waste treatment system.

[0101] refer to Figure 2 The treatment method of the organic solid waste treatment system in this embodiment includes steps SS1 to SS5.

[0102] Step SS1: Before starting the multistage distillation column 2, an inhibitor coating is formed on the inner wall of the multistage distillation column 2 and the surface of the heating coil 27.

[0103] When applied, the method for forming the inhibitor coating includes steps SS11 to SS12.

[0104] Step SS11: Spray the inhibitor suspension onto the inner wall of the multi-stage distillation column 2 and the surface of the heating coil 27.

[0105] When applied, the inhibitor can be zinc borate, which has good thermal stability and can form a smooth ceramic layer at high temperatures to inhibit tar adhesion.

[0106] In practical applications, the concentration of the inhibitor suspension is 10wt% to 15wt% to ensure a uniform and dense coating. When the concentration of the inhibitor suspension is below 10wt%, the resulting inhibitor coating is too thin and prone to peeling; when the concentration of the inhibitor suspension is above 15wt%, the resulting inhibitor coating is too thick and prone to cracking, and the nozzle 32 is prone to clogging.

[0107] Step SS12: After spraying the inhibitor suspension onto the inner wall of the multi-stage distillation column 2 and the surface of the heating coil 27, the temperature inside the multi-stage distillation column 2 is raised to 150°C to 200°C and kept at that temperature to dry, forming an inhibitor suspension and an inhibitor coating.

[0108] When applied, the thickness of the inhibitor coating is 50 to 100 micrometers, which can provide an effective anti-adhesion barrier and is not prone to cracking and peeling due to differences in the coefficient of thermal expansion.

[0109] Step SS2: Mix the solid residue with the azeotropic agent vapor in a countercurrent manner to obtain the first mixture.

[0110] In application, tetrahydronaphthalene is used as the azeotropic agent. Tetrahydronaphthalene has high thermal stability and is easily vaporized and recovered. At the same time, tetrahydronaphthalene can form an azeotropic system with tar-like substances in the solid residue, lowering the apparent boiling point of the solid residue and causing it to volatilize at a lower temperature. This reduces the risk of tar polymerization and coking during heating and improves separation efficiency. Specifically, the apparent boiling point of the first mixture is 50°C to 80°C, which can reduce distillation energy consumption and reduce the occurrence of free radical polymerization reactions at high temperatures, thus inhibiting coking.

[0111] In practical applications, the content of azeotropic agent in the first mixture is 5wt% to 8wt%, which can effectively reduce the apparent boiling point of the solid residue without excessively diluting the solid residue and increasing the burden on subsequent separation.

[0112] Step SS3: Start the multi-stage distillation column 2 and sequentially distill the first mixture in the low-boiling point section 22, the medium-boiling point section 23, and the high-boiling point section 24 of the multi-stage distillation column 2.

[0113] In application, the temperature control range of the low-boiling point section 22 is 80℃ to 150℃, used to separate components with boiling points in the range of 80℃ to 150℃. The temperature control range of the medium-boiling point section 23 is 150℃ to 280℃, used to separate components with boiling points in the range of 150℃ to 280℃. The temperature control range of the high-boiling point section 24 is 280℃ to 450℃, used to separate components with boiling points in the range of 280℃ to 450℃.

[0114] Step SS4: During the distillation process, inhibitor powder is continuously sprayed into the multi-stage distillation column 2.

[0115] When applied, the amount of inhibitor powder injected is 0.5% to 1% of the mass of the first mixture. It can form a dynamic protective layer during distillation, which can encapsulate tar droplets and repair the inhibitor coating. At the same time, it can prevent excessive inhibitor powder from entering the product and affecting the product purity.

[0116] Step SS5: The steam from the outlet 25 of the low-boiling-point section 22, the medium-boiling-point section 23, and the high-boiling-point section 24 is subjected to a three-stage gradient condensation treatment. The steam from the low-boiling-point section 22 at 80℃ to 150℃ is collected as light oil product, the steam from the medium-boiling-point section 23 at 150℃ to 280℃ is collected as medium oil product, and the steam from the high-boiling-point section 24 at 280℃ to 450℃ is collected as heavy tar product.

[0117] When applied, step SS5 includes steps SS51 to SS53.

[0118] Step SS51: The vapor from the low-boiling-point section 22 distillate outlet 25 is sequentially passed through a primary condenser 41 at 70℃±5℃ to collect heavy components with boiling points above 150℃, through a secondary condenser 42 at 40℃±5℃ to collect light oil products with boiling points in the range of 80℃ to 150℃, and through a tertiary condenser 43 at 5℃±5℃ to collect extremely light components with boiling points below 80℃.

[0119] Step SS52: The vapor from the outlet 25 of the middle boiling point section 23 is sequentially passed through a primary condenser 41 at 140℃±5℃ to collect heavy components with boiling points above 280℃, through a secondary condenser 42 at 80℃±5℃ to collect medium-quality oil products with boiling points in the range of 150℃ to 280℃, and through a tertiary condenser 43 at 20℃±5℃ to collect light components with boiling points below 150℃.

[0120] Step SS53: The steam from the outlet 25 of the high-boiling-point section 24 is sequentially passed through a primary condenser 41 at 260℃±5℃ to collect components with boiling points above 450℃, through a secondary condenser 42 at 180℃±5℃ to collect heavy tar products with boiling points in the range of 280℃ to 450℃, and through a tertiary condenser 43 at 100℃±5℃ to collect medium-boiling-point components with boiling points below 280℃.

[0121] In practical applications, step SS5 includes steps SS54 to SS58.

[0122] Step SS54: The heavy components captured by the primary condenser 41 of the steam in the low-boiling-point section 22 are returned to the high-boiling-point section 24 of the multi-stage distillation column 2 for secondary distillation.

[0123] Step SS55: The light components captured by the three-stage condenser 43 of the vapor in the low-boiling-point section 22 are returned to the low-boiling-point section 22 of the multi-stage distillation column 2 for secondary distillation.

[0124] Step SS56: The heavy components captured by the first-stage condenser 41 in the middle boiling point section 23 of the steam are returned to the high boiling point section 24 of the multi-stage distillation column 2 for secondary distillation.

[0125] Step SS57: The light components captured by the three-stage condenser 43 in the middle boiling point section 23 of the steam are returned to the low boiling point section 22 of the multi-stage distillation column 2 for secondary distillation.

[0126] Step SS58: The light components captured by the three-stage condenser 43 of the steam in the high-boiling-point section 24 are returned to the medium-boiling-point section 23 of the multi-stage distillation column 2 for secondary distillation.

[0127] Obviously, the above embodiments are merely illustrative examples for clear explanation and are not intended to limit the implementation. Those skilled in the art will recognize that other variations or modifications can be made based on the above description. It is neither necessary nor possible to exhaustively list all possible implementations here. However, obvious variations or modifications derived therefrom are still within the scope of protection of this invention.

Claims

1. An organic solid waste treatment system, characterized in that, include: A mixing device is used to mix the solid residue discharged from the low-temperature oil magnetic pyrolysis equipment with an azeotropic agent to reduce the apparent boiling point of tar-like substances. A multi-stage distillation column, connected to the mixing device, includes a low-boiling-point section, a medium-boiling-point section, and a high-boiling-point section, used for heating and distilling components with different boiling point ranges to separate them. A crystallization inhibitor spraying device is connected to the multi-stage distillation column and is used to spray crystallization inhibitors onto the inner wall of the multi-stage distillation column and the surface of the components inside the multi-stage distillation column during the distillation process to inhibit the adhesion of tar polymerization products. A gradient condenser array is connected to the outlets of each boiling point fraction of the multi-stage distillation column to perform multi-stage condensation and collection of the distilled vapor.

2. The organic solid waste treatment system according to claim 1, characterized in that, The mixing device is provided with a first air outlet and a first feed inlet at the top; the mixing device is provided with a material distributor, a ceramic packing layer and a gas distributor in sequence from top to bottom; the mixing device is provided with a first air inlet and a first feed outlet at the bottom; The material distributor includes a rotary spreading disc, which is located below the first feed inlet and is used to evenly spread solid residue. The gas distributor includes an annular jet pipe connected to the first air inlet, and the annular jet pipe is provided with multiple upward jet holes for uniformly spraying azeotropic agent vapor. The ceramic packing layer includes multiple stacked Raschig rings to increase the contact area and contact time between solid residues and azeotropic vapors.

3. The organic solid waste treatment system according to claim 2, characterized in that, The multi-stage distillation column is provided with a second feed inlet at the top, and the second feed inlet is connected to the first discharge outlet; The multi-stage distillation column is provided with the following sections from top to bottom: a low-boiling point section, a medium-boiling point section, and a high-boiling point section; each boiling point section is provided with a fraction outlet; each boiling point section is provided with multiple layers of trays, and heating coils are provided between adjacent trays to control the temperature of the corresponding boiling point section. The multi-stage distillation tower is equipped with a second discharge port at the bottom, which is used to discharge components with a boiling point higher than 450°C for subsequent solidification treatment.

4. The organic solid waste treatment system according to claim 1, characterized in that, The crystallization inhibitor injection device includes a coating mechanism and a powder spraying mechanism; The coating mechanism includes multiple sets of annular spray pipes, each set of annular spray pipes being respectively installed at the top of the multi-stage distillation column, the low-boiling point section, the medium-boiling point section, and the high-boiling point section; each annular spray pipe is equipped with multiple rotatable nozzles for spraying the inhibitor suspension onto the inner wall of the multi-stage distillation column and the surface of the heating coil. The powder spraying mechanism includes a first nozzle group, a second nozzle group, a third nozzle group, and a fourth nozzle group; wherein, the first nozzle group is located at the top of the multi-stage distillation column with the nozzles facing downwards; the second nozzle group is located between the trays in the low-boiling-point section with the nozzles horizontally positioned; the third nozzle group is located between the trays in the medium-boiling-point section with the nozzles horizontally positioned; and the fourth nozzle group is located on one side of the heating coil in the high-boiling-point section with the nozzles facing the heating coil.

5. The organic solid waste treatment system according to claim 1, characterized in that, The gradient condensation trap array includes a first condensation structure, a second condensation structure, and a third condensation structure; Each condensation structure includes a primary condensation trap, a secondary condensation trap, and a tertiary condensation trap connected in series. The first-stage condenser of the first condensing structure is connected to the outlet of the low-boiling-point fraction; the first-stage condenser of the second condensing structure is connected to the outlet of the medium-boiling-point fraction; and the first-stage condenser of the third condensing structure is connected to the outlet of the high-boiling-point fraction. Both the first-stage condenser of the first condensing structure and the first-stage condenser of the second condensing structure are equipped with a first reflux pipe. One end of each first reflux pipe is connected to the liquid collection tank outlet of the corresponding first-stage condenser, and the other end of the first reflux pipe is connected to the upper reflux port of the high-boiling point section of the multi-stage distillation column. The third reflux pipe is provided in the three-stage condenser of the third condensing structure. One end of the third reflux pipe is connected to the liquid collection tank outlet of the three-stage condenser of the third condensing structure, and the other end of the third reflux pipe is connected to the upper reflux port of the middle boiling point section of the multi-stage distillation column. Both the first and second condensing structures have a second reflux pipe in their three-stage condenser traps. One end of each second reflux pipe is connected to the outlet of the liquid collection tank of the corresponding three-stage condenser trap, and the other end of the second reflux pipe is connected to the upper reflux port of the low-boiling point section of the multi-stage distillation column. The primary condenser of the third condensation group is equipped with a slag discharge pipeline for collecting components with boiling points higher than 450°C for subsequent solidification treatment.

6. A method for treating organic solid waste according to any one of claims 1 to 5, characterized in that, include: Before starting the multi-stage distillation column, an inhibitor coating is formed on the inner wall of the multi-stage distillation column and the surface of the heating coil. The solid residue is mixed with the azeotropic agent vapor in a countercurrent manner to obtain a first mixture; Start the multi-stage distillation column and sequentially distill the first mixture in the low-boiling-point section, the medium-boiling-point section, and the high-boiling-point section of the multi-stage distillation column. During the distillation process, inhibitor powder is continuously sprayed into the multi-stage distillation tower; The steam from the outlets of the low-boiling-point, medium-boiling-point, and high-boiling-point fractions was subjected to a three-stage gradient condensation process. Components with different boiling ranges were separated and collected through gradient condensation: components with boiling points in the range of 80℃ to 150℃ were classified as light oil products, components with boiling points in the range of 150℃ to 280℃ were classified as medium oil products, and components with boiling points in the range of 280℃ to 450℃ were classified as heavy tar products.

7. The treatment method of the organic solid waste treatment system according to claim 6, characterized in that, The method for forming the inhibitor coating includes: spraying an inhibitor suspension onto the inner wall of a multi-stage distillation column and the surface of a heating coil, then raising the temperature inside the multi-stage distillation column to 150°C to 200°C and maintaining the temperature to dry, thereby forming an inhibitor suspension and an inhibitor coating; wherein the concentration of the inhibitor suspension is 10wt% to 15wt%; and the thickness of the inhibitor coating is 50 micrometers to 100 micrometers. The first mixture has an apparent boiling point of 50°C to 80°C, and the azeotropic agent content in the first mixture is 5wt% to 8wt%; wherein the azeotropic agent is tetrahydronaphthalene.

8. The treatment method of the organic solid waste treatment system according to claim 6, characterized in that, The temperature control range of the low boiling point section is 80°C to 150°C, which is used to separate components with boiling points in the range of 80°C to 150°C. The temperature control range of the intermediate boiling point range is 150°C to 280°C, which is used to separate components with boiling points in the range of 150°C to 280°C. The temperature control range of the high boiling point section is 280℃ to 450℃, which is used to separate components with boiling points in the range of 280℃ to 450℃. The amount of the inhibitor powder injected is 0.5% to 1% of the mass of the first mixture.

9. The treatment method of the organic solid waste treatment system according to claim 6, characterized in that, The three-stage gradient condensation treatment of the steam from the low-boiling-point, medium-boiling-point, and high-boiling-point fraction outlets includes: The vapor from the low-boiling-point fraction outlet is sequentially passed through a primary condenser at 70℃±5℃ to collect heavy components with boiling points above 150℃, through a secondary condenser at 40℃±5℃ to collect light oil products with boiling points in the range of 80℃ to 150℃, and through a tertiary condenser at 5℃±5℃ to collect extremely light components with boiling points below 80℃. The vapor from the mid-boiling point fraction outlet is sequentially passed through a primary condenser at 140℃±5℃ to collect heavy components with boiling points above 280℃, through a secondary condenser at 80℃±5℃ to collect medium-quality oil products with boiling points in the range of 150℃ to 280℃, and through a tertiary condenser at 20℃±5℃ to collect light components with boiling points below 150℃. The vapor from the high-boiling-point fraction outlet is sequentially passed through a primary condenser at 260℃±5℃ to collect components with boiling points above 450℃, through a secondary condenser at 180℃±5℃ to collect heavy tar products with boiling points in the range of 280℃ to 450℃, and through a tertiary condenser at 100℃±5℃ to collect medium-boiling-point components with boiling points below 280℃.

10. The treatment method of the organic solid waste treatment system according to claim 6, characterized in that, The three-stage gradient condensation treatment of the steam from the low-boiling-point, medium-boiling-point, and high-boiling-point fraction outlets includes: The heavy components that are captured by the first-stage condenser in the low-boiling-point section of the multi-stage distillation column are returned to the high-boiling-point section for secondary distillation, while the light components that are captured by the third-stage condenser in the low-boiling-point section of the multi-stage distillation column are returned to the low-boiling-point section for secondary distillation. The heavy components, which are captured by a primary condenser in the middle boiling point section of the multi-stage distillation column, are returned to the high boiling point section for secondary distillation. The light components, which are captured by a tertiary condenser in the middle boiling point section of the multi-stage distillation column, are returned to the low boiling point section for secondary distillation. The light components captured by the three-stage condenser in the high-boiling-point section of the steam are returned to the middle-boiling-point section of the multi-stage distillation column for secondary distillation.

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