Apparatus for treating oil-containing solid waste and method of operation thereof

Abstract

The application provides a device for treating oil-containing solid waste and a working method thereof, and belongs to the technical field of solid waste treatment. In order to solve the problem of high energy consumption in treating oil-containing solid waste in the prior art, the device for treating oil-containing solid waste comprises a dry-wet separation device (2), a dry distillation reactor (8) and a riser burner (16), the dry distillation reactor (8) contains a ceramic membrane filter (9) and a horizontal cyclone separator (36), the heat carrier particles can heat the solid waste dry material and make the solid waste dry material have a dry distillation reaction in the dry distillation reactor (8), and the waste semi-coke material can enter the riser burner (16) to burn to form heat carrier particles. The device for treating oil-containing solid waste utilizes the ash after the pyrolysis product is burned as a heat carrier, does not refer to other heat carriers and heat sources, can reduce energy consumption, and reduces the overall heat load of the system.

Description

Technical Field

[0001] This invention relates to the field of solid waste treatment technology, specifically to a device for treating oily solid waste, and a method for operating the device for treating oily solid waste. Background Technology

[0002] Solid waste includes oil-containing solid waste, which mainly contains oily sludge and oil-based drill cuttings. In the petroleum and petrochemical industry, oily sludge originates from upstream oil extraction, including spilled oil sludge, oil pits, and oil leaks; midstream oil gathering, transportation, and storage pollution, including oil leaks, tank sludge, and cruise ship hull sludge; and downstream oil refining processes, including sludge from oil separators, flotation tank scum, and residual biological activated sludge. Oil-based drill cuttings mainly originate from the drilling process using oil-based drilling fluids. Because they contain harmful organic matter and heavy metals, direct discharge or landfilling without treatment will severely impact the ecological environment. The volatilization of oil and gas from oily sludge and oil-based drill cuttings causes excessive total hydrocarbon concentrations in the air within production areas, exacerbating the greenhouse effect. Oily sludge and oil-based drill cuttings also cause severe exceedances of COD, BOD, and petroleum hydrocarbons in water, and allow toxic substances such as heavy metals, polycyclic aromatic hydrocarbons, and phenols to seep into the soil, polluting water resources. The existing methods for treating oily sludge and oil-based drill cuttings mainly consist of outsourced disposal and fixed-device treatment. Currently, the main technologies used in actual production include centrifugal separation, hot washing, hot desorption, and incineration.

[0003] Pyrolysis is currently the most widely used technology for treating oily sludge and oil-based drill cuttings. Pyrolysis processes mainly include rotary kiln pyrolysis, fluidized bed pyrolysis, fixed bed pyrolysis, and moving bed pyrolysis.

[0004] Rotary kiln pyrolysis typically employs a slow, indirect heating method. The most significant advantage of this process is its broad tolerance for the properties, forms, and sizes of raw materials. Furthermore, the process is simple and flexible to operate, allowing for precise control of material residence time.

[0005] The advantages of fluidized bed pyrolysis technology can be mainly summarized in three points: the suspended medium facilitates gas-solid contact, achieving uniform bed temperature; heat transfer efficiency is significantly improved, and the equipment size is significantly smaller than that of a fixed bed reactor; the equipment has a wide range of applications. The main disadvantages are: the high-speed flow of fluidizing gas carries away a large amount of heat, reducing the reactor's thermal efficiency; the material diameter needs to be less than 1 cm, as improper particle size control can not only damage the fluidization effect but also generate secondary pollution.

[0006] Fixed-bed pyrolysis requires materials to enter the reactor in an inert gas atmosphere. By setting a reasonable heating rate, the materials are heated to a specified temperature. The pyrolysis volatiles are liquefied into an oil phase through a condenser, and then the pyrolysis oil and gaseous products are collected separately.

[0007] The characteristics of moving bed pyrolysis process are: it can remove volatiles generated by pyrolysis in a timely and effective manner, and inhibit the secondary cracking of volatiles at high temperature; it avoids coking and blockage caused by condensation and deposition of pyrolysis oil in the reactor, and efficiently completes the pyrolysis reaction.

[0008] Current pyrolysis processes for sludge and drill cuttings, including fluidized bed, rotary kiln, fixed bed, and moving bed processes, all face the problem of high energy consumption and the need for external heat sources. Therefore, the heating methods used are basically external heating. This invention innovatively adopts internal combustion heating technology to solve the problem of high energy consumption in the pyrolysis of sludge and oil-based drill cuttings. Summary of the Invention

[0009] To address the high energy consumption problem in the existing technology for treating oily solid waste, this invention provides a device and its operating method for treating oily solid waste. This device uses the ash residue after the combustion of pyrolysis products as a heat carrier, without using other heat carriers or heat sources, which can reduce energy consumption and reduce the overall heat load of the system.

[0010] The technical solution adopted by this invention to solve its technical problem is:

[0011] An apparatus for treating oily solid waste includes a wet-dry separation device, a dry distillation reactor, and a riser burner. The wet-dry separation device can initially remove oil and water from the oily solid waste to form an oil-water mixture and dry solid waste. The dry solid waste and the heat carrier particles discharged from the riser burner can enter the dry distillation reactor, which contains a ceramic membrane filter and a horizontal cyclone separator. In the dry distillation reactor, the heat carrier particles can heat the dry solid waste and cause it to undergo a dry distillation reaction to form combustible gas, steam, and semi-coke waste. The semi-coke waste can enter the riser burner for combustion to form high-temperature gas and heat carrier particles.

[0012] A method of operating an apparatus for treating oily solid waste, comprising the following steps:

[0013] The dry-wet separation device initially removes oil and water from oily solid waste, forming an oil-water mixture and dry solid waste.

[0014] The dry solid waste discharged from the dry-wet separation unit and the heat carrier particles discharged from the riser burner are mixed and then enter the lower chamber of the dry distillation reactor.

[0015] In the lower chamber of the pyrolysis reactor, the heat carrier particles heat the solid waste dry material and cause the solid waste dry material to undergo a pyrolysis reaction to form combustible gas, steam and waste semi-coke. The waste semi-coke and the heat carrier particles are discharged from the lower end of the pyrolysis reactor. The combustible gas and steam enter the upper chamber of the pyrolysis reactor after filtration. The combustible gas and steam condense to form a liquid.

[0016] The waste semi-coke and the heat carrier particles discharged from the dry distillation reactor enter the riser burner, where the waste semi-coke is burned to form high-temperature gas and heat carrier particles.

[0017] A portion of the mixture of high-temperature gas and heat carrier particles discharged from the riser burner is separated in the heat carrier separator. The separated heat carrier particles are returned to the dry distillation reactor, and the separated high-temperature gas enters the high-temperature ash separator. Another portion of the mixture of high-temperature gas and heat carrier particles discharged from the riser burner also enters the high-temperature ash separator.

[0018] The heat carrier particles separated by the high-temperature ash separator are transported to the medium-temperature ash separator by the high-temperature ash pneumatic conveyor. The gas separated by the medium-temperature ash separator enters the riser burner for combustion through the combustion air supply pipeline. The combustion air supplied by the fan enters the medium-temperature ash pneumatic conveyor and provides power to it. The combustion air supplied by the fan and the heat carrier particles separated by the medium-temperature ash separator are mixed in the medium-temperature ash pneumatic conveyor. The heat carrier particles separated by the medium-temperature ash separator heat the combustion air supplied by the fan. The medium-temperature ash pneumatic conveyor then transports the heat carrier particles separated by the medium-temperature ash separator to the low-temperature ash separator. The gas separated by the low-temperature ash separator enters the high-temperature ash pneumatic conveyor and provides power to it. The gas separated by the low-temperature ash separator and the heat carrier particles separated by the high-temperature ash separator are mixed in the high-temperature ash pneumatic conveyor. The heat carrier particles separated by the high-temperature ash separator heat the gas separated by the low-temperature ash separator.

[0019] The gas separated by the high-temperature ash separator enters the waste heat boiler for complete combustion.

[0020] The beneficial effects of this invention are:

[0021] 1. Using the ash residue after the combustion of pyrolysis products as a heat carrier, without using other heat carriers and heat sources, can reduce energy consumption and the overall heat load of the system.

[0022] 2. The hot ash formed by the high-temperature combustion of semi-coke produced by pyrolysis in a circulating fluidized bed is used as a heat carrier. Heat is transferred through direct contact with solid waste via heat conduction, resulting in high heat transfer efficiency and higher oil yield than other heating methods. At the same time, the oil is lighter in quality.

[0023] 3. To address the issues of high ash content and fine dust particle size during the dry distillation of solid waste, this reactor employs a two-stage separation method, combining a ceramic membrane filter and a horizontal cyclone separator, resulting in excellent separation and filtration performance.

[0024] 4. It can realize the recycling of energy and the harmless and resource-based treatment of oily solid waste. Attached Figure Description

[0025] The accompanying drawings, which form part of this application, are used to provide a further understanding of the invention. The illustrative embodiments of the invention and their descriptions are used to explain the invention and do not constitute an improper limitation of the invention.

[0026] Figure 1 This is a schematic diagram of the equipment for treating oily solid waste according to the present invention.

[0027] Figure 2 yes Figure 1 Enlarged diagram on the left side of the middle section.

[0028] Figure 3 yes Figure 1 Enlarged diagram on the right side of the image.

[0029] Figure 4 Is it dry? Figure 1 Enlarged schematic diagram of the medium-distillation reactor section.

[0030] Figure 5 This is a three-dimensional schematic diagram of a horizontal cyclone separator.

[0031] Figure 6 This is a front view schematic diagram of a horizontal cyclone separator.

[0032] 1. Feeding hopper; 2. Dry-wet separation device; 3. Oil-water extrusion screw; 4. Mixing screw; 5. Compensator; 6. Flange; 7. Distributor; 8. Retort reactor; 9. Ceramic membrane filter; 10. First screw feeder; 11. Slag discharge port; 12. Semi-coke mixture riser; 13. Second screw feeder; 14. Fuel and heat carrier pellet feeder; 15. Ignition and gas afterburner; 16. Riser burner; 17. Screw return feeder; 18. Heat carrier material riser; 19. Heat carrier material conveyor. Pipe; 20. Bypass; 21. Heat carrier separator; 22. Heat carrier metering feeder; 23. Mixing device; 24. High-temperature ash separator; 25. Medium-temperature ash separator; 26. Low-temperature ash separator; 27. High-temperature ash metering feeder; 28. Medium-temperature ash metering feeder; 29. ​​High-temperature ash pneumatic conveyor; 30. Medium-temperature ash pneumatic conveyor; 31. Fan; 32. Waste heat boiler; 33. Electrostatic precipitator; 34. Wet desulfurization tower; 35. Chimney; 36. Horizontal cyclone separator; 37. Combustion air supply pipeline;

[0033] 801. Partition;

[0034] 3601, Fixed plate; 3602, Accelerator; 3603, Separator tank; 3604, Solid particulate matter outlet; 3605, Gas outlet; 3606, Separator inlet. Detailed Implementation

[0035] It should be noted that, unless otherwise specified, the embodiments and features described in this application can be combined with each other. The present invention will now be described in detail with reference to the accompanying drawings and embodiments.

[0036] For ease of understanding and description, the following description of the present invention uses absolute positional relationships. Unless otherwise specified, the directional term "above" indicates... Figure 1 The direction above, the directional word "down" indicates Figure 1 The lower side of the middle, the directional word "left" indicates Figure 1 The left side of the direction, the directional word "right" indicates Figure 1 The right-hand direction in the text, the directional word "front" indicates perpendicular to. Figure 1 The direction of the paper and pointing inwards from the paper; the directional word "back" indicates perpendicular to the paper. Figure 1 The orientation of the paper is directed towards the outer edge of the paper. This invention is described from the perspective of a reader or user, but the aforementioned directional terms should not be construed as limiting the scope of protection of this invention. Regarding the dimensions and angles of the components, those skilled in the art can determine them specifically according to actual needs.

[0037] like Figures 1 to 2 As shown in the embodiment of the present invention, an apparatus for treating oily solid waste includes a wet-dry separation device 2, a dry distillation reactor 8, and a riser burner 16. The wet-dry separation device 2 can initially remove oil and water from the oily solid waste to form an oil-water mixture and dry solid waste. The dry solid waste discharged from the wet-dry separation device 2 and the heat carrier particles discharged from the riser burner 16 can enter the dry distillation reactor 8. The dry distillation reactor 8 contains a ceramic membrane filter 9 and a horizontal cyclone separator 36. In the dry distillation reactor 8, the heat carrier particles can heat the dry solid waste and cause the dry solid waste to undergo a dry distillation reaction to form combustible gas, steam, and waste semi-coke. The waste semi-coke can enter the riser burner 16 for combustion to form high-temperature gas and heat carrier particles.

[0038] The structure of the dry-wet separation device 2 is roughly the same as that of the existing screw press. The dry-wet separation device 2 contains an oil-water extrusion screw 3, a filter sleeve and a shell arranged sequentially from the inside to the outside. The shell is provided with a raw material inlet, a dry material outlet and an oil-water outlet. The shell of the dry-wet separation device 2 is also provided with a heat source inlet and a heat source outlet. The oil-containing solid waste entering the dry-wet separation device 2 can be de-oiled and dewatered during the heating process using a heat source.

[0039] The raw material inlet of the dry-wet separation device 2 is connected to a feeding hopper 1. After the oily solid waste enters the dry-wet separation device 2, under the dual action of heating by the heat source and oil-water extrusion screw 3, most of the oil and water flows out along the oleophobic slits on the filter sleeve and is collected in the collection tank before being sent to the oil-water treatment system for further processing, thus completing the initial deoiling of the oily solid waste. In addition, the oil-water extrusion screw 3, in conjunction with the die head, can process the dry solid waste into granules.

[0040] like Figures 1 to 2 As shown, the equipment for treating oily solid waste also includes a mixing device 23. The dry solid waste discharged from the dry-wet separation device 2 and the heat carrier particles discharged from the riser burner 16 can enter the mixing device 23 for mixing. The dry material outlet of the dry-wet separation device 2 is connected to the inlet of the mixing device 23. A primary mixing chamber can be set outside the inlet of the mixing device 23. The dry solid waste discharged from the dry-wet separation device 2 and the heat carrier particles discharged from the riser burner 16 are mixed in the primary mixing chamber before entering the mixing device 23. A heat carrier metering feeder 22 can be set on the pipe through which the heat carrier particles are discharged from the riser burner 16 to precisely control the amount of heat carrier particles added.

[0041] The distillation reactor 8 contains an upper chamber and a lower chamber arranged vertically, which are independent of each other and are separated by a partition 801. The equipment for treating oily solid waste also includes a distributor 7, which transports the mixture of dry solid waste and heat carrier particles from the mixing device 23 to the lower chamber of the distillation reactor 8. The mixing device 23 includes an inner and outer mixing screw 4 and a casing. The dry solid waste and heat carrier particles can be mixed in the mixing device 23 and then enter the lower chamber of the distillation reactor 8 through the distributor 7.

[0042] The feeder 7 is a hollow tubular structure. The feeder 7 passes through the upper chamber of the dry distillation reactor 8. One end of the feeder 7 is located in the lower chamber of the dry distillation reactor 8, and the other end of the feeder 7 is located outside the dry distillation reactor 8. The other end of the feeder 7 is connected to the outlet of the mixing device 23 through the expansion joint 5. The other end of the feeder 7 is connected to the expansion joint 5 through the flange 6. The mixing screw 4 passes through the expansion joint 5.

[0043] After the solid waste dry material and heat carrier particles enter the lower chamber of the dry distillation reactor 8, the solid waste dry material and heat carrier particles continue to move downward under the action of gravity. The heat carrier particles release heat and heat the solid waste dry material. During this process, the solid waste dry material undergoes a dry distillation reaction to form combustible gas, steam and waste semi-coke.

[0044] like Figure 1 , Figure 2 , Figures 4 to 6 As shown, the horizontal cyclone separator 36 is located in the upper chamber of the dry distillation reactor 8. The horizontal cyclone separator 36 has a basically the same structure as the existing horizontal cyclone separator. The horizontal cyclone separator 36 includes a fixed disk 3601, an accelerator 3602, a separation tank 3603, a solid particulate matter outlet 3604, a gas outlet 3605, and a separator inlet 3606. A condensing pipeline and a condensing device are connected in sequence to the gas outlet 3605. The condensing device is located outside the dry distillation reactor 8, and the condensing pipeline passes through the shell of the dry distillation reactor 8.

[0045] Multiple ceramic membrane filters 9 are located in the lower chamber of the dry distillation reactor 8. The ceramic membrane filters 9 are in an upright state. The upper end of the ceramic membrane filters 9 is connected to the partition plate 801. The outlet of the ceramic membrane filters 9 is located at the upper end and is connected to the upper chamber of the dry distillation reactor 8. The combustible gas and steam (dry distillation gas) formed by the dry distillation reaction of the solid waste in the lower chamber of the dry distillation reactor 8 can pass through the ceramic membrane filters 9 and enter the upper chamber of the dry distillation reactor 8 and enter the separator inlet 3606. The lower end of the lower chamber of the dry distillation reactor 8 is provided with a lower outlet.

[0046] The pyrolysis gas carries smaller dust particles into the ceramic membrane filter 9 and forms a dust cake in the ceramic membrane filter 9. The pyrolysis gas passes through the ceramic membrane filter 9 and the horizontal cyclone separator 36 to complete dust removal. The horizontal cyclone separator 36 separates the pyrolysis gas and sends it to the condensation device to complete the separation and recovery of oil, gas and water. The ceramic filter membrane elements in the ceramic membrane filter 9 are arranged into several gas collecting umbrellas on the outer wall. The dust cake formed on the ceramic membrane filter 9 becomes heavier as the thickness increases. High-pressure gas is used to backflush the dust on the ceramic membrane filter 9 to periodically remove the dust cake from the outer surface of the ceramic filter elements, thereby regenerating the ceramic filter elements.

[0047] like Figures 1 to 2As shown, the equipment for treating oily solid waste also includes a semi-coke mixture riser 12 and a first screw feeder 10. The riser burner 16 is roughly pear-shaped and contains a combustion chamber. The inlet of the riser burner 16 is located at the lower end. The semi-coke mixture riser 12 is vertical and located below the riser burner 16. The upper end of the semi-coke mixture riser 12 is connected to the inlet of the riser burner 16. The waste semi-coke and heat carrier particles discharged from the lower outlet of the lower chamber of the dry distillation reactor 8 can sequentially enter the combustion chamber of the riser burner 16 through the first screw feeder 10 and the semi-coke mixture riser 12 for combustion. The lower end of the semi-coke mixture riser 12 is a slag discharge port 11.

[0048] The equipment for treating oily solid waste also includes a combustion air supply line 37 and a second screw feeder 13. The outlet of the combustion air supply line 37 is connected to the lower part of the semi-coke mixture riser 12. The outlets of the first screw feeder 10 and the second screw feeder 13 are both connected to the middle part of the semi-coke mixture riser 12. A fuel and heat carrier pellet feeder 14 is connected to the inlet of the second screw feeder 13. A start-up ignition and gas supplementary combustion device 15 is connected to the upper part of the semi-coke mixture riser 12. A screw return feeder 17 is installed inside the upper part of the riser burner 16. The fuel and heat carrier pellets that need to be replenished by the system are fed into the semi-coke mixture riser 12 through the fuel and heat carrier pellet feeder 14 and the second screw feeder 13. The air jet force in the combustion air supply line 37 can blow the waste semi-coke and heat carrier pellets into the combustion chamber of the riser burner 16.

[0049] like Figures 1 to 2 As shown, the equipment for treating oily solid waste also includes a heat carrier material riser 18, a heat carrier material conveying pipe 19, and a heat carrier separator 21 connected in sequence. The outlet of the riser burner 16 is located at the upper end. The heat carrier material riser 18 is in an upright state and is located above the riser burner 16. The inlet of the heat carrier material riser 18 is connected to the outlet of the riser burner 16. The high-temperature gas generated by combustion in the riser burner 16 and the heat carrier particles can pass through the heat carrier material riser 18 and the heat carrier material conveying pipe 19 in sequence and then enter the heat carrier separator 21. The heat carrier particles separated by the heat carrier separator 21 can enter the dry distillation reactor 8. The heat carrier separator 21 can be a cyclone separator. The solid outlet of the heat carrier separator 21 is connected to the inlet of the mixing device 23. The heat carrier metering feeder 22 is located on the pipe between the solid outlet of the heat carrier separator 21 and the inlet of the mixing device 23.

[0050] The preheated combustion air supplied by the combustion air supply line 37 lifts the mixture of waste semi-coke and heat carrier particles, as well as the fuel required by the system, into the combustion chamber of the riser burner 16, which has a higher temperature and a certain amount of circulating material. Due to the increased cross-section of the combustion chamber, the above-mentioned materials will burn here. With the continuous replenishment of preheated combustion air and materials, the burned material - heat carrier particles - is carried by the high-temperature flue gas and transported to the heat carrier separator 21 through the heat carrier material riser 18 and the heat carrier material conveying pipe 19. The top of the riser burner 16 is equipped with a spiral return feeder 17. The spiral return feeder 17 has a spiral blade structure and can rotate. Some of the larger particles that are not burned will be decelerated and return to the riser burner 16 to continue burning when they are touched by the spiral return feeder 17, so that the material can be fully burned.

[0051] The bottom of the riser burner 16 is equipped with a start-up ignition and gas supplementary combustion unit 15, which is used for ignition and start-up when the system starts. If the heat of the semi-coke is insufficient, gas produced by the system itself or gas from other gas sources can be supplemented by this burner to meet the system's heat balance. The high-temperature gas and heat carrier particles generated by combustion in the riser burner 16 are separated in the heat carrier separator 21. The separated heat carrier particles enter the mixing device 23 under the precise control of the heat carrier metering feeder 22, and are initially mixed with the pre-dehydrated solid waste dry material, entering a new dry distillation cycle.

[0052] like Figures 1 to 3As shown, the equipment for treating oily solid waste also includes a bypass 20, a high-temperature ash separator 24, a medium-temperature ash separator 25, a low-temperature ash separator 26, a high-temperature ash pneumatic conveyor 29, a medium-temperature ash pneumatic conveyor 30, a fan 31, a waste heat boiler 32, an electrostatic precipitator 33, a wet desulfurization tower 34, and a chimney 35. The high-temperature ash separator 24, the medium-temperature ash separator 25, and the low-temperature ash separator 26 are all cyclone separators. The inlet end of the bypass 20 is connected to the heat carrier material conveying pipe 19. A valve is installed on bypass 20. The outlet of bypass 20 is connected to the inlet of high-temperature ash separator 24. Heat carrier separator 21 has an inlet, a solid outlet, and a gas outlet. The gas outlet of heat carrier separator 21 is connected to the inlet of high-temperature ash separator 24. The solid outlet of high-temperature ash separator 24 is connected to the material inlet of high-temperature ash pneumatic conveyor 29. A high-temperature ash metering feeder 27 is installed on the pipeline between the solid outlet of high-temperature ash separator 24 and the material inlet of high-temperature ash pneumatic conveyor 29. The outlet of the high-temperature ash pneumatic conveyor 29 is connected to the inlet of the medium-temperature ash separator 25. The solid outlet of the medium-temperature ash separator 25 is connected to the material inlet of the medium-temperature ash pneumatic conveyor 30. A medium-temperature ash metering feeder 28 is installed on the pipeline between the solid outlet of the medium-temperature ash separator 25 and the material inlet of the medium-temperature ash pneumatic conveyor 30. The gas outlet of the medium-temperature ash separator 25 is connected to the inlet of the combustion air supply pipeline 37. The gas inlet of the medium-temperature ash pneumatic conveyor 30 is connected to the (combustion) fan 31. The outlet of the medium-temperature ash pneumatic conveyor 30 is connected to the inlet of the low-temperature ash separator 26. The solid outlet of the low-temperature ash separator 26 is connected to an ash discharge pipeline. The gas outlet of the low-temperature ash separator 26 is connected to the gas inlet of the high-temperature ash pneumatic conveyor 29. The solid outlet of the low-temperature ash separator 26 serves as an ash discharge port. The gas outlet of the high-temperature ash separator 24 is connected to the furnace of the waste heat boiler 32. The waste heat boiler 32, the electrostatic precipitator 33, the wet desulfurization tower 34, and the chimney 35 are connected in sequence.

[0053] Excess hot ash is bypassed by 20 and combined with high-temperature flue gas from heat carrier separator 21 before being transported to high-temperature ash separator 24 for separation. The amount of heat carrier particles (hot ash) entering high-temperature ash separator 24 can be regulated by valves on bypass 20. The hot ash separated by high-temperature ash separator 24 is then controlled by high-temperature ash metering feeder 27 and enters high-temperature ash pneumatic conveyor 29, where it is transported to medium-temperature ash separator 25 by preheated combustion air. During the transport process, the combustion air and high-temperature ash undergo heat transfer and are preheated again. After separation by medium-temperature ash separator 25, it is sent to semi-coke via combustion air supply pipeline 37. The mixed material riser 12 then completes the lifting and combustion of the semi-coke and heat carrier particles. The medium-temperature ash, after passing through the medium-temperature ash separator 25, enters the medium-temperature ash pneumatic conveyor 30 under the control of the medium-temperature ash metering feeder 28. It is then pneumatically conveyed to the low-temperature ash separator 26 by combustion air supplied from the blower 31. During this conveying process, the combustion air and medium-temperature ash undergo heat transfer, resulting in initial preheating. After separation by the low-temperature ash separator 26, the preheated combustion air is conveyed to the high-temperature ash pneumatic conveyor 29, which then conveys the high-temperature ash back to the medium-temperature ash separator 25. During this conveying process, the combustion air and high-temperature ash undergo heat transfer again, resulting in further preheating. The high-temperature flue gas containing a certain amount of combustible gas, separated by the high-temperature ash separator 24, is conveyed to the waste heat boiler 32. To ensure complete combustion, the waste heat boiler is equipped with supplementary combustion air, and the heat is used to produce steam. The waste flue gas is treated by environmental protection facilities such as the electrostatic precipitator 33 and the wet desulfurization tower 34 before being discharged through the chimney 35.

[0054] The following describes the operating method of the above-mentioned equipment for treating oily solid waste, including the following steps:

[0055] The dry-wet separation device 2 initially removes oil and water from the oily solid waste and forms an oil-water mixture and dry solid waste material, which are then separated.

[0056] The dry solid waste discharged from the dry-wet separation device 2 and the heat carrier particles discharged from the riser burner 16 are mixed in the mixing device 23 to form a mixture of dry solid waste and heat carrier particles. The mixture of dry solid waste and heat carrier particles enters the lower chamber of the dry distillation reactor 8 through the distributor 7.

[0057] In the lower chamber of the dry distillation reactor 8, the heat carrier particles heat the solid waste dry material and cause it to undergo a dry distillation reaction to form combustible gas, steam, and waste semi-coke. The waste semi-coke and the heat carrier particles are discharged from the lower end of the dry distillation reactor 8. The combustible gas and steam (i.e., dry distillation gas) and a small amount of heat carrier particles enter the upper chamber of the dry distillation reactor 8 after being filtered by the ceramic membrane filter 9. The combustible gas and steam and a small amount of heat carrier particles enter the horizontal cyclone separator 36. The horizontal cyclone separator 36 separates the combustible gas and steam, which enter the condenser and are condensed to form a liquid.

[0058] The waste semi-coke and the heat carrier particles discharged from the dry distillation reactor 8 are sequentially fed into the riser burner 16 through the first screw feeder 10 and the semi-coke mixture riser 12. In the riser burner 16, the waste semi-coke is burned to form high-temperature gas and heat carrier particles.

[0059] A portion of the high-temperature gas and heat carrier particles discharged from the riser burner 16 enter the heat carrier separator 21 sequentially through the heat carrier material riser 18 and the heat carrier material conveying pipe 19. The high-temperature gas and heat carrier particles are separated in the heat carrier separator 21. The separated heat carrier particles enter the mixing device 23 and return to the lower chamber of the dry distillation reactor 8. The separated high-temperature gas enters the high-temperature ash separator 24. Another portion of the high-temperature gas and heat carrier particle mixture discharged from the riser burner 16 also enters the high-temperature ash separator 24.

[0060] The heat carrier particles separated by the high-temperature ash separator 24 are conveyed to the medium-temperature ash separator 25 by the high-temperature ash pneumatic conveyor 29. The gas separated by the medium-temperature ash separator 25 enters the riser burner 16 for combustion support through the combustion air supply pipeline 37. The combustion air supplied by the fan 31 enters the medium-temperature ash pneumatic conveyor 30 and provides power to it. The combustion air supplied by the fan 31 and the heat carrier particles separated by the medium-temperature ash separator 25 are mixed in the medium-temperature ash pneumatic conveyor 30. The combustion air supplied by the heating fan 31 is transported by the medium-temperature ash pneumatic conveyor 30 to the low-temperature ash separator 26, where the heat carrier particles separated by the medium-temperature ash separator 25 are transported. The gas separated by the low-temperature ash separator 26 enters the high-temperature ash pneumatic conveyor 29 and provides power to it. The gas separated by the low-temperature ash separator 26 and the heat carrier particles separated by the high-temperature ash separator 24 are mixed in the high-temperature ash pneumatic conveyor 29, and the heat carrier particles separated by the high-temperature ash separator 24 heat the gas separated by the low-temperature ash separator 26.

[0061] The gas separated by the high-temperature ash separator 24 enters the waste heat boiler 32 for complete combustion, and its heat is used to produce high-temperature steam. The waste flue gas generated by the waste heat boiler 32 is treated by the electrostatic precipitator 33 and the wet desulfurization tower 34 in sequence before being discharged through the chimney 35.

[0062] Based on experimental results and calculations using existing formulas, 1 kg of received Jiji sludge can be pyrolyzed to yield 0.15 kg of pyrolysis oil. During the pyrolysis process, 5.94 kg of ash generated from the combustion of pyrolysis semi-coke is required as heat carrier particles to provide the energy needed to raise the temperature of the sludge to 520℃. During the semi-coke combustion process, in addition to the combustion of the pyrolysis gas in the fluidized bed and the combustion of the semi-coke itself, 0.03 kg of liquefied petroleum gas is also needed to provide heat to burn the ash to 800℃. Simultaneously, material and heat balance calculations were performed for the entire process, considering both input and output. The input materials include sludge, air, and liquefied petroleum gas, totaling 2.34 kg. The output materials include pyrolysis oil, water, and soot, totaling 2.36 kg. The total heat input is 10102.55 kJ, and the total heat output is 6790.31 kJ, resulting in a loss of 3312.24 kJ and a thermal efficiency of 63.3%.

[0063] The above description is merely a specific embodiment of the present invention and should not be construed as limiting the scope of the invention. Therefore, any substitution of equivalent components or equivalent changes and modifications made within the scope of protection of this patent should still fall within the scope of this patent. Furthermore, the technical features, technical features and technical solutions, and technical solutions in this invention can be freely combined and used.

Claims

1. A device for treating oily solid waste, characterized in that, The equipment for treating oily solid waste includes a dry-wet separation device (2), a dry distillation reactor (8), and a riser burner (16). The dry-wet separation device (2) can initially remove oil and water from the oily solid waste and form an oil-water mixture and dry solid waste. The dry solid waste and the heat carrier particles discharged from the riser burner (16) can enter the dry distillation reactor (8). The dry distillation reactor (8) contains a ceramic membrane filter (9) and a horizontal cyclone separator (36). In the dry distillation reactor (8), the heat carrier particles can heat the dry solid waste and cause the dry solid waste to undergo a dry distillation reaction to form combustible gas, steam, and waste semi-coke. The waste semi-coke can enter the riser burner (16) and burn to form high-temperature gas and heat carrier particles. The equipment for treating oily solid waste also includes a mixing device (23). The dry-wet separation device (2) contains an oil-water extrusion screw (3), a filter sleeve and a shell arranged sequentially from the inside to the outside. The shell is provided with a raw material inlet, a dry material outlet and an oil-water outlet. The dry material outlet of the dry-wet separation device (2) is connected to the inlet of the mixing device (23). The dry solid waste discharged from the dry-wet separation device (2) and the heat carrier particles discharged from the riser burner (16) can enter the mixing device (23) for mixing. The equipment for treating oily solid waste also includes a distributor (7), the dry distillation reactor (8) contains an upper chamber and a lower chamber arranged vertically, the upper chamber and the lower chamber are independent of each other, a partition (801) is provided between the upper chamber and the lower chamber, the mixing device (23) contains an inner and outer mixing screw (4) and a casing, the dry solid waste and heat carrier particles can be mixed in the mixing device (23) and then enter the lower chamber of the dry distillation reactor (8) through the distributor (7); The horizontal cyclone separator (36) is located in the upper chamber of the dry distillation reactor (8). The horizontal cyclone separator (36) includes a fixed plate (3601), an accelerator (3602), a separation tank (3603), a solid particulate matter outlet (3604), a gas outlet (3605), and a separator inlet (3606). A condenser pipeline and a condenser device are connected in sequence outside the gas outlet (3605). The ceramic membrane filter (9) is located in the lower chamber of the dry distillation reactor (8). The ceramic membrane filter (9) is connected to the partition plate (801). The outlet of the ceramic membrane filter (9) is connected to the upper chamber of the dry distillation reactor (8). The combustible gas and steam formed by the dry distillation reaction of the solid waste in the lower chamber of the dry distillation reactor (8) can pass through the ceramic membrane filter (9) and enter the upper chamber of the dry distillation reactor (8) and then enter the separator inlet (3606). The lower end of the lower chamber of the dry distillation reactor (8) is provided with a lower outlet.

2. The equipment for treating oily solid waste according to claim 1, characterized in that, The feeder (7) passes through the upper chamber of the dry distillation reactor (8). One end of the feeder (7) is located in the lower chamber of the dry distillation reactor (8). The other end of the feeder (7) is connected to the outlet of the mixing device (23) through the expansion compensator (5). The mixing screw (4) passes through the expansion compensator (5). The dry and wet separation device (2) is also equipped with a heat source inlet and a heat source outlet.

3. The equipment for treating oily solid waste according to claim 1, characterized in that, The equipment for treating oily solid waste also includes a semi-coke mixture riser (12) and a first screw feeder (10). The inlet of the riser burner (16) is located at the lower end. The semi-coke mixture riser (12) is in an upright state and is located below the riser burner (16). The upper end of the semi-coke mixture riser (12) is connected to the inlet of the riser burner (16). The waste semi-coke material discharged from the dry distillation reactor (8) can enter the riser burner (16) in sequence through the first screw feeder (10) and the semi-coke mixture riser (12).

4. The equipment for treating oily solid waste according to claim 3, characterized in that, The equipment for treating oily solid waste also includes a combustion air supply line (37) and a second screw feeder (13). The outlet of the combustion air supply line (37) is connected to the lower part of the semi-coke mixture riser (12). The outlets of the first screw feeder (10) and the second screw feeder (13) are both connected to the middle part of the semi-coke mixture riser (12). The upper part of the semi-coke mixture riser (12) is connected to a start-up ignition and gas supplementary combustion device (15). The upper part of the riser burner (16) is equipped with a screw return device (17).

5. The equipment for treating oily solid waste according to claim 4, characterized in that, The equipment for treating oily solid waste also includes a heat carrier material riser (18), a heat carrier material conveying pipe (19), and a heat carrier separator (21) connected in sequence. The outlet of the riser burner (16) is located at the upper end. The heat carrier material riser (18) is in an upright state and is located above the riser burner (16). The inlet of the heat carrier material riser (18) is connected to the outlet of the riser burner (16). The high-temperature gas formed by combustion in the riser burner (16) and the heat carrier particles can pass through the heat carrier material riser (18) and the heat carrier material conveying pipe (19) in sequence and then enter the heat carrier separator (21). The heat carrier particles separated by the heat carrier separator (21) can enter the dry distillation reactor (8).

6. The equipment for treating oily solid waste according to claim 5, characterized in that, The equipment for treating oily solid waste also includes a bypass (20), a high-temperature ash separator (24), a medium-temperature ash separator (25), a low-temperature ash separator (26), a high-temperature ash pneumatic conveyor (29), a medium-temperature ash pneumatic conveyor (30), a fan (31), a waste heat boiler (32), an electrostatic precipitator (33), a wet desulfurization tower (34), and a chimney (35). The inlet end of the bypass (20) is connected to the heat carrier material conveying pipe (19), and the outlet end of the bypass (20) is connected to the inlet of the high-temperature ash separator (24). The heat carrier separator (21) has an inlet, a solid outlet, and a gas outlet. The gas outlet of the heat carrier separator (21) is connected to the inlet of the high-temperature ash separator (24), and the solid outlet of the high-temperature ash separator (24) is connected to the material inlet of the high-temperature ash pneumatic conveyor (29). The outlet of 9) is connected to the inlet of the medium-temperature ash separator (25). The solid outlet of the medium-temperature ash separator (25) is connected to the material inlet of the medium-temperature ash pneumatic conveyor (30). The gas outlet of the medium-temperature ash separator (25) is connected to the inlet of the combustion air supply pipeline (37). The gas inlet of the medium-temperature ash pneumatic conveyor (30) is connected to the outlet of the blower (31). The outlet of the medium-temperature ash pneumatic conveyor (30) is connected to the inlet of the low-temperature ash separator (26). The solid outlet of the low-temperature ash separator (26) is connected to the ash discharge pipeline. The gas outlet of the low-temperature ash separator (26) is connected to the gas inlet of the high-temperature ash pneumatic conveyor (29). The gas outlet of the high-temperature ash separator (24) is connected to the furnace of the waste heat boiler (32). The waste heat boiler (32), the electrostatic precipitator (33), the wet desulfurization tower (34) and the chimney (35) are connected in sequence.

7. A method of operating the apparatus for treating oily solid waste as described in claim 6, characterized in that, Includes the following steps: The dry-wet separation device (2) initially removes oil and water from oily solid waste and forms an oil-water mixture and dry solid waste material; The dry solid waste discharged from the dry-wet separation device (2) and the heat carrier particles discharged from the riser burner (16) are mixed and then enter the lower chamber of the dry distillation reactor (8); In the lower chamber of the dry distillation reactor (8), the heat carrier particles heat the solid waste dry material and cause the solid waste dry material to undergo a dry distillation reaction to form combustible gas, steam and waste semi-coke. The waste semi-coke and the heat carrier particles are discharged from the lower end of the dry distillation reactor (8). The combustible gas and steam enter the upper chamber of the dry distillation reactor (8) after filtration. The combustible gas and steam condense to form liquid. The waste semi-coke and the heat carrier particles discharged from the dry distillation reactor (8) enter the riser burner (16), where the waste semi-coke is burned to form high-temperature gas and heat carrier particles. A portion of the mixture of high-temperature gas and heat carrier particles discharged from the riser burner (16) is separated in the heat carrier separator (21). The separated heat carrier particles are returned to the dry distillation reactor (8), and the separated high-temperature gas enters the high-temperature ash separator (24). Another portion of the mixture of high-temperature gas and heat carrier particles discharged from the riser burner (16) also enters the high-temperature ash separator (24). The heat carrier particles separated by the high-temperature ash separator (24) are transported to the medium-temperature ash separator (25) by the high-temperature ash pneumatic conveyor (29). The gas separated by the medium-temperature ash separator (25) enters the riser burner (16) for combustion through the combustion air supply pipeline (37). The combustion air supplied by the fan (31) enters the medium-temperature ash pneumatic conveyor (30) and provides power to the medium-temperature ash pneumatic conveyor (30). The combustion air supplied by the fan (31) and the heat carrier particles separated by the medium-temperature ash separator (25) are mixed in the medium-temperature ash pneumatic conveyor (30). The heat carrier separated by the medium-temperature ash separator (25) is further separated. Combustion air supplied by the particle heating blower (31) is transported by the medium-temperature ash pneumatic conveyor (30) to the low-temperature ash separator (26) through the medium-temperature ash separator (25). The gas separated by the low-temperature ash separator (26) enters the high-temperature ash pneumatic conveyor (29) and provides power to the high-temperature ash pneumatic conveyor (29). The gas separated by the low-temperature ash separator (26) and the heat carrier particles separated by the high-temperature ash separator (24) are mixed in the high-temperature ash pneumatic conveyor (29). The heat carrier particles separated by the high-temperature ash separator (24) heat the gas separated by the low-temperature ash separator (26). The gas separated by the high-temperature ash separator (24) enters the waste heat boiler (32) for complete combustion.

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