Oil-containing sludge reduction treatment device and method

Abstract

The application provides an oil-containing sludge reduction treatment device and method, relates to the technical field of oil-containing sludge treatment, and comprises a shell. An inside of the shell is provided with a fermentation chamber. Two ends of the shell are respectively provided with a feeding port and a discharging port which are in communication with the fermentation chamber. A side wall of the fermentation chamber is provided with capillary holes which are in communication with the fermentation chamber. The side wall of the fermentation chamber is provided with a heating component. A top of the fermentation chamber is provided with a gas outlet. A stirring and conveying mechanism is arranged in the inside of the shell and is used for stirring and conveying materials in the fermentation chamber. The problems of great difficulty in solid-liquid separation, complex operation, high cost and large floor area in the oil-containing sludge reduction treatment process in the prior art are solved.

Description

Technical Field

[0001] This invention belongs to the field of oily sludge treatment technology, and more specifically, relates to an oily sludge reduction treatment device and method. Background Technology

[0002] Petroleum is a vital resource, playing a pivotal role in national economic development. However, the extraction, transportation, and processing of petroleum generate oily sludge. Oily sludge is an emulsified system composed of petroleum hydrocarbons, colloids, asphalt, mud, sand, water, and other organic and inorganic substances, and falls under the category of hazardous waste. The discharge of oily sludge causes serious pollution to soil, air, and water bodies. Since oily sludge contains valuable oil resources, biological treatment of oily sludge and recovery of oil products are important means of protecting the environment and achieving resource recycling.

[0003] Currently, oily sludge treatment devices often require multiple equipment units to achieve the goals of pollutant treatment and oil resource recovery, and rely primarily on high-speed centrifugation for solid-liquid separation, resulting in high energy consumption and complex operation. Finding a simpler and more economical way to achieve efficient oily sludge treatment and high-purity oil recovery is a crucial measure to improve the treatment efficiency, effectiveness, and economics of biological oily sludge treatment devices.

[0004] Biological aerobic fermentation is a cost-effective and environmentally friendly method for treating oily sludge. It utilizes microorganisms to degrade the oil in the sludge using the oil as a carbon source, thereby destabilizing the sludge system and absorbing and degrading pollutants, as well as some oil and water. In particular, high-temperature microbial fermentation technology has the advantages of short cycle and high efficiency, and can be combined with demulsifiers to achieve deep volume reduction of oily sludge.

[0005] To address the problems of complex operation, difficult oil recovery, and high operating costs of existing oily sludge treatment devices, the use of high-temperature biological aerobic fermentation coupled with demulsification technology to optimize oily sludge treatment devices can achieve high-quality oil recovery at low cost, improve the treatment efficiency of oily sludge and reduce treatment costs.

[0006] CN115504643A discloses a combined biological and physical method for the efficient treatment of oily sludge. This method proposes using an air flotation device to form floating flocs containing contaminants and microbubbles, followed by crude oil recovery from the oily sludge. While this method achieves oil separation, the resulting oily sludge contains a mixture of oil and contaminants, leading to low oil purity, increased separation difficulty, and higher costs for oil recovery.

[0007] CN113816577A discloses a rotary microbial fermentation device for treating oily sludge. The device includes a supporting frame, reaction components, and a rotating component. By rotating the turntable, the oily sludge is tumbled, which fully mixes the oily sludge and bacterial solution, enhancing the fermentation process. However, the oil cannot be recovered after the oily sludge is treated, and the economic efficiency of the device needs to be further improved.

[0008] Therefore, there is an urgent need in the field to optimize the current equipment and methods to further enhance the separation and recovery of water and oil in oily sludge, especially the recovery of oil resources, simplify the equipment and reduce the operating cost of the equipment, and further reduce the treatment cost of oily sludge. Summary of the Invention

[0009] The purpose of this invention is to address the shortcomings of existing technologies by providing an oily sludge reduction treatment device and method, which solves the problems of difficult solid-liquid separation, complex operation, high cost, and large footprint in the oily sludge reduction treatment process of existing technologies.

[0010] To achieve the above objectives, the present invention provides an oily sludge reduction treatment device, the device comprising:

[0011] The shell has a fermentation chamber inside. The two ends of the shell are respectively provided with an inlet and an outlet communicating with the fermentation chamber. The side wall of the fermentation chamber is provided with capillary channels communicating with the fermentation chamber. A heating element is provided inside the side wall of the fermentation chamber. An air outlet is provided at the top of the fermentation chamber.

[0012] A stirring and conveying mechanism is disposed inside the housing and is used to stir and convey the materials in the fermentation chamber.

[0013] Oily sludge, demulsifier, and biological liquid with the function of fermenting oily sludge can enter the fermentation chamber through the feed inlet. Under the action of the heating element, the temperature in the fermentation chamber rises, and the oily sludge ferments in the fermentation chamber, producing oil-water mixed liquid, gas, and solid products. Under the action of the stirring and conveying mechanism, the material is turned over and transported towards the discharge port. The liquid can be collected by the absorption of the capillary channels, and the gas can be discharged through the gas outlet.

[0014] Optionally, a liquid collection tank communicating with the capillary channel is provided on the outer side of the outer wall of the shell, and a drain outlet is provided at the bottom of the liquid collection tank.

[0015] The collection tank is used to collect the liquid that flows out through the capillary channels, and the liquid collected in the collection tank can be discharged through the drain port for the next step of oil-water separation.

[0016] Optionally, it also includes an oil-water separation structure, which is connected to the drain port via a liquid delivery pipeline.

[0017] The liquid collected in the collection tank can be separated in the oil-water separation structure. The separated oil can be recycled and reused, and the separated water can be sent to the plant's wastewater treatment unit for treatment.

[0018] Optionally, the oil-water separation structure includes:

[0019] An oil-water separator tank, wherein a partition is vertically arranged inside the oil-water separator tank, the partition dividing the interior of the oil-water separator tank into a first space and a second space that are connected at the bottom;

[0020] An oil storage tank is located below the oil-water separator.

[0021] A floating roof is movably disposed within the second space. The floating roof is capable of floating at the oil-water interface. A first limiting part and a second limiting part connected to the inner wall of the oil-water separator are respectively provided above and below the floating roof. The floating roof has multiple oil passages.

[0022] A hollow fiber bundle, the upper end of which penetrates the floating roof and forms an extension above the floating roof, the lower end of which extends into the oil storage tank, and capillary channels are formed inside the hollow fiber bundle.

[0023] A sealing part is provided between the oil-water separator and the oil storage tank so that the oil-water separator is connected to the oil storage tank only through the capillary channel.

[0024] Specifically, the liquid collected in the collection tank is transported to the first space through the infusion pipeline. After passing through the first space, it enters the second space from the bottom of the oil-water separator. As the amount of liquid input increases, the liquid level in the oil-water separator increases, and the oil and water separate into layers, with the oil on top of the water. The floating plate in the second space floats at the oil-water interface. Through the capillary channels formed by the hollow fiber bundles on the floating plate, the oil on the upper side can be guided into the oil storage tank located below the oil-water separator, while the water in the oil-water separator remains in the second space, thus achieving oil-water separation.

[0025] In one specific embodiment of the present invention, a plurality of hollow capillary fibers form a capillary fiber bundle, and each hollow fiber is provided with a capillary channel.

[0026] In another specific embodiment of the present invention, multiple hollow capillary fibers form a capillary fiber bundle. Not only is a capillary channel provided in each hollow fiber, but a capillary channel is also formed between adjacent capillary fiber bundles. Since the cross-section of the capillary channel formed between adjacent capillary fiber bundles is not circular, the diameter of the capillary channel can be characterized by the average pore size.

[0027] Optionally, the lower end of the side wall of the oil storage tank is provided with an oil drain port, and an oil drain valve is provided inside the oil drain port; the lower end of the side wall of the oil-water separator is provided with a drain outlet, and a drain valve is provided inside the drain outlet; a level gauge is provided inside the oil storage tank; and a first position sensor and a second position sensor are respectively provided on the side of the first limiting part and the second limiting part that are close to each other.

[0028] The first and second limiting parts restrict the position of the floating roof, keeping it between them. When the floating roof rises to contact the first limiting part, the first position sensor is triggered, at which point the drain valve needs to be opened to drain some water. When the floating roof descends to contact the second limiting part, the second position sensor is triggered, at which point the amount of liquid input from the collection tank to the oil-water separator needs to be increased. When the liquid level detected by the level gauge exceeds the set liquid level height, the oil drain valve needs to be opened to recover and discharge the oil in the storage tank.

[0029] The first and second position sensors can be ranging sensors, photoelectric sensors, or position switches.

[0030] Optionally, the density of the floating roof is 0.850–0.950 g / cm³. 3 .

[0031] The density of the floating roof ensures that it can float at the oil-water interface.

[0032] Optionally, the pore size of the capillary channel is 0.05-4 micrometers.

[0033] Optionally, a hydrophobic coating is provided on the inner wall of the capillary channel, and the water droplet contact angle of the hydrophobic coating is 95-140°.

[0034] The inner wall of the capillary channels in the hollow fiber bundle is coated with a hydrophobic coating, which can accelerate the self-absorption of oil and improve the oil-water separation efficiency.

[0035] Optionally, the pore size of the capillary channel is 0.01-2 micrometers.

[0036] In this invention, the capillary channels can be formed by any method. According to one specific embodiment, the capillary channels are formed by stamping; according to another specific embodiment, the capillary channels are capillary holes with protective sleeves embedded during equipment processing, which can connect the oily sludge end and the liquid collection tank end; according to yet another embodiment, the sidewall of the first chamber with capillary channels is integrally formed using a channel model, for example, by integrally forming using a channel model during steel rolling; according to yet another embodiment, the sidewall of the first chamber with capillary channels is processed by spray etching, making the device easy to manufacture.

[0037] Optionally, the volume ratio of the capillary channels relative to the total volume of the sidewalls of the fermentation chamber is 0.5-4%, preferably 2%.

[0038] When manufacturing the device of the present invention, the parameters of the capillary channels can be adjusted, including but not limited to pore size and volume ratio (i.e., open area ratio).

[0039] A preferred aperture combined with a preferred volume ratio can achieve better oil-water separation results.

[0040] Optionally, the stirring and conveying mechanism includes a rotating shaft that rotatably passes through the fermentation chamber. One end of the rotating shaft is connected to a drive motor, and stirring and conveying blades are provided on the outer periphery of the rotating shaft.

[0041] The pivot can be set horizontally or tilted.

[0042] Optionally, the drive motor is a variable frequency motor.

[0043] The output power of the variable frequency motor is adjustable. The residence time of oily sludge in the fermentation chamber can be controlled from 6 to 24 hours, preferably 12 hours, by the rotation speed of the stirring and conveying mechanism. The stirring and conveying mechanism can be divided into three sections with variable frequency output power, which can control the oily sludge to be conveyed at different speeds in the three parts of the fermentation chamber.

[0044] Optionally, it also includes an air intake structure, the output end of which is connected to the fermentation chamber and is used to deliver acidic gas and oxygen into the fermentation chamber.

[0045] Acidic gases react with oily sludge, lowering its pH, which facilitates the demulsification process, reduces the stability of the emulsion system, and decreases the viscosity of the oily sludge. Oxygen provides oxygen for the fermentation of the oily sludge, promoting fermentation.

[0046] According to a preferred embodiment of the present invention, the air intake structure delivers air containing SO2, CO2, and NO that has undergone dust removal treatment to the fermentation chamber. x Waste gas from the factory area containing acidic gases and oxygen.

[0047] Optionally, the intake structure includes:

[0048] An air intake passage is provided inside the rotating shaft along the axial direction of the rotating shaft;

[0049] Multiple air distribution ports are provided, which are opened on the rotating shaft along the axial direction of the rotating shaft and connect the air intake channel to the fermentation chamber;

[0050] An air inlet is located at one end of the rotating shaft near the drive motor.

[0051] Waste gas from the plant enters the intake channel through the inlet, is transported along the intake channel, and is discharged into the fermentation chamber through multiple gas distribution ports on the rotating shaft. The waste gas is distributed from the gas distribution ports on the rotating shaft, with the distribution position close to the center of the fermentation chamber and close to the stirring position of the impeller of the stirring blade, which allows the gas to be better mixed with the oily sludge. At the same time, the introduction of waste gas from the plant creates a slightly positive pressure environment in the fermentation chamber, which can promote the absorption and recovery of oil and water liquids through the capillary pores.

[0052] Optionally, each of the air distribution ports is provided with an opening adjustment valve.

[0053] The air vents can be evenly distributed on the rotating shaft, but the opening adjustment valve on each air vent can adjust the amount of air at each position by adjusting the opening of the air vent. Good air distribution can result in good oxygen content distribution and improve fermentation effect.

[0054] Optionally, three oxygen content detectors are sequentially arranged in the fermentation chamber along the material conveying direction. The three oxygen content detectors are used to detect the oxygen concentration in the front, middle and rear parts of the fermentation chamber, respectively.

[0055] The distribution of oxygen within the fermentation chamber can be detected by three oxygen content detectors located at the front, middle, and rear of the chamber, respectively, which facilitates its regulation.

[0056] Optionally, multiple temperature detection components are sequentially arranged in the fermentation chamber along the material conveying direction, and the multiple temperature detection components are used to detect the temperature at multiple locations in the fermentation chamber.

[0057] The setup of multiple temperature detection components allows for the measurement of temperature at different locations within the fermentation chamber, facilitating temperature control. The front section is for high-temperature demulsification with a relatively high temperature, while the middle and rear sections are for fermentation with a relatively low temperature, preventing excessively high temperatures from damaging the activity of the biological liquid.

[0058] Optionally, the heating element is a segmented frequency conversion heating rod arranged along the axial direction of the fermentation chamber, which can heat the material in the fermentation chamber in segments.

[0059] The fermentation chamber is heated in segments by segmented frequency conversion heating rods, and the temperature distribution inside the fermentation chamber can be adjusted according to the detection results of the temperature detection component.

[0060] Optionally, the liquid collection tank is connected to a negative pressure generating structure, which is used to create a negative pressure environment within the liquid collection tank.

[0061] Specifically, the negative pressure generating structure is connected to the liquid collection tank through a negative pressure pipe. The negative pressure pipe can be equipped with an air pump to maintain a micro-negative pressure environment in the liquid collection tank, thereby enhancing the absorption of oil and water liquids into the liquid collection tank through the capillary channels.

[0062] Optionally, a material return pipe is connected to the discharge port, and a variable frequency return pump is installed on the material return pipe. The material return pipe is connected to the feed port.

[0063] The material reflux pipe is equipped with a variable frequency reflux pump, which can adjust the reflux ratio of solid products after fermentation.

[0064] The present invention also provides a method for reducing the volume of oily sludge, utilizing the above-mentioned oily sludge reduction treatment device, the method comprising:

[0065] Oily sludge, demulsifier, and biological bacterial solution with the function of fermenting oily sludge are fed into the fermentation chamber through the inlet;

[0066] The materials within the fermentation chamber are heated, stirred, and conveyed.

[0067] At least a portion of the liquid produced in the fermentation chamber is drained through capillary channels;

[0068] At least a portion of the gas generated in the fermentation chamber is discharged through the vent.

[0069] The solid products generated in the fermentation chamber are discharged through the discharge port.

[0070] According to a specific embodiment of the present invention, the bio-liquid with the function of fermenting oily sludge is obtained by sampling from at least one of oilfield soil, oily sludge in storage tanks and oily wastewater, and by high-temperature (70-80℃) culture, enrichment and screening in sterilized crude oil culture medium, and is a bio-liquid containing at least one of Streptococcus sp., Micrococcus cohnsp. and Planococcus migula sp.

[0071] Optionally, the oily sludge has a water content higher than 35%, an oil content higher than 35%, and a total liquid content higher than 80%.

[0072] The oily sludge has a water content of more than 35% to ensure sufficient water supply for microbial growth and fermentation, and an oil content of more than 35% to ensure sufficient oil as a carbon source for microorganisms.

[0073] Optionally, it also includes introducing a fermentation-promoting substance into the fermentation chamber through a feed inlet.

[0074] The fermentation effect of microorganisms in the fermentation chamber is enhanced by using fermentation-promoting substances.

[0075] Optionally, the fermentation-promoting substance is selected from at least one of sawdust, cow dung, and rice straw.

[0076] Optionally, the demulsifier is selected from at least one of sodium lignosulfonate, tetrasodium ethylenediaminetetraacetate, ethylenediamine, polyquaternium salt, polyether polyquaternium salt, glycerol, nonylphenol polyoxyethylene ether, polyacrylate, sodium dodecylbenzenesulfonate, and hexadecyltrimethylammonium bromide.

[0077] Optionally, the amount of the demulsifier added relative to the oily sludge is 0.5 to 6 g / L.

[0078] The moisture content and properties of the oily sludge being treated are adjusted accordingly, with 2.5 g / L being the preferred value.

[0079] Optionally, the survival temperature of the biological bacterial solution is 35-95℃, and the usage temperature of the biological bacterial solution is 60-80℃, preferably 70-75℃.

[0080] Optionally, the method further includes introducing acidic gas and oxygen into the fermentation chamber to mix the acidic gas and oxygen with the oily sludge.

[0081] Optionally, the acidic gas is an acidic gas containing SO2, wherein the SO2 content ranges from 100 to 1000 ppm; and the oxygen content ranges from 6% to 20%.

[0082] Optionally, the acidic gas and oxygen are provided by the waste flue gas from the plant area, wherein the temperature of the waste flue gas is 120-300℃, preferably 150-200℃.

[0083] The waste flue gas from the plant can be used to heat the fermentation chamber.

[0084] The waste gas generated during the fermentation process enters the flue gas purification unit of the factory through the outlet along with the waste flue gas in the factory area. This device has no waste gas emissions and can achieve synergistic purification of the waste flue gas in the factory area. The desulfurization rate of the waste flue gas in the factory area can reach 5-50%.

[0085] Optionally, when the bio-liquid with the function of fermenting oily sludge is introduced into the fermentation chamber through the inlet, it also includes the introduction of a bio-liquid with the function of degrading H2S gas into the fermentation chamber.

[0086] The biological liquid includes both biological liquids that can ferment oily sludge and biological liquids that can degrade H2S gas. Therefore, it has the functions of fermenting oily sludge and degrading H2S gas, and can purify the waste flue gas in the factory area.

[0087] According to a specific embodiment of the present invention, the bio-bacterial liquid with the function of degrading H2S gas is obtained by sampling from at least one of kitchen waste, mineral soil and activated sludge, and by high-temperature cultivation, enrichment and screening in a sterilized crude oil culture medium with H2S atmosphere. The bio-bacterial liquid contains at least one of Dietzia sp., Enterobacteriaceae sp. and Lysinibacillus sp.

[0088] Optionally, the volume ratio of the waste flue gas from the plant area to the oily sludge input into the fermentation chamber is 1:1-500:1, preferably 80:1.

[0089] By adjusting the appropriate amount of waste gas added from the plant area, it is ensured that the waste gas generated from the demulsification and fermentation of oily sludge can be completely carried out of the outlet. Furthermore, the heat exchange between the waste gas and the oily sludge is controlled to prevent excessively high temperatures from causing the fermentation microorganisms to become inactive. Additionally, the water generated after demulsification and fermentation is promoted to be carried away from the fermentation chamber in the form of water vapor by the waste gas from the plant area, thereby improving the purity of oil recovery.

[0090] Optionally, the temperature of the oily sludge in the fermentation chamber is 50-85°C, preferably 70-75°C.

[0091] Heating within the fermentation chamber is accomplished by a combination of heating components and waste flue gas from the plant.

[0092] Optionally, the oxygen concentration in the front part of the fermentation chamber is greater than 15%, and the oxygen concentration in the middle and rear parts of the fermentation chamber is less than 10%.

[0093] Optionally, the residence time of the oily sludge in the fermentation chamber is 6-24 hours, preferably 12 hours.

[0094] Optionally, it also includes providing a negative pressure environment at the end of the capillary channel away from the fermentation chamber.

[0095] Optionally, a portion of the solid product is refluxed back to the fermentation chamber, and the ratio of the flow rate of the solid product refluxed back to the fermentation chamber to the flow rate of the oily sludge input into the fermentation chamber is 1:5 to 1:50, preferably 1:20.

[0096] Optionally, when a liquid collection tank communicating with the capillary channel is provided on the outer side of the outer wall of the shell, and a negative pressure pipe is provided on the liquid collection tank, the gas in the liquid collection tank is extracted so that the pressure in the liquid collection tank is 0.085-0.095 MPa and the pressure in the shell is 0.105-0.13 MPa.

[0097] Optionally, the process also includes oil-water separation of the exported liquid.

[0098] Optionally, the biological liquid with the function of fermenting oily sludge includes at least one of Streptococcus, Micrococcus, and Zoococcus.

[0099] Optionally, the concentration of the biological bacterial solution with the function of fermenting oily sludge is higher than 5 × 10⁻⁶. 7 The amount of the biological bacterial solution with fermentation function for oily sludge is 2-30 kg / mL.

[0100] Optionally, the bio-liquid with the function of degrading H2S gas includes at least one of the genera *Dizzyella*, *Enterobacter*, and *Lysinobacter*.

[0101] Optionally, the concentration of the biological bacterial solution with H2S degradation function is higher than 10. 8 The amount of the biological bacterial solution with H2S degradation function added is 0.1-3 kg / mL.

[0102] According to a specific embodiment of the present invention, the biological liquid includes a biological liquid with the function of fermenting oily sludge and a biological liquid with the function of degrading H2S gas. The weight ratio of the biological liquid with the function of fermenting oily sludge to the biological liquid with the function of degrading H2S gas is in the range of 5:1 to 30:1.

[0103] According to a specific embodiment of the present invention, the method for reducing the volume of oily sludge includes the following steps:

[0104] S1: Feeding

[0105] After the oily sludge to be treated is mixed with a certain proportion of demulsifier, it is fed into the fermentation chamber inside the shell through the feed inlet. The waste flue gas from the plant area after dust removal is fed into the fermentation chamber through the air inlet, air inlet channel and air distribution port. When the device is started for the first time, a certain proportion of biological liquid with the function of fermenting oily sludge and biological liquid with the function of degrading H2S gas are added to the oily sludge through the feed inlet.

[0106] S2: Fermentation

[0107] Inside the fermentation chamber, the oily sludge is stirred and turned by the stirring and conveying mechanism. The gas outlet mixes the waste gas from the plant with the oily sludge evenly to provide oxygen and heat. At the same time, the oily sludge in the fermentation chamber is heated by the heating components to keep the oily sludge at a high temperature for biological fermentation. Under the push of the stirring and conveying mechanism, the oily sludge is continuously turned in the fermentation chamber and transported towards the discharge port.

[0108] S3: Discharge

[0109] The oily sludge that has undergone demulsification and biological fermentation is transported to the discharge port under the stirring and conveying mechanism, and then discharged from the fermentation chamber. The solid products are returned to the inlet in a certain proportion to mix with the oily sludge to be treated and enter the fermentation chamber together. The waste gas in the fermentation chamber is discharged from the fermentation chamber through the gas outlet and transported to the waste gas treatment unit of the plant.

[0110] S4: Separation and Recycling

[0111] After demulsification and biological fermentation, water and oil are drawn into the collection tank through capillary channels at the bottom of the fermentation chamber, and then further enter the oil-water separator. A baffle ensures that the oil and water enter from the bottom of the oil-water separator. The oil is separated into the oil storage tank by a floating plate with hollow fiber bundles. The oil is collected periodically through the oil drain for reuse, and the water is periodically transported to the plant's wastewater treatment unit for treatment through the drain outlet.

[0112] This method has the following technical advantages: (1) High-temperature demulsification combined with high-temperature microbial fermentation enables efficient treatment and reduction of oily sludge in the integrated device, thereby improving the treatment efficiency of oily sludge and reducing treatment costs.

[0113] (2) The waste heat resources of the waste flue gas in the plant area are utilized to purify SO2 in the waste flue gas. At the same time, the waste gas generated during the biological fermentation of oily sludge is diluted and swept away. The biological bacterial liquid with the function of degrading H2S gas degrades H2S generated during the fermentation of oily sludge, eliminating the pollution of waste gas during the biological treatment of oily sludge and improving the environmental benefits of the device.

[0114] (3) The introduction of waste flue gas into the plant area and the setting of the negative pressure generation structure promote the self-absorption separation of solid residue and liquid oil and water after fermentation of oily sludge by the construction of micro pressure difference, thereby achieving simple operation and low cost of solid-liquid separation and improving separation efficiency. The oil-water separation structure achieves efficient and low cost oil-water separation through hollow fiber bundles, realizing the recovery of high-quality oil products and improving the economic benefits of the device.

[0115] (4) During the reduction treatment of oily sludge, the device can efficiently achieve integrated demulsification and biological fermentation in stages by setting multiple temperature detection components and segmented frequency conversion heating rods. It can also be automatically controlled by a PLC control system, so as to realize the simple operation of the device and recover high-quality oil resources, thus improving the ease of operation of the device.

[0116] This invention provides an oily sludge reduction treatment device and method, the advantages of which are as follows: The oily sludge reduction treatment device has a fermentation chamber inside the shell, and a stirring and conveying mechanism is installed in the fermentation chamber. Oily sludge, demulsifier, and biological bacterial liquid with the function of fermenting oily sludge can be introduced into the fermentation chamber through the inlet. At the same time, a heating component heats it to provide a suitable fermentation temperature, so that the oily sludge undergoes biological fermentation in the fermentation chamber and moves towards the outlet under the stirring and conveying action of the stirring and conveying mechanism. Fermentation produces liquid, gas, and solid products. The liquid is oil and water, which are absorbed and discharged in liquid form through capillary channels for collection. The solid products can be discharged through the outlet for further deep treatment and resource utilization. The gas includes waste gas and water vapor generated during the fermentation process, which are discharged through the gas outlet for further deep treatment. This not only avoids gas... Pollution can be eliminated, and water vapor can be discharged in a timely manner, improving the purity of oil recovery. In a preferred embodiment, the waste flue gas from the factory, including acidic gases and oxygen, is introduced into the fermentation chamber through the air intake structure, and a biological liquid with the function of degrading H2S gas is added. The waste heat in the waste flue gas can be utilized to heat the fermentation environment, saving heating energy and ensuring the supply of oxygen. Moreover, the fermentation process can also play a certain role in desulfurization and purification of the waste flue gas. In another preferred embodiment, the drain port on the liquid collection tank located below the shell is also connected to an oil-water separation structure. The liquid in the liquid collection tank enters the second space at the bottom of the oil-water separation tank after passing through the first space. The floating plate in the second space floats at the oil-water interface. Through the capillary channel formed by the hollow fiber bundles on the floating plate, the upper layer of oil is introduced into the oil storage tank located below the oil-water separation tank, realizing oil-water separation and ensuring the quality of the oil.

[0117] Other features and advantages of the present invention will be described in detail in the following detailed description section. Attached Figure Description

[0118] The above and other objects, features and advantages of the present invention will become more apparent from the more detailed description of exemplary embodiments of the invention in conjunction with the accompanying drawings, wherein the same reference numerals generally represent the same components in the exemplary embodiments of the invention.

[0119] Figure 1 A schematic diagram of an oily sludge reduction treatment device according to Embodiment 1 of the present invention is shown.

[0120] Figure 2 Show Figure 1 A schematic diagram of the cross-sectional structure.

[0121] Figure 3 A top view schematic diagram of the oil-water separation structure of an oily sludge reduction treatment device according to Embodiment 1 of the present invention is shown.

[0122] Figure 4 A flowchart of a method for reducing the volume of oily sludge according to Embodiment 2 of the present invention is shown.

[0123] Explanation of reference numerals in the attached figures:

[0124] 1. Shell; 2. Fermentation chamber; 3. Inlet; 4. Outlet; 5. Capillary channel; 6. Heating component; 7. Gas outlet; 8. Liquid collection tank; 9. Heat-conducting layer; 10. Liquid delivery pipeline; 11. Oil-water separator; 12. Baffle; 13. Oil storage tank; 14. Float; 15. First limiting part; 16. Second limiting part; 17. Oil outlet; 18. Hollow fiber bundle; 19. Sealing part; 20. Oil outlet; 21. Oil outlet valve; 22. Drain outlet; 23. Drain valve; 24. Level gauge; 25. Rotating shaft; 26. Drive motor; 27. Stirring and conveying blades; 28. Sealing component; 29. ​​Air inlet channel; 30. Air inlet; 31. Negative pressure pipe; 32. Material return pipe; 33. Exhaust valve; 34. Air distribution port. Detailed Implementation

[0125] Preferred embodiments of the invention will now be described in more detail. While preferred embodiments of the invention are described below, it should be understood that the invention can be implemented in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that the invention will be thorough and complete, and will fully convey the scope of the invention to those skilled in the art.

[0126] Example 1

[0127] like Figures 1 to 3 As shown, this embodiment provides an oily sludge reduction treatment device, which includes:

[0128] The shell 1 has a fermentation chamber 2 inside. The two ends of the shell 1 are respectively provided with an inlet 3 and an outlet 4 communicating with the fermentation chamber 2. The side wall of the fermentation chamber 2 is provided with capillary channels 5 communicating with the fermentation chamber 2. A heating element 6 is provided inside the side wall of the fermentation chamber 2. An air outlet 7 is provided at the top of the fermentation chamber 2.

[0129] A stirring and conveying mechanism is installed inside the housing 1 and is used to stir and convey the materials in the fermentation chamber 2.

[0130] A liquid collection tank 8, which communicates with capillary channels 5, is provided on the outer side of the outer wall of the shell 1. The liquid collection tank 8 is connected to the outer wall of the shell 1, forming a liquid collection space on the outer side of the outer wall of the shell 1. The liquid produced by fermentation in the oily sludge reduction treatment device can be discharged from the first chamber through the capillary channels 5 to the liquid collection tank 8. A drain port is provided at the bottom of the liquid collection tank 8 to realize liquid discharge, keep the space inside the liquid collection tank 8 sufficient, promote the absorption of oil and water by the capillary channels 5, and discharge the liquid into the oil-water separation structure for oil-water separation.

[0131] In this embodiment, as Figure 2 As shown, a heat-conducting layer 9 is provided on the inner wall of the shell 1, and the heating component 6 passes through the heat-conducting layer 9. The heat-conducting layer 9 can improve the thermal conductivity and heating efficiency. In this embodiment, the heat-conducting layer 9 includes heat-conducting oil. Therefore, the shell 1 includes an inner shell and an outer shell, and an interlayer is formed between the inner shell and the outer shell. The heat-conducting oil is filled in the interlayer. At this time, capillary channels 5 are opened on the inner shell, and the outer shell is provided with through holes at corresponding positions. The through holes are connected to the inner shell through the cylinder so that the liquid discharged through the capillary channels 5 can flow out.

[0132] In this embodiment, an exhaust valve 33 is provided on the air outlet 7.

[0133] It also includes an oil-water separation structure, which is connected to the drain port via the infusion pipeline 10.

[0134] The oil-water separation structure includes:

[0135] Oil-water separator 11, with a vertically arranged partition 12 inside the oil-water separator 11, the partition 12 divides the inside of the oil-water separator 11 into a first space and a second space that are connected at the bottom;

[0136] Oil storage tank 13 is located below oil-water separator 11;

[0137] The floating plate 14 is movably disposed in the second space and can float at the oil-water interface. The floating plate 14 is provided with a first limiting part 15 and a second limiting part 16 connected to the inner wall of the oil-water separator 11 above and below, respectively. The floating plate 14 has multiple oil passage ports 17.

[0138] Hollow fiber bundle 18, the upper end of hollow fiber bundle 18 penetrates the floating plate 14 and forms an extension above the floating plate 14, the lower end of hollow fiber bundle 18 extends into the oil storage tank 13, and capillary channels are formed inside hollow fiber bundle 18.

[0139] A sealing part 19 is provided between the oil-water separator 11 and the oil storage tank 13 so that the oil-water separator 11 is connected to the oil storage tank 13 only through a capillary channel.

[0140] In this embodiment, as Figure 3 As shown, four oil inlets 17 are provided to ensure that oil flows from the lower part of the floating plate 14 to the upper part of the floating plate 14 through the oil inlets 17, and to ensure that the floating plate 14 floats smoothly at the interface between water and oil. The first limiting part 15 and the second limiting part 16 are both structures that protrude inward from the inner wall of the oil-water separator 11, so that the floating plate 14 can only move up and down between the two.

[0141] An oil drain port 20 is provided at the lower end of the side wall of the oil storage tank 13, and an oil drain valve 21 is provided inside the oil drain port 20. A drain outlet 22 is provided at the lower end of the side wall of the oil-water separator 11, and a drain valve 23 is provided inside the drain outlet 22. A level gauge 24 is provided inside the oil storage tank 13. A first position sensor and a second position sensor are respectively provided on the side of the first limiting part 15 and the second limiting part 16 that are close to each other.

[0142] In this embodiment, a control system is also included. The control system adopts a PLC. When the floating plate 14 rises to contact the first limit part 15, the first position sensor is triggered. At this time, the drain valve 23 needs to be opened to drain some water. When the floating plate 14 falls to contact the second limit part 16, the second position sensor is triggered. At this time, the input of liquid from the collection tank 8 to the oil-water separator 11 needs to be increased. The opening of the flow valve on the liquid delivery pipeline 10 can be controlled. When the liquid level detected by the level gauge 24 exceeds the set liquid level height, the oil drain valve 21 needs to be opened to recover and discharge the oil in the oil storage tank 13. The PLC automatically controls the above process.

[0143] The density of floating roof 14 is 0.850–0.950 g / cm³. 3 .

[0144] The pore size of capillary channels is 0.05-4 micrometers.

[0145] The inner wall of the capillary channel is coated with a hydrophobic coating, and the water droplet contact angle of the hydrophobic coating is 95-140°.

[0146] The pore size of capillary channel 5 is 0.01-2 micrometers.

[0147] The volume of capillary channels 5 accounts for 0.5-4% of the total volume of the sidewalls of fermentation chamber 2.

[0148] The stirring and conveying mechanism includes a rotating shaft 25, which is rotatably installed inside the fermentation chamber 2. One end of the rotating shaft 25 is connected to a drive motor 26, and stirring and conveying blades 27 are provided on the outer periphery of the rotating shaft 25.

[0149] The mixing and conveying mechanism drives the rotating shaft 25 through the drive motor 26 to rotate the mixing and conveying blades 27. The mixing and conveying blades 27 can mix the material while conveying the material from the position near the feed port 3 to the direction near the discharge port 4. The mixing and conveying blades 27 can be auger blades. The residence time of oily sludge in the first chamber can be controlled by controlling the rotation speed of the rotating shaft 25 and the shape of the mixing and conveying blades 27.

[0150] One end of the rotating shaft 25 passes through the side wall of the housing 1 and is connected to the drive motor 26 located outside the housing 1. A sealing component 28 connected to the housing 1 is provided on the outer periphery of the rotating shaft 25.

[0151] The drive motor 26 is a variable frequency motor.

[0152] It also includes an air intake structure, the output end of which is connected to the fermentation chamber 2 and is used to deliver acidic gas and oxygen into the fermentation chamber 2.

[0153] The intake structure includes:

[0154] The air intake passage 29 is arranged inside the rotating shaft 25 along the axial direction of the rotating shaft 25;

[0155] Multiple air distribution ports 34 are provided on the rotating shaft 25 along the axial direction of the rotating shaft 25 and connect the air intake channel 29 to the fermentation chamber 2.

[0156] Air inlet 30 is located at one end of the rotating shaft 25 near the drive motor 26.

[0157] Each air distribution port 34 is equipped with an opening adjustment valve.

[0158] In this embodiment, the opening regulating valve is connected to the PLC, enabling automatic control.

[0159] Three oxygen content detectors are installed sequentially along the material conveying direction inside fermentation chamber 2. The three oxygen content detectors are used to detect the oxygen concentration in the front, middle and rear parts of fermentation chamber 2, respectively.

[0160] Multiple temperature detection components are sequentially arranged in the fermentation chamber 2 along the material conveying direction. These components are used to detect the temperature at multiple locations within the fermentation chamber 2.

[0161] The heating element 6 is a segmented frequency conversion heating rod arranged along the axial direction of the fermentation chamber 2, which can heat the material in the fermentation chamber 2 in segments.

[0162] The liquid collection tank 8 is connected to a negative pressure generating structure, which is used to create a negative pressure environment within the liquid collection tank 8.

[0163] In this embodiment, the negative pressure generating structure includes a negative pressure pipe 31, an air pump is installed on the negative pressure pipe 31, and the negative pressure pipe 31 is connected to the infusion pipeline 10.

[0164] A material return pipe 32 is connected to the discharge port 4. A variable frequency return pump is installed on the material return pipe 32. The material return pipe 32 is connected to the feed port 3.

[0165] Examples 2A-2H and Comparative Example 1

[0166] The oily sludge was reduced in volume using the oily sludge reduction treatment device described in Example 1, and the steps were as follows: Figure 4 As shown.

[0167] Example 2A

[0168] The oily sludge to be treated has a moisture content of 40%, an oil content of 46%, a solids content of 14%, a total liquid content of 86%, and a pH of 7.6. The temperature of the waste gas from the plant area after dust removal treatment is 162℃, and the SO2 content is 236ppm. The treatment method is as follows:

[0169] S1: Feeding

[0170] The oily sludge to be treated is added to the fermentation chamber 2 through inlet 3 at a flow rate of 5 kg / h. During the initial startup of the device, 5 kg of biological bacterial solution is added at a flow rate of 0.5 kg / h. The biological bacterial solution includes a solution capable of fermenting oily sludge and a solution capable of degrading H2S gas, with a weight ratio of 9:1 and a concentration of each higher than 5*10⁻⁶. 7 cells / mL and 10 8 The fermentation agent was selected as sawdust, and it was added to fermentation chamber 2 through inlet 3 at a flow rate of 0.3 kg / h. The demulsifier was selected as polyether polyquaternary ammonium salt and sodium dodecylbenzene sulfonate in a ratio of 2:1, with an addition flow rate of 2.2 g demulsifier per liter of oily sludge. The waste gas from the plant was discharged at a rate of 0.6 m³ / mL. 3 A flow rate of / h is input into fermentation chamber 2 through air inlet 30;

[0171] S2: Fermentation

[0172] Inside fermentation chamber 2, the material inside is heated by heating component 6 and waste flue gas from the plant area. The two temperature detection positions at the front of fermentation chamber 2 are kept at 85℃, and the remaining four temperature detection positions at the rear of fermentation chamber 2 are kept at 72℃. The opening of the opening regulating valve on the gas distribution port 34 is controlled by the PLC control system to control the detection results of the oxygen content detection instruments at the front, middle and rear of fermentation chamber 2 to be 8%, 17% and 9% respectively. Driven by the stirring and conveying mechanism, the solid material moves continuously from front to back in fermentation chamber 2. The heating and demulsification process is completed in the high temperature and low oxygen zone for 2 hours. The biological fermentation process is completed in the subsequent medium-high temperature and high oxygen zone and the medium-high temperature and low oxygen zone for 8 hours.

[0173] S3: Discharge

[0174] The treated solid products are discharged from the fermentation chamber 2 through the discharge port and returned to the feed port 3 at a flow rate of 0.26 kg / h through the material return pipe 32. They are then mixed with the oily sludge to be treated and reintroduced into the fermentation chamber 2. The waste gas generated during fermentation in the fermentation chamber 2 is discharged from the plant's waste flue gas through the exhaust pipe on the exhaust port 7 to the plant's flue gas treatment unit for treatment. The solid products discharged from the fermentation chamber 2 have a moisture content of 18%, an oil content of 4%, a solid content of 78%, a weight reduction rate of 82%, and a pH of 7.2. The temperature of the gas discharged from the fermentation chamber 2 is 134℃, the SO2 content is 122 ppm, the H2S content is 12 ppm, and the VOCs content is 33 ppm.

[0175] S4: Separation and Recycling

[0176] Waste gas from the plant enters the fermentation chamber 2 through the gas distribution port 34, providing a slight positive pressure of 0.116 MPa. An air pump extracts air from the negative pressure pipe 31, creating a slight negative pressure of 0.091 MPa in the collection tank 8. Capillary channels 5 are located at the bottom of the fermentation chamber 2, with an average pore size of 1.16 micrometers. These capillary channels occupy 2.1% of the bottom volume of the fermentation chamber 2. The slight pressure difference across the capillary channels 5 allows for self-absorption and recovery of the oil-water mixture from the demulsification and fermentation of the oily sludge, which is then collected in the collection tank 8. Most of the water from the demulsification process is absorbed by microorganisms and evaporates at high temperatures to form water vapor. The oil-water mixture in the collection tank 8 is then separated by a baffle 12 and enters the oil-water separator 11 from the bottom. The density of the floating plate 14 in the oil-water separator 11 is 0.882 g / cm³. 3The floating disk 14 floats at the oil-water interface. It is equipped with capillary hollow fiber bundles 18, with capillary channel pores having a diameter of 2.68 micrometers. The capillary hollow fiber bundles 18 occupy 10% of the area of ​​the floating disk 14. Additionally, the floating disk 14 has four oil passages 17, occupying 25% of its area. The inner walls of the capillary channels in the capillary hollow fiber bundles 18 are coated with a hydrophobic coating, resulting in a water droplet contact angle of 106°. The extension of the hollow fiber bundles 18 is 16 mm above the upper surface of the floating disk 14 and is equipped with… The protective sleeve uses capillary hollow fiber bundles 18 to recover oil from the oil-water separator 11 to the oil storage tank 13. The recovered oil has a purity of >99.75%. The oil is discharged into the plant area for reuse by automatically controlling the drain valve 21 through the level gauge 24 and the PLC system. When the floating plate 14 reaches the first limit part 15 in the oil-water separator 11, the PLC control system automatically opens the drain valve 23 to discharge the water at the bottom of the oil-water separator 11 into the plant wastewater treatment system for purification.

[0177] Example 2B

[0178] The oily sludge to be treated has a moisture content of 59%, an oil content of 36%, a solids content of 5%, a total liquid content of 95%, and a pH of 7.5. The waste gas from the plant used in this device has a temperature of 183℃ and an SO2 content of 238ppm. The treatment method is as follows:

[0179] S1: Feeding

[0180] The oily sludge to be treated is added to the fermentation chamber 2 through inlet 3 at a flow rate of 30 kg / h. During the initial startup of the device, 20 kg of high-temperature biological liquid is added at a flow rate of 0.5 kg / h. The biological liquid includes both biological liquid capable of fermenting oily sludge and biological liquid capable of degrading H2S gas, with a weight ratio of 19:1 and a concentration of each higher than 5*10⁻⁶. 7 cells / mL and 10 8 The fermentation promoters were wood chips and cow manure in a 2:1 ratio, added to fermentation chamber 2 through inlet 3 at a flow rate of 0.9 kg / h. Nonylphenol polyoxyethylene ether was used as the demulsifier, added at a flow rate of 2 g per liter of oily sludge. Waste gas from the plant was discharged at a concentration of 3.3 m³ / mL. 3 A flow rate of / h is input into fermentation chamber 2 through air inlet 30;

[0181] S2: Fermentation

[0182] Inside fermentation chamber 2, the material inside is heated by heating component 6 and waste flue gas from the plant area. The two temperature detection positions at the front of fermentation chamber 2 are kept at 82℃, and the remaining four temperature detection positions at the rear of fermentation chamber 2 are kept at 73℃. The opening of the gas outlet 34 is adjusted by the PLC control system to control the detection results of the oxygen content detection instruments at the front, middle and rear of fermentation chamber 2 to be 6%, 20% and 16%, respectively. Driven by the stirring and conveying mechanism, the solid material moves continuously from front to back in fermentation chamber 2. The heating and demulsification process is completed in the high temperature and low oxygen zone for 1 hour. The biological fermentation process is completed in the subsequent medium-high temperature and high oxygen zone and the medium-high temperature and low oxygen zone for 9 hours.

[0183] S3: Discharge

[0184] The treated solid products are discharged from the fermentation chamber 2 through the discharge port and returned to the feed port 3 at a flow rate of 0.7 kg / h through the material return pipe 32. They are then mixed with the oily sludge to be treated and reintroduced into the fermentation chamber 2. The waste gas generated during fermentation in the fermentation chamber 2 is discharged from the plant's waste flue gas through the exhaust pipe on the exhaust port 7 to the plant's flue gas treatment unit for treatment. The solid products discharged from the fermentation chamber 2 have a water content of 17%, an oil content of 5%, a solid content of 78%, a weight reduction rate of 94%, and a pH of 7.0. The temperature of the gas discharged from the fermentation chamber 2 is 128℃, the SO2 content is 173 ppm, the H2S content is 12 ppm, and the VOCs content is 35 ppm.

[0185] S4: Separation and Recycling

[0186] Waste gas from the plant enters the fermentation chamber 2 through the gas distribution port 34, providing a slight positive pressure of 0.116 MPa. An air pump extracts air from the negative pressure pipe 31, creating a slight negative pressure of 0.086 MPa in the collection tank 8. Capillary channels 5 are located at the bottom of the fermentation chamber 2, with an average pore size of 0.95 micrometers. These capillary channels occupy 2.8% of the bottom volume of the fermentation chamber 2. The slight pressure difference across the capillary channels 5 enables self-absorption and recovery of the oil-water mixture separated from the demulsified and fermented oily sludge, which is then collected in the collection tank 8. The density of the floating plate 14 in the oil-water separator 11 is 0.912 g / cm³. 3The floating disk 14 floats at the oil-water interface. It is equipped with capillary hollow fiber bundles 18, wherein the pore size of the capillary channels is 1.35 micrometers. The capillary hollow fiber bundles 18 occupy 16% of the area of ​​the floating disk 14. In addition, the floating disk 14 contains four oil passages 17, occupying 24% of the area of ​​the floating disk 14. The inner walls of the capillary channels in the capillary hollow fiber bundles 18 are coated with a hydrophobic coating, resulting in a water droplet contact angle of 102°. The extension of the hollow fiber bundles 18 is 10 mm higher than the floating disk 14. Oil in the oil-water separator 11 is recovered to the oil storage tank 13 through capillary hollow fiber bundles 18. The recovered oil has a purity of >99.30%. The high-quality oil is discharged into the plant area for reuse by automatically controlling the drain valve 21 through the level gauge 24 and PLC system. When the floating plate 14 reaches the first limit part 15 in the oil-water separator 11, the PLC control system automatically opens the drain valve 23 to discharge the water at the bottom of the oil-water separator 11 into the plant wastewater treatment system for purification.

[0187] Example 2C

[0188] The oily sludge to be treated has a moisture content of 39%, an oil content of 52%, a solids content of 9%, a total liquid content of 91%, and a pH of 7.9. The waste flue gas used in this device has a temperature of 178℃ and an SO2 content of 268ppm. The treatment method is as follows:

[0189] S1: Feeding

[0190] The oily sludge to be treated is added to the fermentation chamber 2 through inlet 3 at a flow rate of 6 kg / h. During the initial startup of the device, 10 kg of high-temperature biological liquid is added at a flow rate of 0.5 kg / h. The biological liquid includes both a liquid capable of fermenting oily sludge and a liquid capable of degrading H2S gas, with a weight ratio of 9:1 and concentrations of both exceeding 5*10⁻⁶. 7 cells / mL and 10 8 The fermentation agent was wood chips, added to fermentation chamber 2 through inlet 3 at a flow rate of 0.5 kg / h. The demulsifiers were sodium ethylenediaminetetraacetate and sodium lignosulfonate in a 1:5 ratio, added at a flow rate of 2.6 g / L of oily sludge. The waste gas from the plant was discharged at a rate of 0.8 m³ / mL. 3 A flow rate of / h is input into fermentation chamber 2 through air inlet 30;

[0191] S2: Fermentation

[0192] Inside fermentation chamber 2, the material inside is heated by heating component 6 and waste flue gas from the plant area. The temperature detection positions at the front two parts of fermentation chamber 2 are maintained at 86℃, and the remaining four temperature detection positions at the rear fermentation chamber 2 are maintained at 75℃. The opening of the gas distribution port 34 is controlled by the PLC control system to control the detection results of the oxygen content detection instruments at the front, middle and rear of fermentation chamber 2 to be 5%, 18% and 10% respectively. Driven by the stirring and conveying mechanism, the solid material moves continuously from front to back in fermentation chamber 2. The heating and demulsification process is completed in the high temperature and low oxygen zone for 2 hours. The biological fermentation process is completed in the subsequent medium-high temperature and high oxygen zone and the medium-high temperature and low oxygen zone for 10 hours.

[0193] S3: Discharge

[0194] The treated solid products are discharged from the fermentation chamber 2 through the discharge port and returned to the feed port 3 at a flow rate of 0.2 kg / h through the material return pipe 32. They are then mixed with the oily sludge to be treated and reintroduced into the fermentation chamber 2. The waste gas generated during fermentation in the fermentation chamber 2 is discharged from the plant's waste flue gas through the exhaust pipe on the exhaust port 7 to the plant's flue gas treatment unit for treatment. The solid products discharged from the fermentation chamber 2 have a water content of 11%, an oil content of 7%, a solid content of 82%, a weight reduction rate of 89%, and a pH of 7.3. The temperature of the gas discharged from the fermentation chamber 2 is 129℃, the SO2 content is 153 ppm, the H2S content is 19 ppm, and the VOCs content is 38 ppm.

[0195] S4: Separation and Recycling

[0196] Waste gas from the plant enters the fermentation chamber 2 through the gas distribution port 34, providing a slight positive pressure of 0.121 MPa. An air pump extracts air from the negative pressure pipe 31, creating a slight negative pressure of 0.088 MPa in the collection tank 8. Capillary channels 5 are located at the bottom of the fermentation chamber 2, with an average pore size of 0.98 micrometers. These capillary channels occupy 2.3% of the bottom volume of the fermentation chamber 2. The slight pressure difference across the capillary channels 5 allows for self-absorption and recovery of the oil-water mixture from the demulsification and fermentation of the oily sludge, which is then collected in the collection tank 8. Most of the water from the demulsification process is absorbed by microorganisms and evaporates at high temperatures to form water vapor. The oil-water mixture in the collection tank 8 is then separated by a baffle 12 and enters the oil-water separator 11 from the bottom. The density of the floating plate 14 in the oil-water separator 11 is 0.893 g / cm³. 3The floating disk 14 floats at the oil-water interface. It is equipped with capillary hollow fiber bundles 18, with capillary channel pores having a diameter of 1.62 micrometers. The capillary hollow fiber bundles 18 occupy 12.5% ​​of the area of ​​the floating disk 14. Additionally, the floating disk 14 contains four oil passages 17, occupying 28% of its area. The inner walls of the capillary channels 5 in the capillary hollow fiber bundles 18 are coated with a hydrophobic coating, resulting in a water droplet contact angle of 113°. The extension of the hollow fiber bundles 18 is 10 cm higher than the floating disk 14. mm, the oil in the oil-water separator 11 is recovered to the oil storage tank 13 through the capillary hollow fiber bundle 18. The purity of the recovered oil is >99.80%. The oil discharge valve 21 is controlled by the level gauge 24 and the PLC system to collect high-quality oil for reuse in the plant area. When the floating plate 14 reaches the first limit part 15 in the oil-water separator 11, the PLC control system automatically opens the drain valve 23 to discharge the water at the bottom of the oil-water separator 11 into the plant wastewater treatment system for purification.

[0197] Comparative Example 1

[0198] The same apparatus as in Example 2A was used, but instead of using waste flue gas from the factory, air was used. The output power of the heating element 6 was kept the same as in Example 2A. To maintain a consistent oxygen concentration in the fermentation chamber 2 when using air, the air flow rate was changed to 0.03 m³ / s. 3 / h.

[0199] In S1, except that the waste flue gas from the plant area is replaced with air, the other feeding conditions are the same as those in Example 2A.

[0200] During the S2 fermentation process, the temperature at the two temperature monitoring positions at the front of fermentation chamber 2 was 78℃, and the temperature at the other four temperature monitoring positions in the middle and rear of fermentation chamber 2 was 65℃.

[0201] During the discharge process of S3, the solid product discharged from fermentation chamber 2 has a moisture content of 23%, an oil content of 30%, a solid content of 47%, a weight loss rate of 70%, and a pH of 7.6. The temperature of the gas discharged from fermentation chamber 2 is 28℃, the SO2 content is 1ppm, the H2S content is 166ppm, and the VOCs content is 382ppm.

[0202] During the S4 separation and recovery process, no waste gas enters the fermentation chamber 2. After the air is replaced, in order to maintain the oxygen concentration in the fermentation chamber 2 as consistent with that in Example 2A, the air flow rate is reduced compared to the waste gas flow rate in the plant area. The slight positive pressure in the fermentation chamber 2 is reduced to 0.103 MPa. Due to the pressure drop, the volume of the recovered oil-water mixture is reduced by 23% compared to Example 2A.

[0203] Compared with Example 2A, it was found that after the waste flue gas in the plant area was replaced with air, the temperature in fermentation chamber 2 decreased, the pH of the oily sludge was higher, and the overall oily sludge reduction effect was reduced. Due to the reduction in air flow, the micro-positive pressure in fermentation chamber 2 decreased, resulting in a reduction in oil and water recovery. The concentration of pollutants such as H2S and VOCs generated during the demulsification and fermentation process of oily sludge was high when carried out by the air, which meant that the air used after being discharged from fermentation chamber 2 needed to be purified before it could be discharged, thus reducing the environmental performance.

[0204] Examples 2D1-2D19

[0205] The apparatus and method used are the same as those in Example 2A, but the composition of the waste flue gas from the plant area differs. The parameters of the treated oily sludge corresponding to the different waste flue gas composition contents are shown in Table 1 below:

[0206] Table 1

[0207]

[0208] The comparison revealed that when the device performs oily sludge reduction treatment, the waste flue gas from the plant has a certain temperature and SO2 content. During the treatment process, it can not only synergistically treat SO2, but also regulate the pH of the oily sludge, thereby enhancing the demulsification and biological treatment effects of the oily sludge and strengthening the oily sludge reduction effect.

[0209] When the flue gas temperature is between 120-300℃, the reduction effect of oily sludge is better, with a reduction rate of over 75%, especially when the flue gas temperature is between 150-200℃, the reduction rate is over 80%. When the SO2 content is above 100ppm, the oily sludge can be regulated to have a lower and more suitable pH, resulting in a better reduction effect of over 75%. When SO2 is less than 100ppm, the pH of the oily sludge is higher, the reduction effect is worse, and the reduction rate is less than 75%.

[0210] Examples 2E1-2E7

[0211] The same apparatus and method as in Example 2C were used, but the temperature distribution and oxygen content in the front, middle and rear parts of fermentation chamber 2 were different during the treatment process. The parameters of the treated oily sludge corresponding to the different temperature and oxygen content distributions are shown in Table 2 below:

[0212] Table 2

[0213]

[0214] The comparison revealed that adjusting the temperature and oxygen content in the front, middle, and rear parts of fermentation chamber 2 could improve the demulsification and fermentation treatment effect of oily sludge.

[0215] When temperature and oxygen concentration are controlled in zones within fermentation chamber 2 (Example 2C), the reduction rate of oily sludge can reach as high as 89%; when only oxygen concentration is controlled in zones (Examples 2E1-2E3), even with optimized temperature parameters, the reduction rate is only up to 87%; when only temperature is controlled in zones (Examples 2E6 and 2E7), the reduction rate can only reach 87%; for non-zone control of temperature and oxygen concentration (Examples 2E4 and 2E5), the reduction effect of oily sludge is significantly worse, with reduction rates of 75% and 83%.

[0216] Examples 2F1-2F17

[0217] Using the same apparatus and method as in Example 2A, but changing the amount of biological liquid added to fermentation chamber 2, the flow rate of fermentation-promoting substances, and the sludge return flow rate, the corresponding parameters of the treated oily sludge are shown in Table 3 below:

[0218] Table 3

[0219]

[0220]

[0221] Comparative analysis revealed that adjusting the appropriate amount of high-temperature biological solution, sawdust feed rate, and sludge return flow rate can achieve a high oil sludge reduction rate. Maintaining the biological solution dosage within the range of 2-30 kg maintains an oil sludge reduction rate of over 80%. Simultaneously maintaining a sawdust feed rate of 0.3 kg / h and a sludge return flow rate of 0.26 kg / h ensures a high oil sludge treatment efficiency.

[0222] Examples 2G1-2G17

[0223] The same apparatus and method as in Example 2A were used, but the capillary channel 5 size, capillary channel 5 volume ratio, and micro-pressure difference were different. The results of the oil sludge reduction rate after treatment corresponding to different capillary channel 5 size, capillary channel 5 volume ratio, and micro-pressure difference parameters are shown in Table 4 below:

[0224] Table 4

[0225]

[0226]

[0227] The comparison revealed that maintaining the pore size of capillary channel 5 below 2μm resulted in better oil sludge reduction. Furthermore, capillary channel 5 required a certain volume fraction. When the volume fraction was above 0.5-4.0%, the oil sludge reduction rate was higher, remaining above 75%. The presence of micro-pressure difference also significantly affected the oil sludge reduction effect. Within the micro-pressure difference range of ≤0.045, the larger the micro-pressure difference, the better the oil sludge treatment effect.

[0228] Examples 2H1-2H15

[0229] Using the same apparatus and method as in Example 2A, but with differences in the capillary channel pore size, capillary channel area ratio, oil outlet area ratio 17, and hydrophilicity of the hydrophobic coating on the inner wall of the capillary channel in the hollow fiber bundle 18 of the oil-water separator 11, the resulting oil purity is shown in Table 5 below:

[0230] Table 5

[0231]

[0232]

[0233] The comparison revealed that controlling the capillary channel pore size to 4μm can achieve better oil recovery purity. Adjusting the appropriate area ratio of hollow fiber bundle 18 and oil passage 17 is beneficial to improving the purity of recovered oil. When the water droplet contact angle of the hydrophobic coating is above 90°, high-purity oil resources can be recovered.

[0234] Compared with CN115504643A and CN113816577A, this embodiment uses an integrated fermentation chamber 2 to achieve efficient demulsification and biological fermentation of oily sludge. It also enhances the heating and demulsification effect of oily sludge by utilizing waste flue gas from the plant through porous gas distribution, and achieves self-aspiration recovery of oil and water resources through the construction of micro-pressure difference capillary channels 5. Furthermore, it achieves oil-water separation through the design of a floating disc 14 with hollow fiber bundles 18, realizing the recovery of high-quality oil (>98.5%) resources. The device is equipped with a PLC control system, which can automatically control the temperature and oxygen distribution to optimize the demulsification and fermentation effect of oily sludge. The PLC control system can simplify the operation of the device and realize the automatic opening and closing of the device valves, improving the operability and economy of the device for biological treatment of oily sludge.

[0235] The various embodiments of the present invention have been described above. These descriptions are exemplary and not exhaustive, nor are they limited to the disclosed embodiments. Many modifications and variations will be apparent to those skilled in the art without departing from the scope and spirit of the described embodiments.

Claims

1. A device for reducing the volume of oily sludge, characterized in that, The device includes: The shell has a fermentation chamber inside. The two ends of the shell are respectively provided with an inlet and an outlet communicating with the fermentation chamber. The side wall of the fermentation chamber is provided with capillary channels communicating with the fermentation chamber. A heating element is provided inside the side wall of the fermentation chamber. An air outlet is provided at the top of the fermentation chamber. A stirring and conveying mechanism is disposed inside the housing and is used to stir and convey the materials in the fermentation chamber. An air intake structure, the output end of which is connected to the fermentation chamber and is used to supply acidic gas and oxygen into the fermentation chamber; The outer side of the outer wall of the shell is provided with a liquid collection tank that communicates with the capillary channel, and the bottom of the liquid collection tank is provided with a drain outlet. An oil-water separation structure is provided, wherein the oil-water separation structure is connected to the drain port via a liquid delivery pipeline; The oil-water separation structure includes: An oil-water separator tank, wherein a partition is vertically arranged inside the oil-water separator tank, the partition dividing the interior of the oil-water separator tank into a first space and a second space that are connected at the bottom; An oil storage tank is located below the oil-water separator. A floating roof is movably disposed within the second space. The floating roof is capable of floating at the oil-water interface. A first limiting part and a second limiting part connected to the inner wall of the oil-water separator are respectively provided above and below the floating roof. The floating roof has multiple oil passages. A hollow fiber bundle, the upper end of which penetrates the floating disk and forms an extension above the floating disk, the lower end of which extends into the oil storage tank, a capillary channel is formed inside the hollow fiber bundle, and a hydrophobic coating is provided on the inner wall of the capillary channel, the water droplet contact angle of the hydrophobic coating being 95-140°. A sealing part is provided between the oil-water separator and the oil storage tank so that the oil-water separator is connected to the oil storage tank only through the capillary channel.

2. The oily sludge reduction treatment device according to claim 1, characterized in that, The lower end of the side wall of the oil storage tank is provided with an oil drain port, and an oil drain valve is provided inside the oil drain port. The lower end of the side wall of the oil-water separator is provided with a drain outlet, and a drain valve is provided inside the drain outlet. A level gauge is provided inside the oil storage tank. A first position sensor and a second position sensor are respectively provided on the side of the first limiting part and the second limiting part that are close to each other.

3. The oily sludge reduction treatment device according to claim 1, characterized in that, The density of the floating roof is 0.850~0.950 g / cm³. 3 .

4. The oily sludge reduction treatment device according to claim 1, characterized in that, The capillary channel has a pore size of 0.05-4 micrometers.

5. The oily sludge reduction treatment device according to claim 1, characterized in that, The pore size of the capillary channels is 0.01-2 micrometers.

6. The oily sludge reduction treatment device according to claim 1, characterized in that, The volume ratio of the capillary channels is 0.5-4% relative to the total volume of the sidewalls of the fermentation chamber.

7. The oily sludge reduction treatment device according to claim 1, characterized in that, The stirring and conveying mechanism includes a rotating shaft that rotatably passes through the fermentation chamber. One end of the rotating shaft is connected to a drive motor, and stirring and conveying blades are provided on the outer periphery of the rotating shaft.

8. The oily sludge reduction treatment device according to claim 7, characterized in that, The drive motor is a variable frequency motor.

9. The oily sludge reduction treatment device according to claim 7, characterized in that, The air intake structure includes: An air intake passage is provided inside the rotating shaft along the axial direction of the rotating shaft; Multiple air distribution ports are provided, which are opened on the rotating shaft along the axial direction of the rotating shaft and connect the air intake channel to the fermentation chamber; An air inlet is located at one end of the rotating shaft near the drive motor.

10. The oily sludge reduction treatment device according to claim 9, characterized in that, Each of the air distribution ports is equipped with an opening adjustment valve.

11. The oily sludge reduction treatment device according to claim 1, characterized in that, Three oxygen content detectors are sequentially arranged in the fermentation chamber along the material conveying direction. The three oxygen content detectors are used to detect the oxygen concentration in the front, middle and rear parts of the fermentation chamber, respectively.

12. The oily sludge reduction treatment device according to claim 1, characterized in that, Multiple temperature detection components are sequentially arranged in the fermentation chamber along the material conveying direction. These multiple temperature detection components are used to detect the temperature at multiple locations within the fermentation chamber.

13. The oily sludge reduction treatment device according to claim 12, characterized in that, The heating element is a segmented frequency conversion heating rod arranged along the axial direction of the fermentation chamber, which can heat the material in the fermentation chamber in segments.

14. The oily sludge reduction treatment device according to claim 1, characterized in that, The liquid collection tank is connected to a negative pressure generating structure, which is used to create a negative pressure environment within the liquid collection tank.

15. The oily sludge reduction treatment device according to claim 1, characterized in that, A material return pipe is connected to the discharge port, and a variable frequency return pump is installed on the material return pipe. The material return pipe is connected to the inlet.

16. A method for reducing the volume of oily sludge, utilizing the oily sludge reduction treatment device according to any one of claims 1-15, characterized in that, The method includes: Oily sludge, demulsifier, and biological bacterial solution with the function of fermenting oily sludge are fed into the fermentation chamber through the inlet; Acidic gas and oxygen are introduced into the fermentation chamber to mix the acidic gas and oxygen with the oily sludge; The materials within the fermentation chamber are heated, stirred, and conveyed. At least a portion of the liquid produced in the fermentation chamber is drained through capillary channels; At least a portion of the gas generated in the fermentation chamber is discharged through the vent. The solid products generated in the fermentation chamber are discharged through the discharge port; The exported liquid is subjected to oil-water separation.

17. The method for reducing the volume of oily sludge according to claim 16, characterized in that, The oily sludge has a water content higher than 35%, an oil content higher than 35%, and a total liquid content higher than 80%.

18. The method for reducing the volume of oily sludge according to claim 16, characterized in that, It also includes introducing fermentation-promoting substances into the fermentation chamber through the feed inlet.

19. The method for reducing the volume of oily sludge according to claim 18, characterized in that, The fermentation-promoting substance is selected from at least one of sawdust, cow dung, and rice straw.

20. The method for reducing the volume of oily sludge according to claim 16, characterized in that, The demulsifier is selected from at least one of sodium lignosulfonate, ethylenediaminetetraacetic acid tetrasodium, ethylenediamine, polyquaternium salt, polyether polyquaternium salt, glycerol, nonylphenol polyoxyethylene ether, polyacrylate, sodium dodecylbenzenesulfonate, and hexadecyltrimethylammonium bromide.

21. The method for reducing the volume of oily sludge according to claim 16, characterized in that, The amount of demulsifier added relative to the oily sludge is 0.5~6 g / L.

22. The method for reducing the volume of oily sludge according to claim 16, characterized in that, The survival temperature of the biological bacterial solution is 35-95℃, and the usage temperature of the biological bacterial solution is 60-80℃.

23. The method for reducing the volume of oily sludge according to claim 16, characterized in that, The acidic gas is an acidic gas containing SO2, wherein the SO2 content ranges from 100 to 1000 ppm; the oxygen content ranges from 6% to 20%.

24. The method for reducing the volume of oily sludge according to claim 23, characterized in that, The acidic gas and oxygen are provided by the waste flue gas from the factory area, and the temperature of the waste flue gas from the factory area is 120-300℃.

25. The method for reducing the volume of oily sludge according to claim 24, characterized in that, When the bio-liquid with the function of fermenting oily sludge is introduced into the fermentation chamber through the inlet, it also includes the introduction of bio-liquid with the function of degrading H2S gas into the fermentation chamber.

26. The method for reducing the volume of oily sludge according to claim 24, characterized in that, The volume ratio of the waste flue gas from the plant area to the oily sludge input into the fermentation chamber is 1:1 to 500:

1.

27. The method for reducing the volume of oily sludge according to claim 16, characterized in that, The temperature of the oily sludge in the fermentation chamber is 50-85℃.

28. The method for reducing the volume of oily sludge according to claim 16, characterized in that, The oxygen concentration in the front part of the fermentation chamber is greater than 15%, while the oxygen concentration in the middle and rear parts of the fermentation chamber is less than 10%.

29. The method for reducing the volume of oily sludge according to claim 16, characterized in that, The oily sludge stays in the fermentation chamber for 6-24 hours.

30. The method for reducing the volume of oily sludge according to claim 16, characterized in that, It also includes providing a negative pressure environment at the end of the capillary channel away from the fermentation chamber.

31. The method for reducing the volume of oily sludge according to claim 16, characterized in that, A portion of the solid product is returned to the fermentation chamber, and the ratio of the flow rate of the solid product returned to the fermentation chamber to the flow rate of the oily sludge input into the fermentation chamber is 1:5 to 1:

50.

32. The method for reducing the volume of oily sludge according to claim 16, characterized in that, When a liquid collection tank communicating with the capillary channel is provided on the outer side of the outer wall of the shell, and a negative pressure pipe is provided on the liquid collection tank, the gas in the liquid collection tank is extracted so that the pressure in the liquid collection tank is 0.085~0.095MPa and the pressure in the shell is 0.105~0.13MPa.

33. The method for reducing the volume of oily sludge according to claim 16, characterized in that, The biological liquid with the function of fermenting oily sludge includes at least one of Streptococcus, Micrococcus, and Zoococcus.

34. The method for reducing the volume of oily sludge according to claim 33, characterized in that, The concentration of the bio-liquid with the function of fermenting oily sludge is higher than 5×10⁻⁶. 7 The amount of the biological bacterial solution with fermentation function for oily sludge is 2-30 kg / mL.

35. The method for reducing the volume of oily sludge according to claim 25, characterized in that, The bio-liquid with the function of degrading H2S gas includes at least one of the genera *Dizzyella*, *Enterobacter*, and *Lysinobacter*.

36. The method for reducing the volume of oily sludge according to claim 35, characterized in that, The concentration of the bio-liquid with H2S gas degradation function is higher than 10%. 8 The amount of the biological bacterial solution with H2S degradation function added is 0.1-3 kg / mL.

37. The method for reducing the volume of oily sludge according to claim 22, characterized in that, The operating temperature of the biological bacterial solution is 70-75℃.

38. The method for reducing the volume of oily sludge according to claim 24, characterized in that, The temperature of the waste flue gas in the plant area is 150-200℃.

39. The method for reducing the volume of oily sludge according to claim 27, characterized in that, The temperature of the oily sludge in the fermentation chamber is 70-75℃.

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