Efficient separation system for three-phase components of oily sludge and separation method thereof

Abstract

The invention discloses an efficient separation system for three-phase components of oily sludge and a separation method of the efficient separation system. The system comprises a homogenizing and tempering tank for dilution and viscosity reduction, a demulsification unit for chemical agent demulsification and thermal vibration agglomeration demulsification, a separation unit for three-phase separation and a recovery unit for recovering oil liquid, wastewater and oil sludge waste residues, an oil-containing sludge inlet of the homogenizing and conditioning tank is communicated with an oil-containing sludge outlet of the oil-containing sludge storage tank, a water inlet of the homogenizing and conditioning tank is communicated with a water outlet of the wastewater heating tank, and an oil-containing sludge outlet of the homogenizing and conditioning tank is communicated with an oil-containing sludge inlet of the demulsification unit; an oil-containing sludge outlet of the demulsification unit is communicated with an oil-containing sludge inlet of the separation unit; an oil phase outlet, a water phase outlet and an oil sludge solid phase outlet of the separation unit are respectively communicated with an oil phase inlet, a water phase inlet and an oil sludge solid phase inlet of the recovery unit; the oil-containing sludge is destabilized in a multi-stage enhanced synergistic demulsification mode, and efficient separation of three-phase components of the oil-containing sludge is realized through solid-liquid separation and oil-water separation.

Description

Technical Field

[0001] The invention relates to the technical field of oily sludge treatment, and in particular to a high-efficiency separation system and a separation method for three-phase components of oily sludge. Background Art

[0002] With the high-quality development of the national economy, the demand for oil resources continues to increase. At the same time, the output of oily sludge solid waste in the process of oil extraction, transportation, storage, refining and other treatment processes is also increasing. At present, the estimated annual output of oily sludge in my country's petrochemical industry has exceeded 6 million tons, and the cumulative total inventory will reach 143 million tons. A medium-sized refinery also produces more than 30,000 tons of oily sludge each year. The treatment of oily sludge has always been a problem that has plagued petrochemical companies, posing a serious threat to the environment and human health.

[0003] According to the source of production, oily sludge can be divided into oilfield sludge, storage and transportation sludge, tank bottom sludge, refinery sludge and accident sludge. On the one hand, oily sludge mainly contains three major components, namely petroleum hydrocarbons (especially polycyclic aromatic hydrocarbons), heavy metals and pathogenic microorganisms. Typical oily sludge contains 15% to 90% oil, 20% to 70% water and 5% to 45% solids. The oil phase contains high concentrations of aromatic hydrocarbons, saturated hydrocarbons, resins and asphaltene, and the resource utilization value is extremely high; on the other hand, oily sludge is usually a semi-solid waste composed of oil-in-water emulsion, water-in-oil emulsion and solid suspension. Generally speaking, the particles in oily sludge are small and flocculent, with high water holding capacity, and the solid particles, oil and water form a stable emulsion structure, which leads to high viscosity and difficulty in precipitation of oily sludge, making it difficult to handle.

[0004] At present, there are still many problems in the existing oil sludge separation process, such as low oil phase recovery rate after treatment, high oil and water content of solid waste, and average separation effect; large amount of chemical agents used, which easily causes secondary pollution; long process flow, high separation cost, and great operation difficulty.

[0005] The Chinese invention patent with announcement number CN110922015B discloses a harmless treatment method and system for fluidized oily sludge. The fluidized oily sludge is treated by multiple methods such as flotation oil removal, centrifugal separation, and high-temperature pyrolysis, thereby reducing the solid phase oil content. However, since the flotation method is only applicable to low-viscosity oily sludge, and the pyrolysis equipment is expensive, difficult to operate, and easily causes air pollution, it is difficult to apply in actual situations.

[0006] A Chinese utility model with announcement number CN213924380U discloses an oilfield water-oil sludge separation system, which adds reagents to the oilfield sludge, heats it with an electric heating system, and then stirs it through a demulsification sedimentation separation tank to separate the oil, water and solid layers. However, the separation efficiency of the sedimentation separation method is not high, and the process requires a large amount of reagents. Summary of the invention

[0007] In order to overcome the shortcomings of the above-mentioned prior art, the purpose of the present invention is to provide an efficient separation system and separation method for the three-phase components of oily sludge, and to destabilize the oily sludge by a multi-stage enhanced demulsification method. The oily sludge can be destabilized by homogenizing and tempering pretreatment, agent enhanced demulsification coupled with a multi-layer porous partition and a high-frequency torrent collision method, which can reduce the oil-water interfacial tension in the oily sludge system, strengthen the aggregation and growth of solid phase particles, destroy the stable emulsified state of the oily sludge, and deeply destabilize the oily sludge. Then, after solid-liquid separation and oil-water separation, efficient separation of the three-phase components of the oily sludge can be achieved.

[0008] In order to achieve the above object, the technical solution adopted by the present invention is as follows:

[0009] An efficient separation system for three-phase components of oily sludge, comprising:

[0010] Homogenizing and conditioning tank 1: used for diluting and reducing the viscosity of the oily sludge; the oily sludge inlet of the homogenizing and conditioning tank 1 is connected to the oily sludge outlet of the oily sludge storage tank 7, and the water inlet of the homogenizing and conditioning tank 1 is connected to the water outlet of the wastewater heating tank 5;

[0011] Demulsification unit 2: used for chemical demulsification and thermal vibration agglomeration demulsification treatment of oily sludge; the oily sludge inlet of the demulsification unit 2 is connected with the oily sludge outlet of the homogenization and conditioning tank 1;

[0012] Separation unit 3: used for performing three-phase separation on the demulsified oily sludge; the oily sludge inlet of the separation unit 3 is connected with the oily sludge outlet of the demulsification unit 2;

[0013] Recovery unit 4: used to recover oil, wastewater and sludge waste residue; the inlets of the oil phase, water phase and sludge solid phase of the recovery unit 4 are connected to the outlets of the oil phase, water phase and sludge solid phase of the separation unit 3 respectively.

[0014] An extractor 101 is provided in the homogenizing and conditioning tank 1, the water inlet of the extractor 101 is connected to the water outlet of the wastewater heating tank 5, and the oily sludge inlet of the extractor 101 is connected to the oily sludge outlet of the oily sludge storage tank 7; an oily sludge reflux inlet connected to the oily sludge outlet of the homogenizing and conditioning tank 1 is provided at the top of the homogenizing and conditioning tank 1.

[0015] The demulsification unit 2 includes a synergistic homogenizer 21 connected to the oily sludge outlet of the homogenization and conditioning tank 1, the agent inlet of the synergistic homogenizer 21 is connected to the agent outlet of the agent tank 9, the oily sludge outlet of the synergistic homogenizer 21 is connected to the oily sludge inlet of the jet mixer 22, the water vapor inlet of the jet mixer 22 is connected to the water vapor outlet of the wastewater heating tank 5 through the steam drum 6, and the oily sludge outlet of the jet mixer 22 is connected to the oily sludge inlet of the oscillating flow nucleator 23.

[0016] The synergistic homogenizer 21 includes a first shell 218 and a motor 211 arranged on the top of the first shell 218. The power output shaft of the motor 211 is connected to a rotating shaft 212 extending into the first shell 218. The other end of the rotating shaft 212 is connected to a rotating cavity 216 arranged in the first shell 218. A filler 217 and an oily sludge pipeline 213 and a drug pipeline 214 arranged in parallel on the inner side of the filler 217 are arranged in the rotating cavity 216. The shape of the filler 217 is a mesh, spherical, annular or irregular pore structure, and the specific surface area of ​​the filler 217 is 120-800m 2 / m 3 The oily sludge pipeline 213 and the reagent pipeline 214 are evenly provided with a plurality of nozzles 215 facing the filler 217 .

[0017] The oscillating flow nucleator 23 includes a second outer shell 231, in which 6-10 layers of porous partitions 232 are evenly arranged, and the interlayer spacing of the porous partitions 232 is 150-300 mm; a plurality of openings 233 are processed on the porous partition 232, and the openings 233 include a contraction section 234, a throat diameter 235 and an expansion section 236, and the angle α of the contraction section 234 is 25-35°, and the angle β of the expansion section 236 is 45-65°.

[0018] The separation unit 3 includes a solid-liquid separator 31 connected to the oily sludge outlet of the oscillating flow nucleator 23 through a conveying pump, the oil-water outlet of the solid-liquid separator 31 is connected to the oil-water inlet of the oil-water separator 32, and the low oil-water phase outlet of the oil-water separator 32 is connected to the low oil-water phase inlet of the wastewater deoiling tank 33; a bubble generator 331 is provided at the inner bottom end of the wastewater deoiling tank 33, and the gas inlet of the bubble generator 331 is connected to the gas outlet of the gas storage tank 8; during system operation, the oily floating liquid and part of the wastewater outlet of the wastewater deoiling tank 33 are connected to the water inlet of the wastewater heating tank 5; when the system is initially operated, the water inlet of the wastewater heating tank 5 is connected to the water outlet of the water storage tank 10.

[0019] The recovery unit 4 includes a waste residue storage tank 41 connected to the sludge solid phase outlet of the solid-liquid separator 31, an oil storage tank 42 connected to the oil phase outlet of the oil-water separator 32, and a wastewater storage tank 43 connected to the water phase outlet of the wastewater deoiling tank 33.

[0020] A method for efficiently separating three-phase components of oily sludge, using the above-mentioned efficient separation system for oily sludge for separation, comprises the following steps:

[0021] Step 1: homogenizing and conditioning the oily sludge;

[0022] The oily sludge and hot water are transported to the homogenization and conditioning tank 1 for extraction and mixing for 15-25 minutes, and the oily sludge after the previous extraction and mixing is further returned to the homogenization and conditioning tank 1 for circulation and mixing to obtain homogenized oily sludge;

[0023] Step 2: transport the oily sludge homogenized in step 1 to the demulsification unit 2 for two-step demulsification treatment using chemical agents and thermal vibration agglomeration;

[0024] The oily sludge homogenized in step 1 is transported to the synergistic homogenizer 21 in the demulsification unit 2 for rotating centrifugal mixing for 3-5 minutes, and then transported to the jet mixer 22 for mixing and dispersion with the heat medium. The temperature of the oily sludge after mixing is 65-85°C; then transported to the vibration nucleator 23 for thermal vibration agglomeration and demulsification for 15-30 minutes to obtain the demulsified oily sludge;

[0025] Step 3: The oily sludge after demulsification in step 2 is transported to the solid-liquid separator 31 of the separation unit 3 for solid-liquid separation to obtain oily sludge waste residue and oil-water mixture; the oil-water mixture is transported to the oil-water separator 32 of the separation unit 3 for primary oil-water separation to obtain oil liquid and low-oil wastewater; the low-oil wastewater is transported to the wastewater deoiling tank 33 for secondary oil-water separation under the action of gas to obtain oil-containing floating liquid and wastewater;

[0026] Step 4: The oil-containing suspension and part of the wastewater in step 3 are heated to become water vapor and hot water. The water vapor is sent to the jet mixer 22 of step 2 as a heat medium, and the hot water is sent to the homogenization and conditioning tank 1 of step 1.

[0027] The oily sludge after homogenization in step 1 has a temperature of 40-60° C., a solid content of 10-30%, and a viscosity of ≤1500 mPa·s;

[0028] In the step 2, the mixed addition amount of the demulsifier, flocculant and pH regulator is 0.3-1.0% of the homogenized oily sludge; by mass ratio, demulsifier: flocculant: pH regulator = (5-7): (3-6): (1-2); the pH of the demulsification environment is 7.5-9.0; the heat medium is water vapor at 110-130° C., and the flow rate of the heat medium is 15-25% of the flow rate of the oily sludge after demulsification; the viscosity of the oily sludge after thermal vibration agglomeration demulsification is ≤1000mPa·s.

[0029] The demulsifier in step 2 is one or more combinations of polyethylene oxide-propylene oxide ether, polyoxyethylene polyoxypropylene octadecyl alcohol ether, polyoxyethylene polyoxypropylene polyether, and nonylphenol polyoxyethylene ether; the flocculant is one or more combinations of polyferric chloride, polyferric sulfate, polysilicon aluminum chloride, polysilicon aluminum iron, and polyacrylamide; the pH adjuster is one or more combinations of sodium hydroxide, triethanolamine, citric acid, and hydrochloric acid; the gas in step 3 is nitrogen, carbon dioxide, or air.

[0030] Compared with the prior art, the present invention has the following beneficial effects:

[0031] 1. The present invention adopts a multi-stage enhanced demulsification method to demulsify the oily sludge, that is, the centrifugal membrane method of the synergistic homogenizer is coupled with the high-frequency turbulence collision method of the multi-layer porous partition of the oscillating flow nucleator, which not only greatly reduces the oil-water interfacial tension in the oily sludge system, but also makes the difficult-to-treat solid particles in the system aggregate and agglomerate, and completely realizes the deep destabilization of the oil, water and solid phases; compared with the traditional physical-chemical viscosity reduction and demulsification method, this method has a higher degree of demulsification and a better separation effect of the three phases of oily sludge.

[0032] 2. The present invention realizes efficient mixing of oily sludge and reagents in the rotating chamber of the synergistic homogenizer by providing a synergistic homogenizer. Compared with the traditional mixing method of the stirring shaft, the interaction between the oily sludge and the reagents is more sufficient and more efficient, the demulsification effect is more significant, and the consumption of the reagents is greatly reduced, thereby reducing the treatment cost.

[0033] 3. The present invention sets up a vibration flow nucleator, and realizes multi-layer oscillation and multiple agglomeration of oily sludge through the multi-layer porous partition structure of the vibration flow nucleator, which completely solves the technical problems of difficult treatment and separation of solid phase particles commonly existing in the process of demulsification of oily sludge, and improves the separation effect of oil, water and solid three phases.

[0034] 4. The present invention transports the heat medium and the pre-demulsified oily sludge into the oscillating flow nucleator together, and the heat medium and the oily sludge directly exchange heat, thereby accelerating molecular movement and reducing the risk of clogging of the porous partition.

[0035] 5. The present invention provides a solid-liquid separator and an oil-water separator to perform solid-liquid separation and oil-water separation on the oily sludge in turn, thereby effectively separating the three phases of oil, water and solid, overcoming the defect that a single device is difficult to achieve comprehensive separation, and significantly improving the separation effect.

[0036] 6. The present invention recycles the separated wastewater by setting up a wastewater heating tank. Part of the separated wastewater is recycled to participate in the homogenization and tempering treatment of the oily sludge, and part of it is sent to the oscillating flow nucleator as a heat medium to participate in the thermal vibration agglomeration and demulsification of the oily sludge. The reuse of wastewater in the system effectively saves water resources and realizes the resource utilization of wastewater.

[0037] In summary, the present invention adopts a multi-stage enhanced demulsification method to destabilize the oily sludge. The oil-water interfacial tension in the oily sludge system is reduced through homogenization and tempering pretreatment, chemical enhanced demulsification coupled with a multi-layer porous partition and a high-frequency torrent collision method, the solid phase particle aggregation growth is enhanced, and the stable emulsified state of the oily sludge is destroyed, so that the oily sludge is deeply destabilized, and then solid-liquid separation and oil-water separation are performed to achieve efficient separation of the three-phase components of the oily sludge. The method for separating the three-phase components of the oily sludge is simple in process, small in equipment footprint, low in process energy consumption, and good in oil, water and solid separation of the oily sludge, and has broad market application prospects. BRIEF DESCRIPTION OF THE DRAWINGS

[0038] Figure 1 It is a structural schematic diagram of a high-efficiency separation system for three-phase components of oily sludge.

[0039] Figure 2 It is a structural schematic diagram of the efficiency-enhancing homogenizer provided by the present invention.

[0040] Figure 3 It is a schematic diagram of the structure of the oscillating flow nucleation device provided by the present invention.

[0041] Figure 4 The present invention Figure 3 Cross-sectional view at AA in the middle.

[0042] Figure 5 The present invention Figure 3 Schematic diagram of the enlarged structure at point B in the middle.

[0043] In the figure: homogenizing and tempering tank 1, extractor 101, demulsifier unit 2, synergist homogenizer 21, motor 211, rotating shaft 212, oily sludge pipeline 213, reagent pipeline 214, nozzle 215, rotating cavity 216, filler 217, first shell 218, jet mixer 22, oscillating flow nucleator 23, second shell 231, porous partition 232, opening 233, contraction section 234, throat diameter 235, expansion section 236, separation unit 3, solid-liquid separator 31, oil-water separator 32, wastewater deoiling tank 33, bubble generator 331, recovery unit 4, oily sludge waste residue storage tank 41, oil storage tank 42, wastewater storage tank 43, wastewater heating tank 5, steam drum 6, oily sludge storage tank 7, gas storage tank 8, reagent tank 9, water storage tank 10. DETAILED DESCRIPTION

[0044] The technical scheme of the present invention will be described in detail below in conjunction with the accompanying drawings and embodiments; it should be noted that, in the absence of conflict, the embodiments of the present invention and the features in the embodiments can be combined with each other. In Examples 1 to 14 of the present invention, the solid content of the oil phase separated from the oily sludge is determined by centrifugation, and the water content is determined by distillation, referring to the standard GB / T 260-2016 "Determination of water content of petroleum products by distillation"; the oil content of the separated wastewater is determined by infrared spectrophotometry, referring to the standard HJ637-2012 "Water quality - determination of petroleum and animal and plant oils - infrared spectrophotometry".

[0045] like Figure 1 As shown, a high-efficiency separation system for three-phase components of oily sludge comprises:

[0046] The homogenizing and conditioning tank 1 is used for diluting and reducing the viscosity of the oily sludge; the oily sludge inlet of the homogenizing and conditioning tank 1 is connected with the oily sludge outlet of the oily sludge storage tank 7, and a delivery pump is provided on the pipeline between the oily sludge storage tank 7 and the homogenizing and conditioning tank 1, which is used to transport the oily sludge in the oily sludge storage tank 7 to the homogenizing and conditioning tank 1 through the pipeline; the water inlet of the homogenizing and conditioning tank 1 is connected with the water outlet of the wastewater heating tank 5 through the delivery pump, and the water inlet of the wastewater heating tank 5 is connected with the water outlet of the external water storage tank 10. At the beginning of the system operation, fresh water is transported from the external water storage tank 10 to the wastewater heating tank 10. Tank 5; the oily sludge outlet of the homogenizing and conditioning tank 1 is connected to the oily sludge inlet of the demulsification unit 2; the homogenizing and conditioning tank 1 is provided with an extractor 101 for evenly mixing the oily sludge with hot water, the water inlet of the extractor 101 is connected to the water outlet of the wastewater heating tank 5, and the oily sludge inlet of the extractor 101 is connected to the oily sludge outlet of the oily sludge storage tank 7; the top of the homogenizing and conditioning tank 1 is provided with an oily sludge reflux inlet connected to the oily sludge outlet of the homogenizing and conditioning tank 1, for returning part of the oily sludge to the homogenizing and conditioning tank 1 for further enhanced mixing and viscosity reduction;

[0047] The demulsification unit 2 is used for demulsifying the oily sludge by chemical agents and thermal vibration agglomeration demulsification; the oily sludge inlet of the demulsification unit 2 is connected to the oily sludge outlet of the homogenization and conditioning tank 1 through a delivery pump; the demulsification unit 2 includes a synergistic homogenizer 21 connected to the oily sludge outlet of the homogenization and conditioning tank 1, and a delivery pump is provided on the pipeline between the synergistic homogenizer 21 and the homogenization and conditioning tank 1, which is used to transport the oily sludge in the homogenization and conditioning tank 1 to the synergistic homogenizer 21 through the pipeline; the agent inlet of the synergistic homogenizer 21 is connected to the agent outlet of the agent tank 9, the oily sludge outlet of the synergistic homogenizer 21 is connected to the oily sludge inlet of the jet mixer 22, the water vapor inlet of the jet mixer 22 is connected to the water vapor outlet of the wastewater heating tank 5 through the steam drum 6, and the oily sludge outlet of the jet mixer 22 is connected to the oily sludge inlet of the vibration flow nucleator 23.

[0048] like Figure 2 As shown, the synergistic homogenizer 21 includes a first shell 218 and a motor 211 arranged on the top of the first shell 218, the power output shaft of the motor 211 is connected to the rotating shaft 212 extending into the first shell 218, the other end of the rotating shaft 212 is connected to the rotating cavity 216 arranged in the first shell 218, and the rotating cavity 216 is provided with a filler 217 and an oily sludge pipeline 213 and a drug pipeline 214 arranged in parallel on the inner side of the filler 217; the shape of the filler 217 is a mesh, spherical, annular or irregular pore structure, and the specific surface area of ​​the filler 217 is 120-800m 2 / m 3 The oily sludge pipeline 213 and the reagent pipeline 214 are evenly provided with a plurality of nozzles 215 facing the filler 217 .

[0049] The jet mixer 22 includes a liquid inlet section, a pressure section and an injection section, wherein the liquid inlet section is in a conical contraction shape, the pressure section is in a circular tubular shape, and the injection section is in a conical diffusion shape, and the two ends of the pressure section are respectively connected to the liquid inlet section and the injection section; under the condition of high-speed flow of the heat medium, the oily sludge after pre-demulsification is sucked into the pressure section by the annular negative pressure formed by the high-speed airflow, and the heat medium and the oily sludge in the pressure zone are ejected at a high speed after the pressure is released, and the oily sludge and the heat medium are forced to disperse and are fully mixed and heated.

[0050] like Figure 3 As shown, the oscillating flow core concentrator 23 includes a second shell 231, and 6-10 layers of porous partitions 232 are evenly arranged in the second shell 231, and the interlayer spacing of the porous partitions 232 is 150-300mm; the porous partitions 232 are processed with a plurality of openings 233, such as Figure 4 As shown, the opening 233 includes a contraction section 234, a throat diameter 235 and an expansion section 236. The angle α of the contraction section 234 is 25-35°, and the angle β of the expansion section 236 is 45-65°. Figure 5 As shown, the oily sludge passes through the contraction section 234, the throat diameter 235 and the expansion section 236 in sequence, and collides with the multi-layer porous partition 232 at high frequency, wherein the emulsified particles aggregate and grow, causing the oily sludge to become deeply unstable for a second time, and generating an oil-water-slag three-phase interface.

[0051] The separation unit 3 is used to perform solid-liquid separation on the oily sludge after demulsification to obtain oily sludge waste residue and oil-water mixture, and then perform oil-water separation on the separated oil-water mixture to obtain oil liquid and low-oil wastewater, and finally treat the low-oil wastewater based on the flotation principle to obtain oily floating liquid and wastewater; the oily sludge inlet of the separation unit 3 is connected to the oily sludge outlet of the demulsification unit 2 through a delivery pump; the separation unit 3 includes a solid-liquid separator 31 connected to the oily sludge outlet of the oscillating flow nucleator 23, and a delivery pump is provided on the pipeline between the solid-liquid separator 31 and the oscillating flow nucleator 23, which is used to transport the oily sludge after demulsification treatment through the pipeline to In the solid-liquid separator 31; the solid-liquid separator 31 is provided with an oil sludge solid phase outlet, and the oil-water outlet of the solid-liquid separator 31 is connected to the oil-water inlet of the oil-water separator 32; the oil-water separator 32 is provided with an oil phase outlet, and the low oil-water phase outlet of the oil-water separator 32 is connected to the low oil-water phase inlet of the wastewater deoiling tank 33, and the wastewater deoiling tank 33 is provided with a water phase outlet, and the inner bottom of the wastewater deoiling tank 33 is provided with a bubble generator 331, and the gas inlet of the bubble generator 331 is connected to the gas outlet of the gas storage tank 8; during the operation of the system, the oil-containing floating liquid and part of the wastewater outlet of the wastewater deoiling tank 33 are connected to the water inlet of the wastewater heating tank 5;

[0052] The recovery unit 4 is used to recover oil, wastewater and sludge waste residue. The inlets of the oil phase, water phase and sludge solid phase of the recovery unit 4 are respectively connected to the outlets of the oil phase, water phase and sludge solid phase of the separation unit 3; the recovery unit 4 includes a waste residue storage tank 41 connected to the sludge solid phase outlet of the solid-liquid separator 31, an oil storage tank 42 connected to the oil phase outlet of the oil-water separator 32, and a wastewater storage tank 43 connected to the water phase outlet of the wastewater de-oiling tank 33.

[0053] The solid-liquid separator 31 is used to perform solid-liquid separation on the oily sludge after demulsification treatment, that is, the treated oily sludge is sent to the high-speed rotating solid-liquid separator 31, and under the action of strong centrifugal force, the solid particles with higher density are deposited on the wall surface, and are pushed to the slag discharge port by the blades of the spiral pusher inside the solid-liquid separator, and then enter the oil sludge waste storage tank 41, while the oil-water mixture with lower density overflows and is discharged into the solid-liquid separator 31, and overflows through the oil-water outlet of the solid-liquid separator 31;

[0054] The oil-water separator 32 is used to separate oil and water from an oil-water mixture with a relatively low density, that is, under the action of the strong centrifugal force generated by high-speed rotation, the oil-water mixture is dispersed, wherein the separated oil phase enters the oil storage tank 42, and the remaining low-oil wastewater enters the wastewater deoiling tank 33; the bubble generator 331 of the wastewater deoiling tank 33 continuously introduces highly dispersed tiny bubbles from the bottom into the low-oil wastewater, so that the oil phase in the wastewater moves upward with the floating of the bubbles until it reaches the surface of the liquid, thereby further reducing the oil content in the wastewater; the gas in the bubble generator 331 comes from the gas storage tank 8.

[0055] A method for efficiently separating three-phase components of oily sludge, using the above-mentioned efficient separation system for oily sludge for separation, comprises the following steps:

[0056] Step 1: homogenizing and conditioning the oily sludge;

[0057] The oily sludge and hot water are transported to the homogenization and conditioning tank 1 for extraction and mixing for 15-25 minutes, and the oily sludge after the previous extraction and mixing is further returned to the homogenization and conditioning tank 1 for circulation and mixing, so as to achieve homogenization and viscosity reduction of the oily sludge, and obtain homogenized oily sludge; the homogenized oily sludge has a temperature of 40-60°C, a solid content of 10-30%, and a viscosity of ≤1500mPa·s;

[0058] Step 2: transport the oily sludge homogenized in step 1 to the demulsification unit 2 for two-step demulsification treatment using chemical agents and thermal vibration agglomeration;

[0059] The oily sludge homogenized in step 1 is transported to the synergistic homogenizer 21 in the demulsification unit 2 for rotating centrifugal mixing for 3-5 minutes, and then transported to the jet mixer 22 for mixing and dispersion with the heat medium to further reduce the viscosity of the oily sludge. The temperature of the oily sludge after mixing is 65-85°C; then transported to the vibration nucleator 23 for thermal vibration agglomeration and demulsification for 15-30 minutes to obtain the demulsified oily sludge;

[0060] The mixed addition amount of the demulsifier, flocculant and pH regulator is 0.3-1.0% of the homogenized oily sludge; by mass ratio, demulsifier: flocculant: pH regulator = (5-7): (3-6): (1-2); the pH of the demulsification environment is 7.5-9.0; the demulsifier is one or more combinations of polyethylene oxide-propylene oxide ether, polyoxyethylene polyoxypropylene octadecyl alcohol ether, polyoxyethylene polyoxypropylene polyether, and nonylphenol polyoxyethylene ether; the flocculant is one or more combinations of polyferric chloride, polyferric sulfate, polysilicon aluminum chloride, polysilicon aluminum iron, and polyacrylamide; the pH regulator is one or more combinations of sodium hydroxide, triethanolamine, citric acid, and hydrochloric acid; the heat medium is water vapor at 110-130°C, and the flow rate of the heat medium is 15-25% of the flow rate of the oily sludge after demulsification; the viscosity of the oily sludge after thermal vibration agglomeration and demulsification is ≤1000mPa·s;

[0061] Step 3: The oily sludge after demulsification in step 2 is transported to the solid-liquid separator 31 of the separation unit 3 for solid-liquid separation to obtain oily sludge waste residue and oil-water mixture; the oil-water mixture is transported to the oil-water separator 32 of the separation unit 3 for primary oil-water separation to obtain oil liquid and low-oil wastewater; the low-oil wastewater is transported to the wastewater deoiling tank 33 for secondary oil-water separation under the action of gas to obtain oil-containing floating liquid and wastewater; the gas is nitrogen, carbon dioxide or air;

[0062] Step 4: The oil-containing suspension and part of the wastewater in step 3 are heated to become water vapor and hot water. The water vapor is sent to the jet mixer 22 of step 2 as a heat medium, and the hot water is sent to the homogenization and conditioning tank 1 of step 1.

[0063] Example 1

[0064] In this embodiment, oily sludge produced in an oil production plant is selected. The oil content of the oily sludge is about 50.8%, the water content is about 23.5%, and the residue content is about 25.7%.

[0065] A method for efficiently separating three-phase components of oily sludge, using the above-mentioned efficient separation system for oily sludge for separation, comprises the following steps:

[0066] Step 1: homogenizing and conditioning the oily sludge;

[0067] The oily sludge and hot water are transported to the homogenization and conditioning tank 1 for extraction and mixing for 15 minutes, and the oily sludge after the previous extraction and mixing is further returned to the homogenization and conditioning tank 1 for circulation and mixing, so as to achieve homogenization and viscosity reduction of the oily sludge, and obtain homogenized oily sludge; the homogenized oily sludge has a temperature of 40°C, a solid content of 30%, and a viscosity of 1250 mPa·s;

[0068] Step 2: transport the oily sludge homogenized in step 1 to the demulsification unit 2 for two-step demulsification treatment using chemical agents and thermal vibration agglomeration;

[0069] The oily sludge homogenized in step 1 is transported to the synergistic homogenizer 21 in the demulsification unit 2 for rotating centrifugal mixing for 3 minutes, and then transported to the jet mixer 22 for mixing and dispersion with the heat medium to further reduce the viscosity of the oily sludge. The temperature of the oily sludge after mixing is 70°C; then transported to the vibration flow nucleator 23 for thermal vibration agglomeration and demulsification for 30 minutes to obtain the demulsified oily sludge;

[0070] The mixed addition amount of the demulsifier, flocculant and pH regulator is 0.7% of the homogenized oily sludge; by mass ratio, the demulsifier: flocculant: pH regulator = 5:4:1; the pH of the demulsification environment is 8.5; the demulsifier is polyoxyethylene polyoxypropylene polyether; the flocculant is polysilicon aluminum iron; the pH regulator is sodium hydroxide and triethanolamine, by mass ratio, sodium hydroxide: triethanolamine = 2:1; the heat medium is 120°C water vapor, and the flow rate of the heat medium is 20% of the flow rate of the oily sludge after demulsification; the viscosity of the oily sludge after thermal vibration agglomeration demulsification is 886mPa·s;

[0071] Step 3: The oily sludge after demulsification in step 2 is transported to the solid-liquid separator 31 of the separation unit 3 for solid-liquid separation to obtain oily sludge waste residue and oil-water mixture; the oil-water mixture is transported to the oil-water separator 32 of the separation unit 3 for primary oil-water separation to obtain oil liquid and low-oil wastewater; the low-oil wastewater is transported to the wastewater deoiling tank 33 for secondary oil-water separation under the action of nitrogen to obtain oil-containing floating liquid and wastewater;

[0072] Step 4: The oil-containing suspension and part of the wastewater in step 3 are heated to become water vapor and hot water. The water vapor is sent to the jet mixer 22 of step 2 as a heat medium, and the hot water is sent to the homogenization and conditioning tank 1 of step 1.

[0073] In this embodiment, the filler 217 in the rotating cavity 216 of the synergistic homogenizer 21 is a mesh filler structure with a specific surface area of ​​600m 2 / m 3 The oscillating flow nucleator 23 is evenly provided with 8 layers of porous partitions 232, and the interlayer spacing of the porous partitions 232 is 220 mm; the angle α of the contraction section 234 is 30°, and the angle β of the expansion section 236 is 55°.

[0074] After separation, the solid content and water content in the oil were 0.8% and 38 ppm respectively, and the oil content in the wastewater was 25 ppm.

[0075] Example 2

[0076] The process, parameters and properties of the selected oily sludge in this embodiment are the same as those in Example 1, except that: in step 1, the residence time of the oily sludge in the homogenization and conditioning tank 1 is 25 minutes; the solid content of the homogenized oily sludge is 20% and the viscosity is 1342 mPa·s; in step 2, the viscosity of the oily sludge after thermal vibration agglomeration and demulsification is 910 mPa·s.

[0077] After separation, the solid content and water content in the oil were 0.9% and 41ppm respectively; the oil content in the wastewater was 28ppm.

[0078] Example 3

[0079] The process, parameters and properties of the selected oily sludge in this embodiment are the same as those in Example 2, except that: in step 1, the oily sludge and hot water are transported to the homogenization and conditioning tank 1 for extraction and mixing; the temperature of the homogenized oily sludge is 60° C., the solid content is 10%, and the viscosity is 1089 mPa·s; in step 2, the viscosity of the oily sludge after thermal vibration agglomeration and demulsification is 697 mPa·s.

[0080] After separation, the solid content and water content in the oil were 0.6% and 28ppm respectively; the oil content in the wastewater was 24ppm.

[0081] Example 4

[0082] In this embodiment, oily sludge produced in an oil production plant is selected. The oil content of the oily sludge is about 25.8%, the water content is about 39.4%, and the residue content is about 34.8%.

[0083] A method for efficiently separating three-phase components of oily sludge, using the above-mentioned efficient separation system for oily sludge for separation, comprises the following steps:

[0084] Step 1: homogenizing and conditioning the oily sludge;

[0085] The oily sludge and hot water are transported to the homogenization and conditioning tank 1 for extraction and mixing for 20 minutes, and the oily sludge after the previous extraction and mixing is further returned to the homogenization and conditioning tank 1 for circulation and mixing, so as to achieve homogenization and viscosity reduction of the oily sludge, and obtain homogenized oily sludge; the homogenized oily sludge has a temperature of 50° C., a solid content of 20%, and a viscosity of 1187 mPa·s;

[0086] Step 2: transport the oily sludge homogenized in step 1 to the demulsification unit 2 for two-step demulsification treatment using chemical agents and thermal vibration agglomeration;

[0087] The oily sludge homogenized in step 1 is transported to the synergistic homogenizer 21 in the demulsification unit 2 for rotating centrifugal mixing for 5 minutes, and then transported to the jet mixer 22 for mixing and dispersion with the heat medium to further reduce the viscosity of the oily sludge. The temperature of the oily sludge after mixing is 70°C; then transported to the vibration nucleator 23 for thermal vibration agglomeration and demulsification for 20 minutes to obtain the demulsified oily sludge;

[0088] The mixed addition amount of the demulsifier, flocculant and pH regulator is 1.0% of the homogenized oily sludge; by mass ratio, the demulsifier: flocculant: pH regulator = 5:6:2; the pH of the demulsification environment is 9.0; the demulsifier is nonylphenol polyoxyethylene ether; the flocculant is polyferric sulfate and polysilicon aluminum chloride, by mass ratio, polyferric sulfate: polysilicon aluminum chloride = 3:2; the pH regulator is sodium hydroxide; the heat medium is 120°C water vapor, and the flow rate of the heat medium is 20% of the flow rate of the oily sludge after demulsification; the viscosity of the oily sludge after thermal vibration agglomeration demulsification is 687mPa·s;

[0089] Step 3: The oily sludge after demulsification in step 2 is transported to the solid-liquid separator 31 of the separation unit 3 for solid-liquid separation to obtain oily sludge waste residue and oil-water mixture; the oil-water mixture is transported to the oil-water separator 32 of the separation unit 3 for primary oil-water separation to obtain oil liquid and low-oil wastewater; the low-oil wastewater is transported to the wastewater deoiling tank 33 for secondary oil-water separation under the action of air to obtain oil-containing floating liquid and wastewater;

[0090] Step 4: The oil-containing suspension and part of the wastewater in step 3 are heated to become water vapor and hot water. The water vapor is sent to the jet mixer 22 of step 2 as a heat medium, and the hot water is sent to the homogenization and conditioning tank 1 of step 1.

[0091] In this embodiment, the filler 217 in the rotating cavity 216 of the synergistic homogenizer 21 is a spherical filler structure with a specific surface area of ​​600m 2 / m 3 The oscillating flow nucleator 23 is evenly provided with 8 layers of porous partitions 232, and the interlayer spacing of the porous partitions 232 is 220 mm; the angle α of the contraction section 234 is 30°, and the angle β of the expansion section 236 is 55°.

[0092] After separation, the solid content and water content in the oil were 0.6% and 32 ppm respectively, and the oil content in the wastewater was 41 ppm.

[0093] Example 5

[0094] The process, parameters and properties of the oily sludge in this embodiment are the same as those in embodiment 4, except that: in step 2, the mixed addition amount of the demulsifier, flocculant and pH regulator in the synergistic homogenizer 21 is 0.3% of the homogenized oily sludge; the filler 217 in the rotating cavity 216 of the synergistic homogenizer 21 is an annular structure with a specific surface area of ​​300m 2 / m 3 ; The viscosity of the oily sludge after thermal vibration agglomeration and demulsification in step 2 is 721mPa·s.

[0095] After separation, the solid content and water content in the oil were 0.7% and 36 ppm respectively, and the oil content in the wastewater was 43 ppm.

[0096] Example 6

[0097] The process, parameters and properties of the oily sludge used in this embodiment are the same as those in embodiment 4, except that the filler 217 in the rotating cavity 216 of the synergistic homogenizer 21 in step 2 is a spherical filler structure with a specific surface area of ​​800 m 2 / m 3 ; The viscosity of the oily sludge after thermal vibration agglomeration and demulsification in step 3 is 518mPa·s.

[0098] After separation, the solid content and water content in the oil were 0.5% and 26 ppm respectively, and the oil content in the wastewater was 33 ppm.

[0099] Example 7

[0100] The process, parameters and properties of the oily sludge used in this embodiment are the same as those in embodiment 4, except that the filler 217 in the rotating cavity 216 of the synergistic homogenizer 21 in step 2 uses an irregular pore structure, and its specific surface area is 120m 2 / m 3 ; The viscosity of the oily sludge after thermal vibration agglomeration and demulsification in step 2 is 702mPa·s.

[0101] After separation, the solid content and water content in the oil were 0.7% and 32 ppm respectively, and the oil content in the wastewater was 37 ppm.

[0102] Example 8

[0103] In this embodiment, oily sludge produced in an oil production plant is selected. The oily sludge has an oil content of about 41.8%, a water content of about 30.8%, and a slag content of about 27.4%.

[0104] A method for efficiently separating three-phase components of oily sludge, using the above-mentioned efficient separation system for oily sludge for separation, comprises the following steps:

[0105] Step 1: homogenizing and conditioning the oily sludge;

[0106] The oily sludge and hot water are transported to the homogenization and conditioning tank 1 for extraction and mixing for 20 minutes, and the oily sludge after the previous extraction and mixing is further returned to the homogenization and conditioning tank 1 for circulation and mixing, so as to achieve homogenization and viscosity reduction of the oily sludge, and obtain homogenized oily sludge; the homogenized oily sludge has a temperature of 50° C., a solid content of 20%, and a viscosity of 1074 mPa·s;

[0107] Step 2: transport the oily sludge homogenized in step 1 to the demulsification unit 2 for two-step demulsification treatment using chemical agents and thermal vibration agglomeration;

[0108] The oily sludge homogenized in step 1 is transported to the synergistic homogenizer 21 in the demulsification unit 2 for rotating centrifugal mixing for 5 minutes, and then transported to the jet mixer 22 for mixing and dispersion with the heat medium to further reduce the viscosity of the oily sludge. The temperature of the oily sludge after mixing is 85°C; then transported to the vibration flow nucleator 23 for thermal vibration agglomeration and demulsification for 15 minutes to obtain the demulsified oily sludge;

[0109] The mixed addition amount of the demulsifier, flocculant and pH regulator is 0.7% of the homogenized oily sludge; by mass ratio, the demulsifier: flocculant: pH regulator = 7:3:1; the pH of the demulsification environment is 7.5; the demulsifier is polyethylene oxide-propylene oxide ether and polyoxyethylene polyoxypropylene octadecyl alcohol ether, by mass ratio, polyethylene oxide-propylene oxide ether: polyoxyethylene polyoxypropylene octadecyl alcohol ether = 2:1; the flocculant is polyferric chloride; the pH regulator is citric acid and hydrochloric acid, by mass ratio, citric acid: hydrochloric acid = 1:1; the heat medium is 130°C water vapor, and the flow rate of the heat medium is 15% of the flow rate of the oily sludge after demulsification; the viscosity of the oily sludge after thermal vibration agglomeration demulsification is 653mPa·s;

[0110] Step 3: The oily sludge after demulsification in step 2 is transported to the solid-liquid separator 31 of the separation unit 3 for solid-liquid separation to obtain oily sludge waste residue and oil-water mixture; the oil-water mixture is transported to the oil-water separator 32 of the separation unit 3 for primary oil-water separation to obtain oil liquid and low-oil wastewater; the low-oil wastewater is transported to the wastewater deoiling tank 33 for secondary oil-water separation under the action of carbon dioxide to obtain oil-containing floating liquid and wastewater;

[0111] Step 4: The oil-containing suspension and part of the wastewater in step 3 are heated to become water vapor and hot water. The water vapor is sent to the jet mixer 22 of step 2 as a heat medium, and the hot water is sent to the homogenization and conditioning tank 1 of step 1.

[0112] In this embodiment, the filler 217 in the rotating cavity 216 of the synergistic homogenizer 21 is a mesh filler structure with a specific surface area of ​​600m 2 / m 3 The oscillating flow nucleator 23 is evenly provided with 8 layers of porous partitions 232, and the interlayer spacing of the porous partitions 232 is 220 mm; the angle α of the contraction section 234 is 30°, and the angle β of the expansion section 236 is 55°.

[0113] After separation, the solid content and water content in the oil were 0.8% and 26ppm respectively, and the oil content in the wastewater was 30ppm.

[0114] Example 9

[0115] The process, parameters and properties of the selected oily sludge in this embodiment are the same as those in Example 8, except that: in step 2, the oily sludge is transported to the jet mixer 22 to be mixed and dispersed with 110° C. water vapor, and the temperature of the oily sludge after mixing is 65° C.; and the viscosity of the oily sludge after thermal vibration agglomeration and demulsification in step 2 is 786 mPa·s.

[0116] After separation, the solid content and water content in the oil were 0.9% and 34 ppm respectively, and the oil content in the wastewater was 39 ppm.

[0117] Example 10

[0118] The process, parameters and properties of the oily sludge used in this embodiment are the same as those in Embodiment 8, except that the flow rate of the water vapor entering the jet mixer 22 in step 2 is 25% of the flow rate of the oily sludge after demulsification; and the viscosity of the oily sludge after thermal vibration agglomeration demulsification in step 2 is 599 mPa·s.

[0119] After separation, the solid content and water content in the oil were 0.6% and 23ppm respectively, and the oil content in the wastewater was 27ppm.

[0120] Embodiment 11

[0121] The process, parameters and properties of the oily sludge used in this embodiment are the same as those in embodiment 8, except that: in step 2, the oscillating flow nucleator 23 is evenly provided with 6 layers of porous partitions 232, and the interlayer spacing of the porous partitions 232 is 150 mm;

[0122] After separation, the solid content and water content in the oil were 0.9% and 35 ppm respectively, and the oil content in the wastewater was 38 ppm.

[0123] Example 12

[0124] The process, parameters and properties of the oily sludge used in this embodiment are the same as those in embodiment 8, except that: in step 2, the oscillating flow nucleator 23 is evenly provided with 10 layers of porous partitions 232, and the interlayer spacing of the porous partitions 232 is 300 mm;

[0125] After separation, the solid content and water content in the oil were 0.7% and 23ppm respectively, and the oil content in the wastewater was 26ppm.

[0126] Embodiment 13

[0127] The process, parameters and properties of the oily sludge used in this embodiment are the same as those in Embodiment 8, except that the angle α of the contraction section 234 of the opening 233 of the oscillating flow nucleator 23 in step 2 is 25°, and the angle β of the expansion section 236 is 45°.

[0128] After separation, the solid content and water content in the oil were 0.9% and 37 ppm respectively, and the oil content in the wastewater was 42 ppm.

[0129] Embodiment 14

[0130] The process, parameters and properties of the oily sludge used in this embodiment are the same as those in Embodiment 8, except that the angle α of the contraction section 234 of the opening 233 of the oscillating flow nucleator 23 in step 2 is 35°, and the angle β of the expansion section 236 is 65°.

[0131] After separation, the solid content and water content in the oil were 0.7% and 24 ppm respectively, and the oil content in the wastewater was 26 ppm.

[0132] In summary, the present invention is aimed at oily sludge of different properties. From the results after separation, it can be seen that after separation, the solid content of the oil liquid is ≤1%, the water content of the oil liquid is ≤50ppm, and the oil content in the wastewater is ≤50ppm, showing a good separation effect; separating and recovering oily sludge by the method of the present invention can bring significant economic, environmental and social benefits.

[0133] The above is only a preferred embodiment of the present invention and does not limit the present invention in any way. Any simple modification, change and equivalent change made to the above embodiment according to the technical essence of the invention still falls within the protection scope of the technical solution of the present invention.

Claims

1. An efficient separation system for three-phase components of oily sludge, characterized in that: include: A homogenizing and conditioning tank (1) is used to dilute and reduce the viscosity of the oily sludge; the oily sludge inlet of the homogenizing and conditioning tank (1) is connected to the oily sludge outlet of the oily sludge storage tank (7), and the water inlet of the homogenizing and conditioning tank (1) is connected to the water outlet of the wastewater heating tank (5); Demulsification unit (2): used for performing chemical demulsification and thermal vibration agglomeration demulsification treatment on the oily sludge; the oily sludge inlet of the demulsification unit (2) is connected to the oily sludge outlet of the homogenization and conditioning tank (1); A separation unit (3) is used to perform three-phase separation on the demulsified oily sludge; the oily sludge inlet of the separation unit (3) is connected to the oily sludge outlet of the demulsification unit (2); Recovery unit (4): used for recovering oil, waste water and oily sludge waste residue; the inlets of the oil phase, water phase and oily sludge solid phase of the recovery unit (4) are respectively connected to the outlets of the oil phase, water phase and oily sludge solid phase of the separation unit (3).

2. The high-efficiency separation system for three-phase components of oily sludge according to claim 1, characterized in that: An extractor (101) is arranged in the homogenizing and conditioning tank (1), the water inlet of the extractor (101) is connected to the water outlet of the wastewater heating tank (5), and the oily sludge inlet of the extractor (101) is connected to the oily sludge outlet of the oily sludge storage tank (7); and an oily sludge reflux inlet connected to the oily sludge outlet of the homogenizing and conditioning tank (1) is arranged at the top of the homogenizing and conditioning tank (1).

3. The efficient separation system for three-phase components of oily sludge according to claim 1 is characterized by: The demulsification unit (2) comprises a synergistic homogenizer (21) connected to the oily sludge outlet of the homogenization and conditioning tank (1); the agent inlet of the synergistic homogenizer (21) is connected to the agent outlet of the agent tank (9); the oily sludge outlet of the synergistic homogenizer (21) is connected to the oily sludge inlet of the jet mixer (22); the water vapor inlet of the jet mixer (22) is connected to the water vapor outlet of the wastewater heating tank (5) through the steam drum (6); and the oily sludge outlet of the jet mixer (22) is connected to the oily sludge inlet of the oscillating flow nucleator (23).

4. The high-efficiency separation system for three-phase components of oily sludge according to claim 3 is characterized by: The synergistic homogenizer (21) comprises a first housing (218) and a motor (211) arranged on the top of the first housing (218); a power output shaft of the motor (211) is connected to a rotating shaft (212) extending into the first housing (218); the other end of the rotating shaft (212) is connected to a rotating cavity (216) arranged in the first housing (218); a filler (217) and an oily sludge pipeline (213) and a drug pipeline (214) arranged in parallel on the inner side of the filler (217) are arranged in the rotating cavity (216); the filler (217) is in the shape of a mesh, spherical, annular or irregular pore structure; the specific surface area of ​​the filler (217) is 120-800 m 2 / m 3 The oily sludge pipeline (213) and the reagent pipeline (214) are evenly provided with a plurality of nozzles (215) facing the filler (217).

5. The high-efficiency separation system for three-phase components of oily sludge according to claim 3 is characterized by: The oscillating flow nucleator (23) comprises a second outer shell (231), 6-10 layers of porous partitions (232) are evenly arranged in the second outer shell (231), and the interlayer spacing of the porous partitions (232) is 150-300 mm; a plurality of openings (233) are processed on the porous partition (232), and the openings (233) include a contraction section (234), a throat diameter (235) and an expansion section (236), and the angle α of the contraction section (234) is 25-35°, and the angle β of the expansion section (236) is 45-65°.

6. The high-efficiency separation system for three-phase components of oily sludge according to claim 1, characterized in that: The separation unit (3) comprises a solid-liquid separator (31) connected to the oily sludge outlet of the oscillating flow nucleator (23); the oil-water outlet of the solid-liquid separator (31) is connected to the oil-water inlet of the oil-water separator (32); the low oil-water phase outlet of the oil-water separator (32) is connected to the low oil-water phase inlet of the wastewater deoiling tank (33); a bubble generator (331) is provided at the inner bottom end of the wastewater deoiling tank (33); the gas inlet of the bubble generator (331) is connected to the gas outlet of the gas storage tank (8); during system operation, the oily floating liquid and part of the wastewater outlet of the wastewater deoiling tank (33) are connected to the water inlet of the wastewater heating tank (5); during initial operation of the system, the water inlet of the wastewater heating tank (5) is connected to the water outlet of the water storage tank (10).

7. The high-efficiency separation system for three-phase components of oily sludge according to claim 1 is characterized by: The recovery unit (4) comprises a waste residue storage tank (41) connected to the sludge solid phase outlet of the solid-liquid separator (31), an oil storage tank (42) connected to the oil phase outlet of the oil-water separator (32), and a wastewater storage tank (43) connected to the water phase outlet of the wastewater deoiling tank (33).

8. A method for efficiently separating three-phase components of oily sludge, using the above-mentioned efficient separation system for oily sludge for separation, characterized in that: The following steps are involved: Step 1: homogenizing and conditioning the oily sludge; The oily sludge and hot water are transported to a homogenizing and conditioning tank (1) for extraction and mixing for 15-25 minutes, and the oily sludge extracted and mixed in the previous step is further returned to the homogenizing and conditioning tank (1) for circulation and mixing to obtain homogenized oily sludge; Step 2: The oily sludge homogenized in step 1 is transported to a demulsification unit (2) for demulsification treatment by using chemical agents and thermal vibration agglomeration; The oily sludge homogenized in step 1 is transported to the synergistic homogenizer (21) in the demulsification unit (2) for rotational centrifugal mixing for 3-5 minutes, and then transported to the jet mixer (22) for mixing and dispersion with the heat medium, wherein the temperature of the oily sludge after mixing is 65-85° C.; and then transported to the vibration flow nucleator (23) for thermal vibration agglomeration and demulsification for 15-30 minutes to obtain the demulsified oily sludge; Step 3: The oily sludge after demulsification in step 2 is transported to the solid-liquid separator (31) of the separation unit (3) for solid-liquid separation to obtain oily sludge waste residue and oil-water mixture; the oil-water mixture is transported to the oil-water separator (32) of the separation unit (3) for primary oil-water separation to obtain oil liquid and low-oil wastewater; the low-oil wastewater is transported to the wastewater deoiling tank (33) for secondary oil-water separation under the action of gas to obtain oily floating liquid and wastewater; Step 4: The oil-containing suspension and part of the wastewater in step 3 are heated to form water vapor and hot water. The water vapor is sent to the jet mixer (22) of step 2 as a heat medium, and the hot water is sent to the homogenization and conditioning tank (1) of step 1.

9. The method for efficiently separating three-phase components of oily sludge according to claim 8, characterized in that: The oily sludge after homogenization in step 1 has a temperature of 40-60° C., a solid content of 10-30%, and a viscosity of ≤1500 mPa·s; In the step 2, the mixed addition amount of the demulsifier, flocculant and pH regulator is 0.3-1.0% of the homogenized oily sludge; by mass ratio, demulsifier: flocculant: pH regulator = (5-7): (3-6): (1-2); the pH of the demulsification environment is 7.5-9.0; the heat medium is water vapor at 110-130° C., and the flow rate of the heat medium is 15-25% of the flow rate of the oily sludge after demulsification; the viscosity of the oily sludge after thermal vibration agglomeration demulsification is ≤1000mPa·s.

10. The method for efficiently separating three-phase components of oily sludge according to claim 8, characterized in that: The demulsifier in step 2 is one or more combinations of polyethylene oxide-propylene oxide ether, polyoxyethylene polyoxypropylene octadecyl alcohol ether, polyoxyethylene polyoxypropylene polyether, and nonylphenol polyoxyethylene ether; the flocculant is one or more combinations of polyferric chloride, polyferric sulfate, polysilicon aluminum chloride, polysilicon aluminum iron, and polyacrylamide; the pH adjuster is one or more combinations of sodium hydroxide, triethanolamine, citric acid, and hydrochloric acid; the gas in step 3 is nitrogen, carbon dioxide, or air.

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